Air Emissions From Reinforced Plastics Composite Manufacturing Process Lasco Panel Products: Volume I

United States Environmental Protection Agency Office of Air Quality Planning and Standards Research Triangle Park, NC 27711 EPA-454/R-99-024a August 1999 AIR ©EPA Air Emissions From Reinforced Plastics Composite Manufacturing Process LASCO Panel Products: Volume I •v^n^ ------- FINAL REPORT AIR EMISSIONS FROM REINFORCED PLASTICS COMPOSITE MANUFACTURING PROCESS LASCO PANEL PRODUCTS VOLUME I OF III REPORT TEXT APPENDIX A.I EPA Contract No. 68D70069 Work Assignment No. 2-10 Prepared for: Mr. Solomon Ricks (MD-19) Work Assignment Manager SMTG, EMC, EMAD, OAQPS U.S. Environmental Protection Agency Research Triangle Park, NC 27711 August 1999 P:\i530\finrpt Submitted by PACIFIC ENVIRONMENTAL SERVICES, INC. 5001 South Miami Blvd., Suite 300 PO Box 12077 Research Triangle Park, NC 27709 (919)941-0333 Fax: (919)941-0234 ------- DISCLAIMER This document was prepared by Pacific Environmental Services, Inc. (PES) under EPA Contract No. 68D70069, Work Assignment No. 2-10. This document has passed PES' internal quality assurance review and has been approved for distribution. The contents of this document do not necessarily reflect the views and policies of the U.S. EPA. Mention of trade names does not constitute endorsement by the EPA or PES. n ------- TABLE OF CONTENTS VOLUME I Page 1.0 INTRODUCTION 1-1 2.0 SUMMARY OF TEST RESULTS 2-1 2.1 EMISSIONS TEST LOG 2-1 2.2 PROCESS LINE RESULTS 2-4 2.3 TOTAL TEMPORARY ENCLOSURE - METHOD 25A TOTAL HYDROCARBON RESULTS 2-5 2.4 TOTAL TEMPORARY ENCLOSURE - VOLUMETRIC AIR FLOW RATE RESULTS 2-5 2.5 TOTAL TEMPORARY ENCLOSURE - METHOD 18 RESULTS . . 2-5 2.6 OVEN NOS. 9 AND 10 - METHOD 25A TOTAL HYDROCARBON RESULTS 2-23 2.7 OVEN NOS. 9 AND 10 - VOLUMETRIC FLOW RATE RESULTS 2-23 2.8 OVEN NOS. 9 AND 10 - METHOD 18 HAP RESULTS 2-23 2.9 UNCATALYZED RESIN (UCR) AND GEL COAT SAMPLE RESULTS 2-23 2.10 RESPONSE FACTOR RESULTS 2-41 2.11 METHOD 204 TOTAL TEMPORARY ENCLOSURE VERIFICATION 2-41 3.0 PROCESS DESCRIPTION 3-1 4.0 SAMPLING LOCATIONS 4-1 4.1 MAIN EXHAUST STACK 4-1 4.2 ROOM EXHAUST STACK 4-1 4.3 AUXILIARY EXHAUST STACK 4-4 4.4 NATURAL DRAFT OPENINGS 4-4 4.5 OVEN EXHAUST NO. 9 AND NO. 10 4-4 in ------- TABLE OF CONTENTS (Continued) 5.0 SAMPLING AND ANALYTICAL PROCEDURES 5-1 5.1 LOCATION OF MEASUREMENT SAMPLE/VELOCITY TRAVERSE POINTS 5-1 5.2 DETERMINATION OF STACK GAS VOLUMETRIC • FLOW RATE 5-1 5.3 DETERMINATION OF DRY MOLECULAR WEIGHT 5-4 5.4 EXHAUST GAS MOISTURE CONTENT 5-4 5.5 DETERMINATION OF HAZARDOUS AIR POLLUTANTS 5-4 5.6 DETERMINATION OF TOTAL HYDROCARBONS 5-6 5.7 DETERMINATION OF VOLATILE MATTER CONTENT, DENSITY, VOLUME OF SOLIDS, WEIGHT OF SOLIDS, WATER CONTENT, AND HAPS BY DISTILLATION 5-6 5.8 RESPONSE FACTORS FOR FLAME IONIZATION ANALYZERS 5-10 6.0 QUALITY ASSURANCE/QUALITY CONTROL 6-1 6.1 CALIBRATION OF APPARATUS 6-1 6.2 ONSITE QA/QC 6-3 APPENDIX A - RAW FIELD DATA Appendix A.I Manual Methods Raw Field Data A. 1.1 Method 1 Field Data Sheets (includes flows, moistures, and Method 18) A. 1.2 Condition 1 (includes flows, moistures, and Method 18) A. 1.3 Condition 2 (includes flows, moistures, and Method 18) A. 1.4 Condition 3 (includes flows, moistures, and Method 18) A. 1.5 Condition 4 (includes flows, moistures, and Method 18) A. 1.6 Condition 5 (includes flows, moistures, and Method 18) A. 1.7 Condition 6 (includes flows, moistures, and Method 18) A. 1.8 Condition 7 (includes flows, moistures, and Method 18) A. 1.9 Condition 8 (includes flows, moistures, and Method 18) A. 1.10 Condition 9 (includes flows, moistures, and Method 18) A. 1.11 Condition 10 (includes flows, moistures, and Method 18) A. 1.12 Condition 11 (includes flows, moistures, and Method 18) A. 1.13 Condition 12 (includes flows, moistures, and Method 18) A. 1.14 Condition 13 (includes flows, moistures, and Method 18) A. 1.15 NDO Summary Data iv ------- TABLE OF CONTENTS (Continued) VOLUME II Appendix A.2 Instrumental Methods Raw Field Data A.2.1 TTE Static Pressures A.2.2 Method 25A Calibration Data A.2.3 Condition 1 Method 25A A.2.4 Condition 2 Method 25A A.2.5 Condition 3 Method 25A A.2.6 Condition 4 Method 25A A.2.7 Condition 5 Method 25A A.2.8 Condition 6 Method 25A A.2.9 Condition 7 Method 25A A.2.10 Condition 8 Method 25A A.2.11 Condition 9 and 10 Method 25A A.2.12 Condition 11 Method 25A A.2.13 Condition 12 Method 25A A.2.14 Condition 13 Method 25A A.2.15 Conditions 1-13 Method 25A Strip Charts A.2.16 Oven Nos. 9 and 10 Method 25A VOLUMEIII APPENDIX B - ANALYTICAL DATA B. 1 Method 18 Analytical Data B.2 Method 18 GC Chromatograms APPENDIX C - CALCULATIONS APPENDIX D - QA/QC DATA APPENDIX E - PROJECT PARTICIPANTS ------- LIST OF TABLES VOLUME I Page Table 1.1 LASCO Panel Products Test Matrix 1-6 Table 2.1 Emission Test Log, LASCO Panel Products, Florence, Kentucky .... 2-2 Table 2.2 TTE Total Hydrocarbon Mass Emission Rate Summary 2-6 Table 2.3 Summary of TTE Stack Gas Conditions, and THC Concentrations and Mass Emission Rates, Condition 1 - May 14,1997 2-8 Table 2.4 Summary of TTE Stack Gas Conditions and THC Concentrations - Condition 2 - May 14,1997 2-9 Table 2.5 Summary of TTE Stack Gas Conditions and THC Concentrations - Condition 3 - May 15,1997 2-10 Table 2.6 Summary of TTE Stack Gas Conditions and THC Concentrations - Condition 4 - May 15,1997 2-11 Table 2.7 Summary of TTE Stack Gas Conditions and THC Concentrations - Condition 5 - May 19,1997 2-12 Table 2.8 Summary of TTE Stack Gas Conditions and THC Concentrations - Condition 6 - May 19,1997 2-13 Table 2.9 Summary of TTE Stack Gas Conditions and THC Concentrations - Condition 7 - May 20,1997 2-14 Table 2.10 Summary of TTE Stack Gas Conditions and THC Concentrations - Condition 8 - May 22,1997 2-15 Table 2.11 Summary of TTE Stack Gas Conditions and THC Concentrations - Condition 9 - May 22,1997 2-16 Table 2.12 Summary of TTE Stack Gas Conditions and THC Concentrations - Condition 10 - May 22, 1997 2-17 Table 2.13 Summary of TTE Stack Gas Conditions and THC Concentrations - Condition 11 - May 23,1997 2-18 Table 2.14 Summary of TTE Stack Gas Conditions and THC Concentrations - Condition 12 - May 29,1997 2-19 Table 2.15 Summary of TTE Stack Gas Conditions and THC Concentrations - Condition 13 - May 29,1997 2-20, Table 2.16 TTE Mass Rate Summary - Styrene, Methyl Methacrylate, and Cumene by EPA Method 18 2-21 Table 2.17 Ovens 9 and 10 THC Mass Emission Rate Summary 2-24 VI ------- LIST OF TABLES (Concluded) Table 2.18 Summary of Oven Stack Gas Conditions and THC Concentrations and Mass Emission Rates, Condition 1 - May 14,1997 2-26 Table 2.19 Summary of Oven Stack Gas Conditions and THC Concentrations and Mass Emission Rates, Condition 2 - May 14,1997 2-27 Table 2.20 Summary of Oven Stack Gas Conditions and THC Concentrations and Mass Emission Rates, Condition 3 - May 15,1997 2-28 Table 2.21 Summary of Oven Stack Gas Conditions and THC Concentrations and Mass Emission Rates, Condition 4 - May 15,1997 2-29 Table 2.22 Summary of Oven Stack Gas Conditions and THC Concentrations and Mass Emission Rates, Condition 5 - May 19,1997 2-30 Table 2.23 Summary of Oven Stack Gas Conditions and THC Concentrations and Mass Emission Rates, Condition 6 - May 19, 1997 2-31 Table 2.24 Summary of Oven Stack Gas Conditions and THC Concentrations and Mass Emission Rates, Condition 7 - May 20,1997 2-32 Table 2.25 Summary of Oven Stack Gas Conditions and THC Concentrations and Mass Emission Rates, Condition 8 - May 22,1997 2-33 Table 2.26 Summary of Oven Stack Gas Conditions and THC Concentrations and Mass Emission Rates, Condition 9 - May 22,1997 2-34 Table 2.27 Summary of Oven Stack Gas Conditions and THC Concentrations and Mass Emission Rates, Condition 10 - May 22, 1997 2-35 Table 2.28 Summary of Oven Stack Gas Conditions and THC Concentrations and Mass Emission Rates, Condition 11 - May 23,1997 2-36 Table 2.29 Summary of Oven Stack Gas Conditions and THC Concentrations and Mass Emission Rates, Condition 12 - May 29,1997 2-37 Table 2.30 Summary of Oven Stack Gas Conditions and THC Concentrations and Mass Emission Rates, Condition 13 - May 29,1997 2-38 Table 2.31 Ovens 9 and 10 Mass Emission Rate Summary - Styrene, Methyl Methacrylate, and Cumene by EPA Method 18 2-39 Table 2.32 Summary of Response Factor Results - Styrene Bag Standards 2-42 Table 5.1 Sources, Test Parameters, and Methods Summary LASCO Panel Products - Florence, Kentucky 5-2 Table 6.1 Summary of Temperature Sensors Calibration Requirements 6-2 Table 6.2 Summary of Calibration Results for THC Analyzers Condition Nos. 1-13, LASCO Panel Products 6-5 Table 6.3 Summary of EPA Method 18 Quality Assurance Results Styrene Recovery Efficiencies 6-7 Table 6.4 Summary of Desorption Efficiencies 6-7 vn ------- LIST OF FIGURES VOLUME I Page Figure 1.1 Key Personnel and Responsibility for Testing at LASCO Panel Products 1-2 Figure 1.2 Overview of Sampling Locations 1-5 Figure 2.1 Diagram of Temporary Total Enclosure 2-43 Figure 4.1 Main Exhaust Sample Location 4-2 Figure 4.2 Room Exhaust Sample Location 4-3 Figure 4.3 Auxiliary Exhaust Sampling Location : 4-5 Figure 4.4 Natural Draft Opening Sampling Location 4-6 Figure 4.5 Oven No. 9 Schematic of Sampling Location 4-7 Figure 4.6 Oven No. 10 Schematic of Sampling Location 4-8 Figure 5.1 Schematic of EPA Method 4 Sampling Train 5-5 Figure 5.2 Schematic of EPA Method 18 Sampling System - Sorbent Tube Method 5-7 Figure 5.3 Schematic of Methane/Ethane Sampling System 5-8 Figure 5.4 EPA Method 25A Total Gaseous Organic Analyzer and Sample System 5-9 Figure 5.5 Schematic of Bag Standard Preparation System 5-13 vm ------- 1.0 INTRODUCTION The U.S. Environmental Protection Agency (EPA) Emission Standards Division (ESD) requested that the EPA's Emissions Monitoring and Analysis Division (EMAD), Emission Measurement Center (EMC) provide testing support in the investigation of the reinforced plastics composite manufacturing source category to properly set the maximum achievable control technology (MACT) standards as required by the Clean Air Act Amendments of 1990. The sampling program was conducted through EPA Contract No. 68D20162, Work Assignment No. 4-05. Figure 1.1 represents the test program organization and major lines of communication. The reinforced plastics composite manufacturing process located at LAS CO Panel Products in Florence, Kentucky was selected by the ESD for this emissions testing program for the following reasons: 1. The lamination process (resin and gel coat application areas) is contained in a single room. This room can be treated as a total enclosure with slight modifications. 2. The process line can accommodate a wide variety of operating conditions to simulate worst case production plus the gel coating conditions. 3. The facility was willing to assist with the sampling effort. The "Wide Line" lamination table currently has an enclosure around the wet application areas (resin and gel coat) which controls organic emissions and vents to the roof exhaust. 4. The facility was willing to conduct a careful mass balance (using special scales to weigh raw materials and final product) to determine emissions during the tests so that the mass balance technique could be compared against stack measurements. 1-1 ------- LASCO Panel Products Hilary North (606)371-7720 PES QA/QC Officer Jeffrey L. Van Atten (703) 471-8383 Pretest Site Survey PES Site Specific Test Plan PES EPA/EMC Work Assignment Manager Solomon Ricks (919) 541-5242 PES Program Manager John Chehaske (703) 471-8383 PES Project Manager Dan Scheffel (513)489-6611 Field Testing PES Subcontractors DEECO Analyses PES EPA/ESD Work Assignment Madeleine L. Strum, PhD (919)541-2383 ESD Contractor PES Project Manager Kenneth R.Meardon, PhD (919)941-0333 Report Preparation PES Subcontractors DEECO Enthalpy Analytical. Inc. Figure 1.1 Key Personnel and Responsibility for Testing at LASCO Panel Products ------- The sampling program was designed to support the following BSD objectives: 1. Identify and quantify the hazardous air pollutants (HAPs) emitted by reinforced plastic manufacturing. 2. Identify the sources of HAPs and the total HAPs mass emission rates from the wet application area and the oven area. 3. Evaluate the following ventilation scenarios: • The current enclosure of the wet application area which is referred to as "current." • The current enclosure disconnected and turned off, where there is no capture of emissions in the wet application areas. This is referred to as "open." • Enclosure of all wet application areas, or as much as is possible, with the current exhaust fan disconnected. This is referred to as "closed." (In the original test plan, this condition was referred to as WAE.) 4. Depending on the effectiveness of the industry proposed "closed" system, develop a performance-based emission limitation achieved by the use of a wet area enclosed table system. 5. Assess the existing factors for volatile organic compound emissions from a continuous lamination process for the purposes of updating the information in AP-42 and determining cost effectiveness for MACT options involving emissions abatement. 6. Determine the effect of various process parameters such as line speed, laminate thickness, hazardous air pollutant content of raw material and the addition of a gel coat layer on the emission factor. Monitor and record related process and operating information to support the establishment of the emission limit and the assessment and development of emission factors. The primary objective of the testing program was to obtain total HAPs emitted from the lamination line and resin/gel coat usage rates to develop emission factors. The emission factors (pounds of HAPs emitted per pound of HAP used) were developed for a variety of process conditions. Sampling was performed during 13 process operating conditions. Measurements were made of the total hydrocarbons (THC), styrene, cumene, 1-3 ------- and methyl methacrylate (MMA), and the air flow rate at all enclosure exhausts. It should be noted that styrene and cumene were originally expected to account for more than 99 percent (%) of the total HAP emissions and were the compounds of primary interest. The measurement of MMA was not part of the original test plan, but was added while onsite, after it was discovered that MMA may account for higher percentages of the HAP content depending on the type of product produced. The secondary objective of the sampling program was to obtain data on the emissions of HAPs from the oven area. PES utilized the support services of two subcontractors to provide sampling and analytical support for this test program. Enthalpy Analytical, Inc. performed EPA Method 24 analyses on resin samples, analysis of HAP content of resin samples and vacuum distillations of several different resin samples. DEECO provided onsite gas chromatography HAP analysis of sorbent tube samples, spike tube preparations, ethane/methane analysis of oven bag samples and continuous measurements of total hydrocarbons on the oven exhausts and natural draft openings (NDOs). Figure 1.2 presents an overview of the sample locations at the LASCO site. Included in the diagram are the following locations: main exhaust, room exhaust, auxiliary exhaust, natural draft openings (A, B, C, and D) and ovens 9 and 10. Sample locations are described in detail in Section 4.0. Table 1.1 summarizes the test matrix for the test program. In addition to this introduction, this report contains the following sections: 2.0 SUMMARY OF RESULTS 3.0 PROCESS DESCRIPTION 4.0 SAMPLING LOCATIONS 5.0 SAMPLING AND ANALYTICAL PROCEDURES 6.0 QUALITY ASSURANCE/QUALITY CONTROL PROCEDURES AND RESULTS APPENDICES A. RAW FIELD DATA B. ANALYTICAL DATA C. CALCULATIONS D. QA/QC DATA E. PARTICIPANTS 1-4 ------- Flow Out i o Oven 10 ( J Oven 9 t NDO-B Flow In NDO-C I Flow Out Flow In NDO-A I Flow In Process Line Temporary Total Enclosure Flow Out Flow In NDO-D Auxiliary Exhaust Flow Out Room Exhaust Main Exhaust Figure 1.2 Overview of Sampling Locations 1-5 ------- TABLE 1.1 LASCO PANEL PRODUCTS TEST MATRIX Sample Location Main Wide Line Exhaust Room Exhaust Auxiliary Exhaust Natural Draft Openings A, B, C, D Oven Exhaust No. 9 Oven Exhaust No. 10 Resin Holding Tanks Number of Test Conditions 13 13 2 13 13 13 13 Sample Type THC Styrene, Cumene, MMA THC Styrene, Cumene, MMA THC Styrene, Cumene, MMA THC Styrene, Cumene, MMA THC Styrene, Cumene, MMA Methane/Ethane THC Styrene, Cumene, MMA Methane/Ethane Volatile content, solids, water, density HAPS Sampling Method EPA 25A EPA 18 EPA 25A EPA 18 EPA 25A EPA 18 EPA 25A EPA18 EPA 25A EPA 18 EPA 18 EPA 25A EPA 18 EPA 18 EPA 24 EPA 18 Analytical Method FIA GC/FID FIA GC/FID FIA GC/FID FIA GC/FID FIA GC/FID GC/FID FIA GC/FID GC/FID Gravimetric GC/MS Contractor (Subcontractor) PES PES (DEECO) PES PES (DEECO) PES PES (DEECO) DEECO PES (DEECO) DEECO PES (DEECO) (DEECO) (DEECO) PES (DEECO) (DEECO) (Enthalpy) (Enthalpy) ------- 2.0 SUMMARY OF TEST RESULTS This section provides summaries of the test results obtained from the testing program at LASCO Panel Products. The primary focus of the sampling effort was to measure THC concentrations and calculate mass emission rates from the temporary total enclosure (TTE). Also included are the results of the tests conducted for styrene, MMA, cumene, ethane and methane. The ethane and methane data was only collected from the oven areas to account for emissions as a result of poor burner efficiency. The oven data is included and was a secondary objective of this field effort to evaluate HAP emissions from the oven area. The resin analysis for VOC, water, solids, density and HAPs are not included in this report. The resin results and process data are contained in the ESD Test Reports. 2.1 EMISSIONS TEST LOG Sampling was conducted during the period of May 14 through May 29,1997. Table 2.1 summarizes the emissions test log. Presented in the table are the condition numbers, test runs, dates, sample locations, pollutants and process conditions. Each condition number correlates to a variation in process conditions, which included CURRENT, OPEN, CLOSED, and variations in product, line speed, and panel thickness. The following is a general description of the three room conditions that were examined during this sampling program. For each of the three conditions, the process room was treated as a TTE with all the access doors closed and NDOs minimized. The negative static pressure in the room was maintained at -0.004 inches of water or greater. The current condition was the operation of the process line the normal way it operates each production day. The main exhaust system is exhausting air emissions from the table area to the main roof exhaust stack. The table area is covered partially. Most top areas of the table are covered with panels and side areas mostly open. The initial resin application area is partially closed, with some panels open. The sampling areas consisted of the Main Exhaust which normally draws emission directly from the wet application area, the Room Exhaust which draws fugitive emission from floor level in one corner of the room, four natural draft openings (NDOs), and Ovens 9 and 10 exhaust stacks. 2-1 ------- TABLE 2.1 EMISSION TEST LOG LASCO PANEL PRODUCTS FLORENCE, KENTUCKY Condition No. 1 2 3 4 5 6 Run No. 1,2,3 1,2,3 1,2,3 1,2 1,2,3 1,2,3 Date 5/14/97 5/14/97 5/15/97 5/15/97 5/19/97 5/19/97 Sample Location Main Exhaust Room Exhaust NDOs Oven 9 & 10 Resin Tank Main Exhaust Room Exhaust NDOs Oven 9 & 10 Resin Tank Main Exhaust Room Exhaust NDOs Oven 9 & 10 Resin Tank Main Exhaust Room Exhaust NDOs Oven 9 & 10 Resin Tank Main Exhaust Room Exhaust NDOs Oven 9 & 10 Auxiliary Main Exhaust Room Exhaust NDOs Oven 9 & 10 Pollutant THCa, C8H8b, THC, C8H8, THC, C8H8, THC, CH4C, C2H6d,C8H8 HAPS, Solvent, Moisture, Density THC, C8H8, THC, C8H8, THC, C8H8, THC, CH4, C2H6, C8H8 THC, C8H8, THC, C8H8, THC, C8H8, THC, CH4, C2H6, C8H8 THC, C8H8, THC, C8H8, THC, C8H8, THC, CH4, C2H6, C8H8 THC, C8H8, THC, C8H8, THC, C8H8, THC, CH4, C2H6, C8H8 THC, C8H8, THC, C8H8, THC, C8H8, THC, CH4, C2H6, C8H8 Process Condition Current +Gelcoat Application Tank Supplied 0.06" panel 38.5% HAP with MMA Current + Gelcoat Application Used totes 0.045" panel 38.8% HAP with MMA Current No Gelcoat 0.09" panel 45.2% HAP without MMA Current No Gelcoat Increased line speed to 18 fpm 0.09" panel 45.2% HAP without MMA Open No Gelcoat Removed metal panels and one glass panel. Disconnected exhaust line on table. 84 minute samples 0.06" panel 40.5% HAP with MMA Current No Gelcoat 0.06" panel 40.5% HAP with MMA N) to ------- Table 2.1 (Concluded) Condition No. 7 8 9 10 11 12 13 Run No. 1,2,3 1,2,3 1 1 1,2,3 1,2,3,4 Void No. 2 1,2,3 Date 5/20/97 5/22/97 5/22/97 5/22/97 5/23/97 5/29/97 5/29/97 Sample Location Main Exhaust Room Exhaust NDOs Oven 9 & 10 Main Exhaust Room Exhaust NDOs Oven 9 & 10 Main Exhaust Room Exhaust NDOs Oven 9 & 10 Main Exhaust Room Exhaust NDOs Oven 9 & 10 Main Exhaust Room Exhaust NDOs Oven 9 & 10 Main Exhaust Room Exhaust NDOs Oven 9 & 10 Auxiliary Exhaust Main Exhaust Room Exhaust NDOs Oven 9 & 10 Auxiliary Exhaust Pollutant THC,CgH8, THC, C8H8, THC, C8H8, THC, CH4, C2H6, C8H8 THC, C8H8, THC, C8H8, THC, C8H8, THC, CH4, CjH^, C8H8 THC, C,H8, THC, C8H8, THC, C8H8, THC, CH4, C2H6, C8H8 THC, C8H8, THC, C8H8, THC, C8H8, THC, CH4, C2H6, C8H8 THC, C8H8, THC, C8H8, THC, C8H8, THC,CH4,C2H6,C8H8 THC, C8H8) THC,C8H8, THC, C8H8, THC, CH4, C2H6, C8H8 THC,C8H8, THC, C8H8, THC, C8H8, THC, C8H8, THC, CH4, C2H6, C8H8 THC, C8H8, Process Condition Current No Gelcoat 0.075" panel 40.5% HAP with MMA Current No Gelcoat 0.06" panel 42.4% HAP without MMA Current No Gelcoat 0.09" panel 42.4% HAP without MMA Current No Gelcoat 0.1 29" panel 39.5% HAP without MMA Current No Gelcoat 0.09" panel 39.5% HAP without MMA Open No Gelcoat Panels removed System opened up Auxiliary fan on 0.09" panel 45.2% HAP without MMA Closed No Gelcoat Panels all in place Additional panels + plastic used to enclose all table "wet" areas Auxiliary Fan on 0.09" panel 45.2% HAP without MMA to U) • Total hydrocarbon concentration measured by EPA Method 25A. bStyrene concentration measured by EPA Method 18. 'Methane concentration measured by EPA Method 18. d Ethane concentration measured by EPA Method 18. ------- The open condition involved the removal of panels and enclosures covering the wet application area of the line. The top panels and hinged access panels were removed or opened where possible. The Main Exhaust duct was disconnected so there was no air being pulled directly from the table area. The Main Exhaust pickup lines were all closed (knife dampers closed) and the pickup lines disconnected and taped off. The Main Exhaust fan continued to draw fugitive emissions from above the table area. Thejorjen condition was to simulate uncontrolled emissions from the table area. The Auxiliary Exhaust was operated during the open condition so that pressure negativity could be maintained in the room. The sampling areas consisted of the Main Exhaust, Room Exhaust, Auxiliary Exhaust, three NDOs, and Ovens 9 and 10 exhaust stacks. The closed condition was the operation of the line with everything covered and panels in place on the process line. The Main Exhaust line was disconnected so there was no air flow being pulled directly from the table area. The Main Exhaust pickup lines were all closed (knife dampers closed), and the pickup lines disconnected and taped off. Additional rigid panels were placed on any open areas on the top and sides of the table area. The rigid panels were taped closed where possible. Areas where rigid panels could not be used were covered with foil-faced foam insulation board and taped shut. The table area was estimated to be 98% covered. The Auxiliary Exhaust was operated during the closed condition so that pressure negativity could be maintained in the room. The sampling areas consisted of the Main Exhaust, Room Exhaust, three NDOs, and Ovens 9 and 10 exhaust stacks. During all process conditions (current, open, and closed), the production room was treated as a TTE. All air THC concentrations entering the room enclosure and exiting the room enclosure were measured continuously by EPA Method 25A. A more detailed description of the process conditions is presented in Section 3, Process Description. 2.2 PROCESS LINE RESULTS The room containing the process line was treated as a TTE. The TTE enabled sampling all HAP concentrations entering and leaving the enclosure for the purpose of determining total HAPs emitted from the process line. The TTE is described in detail at the end of this section. The emission points sampled were the following: main exhaust, room exhaust, auxiliary exhaust, and NDOs A, B, C and D. Sampling at the emission points was conducted using EPA Methods 1-4,18 and 25A to determine stack gas velocity, temperature, molecular weight, moisture content, styrene/MMA/cumene concentrations and THC concentrations. Typically, three 60-minute sample runs were conducted for each process condition sampled. Sample run times were modified dependent on process material production rates. 2-4 ------- 2.3 TOTAL TEMPORARY ENCLOSURE - METHOD 25A TOTAL HYDROCARBON RESULTS Table 2.2 presents the THC mass emission rate summary for data collected at the TTE locations. The THC mass rate data represents emissions collected using EPA Method 25 A. The THC mass rate data was calculated using styrene response factors to adjust all data to a styrene basis. The calculated overall THC mass emission rate from the TTE exhaust was determined by adding the THC mass emission rates from the Main Exhaust, Room Exhaust and Auxiliary Exhaust, and subtracting the THC mass emission rates from NDOs A, B, C and D. Conditions 1 and 2 showed the highest THC mass emission rates which represented a "current" condition with the gel coat line in operation. The gel coat line was expected to increase THC mass emission rates. The lowest THC mass emission rates were measured during Condition 13 which was the "closed" condition. Concentrations and mass emission rates were consistent during each sample condition. 2.4 TOTAL TEMPORARY ENCLOSURE - VOLUMETRIC AIR FLOW RATE RESULTS Tables 2.3 through 2.15 present volumetric flow rate data and THC concentration and mass emission rate data collected at the TTE sites. Each table of results represents a sample condition, 13 total conditions were sampled. The sampling sites consisted of the main exhaust, room exhaust, auxiliary exhaust and NDOs A, B, C and D. One volumetric flow rate was performed for each sample run at each location. Flow conditions were very consistent over the sample program. 2.5 TOTAL TEMPORARY ENCLOSURE - METHOD 18 RESULTS Table 2.16 presents the Method 18 results measured at the TTE sample locations. One sample run for styrene, cumene, and MMA was performed for each sample condition (or 1 run per 3 Method 25 A sample runs). The Method 18 data was collected as support for the THC results and as an indicator of the amount of styrene and cumene present at each sample location. The measurement of MMA was not part of the original test plan but was added while onsite. Initial estimates of the HAPs present was that the MMA would account for less than 0.2% of the total HAP content from the process line and was not a compound of concern. While onsite, it was discovered that MMA may account for higher percentages of the HAP content depending on type of product produced. At this point it was decided to measure MMA along with the styrene and cumene HAPs being measured. It should be noted that recovery efficiencies for the MMA were consistently at 70% (70 -130% were the acceptable ranges). The Method 18 laboratory results were adjusted for recovery efficiencies. 2-5 ------- TABLE 2.2 TTE TOTAL HYDROCARBON MASS EMISSION RATE SUMMARY" LASCO Panel Products Condition No. 1 1 1 Run No. 1 2 3 Average 2 2 2 1 2. 3 Average 3 3 3 1 2 3 Average 4 4 4 1 2 3 Average 5 5 5 1 2 3 Average 6 6 6 1 2 3 Average NDO Total, Ib/hr* 0.38 0.34 0.34 0.35 0.64 0.66 0.69 0.66 0.65 0.64 0.64 0.64 0.80 0.80 NA 0.80 0.18 0.18 0.18 0.18 0.20 0.20 0.20 0.20 Main Exhaust, Ib/hi* 70.44 59.32 56.62 62.13 56.92 55.50 55.34 55.92 18.22 17.59 16.74 17.52 18.34 18.37 NA 18.35 11.24 10.00 9.70 10.31 21.40 21.20 21.59 21.40 Room Exhaust, Ib/hr" 13.11 11.13 11.47 11.91 10.51 15.11 14.85 13.49 3.88 4.50 4.42 4.27 3.69 4.04 NA 3.87 3.53 3.98 4.02 3.85 5.42 5.03 3.94 4.80 Auxiliary Exhaust, Ib/hr" NA NA NA NA NA NA NA NA NA NA NA NA NA NA NA 5.02 4.70 4.79 4.84 NA NA NA NA NA Total Overall Enclosure Exhaust, lb/hrd 83.17 70.11 67.75 73.68 66.79 69.95 69.50 68.75 21.45 21.45 20.52 21.14 21.23 21.61 NA 21.42 19.61 18.51 18.32 18.81 26.62 26.03 25.33 25.99 2-6 ------- TABLE 2.2 (Concluded) Condition No. 7 7 7 Run No. 1 2 3 Average 8 8 8 1 2 3 Average 9 10 11 11 11 1 1 1 2 3 Average 12 12 12 1 2 3 Average 13 13 13 1 2 3 Average NDO Total, Ib/hr" 0.14 0.14 0.14 0.14 0.47 0.47 0.46 0.47 0.18 0.21 0.28 0.27 0.28 0.28 0.88 0.88 0.85 0.87 0.77 0.76 0.77 0.77 Main Exhaust, Ib/hi* 18.12 21.69 22.20 20.67 15.98 16.08 17.18 16.41 15.53 15.28 14.11 14.35 14.13 14.20 8.96 7.42 7.05 7.81 4.59 4.34 4.42 4:45 Room Exhaust, Ib/hi* 3.28 3.63 3.38. 3.43 6.65 6.44 5.01 6.04 2.61 2.12 3.81 3.03 2.99 3.28 4.86 4.32 3.97 4.38 3.16 3.25 3.34 3.25 Auxiliary Exhaust, Ib/hr" NA NA NA NA NA NA NA NA NA NA NA NA NA NA 6.05 4.89 4.71 5.22 4.11 3.89 4.11 4.04 Total Overall Enclosure Exhaust, Ib/hr4 21.26 25.18 25.44 23.96 22.17 22.06 21.73 21.99 17.96 17.19 17.64 17.11 16.84 17.20 18.98 15.75 14.88 16.54 11.08 10.72 11.11 10.97 a Oven emissions are not included in this table. b Pound per hour, total of four natural draft openings as styrene equivalent. c Pound per hour, as styrene equivalent. d Pound per hour, Enclosure exhaust adjusted for NDO contribution as styrene equivalent. 2-7 ------- TABLE 2.3 SUMMARY OF TTE STACK GAS CONDITIONS, AND THC CONCENTRATIONS AND MASS EMISSION RATES CONDITION 1 - MAY 14,1997 LASCO Panel Products to 00 Run No. Time Stack Gas Velocity, fps> Volumetric Flow Rate acfmb dscfm" Temperature, op Moisture, % THC Concentration ppm, wef1 ppm .dry" ppm, as styrenef Mass Rate, Ib/hr" Main Exhaust 1 2 3 1034-1134 1225-1325 1546-1646 Average 37.22 33.83 31.62 34.22 3729 3390 3168 3429 3378 3030 2804 3071 92 91 93 92 1.6 3.5 4.1 3.1 2965.4 2730.4 2798.6 2831.5 3013.6 2829.4 2918.2 2921.0 1284.7 1206.2 1244.0 1245.0 70.44 59.32 56.62 62.13 Room Exhaust 1 2 3 1034-1134 1225-1325 1546-1646 Average Run No. 1 2 3 Average 18.86 17.28 17.82 17.99 5281 4838 4993 5037 NDO-A(-) Velocity, fpm" 275 235 230 247 Flow Rate, cfm1 7334 6267 6134 6578 Cone, ppm wetd 6.1 5.0 6.9 6.0 4886 4483 4644 4671 78 81 79 79 1.9 1.6 1.6 1.7 NDO-B (-) Velocity, fpmh 550 600 600 583 Flow Rate, cfin' 138 150 150 146 Cone, ppm wef1 NA 6.0 6.0 6.0 380.5 353.2 351.3 361.7 387.9 358.9 357.0 367.9 165.3 153.0 152.2 156.9 NDO-C (+) Forced Makeup Air Velocity, fpmh 263 230 240 244 Flow Rate, cfm1 665 582 607 618 Cone, ppm wef1 15.9 NA 3.0 9.5 13.11 11.13 11.47 11.91 NDO-D (+) Forced Makeup Air Velocity, Flow Rate, fpmh cfm1 210 531 200 506 200 506 203 514 Cone, ppm wef1 15.9 NA 3.0 9.5 1 Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. e Part per million, dry basis as propane equivalent. ' Part per million as styrene equivalent based on styrene response factor. B Pound per hour. k Feet per minute. 1 Cubic feet per minute. ------- TABLE 2.4 to SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS CONDITION 2 - MAY 14,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps" Volumetric Flow Rate acfmb dscfrtf Temperature, op Moisture, THC Concentration ppm, wet* ppm, dry* ppm, as styrenef Mass Rate, Ib/hr8 Main Exhaust 1 2 3 2020-2125 2155-2255 2337-0038 Average 34.87 33.70 36.20 34.92 3494 3377 3628 3500 3173 3105 3333 3204 92 89 89 90 1.5 0.8 0.9 1.1 2553.6 2562.8 2378.0 2498.1 2592.5 2583.5 2399.6 2525.1 1105.2 1101.3 1022.9 1076.5 56. 55. 55. 92 50 34 55.92 Room Exhaust 1 2 3 2020-2125 2155-2255 2337-0038 Average Run No. 1 2 3 Average 17.86 19.16 19.45 18.82 5001 5369 5450 5273 NDO-A (-) Velocity, fpmh 225 235 225 228 Flow Rate, cfiri 6000 6267 6000 6089 Cone, ppm wef1 5.7 4.5 30.1 13.4 4637 4983 5062 4894 82 82 81 82 1.1 1.0 1.1 1.1 NDO-B (-) Velocity, fpm" 450 350 550 450 Flow Rate, cfm1 113 88 138 113 Cone, ppm wef1 NA NA 4.4 4.4 324.1 433.9 419.4 392.5 327.7 438.3 424.1 396.7 139.7 186.8 180.8 169.1 NDO-C (+) Forced Makeup Air Velocity, fpmh 265 260 260 262 Flow Rate, cfiri 670 658 658 662 Cone, ppm wetd 1.6 2.9 5.4 3.3 10. 15. 14. 51 11 85 13.49 NDO-D (+) Forced Makeup Air „ . .. Flow Velocity, _ . fpm" Rf? v cfm1 200 506 210 531 260 658 223 565 Cone, ppm wetd 1.6 2.9 5.4 3.3 • Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. * Part per million, dry basis as propane equivalent. f Part per million as styrene equivalent based on styrene response factor. 8 Pound per hour. h Feet per minute. 1 Cubic feet per minute. ------- TABLE 2.5 SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS CONDITION 3 - MAY 15,1997 LASCO Panel Products (0 o Run No. Time Stack Gas Velocity, fps8 Volumetric Flow Rate acfmb dscflnc Temperature, op Moisture, % THC Concentration ppm, wef1 ppm, dry" ppm, as styrene' Mass Rate, Ib/hr* Room Exhaust 1 2 3 1425-1525 1559-1659 1735-1836 Average 37.65 36.41 36.36 36.81 3772 3648 3643 3688 3526 3414 3424 3455 80 80 80 80 1.0 0.9 1.1 1.0 739.2 738.1 698.6 725.3 746.7 744.8 706.4 732.6 318.3 317.5 301.1 312.3 18.22 17.59 16.74 17.52 Room Exhaust 1 2 3 1425-1525 1559-1659 1735-1836 Average Run No. 1 2 3 Average 18.76 18.60 18.71 18.69 5255 5213 5241 5236 NDO-A (-) Velocity, Flow Rate, fpmh cfm' 225 6000 240 6400 230 6134 232 6178 Cone, ppm wef1 12.0 15.1 11.3. 12.8 4961 4950 4974 4962 75 75 76 75 0.8 0.9 0.8 0.8 NDO-B (-) Velocity, fpmh 650 650 650 650 Flow Rate, cfiri 163 163 163 163 Cone, ppm wef1 12.3 1.8 8.3 7.5 112.2 130.1 127.5 123.3 113.1 131.3 128.5 124.3 48.2 56.0 54.8 53.0 NDO-C (+) Forced Makeup Air Velocity, Flow Rate, Cone, fpmh cfin1 ppm wef1 245 620 0.6 240 607 1.8 240 607 2.8 242 611 1.7 3.88 4.50 4.42 4.27 NDO-D (+) Forced Makeup Air Velocity, fprn" 260 250 260 257 Flow Rate, cfnY 658 633 658 650 Cone, ppm wef1 0.6 1.8 2.8 1.7 * Feet per second. k Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. c Part per million, dry basis as propane equivalent f Part per million as styrene equivalent based on styrene response factor. ' Pound per hour. h Feet per minute. ' Cubic feet per minute. ------- TABLE 2.6 10 SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS CONDITION 4 - MAY 15,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps° Volumetric Flow Rate acfmb dscfm0 Temperature, op Moisture, % THC Concentration ppm, wef;1 ppm, dry" ppm, as styrenef Mass Rate, lb/hi* Main Exhaust 1 2 3 2005-2105 2130-2230 NA Average 40.44 40.23 NA 40.34 4053 4032 NA 4043 3846 3823 NA 3835 78 78 NA 78 0.9 1.0 NA 1.0 682.8 687.6 NA 685.2 689.0 694.5 NA 691.8 293.7 296.1 NA 294.9 18.34 18.37 NA 18.35 Room Exhaust 1 2 3 2005-2105 2130-2230 NA Average Run No. 1 2 3 Average 18.15 18.32 NA 18.24 5083 5129 NA 5106 NDO-A (-) Velocity, fprn" 250 275 NA 263 Flow Rate, cfrri 6668 7334 NA 7000 Cone, ppm wef1 12.8 18.3 NA 15.6 4846 4886 NA 4866 75 75 NA 75 0.9 0.9 NA 0.9 NDO-B (-) Velocity, fpmh 700 700 NA 700 Flow Rate, cfhv 175 175 NA 175 Cone, ppm wef1 1.6 NA NA 1.6 109.2 118.4 NA 113.8 110.2 119.5 NA 114.8. NDO-C (+) Forced Makeup Air Velocity, Flow Rate, Conc> w cw 55 250 633 1.7 300 759 1.6 NA NA NA 275 696 1.7 47.0 50.9 NA 49.0 3.69 4.04 NA 3.87 NDO-D (+) Forced Makeup Air Velocity, fpm" 275 275 NA 275 ~ 5 696 1.7 696 1.6 NA NA 696 1.7 1 Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. c Part per million, dry basis as propane equivalent f Part per million as styrene equivalent based on styrene response factor. g Pound per hour. h Feet per minute. ' Cubic feet per minute. ------- TABLE 2.7 SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS CONDITION 5 - MAY 19,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps' Volumetric Flow Rate acfinb dscfmc Temperature, °F Moisture, % THC Concentration ppm, wet;1 ppm, dry" ppm, as styrener Mass Rate, Ib/hr8 Main Exhaust 1 2 3 0903-1027 1106-1231 1357-1521 Average 36.59 36.55 36.94 36.69 3667 3663 3701 3677 3345 3314 3308 3322 87 90 92 90 2.0 2.1 2.4 2.2 476.0 426.9 413.5 438.8 485.7 436.1 423.7 448.5 207.1 185.9 180.6 191.2 11.24 10.00 9.70 10.31 Room Exhaust 1 2 3 0903-1027 1106-1231 1357-1521 Average 17.06 17.28 18.21 17.52 4777 4842 5099 4906 4402 4297 4619 4439 80 83 85 83 2.1 2.3 2.2 2.2 113.5 130.9 123.1 122.5 115.9 134.0 125.9 125.3 49.4 57.1 53.7 53.4 3.53 3.98 4.02 3.85 Auxiliary Exhaust 1 2 3 0903-1027 1106-1231 1357-1521 Average Run No. 1 2 3 Average 40.84 40.14 39.28 40.09 5219 5124 5020 5121 NDO-A (-) Velocity, fpmh 325 325 325 325 Flow Rate, cfnV 8668 8668 8668 8668 Cone, ppm wet?1 1.1 4.7 1.1 2.3 4780 4677 4541 4666 Velocity, fpmh 500 400 500 467 83 84 86 84 2.1 2.1 2.1 2.1 148.7 142.3 149.1 146.7 151.9 145.4 152.3 149.8 NDO-B (-) NDO-C (+) Forced Makeup Air Flow Rate, cfhV 125 100 125 117 Conc' Velocity, Flow Rate, Conc' 55 mh cfini 55 0.0 300 759 0.0 0.5 275 696 0.9 3.3 275 696 0.8 1.3 283 717 0.6 64.8 62.0 64.9 63.9 5.02 4.70 4.79 4.84 NDO-D (+) Forced Makeup Air Velocity, fpmh 350 250 250 283 Flow Rate, Conc' 55 886 0.0 633 0.9 633 0.8 717 0.6 " Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. c Part per million, dry basis as propane equivalent. f Part per million as styrene equivalent based on styrene response factor. 8 Pound per hour. h Feet per minute. 1 Cubic feet per minute. ------- TABLE 2.8 SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS CONDITION 6 - MAY 19,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps° Volumetric Flow Rate acfmb dscfinc Temperature, op Moisture, % THC Concentration ppm, wef1 ppm, dry ppm, as styrenef Mass Rate, Ib/hi* Main Exhaust 1 2 3 1605-1706 1734-1855 1936-2018 Average 38.68 38.09 38.07 38.28 3876 3817 3815 3836 3513 3449 3488 3483 88 89 86 88 2.2 2.3 1.9 2.1 861.0 868.0 877.6 868.9 880.4 888.4 894.6 887.8 375.3 378.7 381.4 378.5 21.40 21.20 21.59 21.40 Room Exhaust 1 2 3 1605-1706 1734-1855 1936-2018 Average Run No. 1 2 3 Average 18.23 19.03 19.06 18.77 5107 5331 5341 5260 NDO-A (-) Velocity, fpmh 300 250 275 275 Flow Rate, cfrrf 8001 6668 7334 7334 Cone, ppm wef1 3.9 3.8 2.4 3.4 4663 4868 4920 4817 83 83 81 82 NDO-B (-) Velocity, fpmh 250 250 200 233 Flow Rate, cfm' 62.5 62.5 50 58 Cone, ppm wef1 3.0 9.7 29.6 14.1 2.2 2.2 1.9 2.1 164.2 146.0 113.6 141.3 167.9 149.3 115.8 144.3 NDO-C (+) Forced Makeup Air Velocity, Flow Rate, Conc' ** - 5 250 633 2.7 250 633 5.6 250 633 1.9 250 633 3.4 71.6 63.6 49.4 61.5 5.42 5.03 3.94 4.80 NDO-D (+) Forced Makeup Air Velocity, fpmh 250 250 350 283 Flow Rate, cfm' 633 633 886 717 Conc, ppm wef1 2.7 5.6 1.9 3.4 to u> a Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent ' Part per million, dry basis as propane equivalent. f Part per million as styrene equivalent based on styrene response factor. 8 Pound per hour. h Feet per minute. 1 Cubic feet per minute. ------- TABLE 2.9 SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS CONDITION 7 - MAY 20,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps" Volumetric Flow Rate acfinb dscfm" Temperature, op Moisture, % THC Concentration ppm, wet?1 ppm, dry" ppm, as styrenef Mass Rate, Ib/hr8 Main Exhaust 1 2 3 1449-1613 1705-1828 1913-2036 Average 38.82 38.73 38.86 38.59 3891 3881 3893 3866 3585 3593 3608 3575 84 83 83 83 1.8 1.5 1.4 1.6 717.5 859.4 876.6 817.9 730.7 872.5 889.0 830.8 311.5 371.9 379.0 354.1 18.12 21.69 22.20 20.67 Room Exhaust 1 2 3 1449-1613 1705-1828 1913-2036 Average Run No. 1 2 3 Average 18.16 18.86 18.06 18.36 5085 5291 5060 5145 NDO-A (-) Velocity, Flow Rate, fpmh cfm1 250 6668 250 6668 300 8001 267 7112 Cone, ppm wetd 3.4 2.0 1.9 2.4 4772 4979 4753 4835 77 77 77 77 1.1 0.8 1.0 1.0 NDO-B (-) Velocity, fpmh 200 200 300 233 Flow Rate, cfm1 50 50 75 58 Cone, ppm wet* 3.5 3.8 1.4 2.9 98.1 104.4 101.7 101.4 99.2 105.2 102.7 102.4 NDO-C (+) Forced Makeup Air Velocity, Flow Rate, Conc> f -' S 250 633 2.2 250 633 1.5 300 759 1.0 267 675 1.6 42.3 44.9 43.8 43.6 3.28 3.63 3.38 3.43 NDO-D (+) Forced Makeup Air Velocity, fpmh 300 300 300 300 Flow Rate, cfm' 759 759 759 759 Cone, ppm wef1 2.2 1.5 1.0 1.6 to " Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. c Part per million, dry basis as propane equivalent. Part per million as styrene equivalent based on styrene response factor. 8 Pound per hour. h Feet per minute. ' Cubic feet per minute. ------- TABLE 2.10 N> SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS CONDITION 8 - MAY 22,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, rps" Volumetric Flow Rate acfmb dscfmc Temperature, op Moisture, THC Concentration ppm, wef1 ppm, dry* ppm, as styrenef Mass Rate, Ib/hr8 Main Exhaust 1 2 3 0752-0844 091-9-1049 1139-1309 Average 38.58 38.45 38.47 38.50 3866 3853 3855 3858 3724 3679 3661 3688 74 77 80 77 1.2 1.5 1.5 1.4 612.8 622.3 667.9 634.3 620.2 631.8 678.1 643.3 264.4 269.3 289.1 274.3 15.98 16.08 17.18 16.41 Room Exhaust 1 2 3 0752-0844 0919-1049 1139-1309 Average Run No. 1 2 3 Average 18.95 19.42 18.58 18.98 5309 5441 5202 5317 NDO-A (-) Velocity, fpm" 275 300 300 292 Flow Rate, cfhV 7334 8001 8001 7779 Cone, ppm wef1 11.0 5.6 NA 8.3 5144 5272 5013 5143 71 71 74 72 1.0 1.0 1.0 1.0 NDO-B (-) Velocity, fpmh 550 400 400 450 Flow Rate, cfm' 138 100 100 113 Cone, ppm wef1 NA 2.5 NA 2.5 185.0 174.9 143.1 167.7 186.9 176.7 144.5 169.4 79.7 75.3 61.6 72.2 NDO-C (+) Forced Makeup Air Velocity, Flow Rate, Conc> ^ h f i ppm fpnr cfm1 vv * e wer 550 1392 6.2 350 886 3.0 300 759 NA 400 1012 4.6 6.65 6.44 5.01 6.04 NDQ-D (+) Forced Makeup Air Velocity, Flow Rate, fpmh cfm' 450 1139 400 1012 400 1012 417 1054 Cone, ppm wef1 6.2 3.0 NA 4.6 " Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. A Part per million, wet basis as propane equivalent * Part per million, dry basis as propane equivalent. f Part per million as styrene equivalent based on styrene response factor. g Pound per hour. h Feet per minute. ' Cubic feet per minute ------- TABLE 2.11 to SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS CONDITION 9 - MAY 22,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps1 Volumetric Flow Rate acfm" dscfmc Temperature, op Moisture, THC Concentration ppm, wef1 ppm, dry* ppm, as styrenef Mass Rate, Ib/hr* Main Exhaust 1 2 3 1802-1844 NA NA Average 38.69 NA NA 38.69 3877 NA NA 3877 3624 NA NA 3624 84 NA NA 84 1.6 NA NA 1.6 609.3 NA NA 609:3 619.2 NA NA 619.2 264.0 NA NA 264.0 15.53 NA NA 15.53 Room Exhaust 1 2 3 1802-1844 NA NA Average Run No. 1 2 3 Average 17.74 NA NA 17.74 4971 NA NA 4971 NDO-A (-) Velocity, fpmh 250 NA NA 250 Flow Rate, cfm1 6668 NA NA 6668 Cone, ppm wef1 3.2 NA NA 3.2 4728 NA NA 4728 78 NA NA 78 0.8 NA NA 0.8 NDO-B (-) Velocity, fpmh 300 NA NA 300 Flow Rate, cfm' 75 NA NA 75 Cone, ppm wef1 2.7 NA NA 2.7 79.2 NA NA 79.2 79.8 NA NA 79.8 34.0 NA NA 34.0 NDO-C (+) Forced Makeup Air Velocity, Flow Rate, Conc> fpmh cfm! ppm \VCIT 300 759 2.7 NA NA NA NA NA NA 300 759 2.7 2.61 NA NA 2.61 NDO-D (+) Forced Makeup Air Velocity, fpmh 400 NA NA 400 Flow Rate, Conc' , i ppm Cfm wef 1012 2.7 NA NA NA NA 1012 2.7 " Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. e Part per million, dry basis as propane equivalent. f Part per million as styrene equivalent based on styrene response factor. g Pound per hour. h Feet per minute. ' Cubic feet per minute. ------- TABLE 2.12 SUMMARY OF TIE STACK GAS CONDITIONS AND THC CONCENTRATIONS CONDITION 10 - MAY 22,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps" Volumetric Flow Rate acfin" dscfm" Temperature, op Moisture, % THC Concentration ppm, wetd ppm, dry" ppm, as styrenef Mass Rate, Ib/hr8 Main Exhaust 1 2 3 1959-2050 NA NA Average 38.45 NA NA 38.45 3854 NA NA 3854 3623 NA NA 3623 82 NA NA 82 1.4 NA NA 1.4 600.9 NA NA 600.9 609.4 NA NA 609.4 259.8 NA NA 259.8 15.28 NA NA 15.28 Room Exhaust 1 2 3 1959-2050 NA NA Average Run No. 1 2 3 Average 17.16 NA NA 17.16 4806 NA NA 4806 NDO-A (-) Velocity, fpmh 300 NA NA 300 Flow Rate, Conc' -_ : ppm cfm wef 8001 3.8 NA NA NA NA 8001 3.8 4597 NA NA 4597 76 NA NA 76 0.6 NA NA 0.6 NDO-B (-) Velocity, fpm" 550 NA NA 550 Flow Rate, cfnV 138 NA NA 138 Conc, ppm wef1 2.6 NA NA 2.6 66.1 NA NA 66.1 66.5 NA NA 66.5 NDO-C (+) Forced Makeup Air Velocity, Flow Rate, Conc> e h f i Ppm fpm- cfm' ^ 400 1012 2.6 NA NA NA NA NA NA 400 1012 2.6 28.3 NA NA 28.3 2.12 NA NA 2.12 NDO-D (+) Forced Makeup Air Velocity, fpmh 400 NA NA 400 Flow Rate, Conc' «* S 1012 2.6 NA NA NA NA 1012 2.6 to -J * Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent e Part per million, dry basis as propane equivalent f Part per million as styrene equivalent based on styrene response factor. 8 Pound per hour. h Feet per minute. 1 Cubic feet per minute. ------- TABLE 2.13 SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS CONDITION 11 - MAY 23,1997 LASCO Panel Products to 00 Run No. Time Stack Gas Velocity, fpf Volumetric Flow Rate acfmb dscfinc Temperature, op Moisture, % THC Concentration ppm, wef1 ppm, dry0 ppm,asstyrenef Mass Rate, Ib/hr8 Main Exhaust 1 2 3 0912-1015 1040-1121 1200-1242 Average 38.36 38.42 38.06 38.28 3844 3849 3813 3835 3672 3652 3581 3635 77 79 81 79 1.4 1.7 1.6 1.6 547.5 558.3 561.2 555.7 555.3 568.0 570.3 564.5 236.7 242.1 243.1 240.7 14.11 14.35 14.13 14.20 Room Exhaust 1 2 3 0912-1015 1040-1121 1200-1242 Average Run No. 1 2 3 Average 17.32 16.87 18.24 17.48 4850 4727 5107 4895 NDO-A (-) Velocity, fpm" 300 300 200 267 Flow Rate, cfirf 8001 8001 5334 7112 Cone, ppm wetd 8.0 5.0 3.9 5.6 4694 4557 4863 4705 72 74 77 74 0.9 0.9 0.8 0.9 NDO-B (-) Velocity, fpmh 525 525 525 525 Flow Rate, cfnV 131 131 131 131 Cone, ppm wef1 1.5 0.9 3.1 1.8 116.3 95.2 88.2 99.9 117.4 96.1 88.9 100.8 NDO-C (+) Forced Makeup Air Velocity, fpmh 400 . 400 400 400 Flow Rate, cfin' 1012 1012 1012 1012 Cone, ppm wef1 3.3 1.0 0.8 1.7 50.0 41.0 37.9 43.0 3.81 3.03 2.99 3.28 NDO-D (+) Forced Makeup Air Velocity, fpmh 400 400 400 400 Flow Rate, cfnV 1012 1012 1012 1012 Cone, ppm wef1 3.3 1.0 0.8 1.7 * Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. " Part per million, dry basis as propane equivalent. f Part per million as styrene equivalent based on styrene response factor 8 Pound per hour. h Feet per minute. 1 Cubic feet per minute. ------- 2.11 SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS CONDITION 12 - MAY 29,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps> Volumetric Flow Rate acfm" dscfmc Temperature, op Moisture, % THC Concentration ppm, wef1 ppm, dry" ppm, as styrenef Mass Rate, Ib/hr8 Main Exhaust 1 3 4 0835-0935 1104-1202 1230-1330 Average 36.60 35.63 35.24 35.82 3667 3571 3531 3590 3459 3364 3305 3376 79 80 82 80 1.7 1.6 1.9 1.7 368.0 313.5 304.9 328.8 374.4 318.6 308.3 333.7 159.6 135.8 131.4 142.3 8.96 7.42 7.05 7.81 Room Exhaust 1 3 4 0835-0935 1104-1202 1230-1330 Average 17.05 17.30 16.37 16.91 4774 4846 4587 4736 4541 4610 4350 4500 74 74 75 74 1.6 1.6 1.7 1.6 152.1 133.2 129.6 138.3 154.6 135.4 131.8 140.6 65.9 57.7 56.2 59.9 4.86 4.32 3.97 4.38 Auxiliary Exhaust 1 3 4 0835-0935 1104-1202 1230-1330 . Average Run No. 1 3 4 Average Velocity, fpmh 450 450 450 450 38.53 38.91 37.56 38.33 NDO-A (-) Flow Rate, cfhV 12,002 12,002 12,002 12,002 4924 4967 4800 4897 Cone, ppm wet1 10.8 12.0 11.2 11.3 4694 4731 4547 4657 Velocity, fpmh 1000 950 850 933 72 73 76 74 NDO-B (-) Flow Rate, cfiri 250 238 213 234 1.7 1.6 1.6 1.6 183.0 147.1 147.4 159.2 186.2 149.5 149.8 161.8 NDO-C (+) Forced Makeup Air Cone, Velocity, Flow Rate, ppm wet? fpmh cfrn' 1.4 250 633 0.2 300 759 0.2 300 759 0.6 283 717 Cone, ppm wet1 1.5 0.3 0.4 0.7 79.4 63.7 63.9 69.0 6.05 4.89 4.71 5.22 NDO-D (+) Forced Makeup Air Velocity, rpmh 350 450 400 400 Flow Rate, cfm1 886 1139 1012 1012 Cone, ppm wetd 1.5 0.3 0.4 0.7 * Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. e Part per million, dry basis as propane equivalent f Part per million as styrene equivalent based on styrene response factor 8 Pound per hour. h Feet per minute. ' Cubic feet per minute. ------- TABLE 2.15 SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS CONDITION 13 - MAY 29,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps- Volumetric Flow Rate acfmb dscfmc Temperature, op Moisture, % THC Concentration ppm, wetd ppm, dry" ppm, as styrenef Mass lb/ Rate, hi* Main Exhaust 1 2 3 1518-1614 1637-1737 1801-1901 Average 35.46 35.77 35.56 35.60 3553 3585 3565 3568 3362 3358 3325 3348 77 81 82 80 1.4 1.7 1.9 1.7 194.4 183.8 188.5 188.9 197.2 187.0 192.2 192.1 84.0 79.7 81.9 81.9 4.59 4.34 4.42 4.45 Room Exhaust 1 2 3 1518-1614 1637-1737 1801-1901 Average 16.89 16.68 16.82 16.80 4729 4671 4708 4703 4465 4412 4447 4441 75 75 76 75 1.8 1.8 1.6 1.7 100.3 104.5 106.9 103.9 102.1 106.4 108.6 105.7 43.5 45.4 46.3 45.1 3.16 3.25 3.34 3.25 Auxiliary Exhaust 1 2 3 1518-1614 1637-1737 1801-1901 Average 37.58 37.14 37.59 37.44 NDO-A (-) Run No. velocity, Flow Rate, fpmh cfhV 1 450 12,002 2 450 12,002 3 450 12,002 Average 450 12,002 4797 4741 4799 4779 Cone, ppm wet* 11.7 10.1 8.4 10.1 4536 4471 4529 4512 Velocity, fpmh 950 950 950 950 75 76 76 76 1.6 1.7 1.7 1.7 128.8 123.6 129.0 127.1 130.9 125.7 131.2 129.3 NDO-B (-) NDO-C (+) Forced Makeup Air Flow Rate, Cone, Velocity, Flow Rate, cfhV ppm wef1 fpmh cfm1 238 4.2 300 759 238 1.5 400 1012 238 3.1 400 1012 238 2.9 367 928 Cone, ppm wef1 1.8 1.9 1.8 1.8 55.8 53.6 55.9 55.1 4.11 3.89 4.11 4.04 NDO-D (+) Forced Makeup Air Velocity, fpmh 400 400 400 400 Flow Rate, cfm' 1012 1012 1012 1012 Cone, ppm wef1 1.8 1.9 1.8 1.8 to to o "Feet per second. bActual cubic feet per minute. T)ry standard cubic feet per minute. dPart per million, wet basis as propane equivalent. Tart per million, dry basis as propane equivalent. Tart per million as styrene equivalent based on styrene response factor. Pound per hour. hFeet per minute. 'Cubic feet per minute. ------- TABLE 2.16 (Concluded) Condition No. 7 7 7 Run No. 1 2 3 Average 8 8 8 1 2 3 Average 9 10 11 11 11 1 1 1 2 3 Average 12 12 12 1 2 3 Average 13 13 13 1 2 3 Average NDO" Total, Ib/hi ND ND - ND ND - ND ND ND - - ND ND - 0.36 - - 0.36 Main Exhaust, Ib/hr* 11.25 - 14.33 12.79 10.11 - - 10.11 10.47 VOID 7.97 7.36 - 7.67 5.29 - 4.87 5.08 - 2.80 - 2.80 Room Exhaust, Ib/hi* 1.20 - - 1.20 3.39 - - 3.39 2.08 0.44 1.4J - 0.71 1.09 - - - - 1.781 - - 1.81 Auxiliary Exhaust, Ib/hi* NA NA NA NA NA NA NA NA NA NA NA NA NA NA 4.03 - 3.19 3.61 2.43 - - 2.43 Total Overall Enclosure Exhaust, Ib/hr" 13.99 13.50 12.15 0.44f 8.76 8.69 7.04 • Note: NDO-Aflowrates and concentrations were used to calculate mass rates. b Ib/hr = Pound per hour, total pounds of styrene and MMA measured. 0 ND = Detection limit of analytical instrument. d - = Sample not collected in this test condition. * NA = Not applicable - auxiliary fan not in operation. f Result is not valid due to a voided main exhaust sample. 2-22 ------- The Method 18 analysis showed MMA, styrene and cumene at detection limit (± 1 ppm) values for most of the runs conducted at the NDO sites. If compounds were detected, the TTE results were adjusted based on HAP content at the NDO sites. 2.6 OVEN NOS. 9 AND 10 - METHOD 25A TOTAL HYDROCARBON RESULTS Table 2.17 presents the THC mass emission rate summary for the Oven Nos. 9 and 10 locations. The THC mass emission rate data represents emissions collected using EPA Method 25A and corrected for methane and ethane mass emission rates measured by Method 18. The methane and ethane concentrations were a result of inefficient natural gas dryers; these concentrations were measured and subtracted from the Method 25A total. The final THC mass emission rate data was calculated using styrene response factors to adjust all data to a styrene basis. The oven sampling program was performed simultaneously with the TTE sampling. 2.7 OVEN NOS. 9 AND 10 - VOLUMETRIC FLOW RATE RESULTS Tables 2.18 through 2.30 present flow rate data and THC concentration data collected at the Oven Nos. 9 and 10 sample sites. Each table of results represents a sample condition, 13 total conditions. One volumetric flow rate was performed for each sample run at each location. Flow conditions were very consistent during the sample program. 2.8 OVEN NOS. 9 AND 10 - METHOD 18 HAP RESULTS Table 2.31 presents the Method 18 results measured at the Oven Nos. 9 and 10 sample locations. One sample run for styrene, cumene and MMA was performed for each sample condition. As mentioned in Section 2.5, the Method 18 data was collected as support for the THC results and as an indicator of the amount of styrene, cumene and MMA present at each sample location. The Method 18 results were adjusted for recovery efficiencies. 2.9 UNCATALYZED RESIN (UCR) AND GEL COAT SAMPLE RESULTS Process samples of the UCR and gel coat (gel coat was only used during Conditions 1 and 2) were collected at the beginning and end of each sample run. The process samples were analyzed by EPA Method 24 to determine volatile matter content, water content, density and weight of solids. Analysis was also performed to determine HAP content. Results of the analysis are contained in the ESD Test Report. 2-23 ------- TABLE 2.17 OVENS 9 AND 10 THC MASS EMISSION RATE SUMMARY LASCO Panel Products Condition No. 1 1 1 Run No. 1 2 3 Average 2 2 2 1 2 3 Average 3 3 3 1 2 3 Average 4 4 4 1 2 3 Average 5 5 5 1 2 3 Average 6 6 6 1 2 3 Average Oven No. 9 Exhaust, Ib/hr" 0.27 0.31 0.28 0.28 0.00 0.00 0.22 0.07 0.43 0.29 0.29 0.34 0.26 0.33 NA 0.29 0.40 0.72 0.60 0.57 1.11 0.85 0.95 0.97 Oven No. 10 Exhaust, Ib/hr" 0.18 0.12 0.11 0.14 0.18 0.07 0.05 0.10 2.24 2.21 2.45 2.30 2.80 2.66 NA 2.73 1.46 1.35 1.43 1.41 1.26 1.54 1.46 1.42 Total Oven Exhaust, Ib/hr" 0.45 0.43 0.39 0.42 0.18 0.07 0.27 0.17 2.67 2.50 2.74 2.64 3.06 2.99 NA 3.02 1.86 2.07 2.03 1.98 2.37 2.39 2.41 2.39 2-24 ------- TABLE 2.17 (Concluded) Condition No. 7 7 7 Run No. 1 2 3 Average 8 8 8 1 2 3 Average 9 10 11 11 11 1 1 1 2 3 Average 12 12 12 1 2 3 Average 13 13 13 1 2 3 Average Oven No. 9 Exhaust, lb/hi* 0.53 0.68 0.61 0.61 0.00 0.23 0.12 0.12 0.32 0.58 0.03 0.20 0.17 0.13 0.75 0.78 0.55 0.69 0.74 0.69 0.96 0.80 Oven No. 10 Exhaust, Ib/hi* 1.81 1.96 1.89 1.89 0.55 0.56 1.10 0.74 2.68 2.16 3.18 3.39 3.23 3.27 2.95 3.40 3.39 3.25 3.94 4.11 4.09 4.05 Total Oven Exhaust, Ib/hr" 2.34 2.64 2.50 2.50 0.55 0.79 1.22 0.86 3.00 2.74 3.21 3.59 3.40 3.40 3.70 4.18 3.94 3.94 4.68 4.80 5.05 4.85 " Pound per hour, as styrene equivalent, excluding methane and ethane. 2-25 ------- TABLE 2.18 SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS AND MASS EMISSION RATES, CONDITION 1 - MAY 14,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps* Volumetric Flow Rate acfmb dscfm0 Temperature, op Moisture, % THC Concentration ppm, wetd Adjusted ppm, wetf ppm, dr/ ppm, as styrene5 Mass Rate, Ib/hr" Oven 9 1 2 3 1034-1134 1225-1325 1546-1646 Average 32.44 32.80 33.18 32.81 2394 2420 2449 2421 1907 1924 1927 1919 169 169 173 170 1.8 1.8 1.8 1.8 118.7 132.3 128.2 126.4 19.7 22.7 20.5 21.0 20.1 23.2 20.9 21.4 8.6 9.9 8.9 9.1 0.27 0.31 0.28 0.28 Oven 10 1 2 3 1034-1134 1225-1325 1546-1646 Average 34.25 34.83 34.98 34.69 2522 2564 2575 2554 1836 1893 1878 1869 218 214 222 218 2.7 2.3 1.9 2.3 43.5 41.7 39.5 41.6 13.7 9.1 8.4 10.4 14.1 9.3 8.6 10.7 6.0 4.0 3.7 4.5 Ovens 9 and 1 0 Total Mass Rate, Ib/hi* 0.18 0.12 0.11 0.14 0.42 to to "Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. e Part per million, wet basis adjusted for NDO contributions. f Part per million, dry basis. 8 Part per million as styrene equivalent based on styrene response factor. h Pound per hour. ------- TABLE 2.19 SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS AND MASS EMISSION RATES, CONDITION 2 - MAY 14,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps" Volumetric Flow Rate acfmb dscfinc Temperature, op Moisture, % THC Concentration ppm, wetd Adjusted ppm, wef ppm, dr/ ppm, as styrene8 Mass Rate, Ib/hr11 Oven 9 1 2 3 2020-2125 2155-2255 2337-0038 Average 32.52 31.62 33.15 32.43 2394 2328 2446 2389 1905 1870 1964 1913 172 165 165 167 1.3 1.2 1.1 1.2 50.4 71.9 108.0 76.8 0.0 0.0 15.7 5.2 0.0 0.0 15.8 5.3 0.0 0.0 6.8 2.3 0.00 0.00 0.22 0.07 Oven 10 1 2 3 2020-2125 '2155-2255 2337-0038 Average 33.66 32.67 33.25 33.19 2478 2405 2454 2446 1825 1769 1807 1800 219 220 219 219 1.4 1.4 1.4 1.4 43.5 38.1 34.6 38.7 14.4 5.8 4.1 8.1 14.6 5.9 4.2 8.2 6.2 2.5 1.8 3.5 Ovens 9 and 10 Total Mass Rate, Ib/hi* 0.18 0.07 0.05 0.10 0.17 to to -J " Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. e Part per million, wet basis adjusted for.NDO contributions. f Part per million, dry basis. 8 Part per million as styrene equivalent based on styrene response factor. h Pound per hour. ------- TABLE 2.20 SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS AND MASS EMISSION RATES, CONDITION 3 - MAY 15,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps1 Volumetric Flow Rate acfmb dscfmc Temperature, Of Moisture, % THC Concentration ppm, wetd Adjusted ppm, wet" ppm, dr/ ppm, as styrene8 Mass Rate, Ib/hr* Oven 9 1 2 3 1425-1525 1559-1659 1735-1836 Average 31.24 31.82 31.96 31.67 2306 2348 2359 2338 1855 1886 1894 1878 167 167 167 167 1.1 1.1 1.1 1.1 87.9 118.9 106.4 104.4 33.5 22.3 22.2 26.0 33.8 22.6 22.4 26.3 14.4 9.6 9.6 11.2 0.43 0.29 0.29 0.34 Oven 10 1 2 3 1425-1525 1559-1659 1735-1836 Average 35.43 34.49 34.71 34.88 2615 2545 2561 2574 1910 1852 1871 1878 229 232 229 230 1.1 1.1 1.1 1.1 185.7 189.1 204.7 193.2 167.3 170.9 186.8 175.0 169.1 172.8 188.9 176.9 72.1 73.7 80.5 75.4 Ovens 9 and 10 Total Mass Rate, Ib/hi* 2.24 2.21 2.45 2.30 2.64 to to oo 0 Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. c Part per million, wet basis adjusted forNDO contributions. f Part per million, dry basis. 8 Part per million as styrene equivalent based on styrene response factor. h Pound per hour. ------- TABLE 2.21 SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS AND MASS EMISSION RATES, CONDITION 4 - MAY 15,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps* Volumetric Flow Rate acfmb dscfrrf Temperature, Of Moisture, % THC Concentration ppm, wetd Adjusted ppm, wet" ppm, dr/ ppm, as styrene8 Mass Rate, lb/hi* Oven 9 1 2 3 2005-2105 2130-2230 NA Average 31.85 32.22 NA 32.03 2345 2372 NA 2359 1890 1917 NA 1904 164 163 NA 164 1.2 1.2 NA 1.2 110.1 113.4 NA 111.8 19.5 24.3 NA 21.9 19.7 24.6 NA 22.1 8.4 10.5 NA 9.4 0.26 0.33 NA 0.29 Oven 10 1 2 3 2005-2105 2130-2230 NA Average 35.29 34.46 NA 34.88 2599 2537 NA 2568 1897 1850 NA 1874 229 230 NA 230 1.1 1.2 NA 1.2 231.0 226.6 NA 228.8 210.8 205.0 NA 207.9 213.1 207.5 NA 210.3 90.8 88.4 NA 89.6 Ovens 9 and 10 Total Mass Rate, Ib/hi* \| 2.80 2.66 NA 2.73 3.02 to " Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. e Part per million, wet basis adjusted for NDO contributions. f Part per million, dry basis. 8 Part per million as styrene equivalent based on styrene response factor. h Pound per hour. ------- TABLE 2.22 SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS AND MASS EMISSION RATES, CONDITION 5 - MAY 19,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps" Volumetric Flow Rate acfmb dscfmc Temperature, op Moisture, % THC Concentration ppm, wef1 Adjusted ppm, wef ppm, dr/ ppm, as styrene8 Mass Rate, lb/ht* Oven 9 1 2 3 0903-1027 1106-1231 1357-1521 Average Oven 10 1 2 3 0903-1027 1106-1231 1357-1521 Average 31.83 32.54 31.28 31.88 2349 2401 2308 2353 1821 1934 1958 1904 34.20 34.84 34.83 34.62 2524 2571 2571 2555 1859 1890 1882 1877 164 164 165 164 2.8 2.5 2.2 2.5 222 223 226 224 2.5 2.5 2.5 2.5 149.8 164.1 139.8 151.2 30.6 52.6 43.6 42.3 31.5 53.9 44.6 43.4 13.4 23.0 19.0 18.5 125.6 121.6 118.1 121.8 110.7 100.8 106.9 106.1 113.5 103.4 109.7 108.9 48.4 44.1 46.8 46.4 Ovens 9 and 10 Total Mass Rate, Ib/hi* 0.40 0.72 0.60 0.57 1.46 1.35 1.43 1.41 1.98 tv) * Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. e Part per million, wet basis adjusted for NDO contributions. f Part per million, dry basis. 8 Part per million as styrene equivalent based on styrene response factor. h Pound per hour. ------- TABLE 2.23 SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS AND MASS EMISSION RATES, CONDITION 6 - MAY 19,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps* Volumetric Flow Rate acrmb dscfin" Temperature, op Moisture, % THC Concentration ppm, wetd Adjusted ppm, wef ppm, dr/ ppm, as styrene8 Mass Rate, Ib/hr* Oven 9 1 2 3 1605-1706 1734-1855 1936-2018 Average 32.68 32.64 32.22 32.51 2412 2409 2378 2400 1948 1942 1923 1938 164 164 162 163 2.2 2.2 2.2 2.2 156.3 161.4 167.2 161.6 80.4 62.2 69.6 70.7 82.2 63.6 71.2 72.3 35.0 27.1 30.4 30.8 1.11 0.85 0.95 0.97 Oven 10 1 2 3 1605-1706 1734-1855 1936-2018 Average 33.52 33.64 33.65 33.60 2474 2482 2484 2480 1814 1835 1837 1829 225 222 222 223 2.3 2.1 1.9 2.1 111.7 139.9 131.0 127.5 98.0 118.6 112.6 109.8 100.3 121.1 114.8 112.1 42.8 51.6 48.9 47.8 Ovens 9 and 10 Total Mass Rate, Ib/hr" 1.26 1.54 1.46 1.42 2.39 to U) * Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. e Part per million, wet basis adjusted for NDO contributions. f Part per million, dry basis. 8 Part per million as styrene equivalent based on styrene response factor. h Pound per hour. ------- TABLE 2.24 SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS AND MASS EMISSION RATES, CONDITION 7 - MAY 20, 1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps- Volumetric Flow Rate acfmb dscfmc Temperature, op Moisture, % THC Concentration ppm, wef1 Adjusted ppm, wef ppm, dry' ppm, as styrene8 Mass Rate, Ib/hr* Oven 9 1 2 3 1449-1613 1705-1828 1913-2036 Average 32.00 32.27 32.56 32.28 2362 2376 2397 2378 1905 1898 1905 1903 164 168 169 167 1.2 1.6 1.9 1.6 146.3 121.8 109.9 126.0 39.4 51.2 45.3 45.3 39.8 52.1 46.1 46.0 17.0 22.2 19.7 19.6 0.53 0.68 0.61 0.61 Oven 10 1 2 3 1449-1613 1705-1828 1913-2036 Average 32.50 34.04 34.27 33.60 2393 2507 2523 2474 1746 1829 1833 1803 229 229 232 230 1.3 1.3 1.3 1.3 165.6 168.0 161.3 165.0 147.7 153.2 147.1 149.3 149.7 155.2 149.0 151.3 63.8 66.2 63.5 64.5 Ovens 9 and 10 Total Mass Rate, lb/hi* 1.81 1.96 1.89 1.89 2.50 to U) to ' Feet per second. b Actual cubic feet per minute. 0 Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. e Part per million, wet basis adjusted for NDO contributions. f Part per million, dry basis. g Part per million as styrene equivalent based on styrene response factor. b Pound per hour. ------- TABLE 2.25 SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS AND MASS EMISSION RATES, CONDITION 8 - MAY 22,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps' Volumetric Flow Rate acfmb dscfmc Temperature, Moisture, THC Concentration ppm, wetd Adjusted ppm, wef ppm, dry* ppm, as styrene8 Mass Rate, Ib/hr* Oven 9 1 2 3 0752-0844 0919-1049 1139-1309 Average 32.10 32.10 32.16 32.12 2363 2361 2367 2364 1926 1927 1929 1927 167 166 167 167 1.7 1.7 1.7 1.7 112.9 131.5 110.8 118.4 0.0 17.3 8.7 8.7 0.0 17.6 8.9 8.8 0.0 7.5 3.8 3.8 0.00 0.23 0.12 0.12 Oven 10 1 2 3 0752-0844 0919-1049 1139-1309 Average 34.24 34.19 34.41 34.28 2521 2517 2533 2524 1918 1883 1854 1885 214 213 215 214 1.3 3.1 4.9 3.1 62.4 64.4 101.1 76.0 40.8 41.6 81.6 54.7 41.3 43.0 85.8 56.4 17.6 18.3 36.6 24.1 Ovens 9 and 10 Total Mass Rate, Ib/ht* 0.55 0.56 1.10 0.74 0.86 to U) * Feet per second. b Actual cubic feet per minute. 0 Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. c Part per million, wet basis adjusted for NDO contributions. f Part per million, dry basis. 8 Part per million as styrene equivalent based on styrene response factor. h Pound per hour. ------- TABLE 2.26 SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS AND MASS EMISSION RATES, CONDITION 9 - MAY 22,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps* Volumetric Flow Rate acfmb dscfmc Temperature, oF Moisture, % THC Concentration ppm, wet1 Adjusted ppm, wef ppm, dry* ppm, as styrene8 Mass Rate, Ib/hr* Oven 9 1 2 3 1802-1844 NA NA Average 31.20 NA NA 31.20 2297 NA NA 2297 1839 NA NA 1839 160 NA NA 160 4.5 NA NA 4.5 Oven 10 1 2 3 1802-1844 NA NA Average 33.30 NA NA 33.30 2452 NA NA 2452 1763 NA NA 1763 230 NA NA 230 4.5 NA NA 4.5 67.0 NA NA 67.0 23.7 NA NA 23.7 24.8 NA NA 24.8 10.6 NA NA 10.6 0.32 NA NA 0.32 222.7 NA NA 222.7 209.5 NA NA 209.5 219.3 NA NA 219.3 93.5 NA NA 93.5 Ovens 9 and 10 Total Mass Rate, Ib/hi* 2.68 NA NA 2.68 3.00 to OJ 1 Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. ° Part per million, wet basis adjusted forNDO contributions. f Part per million, dry basis. 8 Part per million as styrene equivalent based on styrene response factor. h Pound per hour. ------- TABLE 2.27 SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS AND MASS EMISSION RATES, CONDITION 10 - MAY 22,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps* Volumetric Flow Rate acfrnb dscfrnc Temperature, op Moisture, % THC Concentration ppm, wef1 Adjusted ppm, wef PPm, dr/ ppm, as styrene8 Mass Rate, Ib/hr11 Oven 9 1 2 3 1959-2050 NA NA Average 31.12 NA NA 31.12 2297 NA NA 2297 1909 NA .NA 1909 164 NA NA 164 0.2 NA NA 0.2 110.9 NA NA 110.9 44.0 NA ' NA 44.0 44.1 NA NA 44.1 18.8 NA NA 18.8 0.58 NA NA 0.58 Oven 10 1 2 3 1959-2050 NA NA Average 33.38 NA NA 33.38 2464 NA NA 2464 - 1851 NA NA 1851 230 NA NA 230 0.2 NA NA 0.2 189.5 NA NA 189.5 168.0 NA NA 168.0 168.3 NA NA 168.3 71.7 NA NA 71.7 Ovens 9 and 10 Total Mass Rate, Ib/hi* 2.16 NA NA 2.16 2.74 to ' Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. c Part per million, wet basis adjusted for NDO contributions. f Part per million, dry basis. g Part per million as styrene equivalent based on styrene response factor. h Pound per hour.. ------- TABLE 2.28 SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS AND MASS EMISSION RATES, CONDITION 11 - MAY 23,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps" Volumetric Flow Rate acfmb dscfmc Temperature, op Moisture, % THC Concentration ppm, wef1 Adjusted ppm, wef ppm, dr/ ppm, as styrene8 Mass Rate, Ib/hr* Oven 9 1 2 3 0912-1015 1040-1121 1200-1242 Average 32.04 32.40 32.19 32.21 2359 2385 2369 2371 1979 2001 1988 1989 156 156 156 156 0.5 0.5 0.5 0.5 59.2 67.8 71.5 66.2 2.1 14.6 12.4 9.7 2.1 14.7 12.4 9.8 0.9 6.3 5.3 4.2 0.03 0.20 0.17 0.13 Oven 10 1 2 3 0912-1015 1040-1121 1200-1242 Average 33.84 33.08 33.70 33.54 2492 2435 2481 2469 1872 1823 1843 1846 231 230 231 231 0.3 0.5 1.2 0.7 269.2 283.6 273.3 275.4 245.0 267.3 250.8 254.3 245.7 268.6 255.3 255.9 104.7 114.5 108.0 109.1 Ovens 9 and 10 Total Mass Rate, Ib/hi* 3.18 3.39 3.23 3.27 3.40 to 1 Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. e Part per million, wet basis adjusted for NDO contributions. f Part per million, dry basis. g Part per million as styrene equivalent based on styrene response factor. b Pound per hour. ------- TABLE 2.29 SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS AND MASS EMISSION RATES, CONDITION 12 - MAY 29,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps> Volumetric Flow Rate acfrnb dscfmc Temperature, oF Moisture, % THC Concentration ppm, wet!1 Adjusted ppm, wet? ppm, dr/ ppm, as styrene8 Mass Rate, Ib/hr11 Oven 9 1 3 4 0835-0935 1104-1202 1230-1330 Average 60.17 60.03 59.67 59.96 4430 4419 4393 4414 3482 3511 3474 3489 Oven 10 1 3 4 0835-0935 1104-1202 1230-1330 Average 35.14 33.06 34.13 34.11 2587 2508 2512 2536 1920 1842 1818 1860 177 170 173 173 232 231 234 232 3.0 3.0 3.0 3.0 103.5 130.3 112.9 115.6 30.3 31.3 22.1 27.9 31.2 32.2 22.8 28.8 13.3 13.7 9.7 12.3 0.75 0.78 0.55 0.69 0.5 1.6 2.7 1.6 240.9 280.5 284.3 268.6 220.8 262.7 262.5 248.6 221.9 266.9 269.7 252.7 94.6 113.8 115.0 107.7 Ovens 9 and 10 Total Mass Rate, Ib/hi* 2.95 3.40 3.39 3.25 3.94 NJ * Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. * Part per million, wet basis adjusted for NDO contributions. f Part per million, dry basis. 8 Part per million as styrene equivalent based on styrene response factor. h Pound per hour. ------- TABLE 2.30 SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS AND MASS EMISSION RATES, CONDITION 13 - MAY 29,1997 LASCO Panel Products Run No. Time Stack Gas Velocity, fps° Volumetric Flow Rate acfrnb dscfin" Temperature, op Moisture, % THC Concentration ppm, wef1 Adjusted ppm, wef ppm, dr/ ppm, as styrene8 Mass Rate, Ib/hr* Oven 9 1 2 3 1518-1614 1637-1737 1801-1901 Average 59.97 59.81 59.92 59.90 4416 4404 4412 4411 3560 3530 3545 3545 172 171 173 172 1.0 1.6 1.0 1.2 124.6 130.8 121.8 125.7 29.9 27.8 38.6 32.1 30.2 28.3 39.0 32.5 12.9 12.1 16.6 13.8 0.74 0.69 0.96 0.80 Oven 10 1 2 3 1518-1614 1637-1737 1801-1901 Average 33.63 33.83 33.97 33.81 2476 2491 2500 2489 1804 1823 1814 1814 230 226 233 230 2.2 2.2 2.2 2.2 331.8 340.3 334.0 3354 308.9 318.7 318.9 315.5 315.8 325.9 326.0 322.6 134.6 138.9 139.0 137.5 Ovens 9 and 10 Total Mass Rate, Ib/hr* 3.94 4.11 4.09 4.05 4.85 to U) 00 * Feet per second. b Actual cubic feet per minute. c Dry standard cubic feet per minute. d Part per million, wet basis as propane equivalent. e Part per million, wet basis adjusted for NDO contributions. f Part per million, dry basis. 8 Part per million as styrene equivalent based on styrene response factor. h Pound per hour. ------- TABLE 2.31 OVENS 9 AND 10 MASS EMISSION RATE SUMMARY STYRENE, METHYL METHACRYLATE, AND CUMENE BY EPA METHOD 18 LASCO Panel Products Condition No. 1 1 1 Run No. 1 2 3 Average 2 2 2 1 2 3 Average 3 3 3 1 2 3 Average 4 4 4 1 2 3 Average 5 5 5 1 2 3 Average 6 6 6 1 2 3 Average Oven No. 9 Exhaust, Ib/hi* _b - - - 0.040 - - 0.040 - 0.026 - 0.026 - 0.457 - 0.457 0.044 - - 0.044 - 0.050 - 0.050 Oven No. 10 Exhaust, Ib/hi* 0.003 - - 0.003 - 0.157 - 0.157 0.006 - - 0.006 0.006 - - 0.006 - 0.826 - 0.826 0.766 - - 0.766 Total Oven Exhaust, Ib/hr" 0.003 0.197 0.032 0.463 0.870 0.816 2-39 ------- TABLE 2.31 (Concluded) Condition No. 7 7 7 Run No. 1 2 3 Average 8 8 8 1 2 3 Average 9 1 Oven No. 9 Exhaust, lb/hi* 0.006 - - 0.006 - 0.006 - 0.006 0.032 Oven No. 10 Exhaust, Ib/hr" - 1.207 - 1.207 0.241 . - 0.241 - Total Oven Exhaust, Ib/hr8 1.213 0.0247 0.032 10 1 - 1.555 1.555 11 11 11 1 2 3 Average 12 12 12 1 3 4 Average 13 13 13 1 2 3 Average - 0.006 - 0.006 - 0.129 - 0.129 - 0.427 - 0.427 0.614 - - 0.614 0.749 - 2.199 1.474 2.711 - - 2.711 0.620 1.603 3.138 1 Pound per hour, total pounds of styrene and MMA measured. b - = Sample not collected in this test condition. 2-40 ------- 2.10 RESPONSE FACTOR RESULTS The THC concentrations were monitored continuously according to EPA Method 25A guidelines, using flame-ionization analyzers (FIAs). The instruments were calibrated onsite before and after each sample run using EPA Protocol propane-in-air standards. Since the main HAP of interest was styrene, response factors (RFs) were developed to determine instrument responses relative to styrene. A modified EPA proposed Method 204F was used to prepare styrene bag standards. From the bag standards, instrument response factors were developed over three concentration ranges used during sampling. The RF results are presented in Table 2.32. The factors were very consistent over the three calibration ranges. An average RF value of 0.4263 was used to convert all Method 25 A propane results to styrene. The RF laboratory results are contained in Appendix C; 2.11 METHOD 204 TOTAL TEMPORARY ENCLOSURE VERIFICATION The room containing the process line was treated as a TTE, which enabled sampling all HAP concentrations entering and leaving the enclosure. Figure 2.1 is the general layout (not to scale) of the TTE and dimensions of the NDOs and exhaust locations. EPA proposed Method 204, "Criteria for and Verification of a Permanent or Temporary Total Enclosure" presents a five-point criteria for verification of a TTE. The LASCO Wide Line process room was configured to meet these criteria of a TTE. Natural draft openings were minimized and an auxiliary room exhaust fan was added to ensure a minimum negative static of 0.004 inches H2O. The enclosure met the following criteria required of a TTE: A) Natural draft openings (NDOs) are at least four equivalent opening diameters from each VOC emitting point. B) The total area of all NDOs shall not exceed 5% of the surface area of the enclosure's four walls, floor and ceiling. C) The average facial velocity (FV) of air through all NDOs shall be at least 3,600 meters per hour (m/hr) or 200 fpm, or the negative static pressure in the enclosure must be £0.004 in. H2O. The direction of flow through all NDOs shall be into the enclosure. D) All access doors and windows whose areas are not included in Criteria B and are not included in the calculation hi Criteria C shall be closed during routine process operation. 2-41 ------- TABLE 2.32 SUMMARY OF RESPONSE FACTOR RESULTS STYRENE BAG STANDARDS LASCO Panel Products Bag Standar d Runl Run 2 Run 3 Run 4 Run 5 Run 6 Run? Run 8 Syrene Injection, ppm (Styrene)3 67.7 67.9 134.6 189.8 362.2 557.3 1106.2 1659.5 Average Overall Average 0.4263 JUM1 Response, ppm (Propane)b 161.1 160.3 319.0 441.3 855.9 1266 2636 3983 Respon se Factor 0.4202 0.4236 04219 0.4301 0.4232 0.4402 0.4197 0.4166 0.4244 Standard Deviation 0.75% JUM5 Response, ppm (Propane)6 156.9 157.8 316.3 431.4 843.9 1250 2642 4103 Response Factor 0.4315 0.4303 04255 0.4400 0.4292 0.4458 0.4187 0.4045 0.4282 Standard Deviation 1.27% "Part per million, styrene. bPart per million, propane equivalent. 2-42 ------- er 82' Outside Natural Draft Opening (NDO) - A (32" X120") NDO-B (0.5" X 72") Fresh Air Supply (14"X26") NDO-C Doorway (Closed) (36" X 84") Doorway (Closed) (36" X 84") Doorway (Closed) (36" X 84") Overhead Door (Closed) (96" X 120") Main Exhaust (17.5") Oven Area Overhead Door (120" X 168") (Closed) Fresh Air Supply (14" x 26") NDO-D Doorway (Closed) (36" X 84") Auxilary Fan Outside (19.75") Room Exhaust (24"X28") Air Sampling THC Styrene Cumene Methyl Methacrylate Figure 2.1 Diagram of Temporary Total Enclosure 2-43 ------- E) Any exhaust point from the TTE shall be at least 4 equivalent duct or hood diameters from each NDO. PES measured the room, the doorways, the small gaps around the doors, the large swinging doors and the volumetric air flow rate entering and exiting the room. This data was used to demonstrate that the process room meets the criteria for a TTE. The TTE room measured 61 x 82 x 16.7 feet high. There are five doorways (one was used for the auxiliary fan) which measure 36 x 84 inches and two large doors 120 x 168 inches and 96 x 120 inches-all are kept closed. Thus, the TTE met Criteria D. NDO-A is the largest opening and the closest to a VOC lay down area. The opening is 2.7 x 10 feet, an area of 26.67 ft2, and the equivalent diameter of this opening is 5.83 feet. The distance from the nearest opening to the VOC lay down area was more than the required four equivalent diameters, thus Criteria A was met. The total surface area of the TTE room is 14,780 ft2. The total area of the NDOs is 31.98 ft2 which is 0.2% of the total, which met Criteria B. The negative static pressure inside the enclosure must be ^0.004 in. H2O; the enclosure negative static pressure ranged from 0.004 to 0.015 in. H2O, which met Criteria C. All access doors were kept closed during the process operation except for ingress and egress by workers and materials. When access doors were opened, the room remained under negative static pressure. The four 36 x 84 inch doorways had gaps around the bottom of each door about 0.5 inches wide. These gaps were considered NDOs and were measured and labeled NDO-B. Thus, the TTE met Criteria D. All exhaust points from the TTE were at least four equivalent diameters from an NDO, which met Criteria E. 2-44 ------- 3.0 PROCESS DESCRIPTION LAS CO Panel Products is among the largest (perhaps the largest, since the recent addition of the wide line) producer of reinforced plastic panels from the continuous lamination process in the country. Various panel products are produced with applications in both construction and automotive industries. The facility has two narrow "lines" (or continuous lamination machines) and one wide line. The storage and mix preparation processes involved with the application process were not a subject of this testing program. The lamination process begins with the unwinding of a large roll of transparent film onto the dispensing table where a catalyzed resin mixture is applied across the width of the film. This is the wet application area. Reinforcing materials are then added to the resin. A top film is unwound from a second roll of film to cover over the wet mixture. After the top film is added, the material moves into the oven curing area. The emissions from the process come from the evaporation of the monomer, which is either styrene or a combination of styrene, methyl methacrylate, and cumene. The styrene content (98%) and cumene content (1.5%) make up greater than 99% of the total HAP content. The methyl methacrylate was believed to be a small percentage (<0.2%) of the total HAP content, according to LASCO personnel. While onsite, it was discovered that MMA may account for higher percentages of the HAP content depending on the type of product produced. At this point, it was decided to measure MMA along with the other two primary HAP compounds. A fan ducted to a partial enclosure around the table area helps draw air emissions from the wet areas and exhausts the air through a stack on the roof (Main Exhaust site). Process monitoring for this sampling program was provided to ESD by PES through EPA Contract No. 68D10116, Work Assignment No. 6-01. Specific process data is being handled as confidential business information (CBI) through that work assignment. Therefore, a detailed process description and parameters are not included in this test report The following is a general description of the three room conditions that were examined during this sample program. For each of the three conditions, the process room was treated as a TTE with all access doors closed and NDOs minimized. The negative static pressure in the room was maintained at -0.004 inches of water or greater. 3-1 ------- The current condition was the operation of the process line the normal way it operates each production day. The main exhaust system is exhausting air emissions from the table area to the main roof exhaust stack. The table area is covered partially. Most top areas of the table are covered with panels and side areas mostly open. The initial resin application area is partially closed, with some panels open. The sampling areas consisted of the Main Exhaust which normally draws emission directly from the wet application area, the Room Exhaust which draws fugitive emission from floor level in one corner of the room, four natural draft openings (NDOs), and Ovens 9 and 10 exhaust stacks. The open condition involved the removal of panels and enclosures covering the wet application area of the line. The top panels and hinged access panels were removed or opened where possible. The Main Exhaust duct was disconnected so there was no air being pulled directly from the table area. The Main Exhaust pickup lines were all closed (knife dampers closed) and the pickup lines disconnected and taped off. The Main Exhaust fan continued to draw fugitive emissions from above the table area. The open condition was to simulate uncontrolled emissions from the table area. The Auxiliary Exhaust was operated during the open condition so that pressure negativity could be maintained in the room. The sampling areas consisted of the Main Exhaust, Room Exhaust, Auxiliary Exhaust, three NDOs, and Ovens 9 and 10 exhaust stacks. The closed condition was the operation of the line with everything covered and panels in place on the process line. The Main Exhaust line was disconnected so there was no air flow being pulled directly from the table area. The Main Exhaust pickup lines were all closed (knife dampers closed), and the pickup lines disconnected and taped off. Additional rigid panels were placed on any open areas on the top and sides of the table area. The rigid panels were taped closed where possible. Areas where rigid panels could not be used were covered with foil-faced foam insulation board and taped shut. The table area was estimated to be 98% covered. The Auxiliary Exhaust was operated during the closed condition so that pressure negativity could be maintained in the room. The sampling areas consisted of the Main Exhaust, Room Exhaust, three NDOs, and Ovens 9 and 10 exhaust stacks. 3-2 ------- 4.0 SAMPLING LOCATIONS The Wide Line continuous lamination process was contained in a single room with several emission points. The room was treated as a TTE to measure all emissions exiting the room and emissions being drawn into the room through the natural draft openings (NDOs). There were also two oven sampling locations (separate room from the TTE) which were sampled simultaneously with the TTE sampling locations. The oven locations were located inside the building, and sampling was conducted to determine if the ovens emitted any hazardous air pollutants. The air sampling locations were the Main Exhaust, Room Exhaust, Auxiliary Exhaust, NDOs, and OvenNos. 9 and 10. Figure 1.2 in Section 1.0 is an overall schematic of all of the sampling locations. The locations are described below. 4.1 MAIN EXHAUST STACK The main exhaust stack pulls air from the table surface area (wet application area) and exhausts the air emissions through a 17.5 inch inside diameter (ID) round vertical stack through the ceiling. Sampling ports were located 42 inches downstream (2.4 duct diameters) of the induced draft fan exhaust and 37 inches upstream of the exhaust (2.1 duct diameters) to the atmosphere. A total of 16 points, eight per port, were used to traverse the duct for velocity measurements. Figure 4.1 is a schematic of the sampling location. 4.2 ROOM EXHAUST STACK The room exhaust duct pulls room air from the wide line application area and exhausts air through a 24 x 28 inch rectangular vertical stack. The intake was at floor level in the corner of the room nearest the Auxiliary Exhaust. The velocity measurement location was in the wide line application room. The THC/M18 measurement location was in the exhaust duct outside and above the roof. Four equivalent sampling ports were located on the 14 inch side of the duct, approximately 143 inches (5.5 equivalent duct diameters) downstream of the duct work intake and 72 inches (2.8 equivalent duct diameters) upstream of the exhaust fan. A total of 24 points, six per port, were used to traverse the duct. Figure 4.2 is a schematic of the room exhaust sampling location. 4-1 ------- t To Atmosphere 17.5" I.D. Flow 37" 42" Traverse Point Number 1 2 3 4 5 6 7 8 Traverse Point Location 0.50" 1.75" 3.38" 5.63" 11.88" . 14.13" 15.63" 17.00" Fan Figure 4.1 Main Exhaust Sample Location 4-2 ------- Vent Duct Cross-section voc Sampling Port Roof 72" Velocity Sampling Ports Flow 143" Intake X X X X X X X X X X X X X X X X X X X X X X X X I 28" 24" Traverse Point Number 1 2 3 4 5 6 Traverse Point Location 2.38" 7.00" 11.63" 16.38" 21.00" 25.63" Floor Figure 4.2 Room Exhaust Sample Location 4-3 ------- 4.3 AUXILIARY EXHAUST STACK The auxiliary exhaust stack was installed in an existing doorway of the wide line application area about 24 inches above the floor to increase the volume of air exhausted from the enclosure, for purposes of creating a TTE. A section of duct work connected the sealed doorway to an auxiliary exhaust fan with straightening vanes inserted to prevent cyclonic flow. Sampling ports were located approximately 114 inches (5.8 duct diameters) downstream of the doorway and 40 inches (2.0 duct diameters) upstream of the fan intake of the 19.75 inch round horizontal duct. Sixteen traverse points, eight per port, were used to conduct velocity traverses. Figure 4.3 is a schematic of the auxiliary exhaust sampling location. 4.4 NATURAL DRAFT OPENINGS A total of four NDOs were present in the wide line application area TTE. Those openings were the material feed opening to the oven area (designated as NDO-A), the double door outside doorway (NDO-B), and two fresh air supply ducts as part of the HVAC system (designated as NDO-C and NDO-D). NDO-A (material feed opening) dimensions were 120 x 32 inches. NDO-B was 72 inches long by 0.5 inches high. NDO- C and NDO-D dimensions were 14 x 26 inches. A Kurz hot-wire anemometer was used at various points across the face of each opening to measure air velocity into the room enclosure. NDO-A and NDO-B were negative drafts into the enclosure; NDO-C and NDO-D were forced makeup air into the enclosure, as part of the building's HVAC system. Figure 4.4 details the dimensions of each NDO. 4.5 OVEN EXHAUST NO. 9 AND NO. 10 The oven curing zone was a two section process that had a long, enclosed area for curing the fiberglass panels. Each of the two oven sections had individual makeup air supply ducts and a single exhaust duct. All sampling was conducted in the round, horizontal 15-inch inside diameter (ID) duct work, prior to the outlet stack exhaust fan. Sampling ports on No. 9 were located 50 inches (3.3 duct diameters) downstream of a disturbance and 38 inches (2.5 duct diameters) upstream of the exhaust fan. Sampling ports on No. 10 were located 55 inches (3.7 duct diameters) downstream of a disturbance and 38 inches (2.5 duct diameters) upstream of the exhaust fan. A total of 12 points, six per port, were used to traverse the ducts for velocity determinations. Figures 4.5 and 4.6 are schematics of the sampling locations for Oven Nos. 9 and 10. 4-4 ------- Building Enclosure — 114" to r~ / Traverse Point Number 1 2 3 4 5 6 7 8 ^ 40" ^ -i t / f^ 10 71V1 i n Flow / iT 19-f5 ' D to / / // i Auxiliary Traverse Point Location 0.63" 2.13" 3.75" 6.38" 13.40" 15.92" 17.68" 19.12" Fan Flow Sample Ports Figure 4.3 Auxiliary Exhaust Sampling Location ------- Product web 32" 120" Natural Draft Opening A -denotes sample location 72" 0.5" Natural Draft Opening B (sample location outside of doorway-ambient air) 26" Fresh Air Supply Ducts (HVAC System) 14" Natural Draft Openings C & D Figure 4.4 Natural Draft Opening Sampling Locations 4-6 ------- Roof 50" 38" Flow 1 15"I.D.O I Fan Traverse Point Number 1 2 3 4 5 6 Traverse Point Location 0.7" 2.19" 4.44" 10.56" 12.81" 14.34" Figure 4.5 Oven No. 9 Schematic of Sampling Location ------- Roof 55" 38" 00 Flow 15"\|.D.O Fan Traverse Point Number 1 2 3 4 5 6 Traverse Point Location 0.7" 2.19" 4.44" 10.56" 1281" 1434" Figure 4.6 Oven No. 10 Schematic of Sampling Location ------- 5.0 SAMPLING AND ANALYTICAL PROCEDURES The Wide Line continuous lamination process (application and oven curing areas) was sampled for a variety of stack gas constituents following the procedures of EPA Reference Methods 1-4,18, 24,25A, and proposed Methods 204 and 204F. Table 5.1 summarizes the testing parameters, test methods, number of tests, and duration of sampling runs. Brief descriptions of each method are presented below: 5.1 LOCATION OF MEASUREMENT SAMPLE/VELOCITY TRAVERSE POINTS EPA Method 1, "Sample and Velocity Traverses for Stationary Sources," was used to select the measurement sites and to establish velocity and sample traverse point locations. The measurement sites are discussed in Section 4.0. 5.2 DETERMINATION OF STACK GAS VOLUMETRIC FLOW RATE EPA Method 2, "Determination of Stack Gas Velocity and Volumetric Flow Rate," was used in the measurement of stack gas velocity and volumetric flow rate from the exhaust ducts of the wide line lamination process. Type "S" pitot tubes with an assigned coefficient of 0.84 or Standard type pitot tubes with an assigned coefficient of 0.99 and inclined manometer were used to measure differential pressure of the stack gas. Calibrated Type "K" thermocouples were attached to the pitot tubes to measure stack gas temperatures. The average stack gas velocities were calculated from the average square root of the velocity pressure, stack gas temperature, gas molecular weight, and absolute stack gas pressure. Volumetric flow rate is the product of velocity and stack cross- sectional area. Velocities from the natural draft openings were checked with a Kurz hot wire anemometer to verify a minimum face velocity of 200 feet per minute. 5-1 ------- TABLE 5.1 SOURCES, TEST PARAMETERS, AND METHODS SUMMARY LASCO PANEL PRODUCTS - FLORENCE, KENTUCKY Source Main Exhaust Stack Auxiliary Exhaust Stack Room Exhaust Stack Natural Draft Openings A, B, C, & D Oven Exhausts Resin/Gel Coat Mixing Tanks Parameter THC HAPsc- Styrene - Cumene - MMA THC HAPs- Styrene - Cumene - MMA THC HAPs- Styrene - Cumene - MMA THC HAPs- Styrene - Cumene - MMA THC HAPs - Styrene - Cumene - MMA Methane and Ethane Volatiles, H20, Density EPA Test Methods 25A 18 18 18 25A 18 18 18 25A 18 18 18 25A 18 18 18 25A 18 18 18 18 24 No. of Tests 3" ld ld ld 3" ld ld ld 3" ld 1" ld 3" ld 1" ld 3b ld ld ld 3b 1 Time per Test," Minutes 60 20 20 20 60 20 20 20 60 20 20 20 60 60 60 60 60 60 60 60 60 5-2 ------- TABLE 5.1 (Concluded) Source Resin/Gel Coat Mixing Tanks Parameter HAPs - Styrene - Cumene - MMA EPA Test Methods 204F 204F 204F No. of Tests 1" \e r Time per Test,0 Minutes " Time per test run varied between conditions based on process operation and production schedules. b Three test runs were conducted for conditions 1, 2, 3, 5,6, 7, 8, 11, 12, and 13. Two test runs were conducted for Condition 4. One test run was conducted for Conditions 9 and 10. c Styrene and cumene were known HAPs for this site, and MMA was added while onsite based on discussions with Mr. Haberlein, a representative of the reinforced plastics industry. The styrene is believed to comprise 98% of the total HAPs and was the main pollutant of interest. d One Method 18 sample was collected for every three Method 25 A sample runs. e One Method 204F solvent distillation was conducted per condition. 5-3 ------- A pressure transducer was used in the enclosure to continuously monitor negative static in the enclosure. The enclosure was kept at a negative static equal to or greater than -0.004 inches of water column, which is the equivalent of 200 feet per minute through the natural draft openings. 5.3 DETERMINATION OF DRY MOLECULAR WEIGHT EPA Reference Method 3, "Gas Analysis for the Determination of Dry Molecular Weight," was used to measure the percentages of carbon dioxide (CO2) and oxygen (O2) present in each exhaust gas stream. Bacharach Fyrite combustion gas analyzers were used to directly read concentrations of C02 and 02. All of the sources were essentially ambient in nature (zero percent CO2, 21 percent 02). 5.4 EXHAUST GAS MOISTURE CONTENT EPA Method 4, "Determination of Stack Gas Moisture Content," was used to measure exhaust gas moisture content. This determination was made in two ways, dependent upon the temperature of the gas stream. For locations that had a stack gas temperature of 150°F or less, a wet bulb/dry bulb technique was used, utilizing calibrated thermocouples and a psychrometric chart. On the oven exhaust ducts, an EPA Method 4 sampling train was used to collect condensate from the stack gas with a series of Greenburg-Smith impingers contained in an ice water bath. The quantity of condensed moisture was determined gravimetrically and then compared to the total volume of stack gas metered to determine the volume percent moisture content. Figure 5.1 is a schematic of an EPA Method 4 sampling train. 5.5 DETERMINATION OF HAZARDOUS AIR POLLUTANTS (HAPS) EPA Method 18, "Measurement of Gaseous Organic Compound Emissions by Gas Chromatography," was used to determine the concentration and mass emission rate of styrene, cumene, and methyl methacrylate. This method was used in combination with NIOSH Method 1501 for collecting aromatic hydrocarbons on sorbent tube media (coconut shell charcoal) using low flow dry gas meters (100 to 250 cc/min) and vacuum pumps. A pair of sorbent tubes were used in series to prevent sample breakthrough. HAPs were desorbed from the sampling media with carbon disulfide. The first tube was analyzed separately from the back tube to check for sample breakthrough. Analysis was done in duplicate by gas chromatography with flame ionization detection. Methane and ethane concentrations were collected in Tedlar® bags on the two oven exhausts in evacuated canisters and also analyzed by GC/FID to determine the contribution of natural 5-4 ------- FILTER (ESTHER IN STACK OR OUT OF STACK) STACK WALL CONDENSER-ICE BATH SYSTEM INCLUDING SILICA GEL TUBE —3 AIR-TIGHT PUMP Figure 5.1 Schematic of EPA Method 4 Sampling Train ------- gas to the air stream. At least one sorbent tube sample was collected on each exhaust duct during each condition. Spiked samples were also run on at least one exhaust duct per condition, with a control sample run concurrently to determine desorption/recovery efficiency of the sampling and analytical procedures. Figure 5.2 is a schematic of the EPA Method 18 sampling system for sorbent tubes, and Figure 5.3 is a schematic of the collection system for methane and ethane concentrations. 5.6 DETERMINATION OF TOTAL HYDROCARBONS EPA Method 25 A, "Determination of Total Gaseous Organic Concentrations Using a Flame lonization Analyzer," was used to measure total hydrocarbon (THC) concentrations at the sampling locations. THC concentrations were monitored continuously in the main exhaust, room exhaust, auxiliary exhaust, and oven exhausts. At these locations heated Teflon® sample lines were used to prevent polymerization of styrene. One instrument was used to monitor the NDOs by alternating sampling lines between the sampling locations. Unheated Teflon® sampling lines were used at all the NDO locations. The FIAs were calibrated directly and through the sampling system before each test condition began. The instruments were checked for drift by system calibrations after each test run. Calibration gases were EPA Protocol propane-in-air standards. Styrene-in-air calibration standards were used to determine instrument responses. The sampling system consisted of a stainless steel probe and three-way valve with Teflon® tubing connections to switch from calibration to sampling mode. A heated Teflon® line routed stack gas to an internally heated FIA. Instrument responses were recorded on strip chart recorders and Rustrak Ranger® data logging systems. Values presented are based on data logging system averages. Figure 5.4 is a schematic of the sampling system. 5.7 DETERMINATION OF VOLATILE MATTER CONTENT, DENSITY, VOLUME OF SOLIDS, WEIGHT OF SOLIDS, WATER CONTENT, AND HAPS BY DISTILLATION EPA Method 24, "Determination of Volatile Matter Content, Water Content, Density, Volume Solids, and Weight Solids of Surface Coatings," was used in the collection of uncatalyzed resin samples used in the wide line lamination process. Volatile matter contents was determined by ASTM D2369-81. Water content was determined by ASTM D4017-81, using the Karl Fischer titration method. One uncatalyzed resin (UCR) material sample per condition was treated to a solvent distillation by vacuum method. 5-6 ------- Stack Flow t Probe VOST Dry Gas Meter Sorbent Tubes In Series Figure 5.2 Schematic of EPA Method 18 Sampling System - Sorbent Tube Method 5-7 ------- Vent Stack / Wall Filter (Glass Wool) o Probe \ \ 00 Teflon® Sample Line Vacuum Line Male Quick Connectors Ball Check Rigid Leak-Proof Container Flowmeter Charcoal Tube Figure 5.3 Schematic of Methane/Ethane Sampling System ------- Stack 3-way Valve Flow Probe Calibration Line Heated Teflon® Line Zero Air Low C3H8 Mid C3H8 1 High C3H8 Strip Chart Recorder Flame lonization Analyzer Data Logger Figure 5.4 EPA Method 25A Total Gaseous Organic Analyzer and Sample System ------- 5.8 RESPONSE FACTORS FOR FLAME IONIZATION ANALYZERS The initial test plan method for determining styrene response factors was to use a commercially prepared styrene calibration gas. The styrene calibration gas response would then be compared to our calibration curve generated by the EPA Protocol propane standards. The commercially prepared styrene calibration gases (styrene 102 ppm, 143.1 ppm, 250.7 ppm), showed responses which were non-linear. EPA Method 18 tube samples were run on the styrene cylinders, and it was found that the cylinder values were higher than the Method 18 sample results. The cylinder values were believed to be inaccurate and could not be used for comparison. The cylinder styrene values were unstable even at low concentrations and low pressures (<500 psi). It was decided the styrene calibration gases were not stable and could not be used to determine response factors. The alternative plan used EPA modified proposed Method 204F to determine styrene response factors. Bag standards of styrene were prepared in the lab and run on three ranges to determine responses relative to propane. The three ranges were: 0-500 ppm, 0-1000 ppm, and 0-5000 ppm as propane. The average response factor was 0.4263 based on 8 bag standards which were analyzed on two separate flame ionization analyzers (FIAs). The data was very consistent throughout the ranges. The following describes the EPA Method 204F procedure used: Preparing the Response Factor Mixture 1. The amount of VOC introduced to the process is the sum of the products of the weight of each VOC containing liquid used and its VOC content corrected for a response factor (RF). Typically, a sample of the resin is distilled to separate the VOC fraction from the inorganic contents. The distillate is used to prepare a known standard for analysis by an FIA, calibrated against propane standards, to determine its RF. In this case, styrene was the primary VOC, and a 99% + styrene liquid sample was used to prepare bag standards. 2. The styrene concentration in the bag sample should be similar to the gaseous VOC concentration measured in the sample gas stream. To create a specific styrene concentration in the sample bag, the following expression was used: c - ML styrene 5-10 ------- where: Cstyrme = Concentration of bag sample as styrene, mg/liter ML = Mass of styrene liquid injected into bag, mg BV = Volume of bag sample, liters 3. The FIA used EPA Protocol propane-in-air calibration gas standards to develop a linear calibration line. These calibration gases were commercially prepared in concentrations of parts per million (ppm). Therefore it was necessary to convert the styrene concentration from mg/liter to ppm. This conversion was performed by applying the following formula: C h x C x 1000-^- styrene ppm MW where: Cppm = Concentration of bag sample as ppm, styrene Cstyrene = Concentration of bag sample as mg/liter, styrene C = Constant of 24.04 liters per mole. MW = Molecular weight of styrene, 104.15 g/gmol The preparation of the styrene bag sample concentrations were performed in a consistent, repetitive manner. A dry gas meter and pump were set at a constant flow rate of 3 liters per minute to provide the air for the bag sample. A Teflon® line carried the measured air volume into a glass injection impinger which was submersed in oil heated to a temperature of 400 °F. The styrene was introduced into the glass injection impinger by means of a Teflon® coated septum cap. The styrene tainted airstream was transported through a Teflon® line heated to 180 °F and into the Tedlar® bag. The Tedlar® bag was kept in a heated box maintained at a temperature of 135 °F to eliminate condensation and adsorption in the bag. When the Tedlar® bag sample was filled with the required volume of air, the heated line from the glass injection impinger was switched to the FIA. The FIA pumped the styrene bag sample through the heated line to the detector. The response from the styrene bag sample was monitored 5-11 ------- until a stabilized measurement was reached and then for approximately five more minutes. Figure 5.5 is a diagram of the bag standard preparation system. The response on the FIA of the styrene bag standard was measured in the same units as the calibration gases. In this instance, the styrene bag standard was measured in ppm as propane. A response factor (RF) was developed from the ratio of the calculated ppm of styrene in the bag standard verses the measured styrene concentration reported in ppm as propane. The following equation calculated the response factor for each bag sample. C ppm measured where: RF = Response Factor Cppm = Concentration of bag sample as ppm, styrene measured = FIA reading for bag gas sample, ppm as propane 6. To ensure the quality assurance in preparing the styrene bag standards, the following procedures were performed: I. The dry gas meter that measured the volume of air used to fill the Tedlar® bag was calibrated against a reference test meter to develop a dry gas meter calibration coeficient (gamma). II. The ambient air used to fill the styrene bag standard was monitored by the FIA during the entire procedure of creating the standard. The results of the styrene bag standard were corrected according to the measured ambient air VOC concentrations. III. The styrene bag standard preparation system was always purged continuously between styrene bag standards. The Tedlar® bag was also purged after each styrene standard and the purged air was measured on the FIA to ensure that no residual styrene remained in the Tedlar® bag. 5-12 ------- Dry Gas Meter TTsyri Pressure Gauge Boiling Water Bath O Temperature Sensor X Syringe Septum Midget Impinger Heated Container -tx- Air Cylinder Figure 5.5 Schematic of Bag Standard Preparation System ------- IV. The styrene bag samples were analyzed on two separate J.U.M. FIAs to ensure consistent responses to the styrene standards. The gas sample from the styrene bag standard was split to each analyzer. J.U.M. analyzer #1 was used at the main exhaust location at the LASCO Panel Products plant and J.U.M. analyzer #5 was used at the room exhaust location. V. Both J.U.M. analyzers were calibrated according to EPA Reference Method 25A. The maximum mid calibration gas drift was 0.77% of span value and no zero calibration drift was detected for any of the styrene bag standards. VI. The response factors for the J.U.M. analyzer #1 had a standard deviation of 0.75% for the 8 separate styrene bag standards tested. J.U.M. analyzer #5 had a standard deviation of only 1.27% for the response factors developed from the 8 separate styrene bag standards. 5-14 ------- 6.0 QUALITY ASSURANCE/QUALITY CONTROL The following section describes the specific quality assurance/quality control (QA/QC) procedures employed by PES in performing this series of tests. The goals of the QA/QC activities for this project were intended to ensure, to the highest degree possible, the accuracy of the data collected. The procedures contained in the "Quality Assurance Handbook for Air Pollution Measurement Systems, Volume III, Stationary Source Specific Methods," EPA-600/R-94/038c, served as the basis for performance for all testing and related work activities in this project. 6.1 CALIBRATION OF APPARATUS The preparation and calibration of source sampling equipment is essential in maintaining data quality. Brief descriptions of the calibration procedures used by PES follow. Barometers PES uses aneroid barometers which are calibrated against a station pressure value reported by a nearby National Weather Service Station corrected for elevation. Temperature Sensors Bimetallic dial thermometers and Type K thermocouples are calibrated using the procedure described in Section 3.4.2 of the Quality Assurance Handbook. Each temperature sensor is calibrated over the expected range of use against an ASTM 3C or 3F thermometer. Table 6.1 summarizes the types of calibrations performed and the acceptable levels of variance. The calibration data is contained in Appendix E. The temperature sensor calibration results were within the acceptable levels of variance. Thermocouple read-out devices are calibrated using a thermocouple simulator having a range of 0-2400°F. 6-1 ------- TABLE 6.1 SUMMARY OF TEMPERATURE SENSORS CALIBRATION REQUIREMENTS Temperature Sensor Usage Impinger Outlet Thermcouple Dry Gas Meter Thermometer Stack Temperature Thermocouple Number of Calibration Points 2 3 4 Calibration Media Ice Bath (0°C) * * * Ambient Air (20-25°C) * * * Hot Water (40-50°C) * Boiling Water (100°C) * Heated Oil (150-200°C) * Tolerances ±1°C ±3°C ±1.5% of reference temperature ------- Pilot Tubes PES uses Type S and Standard type tubes which are constructed to EPA Method 2 specifications. Type S pitot tubes meeting these criteria are assigned a baseline coefficient to 0.84 and need not be calibrated. Standard pitot tubes are assigned a coefficient of 0.99 and also need not be calibrated. The pitot tube calibration data is contained in Appendix E. The calibration results are within the acceptable levels of variance. Differential Pressure Gauges PES uses Dwyer inclined and inclined/vertical manometers to measure differential pressures. These include velocity pressure, static pressure, and meter orifice pressure. Manometers are selected with sufficient sensitivity to accurately measure pressures over the entire range of expected values. Manometers are primary standards and require no calibration. Dry Gas Meters and Orifices Dry gas meters and orifices are calibrated in accordance with Section 3.3.2 of the Quality Assurance Handbook. This procedure involves direct comparison of the dry gas meter to a reference dry test meter. The reference dry test meter is routinely calibrated using a wet test meter or a liquid displacement technique. Before its initial use in the field, the metering system is calibrated over the entire range of operation. After each field use, the metering system is calibrated at a single intermediate setting based on the previous field test. Acceptable tolerances of the initial and final dry gas meter factors and orifice calibration factors are ±0.02 and ±0.20 from average, respectively. The dry gas meter and orifice calibration data are in Appendix E. The calibration results are within the acceptable levels of variance. 6.2 ONSITEQA/QC The onsite QA/QC activities included: Measurement Sites Prior to sampling, all stack dimensions were checked to verify measurement site locations, location of test ports, and stack inside dimensions. Inside dimensions were checked through all available test ports to determine uniformity of the stack cross- sectional area and the sample test ports were checked to verify that they do not extend beyond the inside wall. The stack inside dimensions, wall thicknesses, and sample port depths were measured to the nearest 1/16 inch. When stack dimensions are found to be 6-3 ------- out of round or uneven, then multiple traverse point locations are required on the pitot tube. Velocity Measurements All velocity measurement apparatus were assembled, leveled, zeroed, and leak- checked prior to use and at the end of each determination. The static pressure was determined at a single point near the center of the stack cross-section. Moisture Stack gas moisture content was determined during each test run using calibrated wet bulb/dry bulb thermocouples and a psychrometric chart on all ambient type sources. EPA Method 4 sampling trains were used at the oven exhaust because of higher (>150°F) stack gas temperatures. All impingers were measured gravimetrically prior to and at the end of each sampling run. Total Hydrocarbon Concentration Total hydrocarbon concentrations (THC) were measured following the guidelines of EPA Method 25 A. The flame ionization analyzers were calibrated with three EPA Protocol propane-in-air gas standards and zero gas. A bias check and response time test were conducted initially. Bias check acceptability is a difference of not more than five percent between direct injection measured values and system injection. The bias check must be within ± 5% to proceed with the sample efforts. Prior to sampling, PES performed the bias check, response time tests and calibration error tests. Calibration drift checks were performed after each test run; acceptable drifts for zero or span gases is ± 3% of span. Table 6.2 summarizes the maximum system calibration bias, calibration error and drift percentages for each FIA per each condition. Calibration data is contained in Appendix A with the field strip charts. Hazardous Air Pollutants Analysis for target hazardous air pollutants (HAPs) was performed onsite by DEECO. Spiked tubes were prepared onsite based on THC measurements conducted during each sampling condition. Sample tube blanks were also collected and analyzed onsite. Samples were desorbed and analyzed within specified holding times for the individual compounds. Following are the laboratory quality assurance procedures. There were duplicate injections of each sample aliquot, with agreement between both injections to within 5% of the mean of the injections. 6-4 ------- TABLE 6.2 SUMMARY OF CALIBRATION RESULTS FOR THC ANALYZERS CONDITION NOS. 1-13 LASCO PANEL PRODUCTS Cond. No. 1 2 3 4 5 6 7 8 9 10 11 12 13 Main Exhaust System Bias, % 1.53 1.92 2.70 2.70 2.29 2.29 1.53 1.53 1.53 1.53 1.91 1.91 1.91 Calib. Error, % 0.98 0.39 0.56 0.83 0.17 1.06 0.08 0.24 0.20 0.20 0.25 0.43 0.43 Drift, % 0.4 0.8 0.4 1.5 0.4 1.1 0.8 0.8 1.2 0.4 1.2 0.8 0.8 Room Exhaust System Bias, % 0.40 1.52 1.13 1.1 1.53 1.53 0.76 2.27 2.27 2.27 2.68 2.68 2.68 Calib. Error, % 0.60 0.41 0.60 0.21 0.06 0.15 0.45 0.34 0.24 0.24 0.36 0.44 1.09 Drift, % 0.8 1.5 3.0 1.2 0.4 1.5 0.4 0.8 0.8 0.0 1.1 1.9 1.9 Auxiliary Exhaust . System Calib. Bias, Error, % % Drift, % NA NA NA NA 1.9 0.24 0.8 NA NA NA NA NA NA 3.44 0.87 3.44 0.87 1.5 1.9 Oven No. 9 System Bias, % 3.6 3.7 2.1 2.8 1.6 1.6 3.1 3.2 3.2 2.5 1.8 2.9 2.2 Calib. Error, % 2.8 2.8 4.1 4.1 2.2 2.2 2.2 2.8 2.8 2.8 2.4 2.2 2.2 Drift, % 0.9 0.8 0.4 0.7 1.3 0.9 0.7 1.3 0.0 1.2 1.0 1.0 0.5 Oven No. 10 System Bias, % 2.0 3.8 3.6 0.7 0.9 1.1 2.5 1.8 1.1 1.4 2.4 2.1 1.3 Calib. Error, % 3.5 1.0 4.8 4.8 2.6 2.6 2.2 2.8 2.8 2.8 3.2 2.0 2.0 Drift, % 1.0 1.0 1.3 0.2 0.5 0.3 1.1 0.1 0.1 0.1 0.3 0.5 0.3 NDOs System Bias, % 3.0 3.4 3.6 3.2 2.8 2.8 4.5 3.2 2.4 2.8 3.2 2.2 4.5 Calib. Error, % 3.2 3.2 3.6 3.6 4.1 4.1 2.6 2.8 2.4 2.4 2.9 2.2 2.8 Drift, % 2.1 0.8 1.6 2.4 1.5 1.2 0.8 2.1 0.2 1.2 1.4 1.4 1.1 Note: Values listed for each condition are maximum for each set of test runs. NA - Not applicable for these conditions. ------- • There were three point calibration curves for all components (based on least squared regression analysis) with the curve range bracketing sample concentrations. • Calibration curves were developed every 24 hours. • All calibration points agreed within 10% of the theoretical value. • For at least every nine samples, a field blank, duplicate and spiked sample were conducted. The blank sample was an unopened sample tube. The duplicate sample results were used to determine method precision. Analysis for the target HAPs were measured following the procedures of EPA Method 18. Sampling media consisted of activated coconut shell charcoal in sorbent tubes, a pair in series. Pre-test and post-test leak checks were conducted on each set of sampling trains. Spiked sorbent tubes were run in duplicate with another set of sample tubes to determine recovery efficiency of the analytical method. Run No. RES-4-1 recovery efficiency was 195%, which was the result of over spiking the tube compared to measured stack values. The spike amount was non- representative of sample conditions, and the data was not used to correct stack concentrations. Run No. AFS-12-4 recovery was borderline at 68%. All other styrene recoveries were within the acceptable range. Styrene and methyl methacrylate results were adjusted for recovery efficiencies. At least one spiked duplicate was run per each of nine samples run. Target compounds were styrene (primary), cumene and methyl methacrylate. Table 6.3 summarizes the Method 18 quality assurance results for the sample tubes spiked with styrene standards and run in duplicate with a separate unspiked sample. Recovery efficiencies are listed for the test runs conducted at the sample locations under different test conditions. EPA Method 18 guidelines specify recovery efficiencies ranging from 70% to 130%, with the majority of the spiked runs within this range. Table 6.4 summarizes the desorption efficiencies for the three compounds of interest: styrene, cumene and methyl methacrylate. Desorption efficiencies for styrene averaged 89.1%; cumene averaged 131.3% and methyl methacrylate efficiencies averaged 80.0%. Methane and Ethane Methane and ethane concentrations were collected in Tedlar gas bags during each THC measurement run on the oven exhausts to determine the natural gas contribution to the total gaseous organic concentration. Volumes recorded were based on air displacement in the evacuated containers with pre-test and post-test pressure measurements. 6-6 ------- TABLE 6.3 SUMMARY OF EPA METHOD 18 QUALITY ASSURANCE RESULTS STYRENE RECOVERY EFFICIENCIES Run No. MES-3-3 RES-4-1 AFS-5-2 MES-6-2 MES-11-2 RES-11-3 MES-12-3 AFS-12-4 Recovery Efficiency, % 94 195 70 103 85 79.0 111 68 Acceptable Range, % 70%- 130% 70%-130% 70%-130% 70%-130% 70%-130% 70%-130% 70%-130% 70%-130% Pass Yes No Yes Yes Yes Yes Yes No ' TABLE 6.4 SUMMARY OF DESORPTION EFFICIENCIES Compound Styrene Styrene Styrene Cumene Cumene Cumene Methyl Methacrylate Methyl Methacrylate Methyl Methacrylate Spike Level, mg 0.9009 4.5045 9.009 0.86 4.30 8.60 0.9306 4.653 9.306 Desorption Efficiency, % 85.0 92.1 90.1 138.0 134.8 121.0 60.7 93.9 85.2 Acceptable Range, % 70%- 130% 70%- 130% 70%-130% 70%-130% 70%-130% 70%-130% 70%- 130% 70%-130% 70%-130% Pass Yes Yes Yes Yes Yes Yes No Yes Yes 6-7 ------- APPENDIX A RAW FIELD DATA ------- Appendix A.I Manual Methods Raw Field Data ------- APPENDIX A. 1.1 Method 1 Field Data Sheets (includes flows, moistures, and Method 18) ------- TRAVERSE POINT LOCATION FOR CIRCULAR DUCTS Plant:. Date: Sampling Location: f)(~ A/->- ^ C Inside of Far Wall to Outside of Nipple: Inside of Near Wall to Outside of Nipple (Nipple Length): Stack I.D.: // " Distance Downstream from Flow Disturbance (Distance 3): £O inches / Stack I.D. = 3. * dd Distance Upstream from Flow Disturbance (Distance A): 30 inchee / Stack 1.0. = 2. ^ dd Calcuiatad Bv: "^- Schematic of Sampling Location Traverse Point Number / L 1 Y r (f Fraction of Length O.o W o.( ------- TRAVERSE POINT LOCATION FOR CIRCULAR DUCTS Plant: Data: A? Sampling Location: 0 u //" '" Inside of Far Wall to Outside of Nipple: Inside of Near Wall to Outside of Nipple (Nipple Length): _y Nipple Length (inches) 0" • L Traverse Point Location (Sum of Col. 4 & 5) 0.7 ZJ1 r.fY /O.ffe /2.. 8/ //. 3y ------- TRAVERSE POINT LOCATION FOR CIRCULAR DUCTS Plant: l-ASCO V^pp\j(_T% Date: - Sampling Location: )T\Al Y\l Insida of Far Wall to Outaida of Nippi.: K//A _ ln.id. of Near Wall to Oub,oa of Nippl. ------- TRAVERSE POINT LOCATION FOR RECTANGULAR DUCTS Plant: _tA Sampling Location:. Duct Width, inches:. Inside of Far Wall to Outside of Nipple:. Inside of Near Wall to Outside of Nipple (Nipple Length):. Duct Length, inches: 3*1 3~ £> Equivalent Diameter = 2xLxW/(L + W) = £>.£. Distance Downstream from Flow Disturbance (Distance B): ~ \S inches / Equivalent Diameter Distance Upstream from Flow Disturbance (Distance A): inches / Equivalent Diameter = i • • « .vJP Calculated Byt A. dd Schematic of Sampling Location Traverse Point Number i 21 J M 5" OD Fraction of Length o,o§3 O,ZT OMH G,5B3 orwTo 0,-iH Length (inches) -2/B > y / Product of Columns 2 & 3 (To nearest 1/8") o2,32_ "7. OC3 It. 8 !^,32_ J2 /. OO ^25".(^€, Nipple Length (inches) A/VA \ / Traverse Point Location (Sum of Col. 4 & 5) 3.3/3 "7 )l£/B I t^/S ai 25 Vq If No Ports, Calculate Distances From Stack Walls For Port Locations Number of Ports Fraction of Width Width (inches) Port Location . Product of Col. 2 & 3* (To Nearest 1/8) -AII points or ports should be an equal distance from each other (0) and 1/2 of -that distance from the stack walls (0/2), where 0 - Width / # of points or ports ------- j at TRAVERSE POINT LOCATION FOR CIRCULAR DUCTS Plant: LASCQ Date: Sampling Location: Hux: \LvAfg-V f2.ce>Kr\ PvVMAO^I I raid* of Far Wall to Outside of Nipple: f^ / A _ Inside of Near Wall to Outside of Nipple (Nipple Length): N I f\ Stack I.O.: Oiatanca Oownstrcam tram Flow Disturbance (Distance 3): inches / Stack 1.0. = -^ dd Distance Ucntream from Flow Oisturtsance (Distance A): O inches / Stack I.D. = <3. 0 dd Calculated 8y: Schematic of Sampling Location Traverse Point Number roauct of jmns 2 & 3 learest 1 /8") .(i3 o7 53 ?8 o 1-2. ^8 IZ. Nipple Length (inches) A///1 \! / • Traverse Point Location (Sum of Cot. 4 & 5) £/e ^Hs 33A/ 6 ^S \|33/3 15% 17% nfa ------- APPENDIX A. 1.2 Condition 1 (includes flows, moistures, and Method 18) ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Sampling Location: Run »: Date: 5 Clock Time: Operators: 2&.S6 Static Pressure, in. HoO: Barometric Pressure, in. Hg: Moisture, %: ^^ Molecular wt., Dry:_2£!jL Pitot Tube?Cp~I Stack Dimension, in. Diameter or Side 1: (7.5" " Side 2: — Wet Bulb, ° F: (A Dry Bulb, ° F: Tr«v«™« Point Number / 7 3 f / c. 7 f / i 3 ^ 5 ( 7 * • Velocity Head . in. H2O /7 .2^ .30 ?/ .33 .36 .2* 37 • 26 .2* .2f .^0 ."2? ,^0 .3Z .2-7 ^P -0.^^18 Stack Tmp. °F ^/ f/ ^7 f2 ?2 42 11 11 ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Location: - 13.6 Plant: Site: HFMKJ EwuL^-r Operators:f/V/P^eRun #'• MfH'1 Date: Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of HpO at Tw (from Table) = (Ps - Fvw) x Vapor Pressure of H2O = Pva = (Pvw) • Phar= 28.aa Pa = T.«^ PS= 2£.So TW = t>e> Td= ftq AT= 2.1 Pvw = 0 . b902> in. Hq in. HO • 2 - in. Hg °P °F °F in. Hg )- 2SOO-(1.3xTw) )X( 2.1 . ) 2800 -(1. 3 x lo Proportion of Water Vapor by Volume = Bws Una - (Ps) T«mp. OF 0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 180 170 180 190 200 210 220 230 240 0 0.0370 0.0031 0.1025 0.1047 0.2478 0.3020 0.5210 0.7392 1.032 1.422 1.932 2.590 3.446 4.525 5.881 7.569 9.652 1220 1520 1941 2347 28.78 3540 4241 5044- 1 3.0398 0.0000 0.1000 0.1710 0.2370 0.3704 3.5407 0.7848 1.080 1.487 1.992 2.672 3.543 4.647 6.034 7.759 9.888 12.48 18.63 1942 2346 2043 3848 43.11 51.76 ( Zt.io ) VAPOR PRESSURES OF V\ In Inches of Mercury 2 0.0417 0.0090 0.1127 0.1003 0.2077 0.3900 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 18.98 1944 24.46 2042 3647 4S42 52.70 3 0.0441 0.0728 0.1100 0.1878 0.2702 0.4052 0.5802 0.6183 1.138 1.561 2.114 2.629 3.744 4.900 6.350 8.180 10.36 13.07 16.34 2027 24.97 30.82 3747 44.74 5348 4 0.0403 3.0708 0.1248 0.1955 0.2891 0.4203 0.6009 0.8482 1.175 1.610 2.178 2.911 3.848 5.031 6.513 8451 10.61 13.37 16.70 20.70 2548 31.13 37.78 4847 5442 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2243 2.998 3.954 5.165 6.680 6.557 10.66 13.67 17.07 21.14 2640 31.78 3640 4641 5840 0.«7l(, in. Hg PER < r?o.z 27 It. << e 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9040 1.253 1.712 2.310 3.081 4.063 5.302 6.850 8.767 11.12 13.98 17.44 2149 2643 3246 3024 4727 5640 7 0.0541 0.0092 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.961 11.38 14.30 17.82 2245 27.07 3342 3040 48.14 5741 8 3.0571 0.0932 0.1502 0.2292 0.3304 0.4858 0.6903 0.9668 1.335 •1.619 2.449 3259 4.289 5.585 7202 9.200 11.65 14.62 1821 2242 2742 3347 40.78 4048 5843 9 0.0598 0.0982 0.1567 0.2383 0.3493 0.5038 0.7144 0.9989 1.378 1.878 2.821 3.331 4.408 5.732 7.384 9424 11.02 1446 1841 2240 28.18 3448 4142 4048 8047 ------- 3 aa cza GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Lfl&tO Date: f '-#-97 Sampling Location: fl\A\/\ £vH«.o«/ Clock Time: /.?26 Run #: MS Barometric P Moisture, %: Stack Dimen Wet Bulb, °F TrovcrM Point Numter / Z 3 1 S c. 7 1 1 ^ 3 y s (, 7 f • -1-7- , Onerators: "7^ ressure, in. h 3.* q: 7A^2. Static Pressure, Molecular wt.. Drv: 2& 0f Pilot sion. in. Diameter or Side 1 : /7,5' " Side V/k^ 5. in. HoO: "^ 0 / TubeT Cp: <4£ •?? 2: : 0f.t. nryflulhOF- #7 V.tooty HMJ in. H20 ^,z./ ^."2-"2- ^.'i'A ^.7.2- 0.W 0.23 03) 0.10 0,04 Q^ o ,VO o ^\ b.VU o .04 o ,»q o ,T.D ^F-0,Y«g^ Stack Temp. °F * (0.32 X %02) + (0.28 X%N2> Md - (0.44 x ) ••• (0.32 X ) f (0.28 x ) Md- Zfc.fc/ % HO % HO 100 M.-( )X(1--^5- Mi- ^%Mk T:. f/ °F- 5V/ P« - Pb + S'P' = ( ) 13.0 P»- •7.<2/'?t^ln-H8 ^P-^ Y0^ — r v« • as.4» x Cp x ^AP x A\|- V« - 65.40 x ( ) x ( v«. ^3 ^^-7 IM •• /,fc> n2 1^« • W« v AA y MA «/m Q«- x Qs • 2, 2 00 £• aedm JJV1.5 pg Q« ..- Q« x 17.847X — x ltd T, Qi.,- X17447X- r •»" 100 ' ^'•'-TB-' °R (°F^460) 13.8 Ts^R) Ps x Ma ,-J JT-y XOO %H,0 i-^S-) x(1--^ dMfcn ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Site: ^fei'" fc^--" Operarnrs- Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar + - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of HpO at Tw Vapor Pressure of H9O = Pva = (Pvw) - 7^/fo Run #: Mg- /- i Pbar = Pg = -&- Tw = Td = AT = (from Table) = Pvw = (Ps - Pvw) x (AT) Xr<5~0t-, t^y - Date: 5^//%^7 2& ?2- , in Hn t.-Ql in HO 23, ?2- in Hn 9f °n £7 ; °P 6 OF / ^^ in Hn 2800-(1.3xTw) Pva=( 2800-(1.3 x Proponion of Water Vapor by Volume = Bws ( /.oof ) 1.001 (Ps) Tamp. °F 0 10 20 20 40 SO 60 70 80 90 100 110 120 130 140 150 100 170 100 190 200 210 220 230 240 0 0.0370 0.0631 0.1025 0.1847 0.2476 0.3820 0.5218 0.7392 1.032 1.422 1.932 2.590 3.440 4.525 5.001 7.569 9.052 1240 1549 1941 2347 20.75 3540 4241 5044- 1 0.0398 0.0060 0.1060 0.1718 0.2576 0.3764 0.5407 0.7648 1.060 1.407 1.002 2.072 3.543 4.047 6.034 7.759 9.005 12.40 15.03 1042 2340 2943 3540 43.11 51.70 in. Hg ( rw^) VAPOR PRESSURES OF WATER &1, \ In Inches of Mercury 2_6»?'^-7 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3006 0.5601 0.7912 1.102 1.513 2.052 2.749 3.042 4.772 0.100 7.952 10.12 12.77 1540 1944 24.40 2942 3047 4342 52.70 3 . 0.0441 0.0728 0.1186 0.1678 0.2782 0.4052 0.5802 0.8183 1.130 1.501 2.114 2.029 3.744 4.900 6.350 0.150 10.30 13.07 10.34 2047 2447 3042 3747 44.74 5345 4 0.0463 0.0768 0.1248 0.1955 0.2091 0.4203 0.0009 0.0462 1.175 1.610 2.170 2.911 3.848 5.031 6.513 0.351 10.01 1347 10.70 20.70 2540 31.13 37.78 4547 5442 5 0.0409 0.0010 0.1302 0.2035 0.3004 0.4359 0.6222 0.6750 1.213 1.660 2443 2.995 3.954 5.165 6.000 6.557 10.00 13.07 17.07 21.14 2040 31.75 3040 4641 5540 a 0.0517 0.0846 0.1370 0.2116 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.001 4.003 5.302 6.050 0.707 11.12 13.90 17.44 2149 2043 3240 3944 4747 7 0.0541 0.0092 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.705 2.379 2.169 4.174 5.442 7.024 8.901 11.30 14.30 17.02 2245 27.07 3342 3949 40.14 5741 • 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4850 0.6903 0.9660 1.335 1.019 2.440 3.259 4.209 5.505 7.202 9400 11.05 14.62 1641 res? 27.02 3347 40.75 4948 5043 9 0.0590 0.0002 0.1567 0.2383 0.3403 0.5035 0.7144 0.0009 1.370 1.075 2421 3451 4.400 5.732 7.364 9.424 11.92 1446 1641 2240 20.10 3443 4142 4049 5947 ------- PlantL Date- METHOD 18 FIELD DATA SHEET Tested Ana!yte:_^y. Location: Run#: Stack l.D.:. Pbar: 2i ^ / - .•». Sample Tube - Operators : Orifice Tank #:. Pump/Rotometer #: Pt: Pretest (mm HaV. ^ooc <&. ic Post-Test (mm Hg)-_ Tt: Pretest Post-Test fF):. Leak Check: Pre: Post: Time: Start! / Ac Finish: /dteSTotal: p. fr< \nii-i. ,! r>/n. &1 r\ t /^r^ . ' )» •1.3C V-^V Time }$to \U'o IbOO /<^C5' Gauge Vacuum (Hg) G C O o Row Setting Mc&fa' ••>,... i ' ^ • / r / ? TrevrM D^I^A HOIIlt Numbar 2 Velocity HMd In. HgO ^92 73 Md - Md • (0.44 X Md- -t- (0.32 x ) + (0.32 X ) •• (0.28 x ) % M.- T.- ---H Stack T.mp. 73 - 13.B 13.6 Vl - 85.48 X Cp x Vs - 85.48 x ( PaxM )x( )x ft/s - V«xA«x8O«/m xM •dm Pt %KLO °«— "Q»* 17.647 x x(1 2_) •" Tt 100 X 17.047 X- 100 ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: / A$£O /hy&xJ-s- Location: /^£>-t~^, f<^ Site: /fa. £xt~ir Operators: Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Pbar j; - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H^O at Tw Vapor Pressure of H-.O = Pva = (Pvw> - -7^- Run: tff-l-3 Date: # phflr= 2>%.T~ Pg= -t-,01- _P2_ Ps= 28,^ i y.b a, TW = fe Trf. 73 AT= 7 (from Table) = Pvw = r ^^ (Ps - Pvw) x (A-T) /"/T-7 in. Hq in. HJO in. Hq °F °F °F in. Hq 2800-(1.3xTw) 7 1. 2800 -(1. 3 x Proportion of Water Vapor by Volume = Bws in. Hg Bw-_ (Pva) (Ps) ( /,/£/ ) O.o 6s\0 o <&• 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.819 2.449 3259 4.289 5.585 7.202 9200 11.65 14.62 1841 2242 2742 3347 40.79 4843 5843 9 0.0598 0.0982 0.1567 . 0.2389 0.3493 0.9039 0.7144 0.9988 1.376 1.679 2.921 3491 4.406 5.732 7.384 9424 1142 1446 1841 2249 28.18 3443 4142 4943 9947 ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant:. Sampling Location: Run#: Date: Clock Time: ( 2. Operators : Barometric Pressure, in. Hg: £%??£ 2ft.BQ Static Pressure, in. H2O:_ Moisture, %: A 9 Molecular wt., Drv: W,^ Pilot Tube, Cp:. Stack Dimension, in. Diameter or Side 1: -2-V " Side 2:_ Wet Bulb, ° F: 67 Dry Bulb, ° F: 1< Tr Point Number n i 3 Velocity in. H20 • D-? .no . 1 1 Stock mp °F T«mp. ° ~77 77 -? r -n Md - (0.44 x %CO2) + (0.32 X %O^) + (0.28 X %f^) Md - (0.44 x ) + (0.32 X ) + (0.28 X ) Md - 2,$.tf % HO % HO M«-Mdx(i-—i_)ia(—-i-) 100 too M« - (Zt-W ) x (1 - ''^ ) 18 ( A^ ) _ / v M«- P«-Pb S.P. 13.8 P«- 28.15 In-Hg ) 13.8 — , / Ta (°R) Ve- 65.40 xCpx ^P x W p9J(Ma V« • 65.40 x ( . V.. A.. tt/« xeo Qt- idm p, %H-0 Q> ..- Qt X 17.847 X jc(1- a— M !• 100 X 17.847 X- 536 100 ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: Lf&0 Site: £00^ £,4^^ Ooerators: Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar ± - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw Vapor Pressure of HA;6 = Pva = Pvw\ - Location: fa 30v«,«.f- tf\- Run: tffi. \|_i Date: .«; Pbar = Z&tf Pq = ~ . 6S -£2- Ps= Z&-IS Tw = 01 Td = 7f AT= ll ffrom Table) = Pvw = C,66» ^ (Ps - Pvw) x (AT) i ^XM?-7 in. Hq ! in. HO in. Hg °F '-°F °F in. Hg 2800-(1.3xTw) 2800 -(1. 3 x Proportion of Water Vapor by Volume = Bws Bws = (Pva) (Ps) ( Tamp. ( z,-75 ) VAPOR PRESSURES OF WATER In Inches of Mercury in. Hg OF 0 to 20 30 40 50 00 70 80 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 0 0.0370 0.0031 0.1025 0.1047 0.2478 0.3020 0.5218 0.7392 1.032 1.422 1.032 2.596 3.446 4.525 5.881 7.589 9.652 1250 1559 19.01 23.47 28.75 3540 4241 5044- 1 0.0398 0.0680 0.1080 0.1718 0.2970 0.3784 3.5407 0.7848 1.066 1.467 1.992 2.672 3.543 4.647 6.034 7.750 9.685 12.48 15.83 19.42 2348 2843 35.86 43.11 51.78 2 0.0417 0.0898 0.1127 0.1803 0.2077 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.740 3.642 4.772 6.100 7.052 10.12 12.77 15.88 1844 24.46 2842 3647 4342 52.70 3 0.0441 0.0728 0.1188 0.1878 0.2782 0.4052 0.5602 0.8183 1.138 1.561 2.114 2.829 3.744 4.900 6.350 6.150 10.38 13.07 18.34 2047 24.87 30.82 3747 44.74 5345 4 0.0403 0.0708 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 0.513 8.351 1041 13.37 16.70 20.70 25.48 31.13 37.78 4847 5442 5 0.0489 0.0810 0.1302 0.203S 0.3004 0.4359 0.6222 0.8750 1.213 1.860 2.243 2.995 3.954 5.185 8.880 6.557 10.66 13.67 17.07 21.14 2640 31.75 46.41 5540 6 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.850 8.767 11.12 13.98 17.44 2148 2843 3248 3844 4747 5840 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.981 11.36 14.30 1742 2245 27.07 33.02 3048 48.14 5741 8 0.0571 0.0932 0.1502 0.2292 0.3304 0.4858 0.6903 0.9668 1.335 1.819 2.449 3559 4589 5.565 7502 9500 11.65 14.62 1841 2242 2742 3347 40.78 4048 5848 9 0.0598 0.0982 0.1587 0.2383 0.3493 0.5035 0.7144 0.9080 1.378 1.878 2.521 3451 4.408 5.732 7.384 9.424 11.82 14.88 1841 2248 28.18 3448 4142 4848 5047 ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant- LftbLD Date: •5"-/^'-?"7 Sampling Location: /£», R^«^~ Clock Time: l$1o Run: RS-/-2- operat«r<:- rjQ- /£>+<-£ Raromptrir Prt»si,ira ip Hg: 2tT f2 Static Pressure, in. HUO: -,&£ Molecular wt.. Drv ^^. ^ V Pitot Tube. CD: _ •?? Stack Dimension, in. Diameter or Side 1 : W " Side 2: ?•%" Wet Bulb. °F: &/ Drv Bulb. °F: ~r(s TrovcrM QA\|K roint Number / Z 3 y $ * i t > V f 0 / Z V ¥ 5 Q « ^ 3 ^ y 0 ^••^^••^•^^^^•^^••M Velocity Head in. H20 , O^ »6 j rt« ,n Md-(0.44x 0 )>(0.32X 2-C )(0.2Bx7f )' Md- W.tf % HO % H20 M..Mdx(i--j— )ia< )00 ) M« - ( )x(1- --— > * 1B( inf> > M«- 2g^7 T;. ^/ °F- ^V/ °R(°F4«» 0 p P-"Pbl3* ' * 13.6 P«- 2&«7 '"-"a ^- 0 ^^^ f Ta ^R) 17^ 1 _. , "U- V« • 65.49 X Cp X VAP X \\| -p, „ M, v«- /7,Z77 «" — V,67 n2 Qt- VtxAaxMa/m Q.. X X00 Q.. y^3^5«n Pt %H7° Of _n-Qi XI 7.647 X x (1 • • ) •to TJ 100 ^•Id" X17.847X — x(1- 1fl0 ) ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: LAff> s'te: ILgr S^t^st Operators: Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Pbar ± - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw Vapor Pressure of H2O - Pva - (Pvw) - Pva=( fl/W? ].(2%$7 -tfcH Location: /^P/^O., /^— f4/P> Run: ^-/-^ Date: $/ Pbar = -2W2- Pq = ~.(e>5 -^- PS = ?l 67 13.6 / i Tw= £Y Td = ~7Ce AT= f1~ (from Tahlp) = Pvw = 0. (oOO^ (Ps-Pvw) x (AT) 2800-(1.3xTw) ?? )< /•&- ) O.Vlb '"A? in. Hg in. H_0 2 in. Hg °F °F °F in. Hg in. Hg 2800 -(1. 3 x Proportion of Water Vapor by Volume = Bws - - ( OMlif } WVVd Tamp. OF 0 10 20 30 40 SO 00 70 BO 90 100 110 120 130 140 150 160 170 160 190 200' 210 220 230 240 (f 0 0.0376 0.0031 0.1025 0.1047 0.2478 0.3020 0.5216 0.7392 1.032 1.422 1.932 2.596 3.446 4.525 5.661 7.569 9.692 1240 1549 19.01 23.47 28.75 3540 4241 5044- 3s) 1 0.0398 0.0660 0.1080 0.1716 •0.2570 0.3764 0.5407 0.7648 1.066 1.467 1.992 2.872 3.343 4.947 6.034 7.799 9.999 12.48 1943 19.42 2348 2943 3948 43.11 91.78 O.oit ttY. ( 2«.&7 ) ^ VAPOR PRESSURES OF WATER _^j?- \ In Inches of Mercury 17/7 2 0.0417 0.0696 0.1127 0.1803 0.2077 0.3906 0.5601 0.7912 1.102 1.313 2.052 2.749 3.642 4.772 6.190 7.992 10.12 12.77 19.98 19.94 24.46 2942 3947 4942 52.70 3 0.0441 0.0728 0.1186 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.829 3.744 4.900 6.390 8.190 10.36 13.07 16.34 2047 2447 30.82 3747 44.74 9348 4 0.0403 0.0768 0.1248 0.1955 0.2091 0.4203 0.6009 0.8462 1.175 1.610 2.176 2.911 3.846 5.031 6.913 9.391 10.61 13.37 16.70 20.70 25.48 31.13 37.78 4847 5442 5 0.0489 0.0610 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2443 2.995 3.994 5.165 6.660 8.557 1046 13.67 17.07 21.14 2640 31.75 3840 4941 5940 6 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.083 5.302 6.850 8.767 11.12 13.98 17.44 21.99 2043 3248 3944 4747 5940 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4666 0.6669 0.9352 1.293 . 1.765 2.379 3.169 4.174 5.442 7.024 6.981 11.38 14.30 17.82 2249 2747 3342 3949 48.14 9741 a 0.0571 0.0932 0.1502 0.2292 0.3304 0.4858 0.6903 0.9666 1.335 1.819 2.449 3.259 4.289 5.585 7.202 9400 11.69. 14.62 1841 CT.H 2742 3347 40.79 4949 5943 9 0.0598 0.0982 0.1567 0.2383 0.3493 0.9039 0.7144 0.9969 1.378 1.678 2.921 3491 4.409 5.732 7.384 9.424 1142 1449 1941 2249 29.19 3449 4142 4949 5947 ^ ------- 3UC3 CZ3 METHOD 18 FIELD DATA SHEET Plant: Date: OS <3 Location:. Run #:_ Stack I.D.:_ Pbar: M.1 - /-3 Sample Tube #t Ae"-JL-fliyAig-l.a4g Operators: T4/awis'. Post: - Leak Check: Pre: Time Travcra* Point Number 3 Gauge Vacuum (Hq) 0 0 0 O 0 Velocity HMd O-7 no O9 / OS 10 ,/o/u Row Setting Stack T.mp. -79 7 "' 71 Tested Anaiyte: Orifice Tank #• Pump/Rotometer #:_ Pt: Pretast (mm Hg): /ecofr. Post-Test (mm Hg)-__f_2£o(/ Tt: Pretest f F): Post-Test Time: Start: <5HI Finish: liHi Total: ljb»»«v> Md - (0.44x%CXl2) •!• (0.32 X%O2) + (0.28 X1,^) Md - (0.44 X ) + (0.32 X ) + (0.28 X ) %H,0 l-T3-> .)ie(--.) °n (°F4«o) i- Mdx(1 %H20 ~Tob~J 100 M«- ') Te- 13.8 P«- 'Z<8.«7 In. Hg 13.0 V« - 85.40 x Cp: V« - 85.48 X ( xJSPx^ PsxMt )x Qs- Qi^,- Qs x 17.647 x ~^- ttd T, xflO 100 Qi^,- X 17.847 X- 100 ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: 1.4&C0 r/^JLc.^ Location: /^V^***. e fa. Site: ]}„ : ftfr/-3 Date: £ Phar= ^9. f2 Pg = -.£6 Ps= Zt.tl Tw= (03 Td= 81 AT= /<£ Pvw= £^222- (AT) r/7> in. Hg in. H_C 2 'in. Hg '°F °F °F in. Hg 2800-(1.3xTw) •fc )x( p. 2800-(1.3 x Proportion of Water Vapor by Volume = Bws ) (Ps) T«mp. OF 0 10 20 30 to 50 00 70 00 90 100 110 120 130 140 150 180 170 160 190 200 210 220 230 240 0 0.0370 0.0031 0.1023 0.1047 . 0.2478 0.3020 0.5218 0.7392 1.032 1.422 1.932 2.598 3.448 4.525 S.381 7.589 9.852 1220 1529 19.01 23.47 28.75 35.00 4241 5044- 1 3.0398 0.0600 0.1080 0.1710 0.2570 0.3764 3.5407 0.7848 1.068 1.467 1.992 2.872 3.543 4.847 6.034 7.759 9.885 12.48 15.83 19.42 23.98 29.33 35.68 43.11 51.78 in. Hg ( 2.«7 ) VAPOR PRESSURES OF WATER •'' ?f. ? _ In Inches of Mercury 2. ~7( &. f 2 0.0417 0.0090 0.1127 0.1803 0.2077 0.3900 0.5601 0.7912 1.102 1.513 2.052 2.749 3.842 4.772 6.190 7.952 10.12 12.77 15.98 19.84 24.46 2942 3847 4342 52.70 3 0.0441 3.0728 0.1100 0.1078 0.2782 0.4052 0.5802 0.0183 1.130 1.561 2.114 2.829 3.744 4.900 0.350 8.150 10.38 13.07 18.34 2027 24.97 30.82 37.07 44.74 5345 4 0.0403 0.0708 0.1248 0.1955 0.2891 0.4203 0.6009 0.8402 1.175 1.610 2.178 2.911 3.848 5.031 0.513 8.351 10.61 13.37 18.70 20.70 25.48 31.13 37.78 4847 5442 5 3.0489 3.0810 3.1302 0.2035 0.3004 0.4359 0.8222 0.8750 1.213 1.660 2243 2.998 3.954 5.185 6.680 6.557 10.88 13.67 17.07 21.14 28.00 31.75 3840 48.41 5540 6 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.083 5.302 0.850 8.787 11.12 13.98 17.44 2149 2843 3248 3924 4727 5840 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4688 0.6689 0.9352 1.293 1.765 2.379 3.189 4.174 5.442 7.024 8.981 11.38 14.30 17.82 2245 27.07 yyp; 3949 48.14 5741 8 0.0571 0.0932 0.1502 0.2292 0.3304 0.4858 0.6903 0.9668 1.335 •1.819 2.449 3259 4.289 5.585 7.202 9.200 11.65 14.62 1821 2242 27.82 3347 40.78 4ffffj 5843 9 0.0598 0.0982 0.1587 0.2383 0.3493 0.5035 0.7144 0.9989 1.378 147S 2.521 3481 4.406 5.732 7.384 9.424 1142 1448 1841 2249 28.18 3443 4142 4043 5947 #J ------- a at » • Plant: t-ASCte Data: 2-M-4 Location Run#: METHOD 18 FIELD DATASHEET Tested Analyte:_ Orifice Tank Stack I.D.: Pbar: Z. 9± - 7-2 Sample Tube Operators: Leak Check: Pre: iX Post:. Time 3 i Gauge Vacuum (Hg) 0 0 Point Number D Velocity HMd Flow Setting Stack T.jnp. 170' Pump/Rotometer #: A/^v Pt: Pretest (mm Hg);_ Post-Test (mm Ha): .010 Tt: Pretest CF):. Post-Test /< Time: Start: rag Finishing Total: - 02: - Md - (0.44 K %CX>2) + (0.32 X Md-(0.44K 0 ) -M0.32X + (0.28 X %r4j) )+(0.28X 7f %H2O ~^b~; f " ln.HQ V«.«5.48xCpX VAP X pxM« V« - 65.48 x ( v«- 32.7^ «/• .# ------- 3 aca i_^ GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Sampling Location: Run#: 9- / - / Date: S'-)V-97 Clock Time: Operators: Static Pressure, in. Barometric Pressure, in. Hg:,9?. ,ao ,31 ,^6 /ClG / 10 , /q f /o <^o rQ^ ,op Stock T«mp. °F I&G IL'1 \(,. ^ JbA /,? /e If, 7 //,^ m (1 r> ,-o i /••) j TJ- /(,» Md - (Q.44x%CC2) Md - (0.44 x & } > (0.32 X t/ ) f (0.28 x 7? ) M« • Mdx(l %H2O 100 " 100 ) x(1 - - 100 13 ) + 18(-^_) 100 13.0 P«- in. Hg V.. 85.49 XCPX^PX -= I TsfR) V«- 65.49 X( A.. .77 )x( as- 32.^ x J.i3 xeo «n - QlX1 7.847 X — x(1 Tl 100 CJi^,- X 17.647 X- 100 ------- Plant Sampling Location $-t Run Number 9 - / • ^ Date: JJTW-^^ Pretest Leak Rate: tOQc cftn @ i£ in. Hg. • • - • i i i ^^ —- Post-Test Leak Rate: . g&c cfm @ /<£_ in. Hg. Post-Test Leak Check: Pitot: wx) Orsat: - FmwM Point Number Sampling Time (mln) /0 Po r?o Clock Time (244iour dock) J24o iteo /3oo I>IO GM Meter Reacting (Vm)n3 4/ 11 $,-)!> <)H?>W> . - Velocity Head (Ap) lnH2O Oriic* Pressure Differential (AH) in H20 Desired \| Actual Stack Temp. a^ • Temperature °F Probe '/////////////////////////////////' APr^ /• W y- fxd \| Filter Impinger Temp. °F Dry Gas Meter Temp. Inlet (Tm in°F) Outlet (Tm out°F) Pump Vacuum (in. Hg) y////////////////////////// 9H ^ y<^> 73 7^ 9^ V * * ^ T«= ~ Tm= ------- SAMPLE RECOVERY DATA PLANT DATE Run No. Sample Box No. A/-/ fab No. . Qg>3 SAMPLE LOCATION TRAIN PREPARER Filter No. A/fr SAMPLE RECOVERY PERSON , ELL. COMMENTS FRONT HALF Acetone Container No. Filter Container No. Description of Filter EPA. 4 IJ vx^U. Liquid Level Marked Sealed Sealed Samples Stored and Locked BACK HALF/MDTSTpKF, Container No. Liquid Level Marked Sealed IMP. NO. 1 2 3 4 . 5 6 CONTENTS ZVT «,o nr »,c £vWv &/,-.« (^1 TOTAL INITIAL VOL (ml) /CO /OO — 200 WEIGHT fgranui INITIAL (iC..S 606, V ^72 ^26.fi 25 2> t.^ FINAL b^?,l tO^.8 44TA fi2>!.3 254S-0 NET ' Z.\o o.4 o.bck^ad 4.S &>l^r$' n/ ------- ^ OC3 f ~3 fcs EPA METHOD 4 MOISTURE CALCULATIONS PLANT: LEA(LO SOURCE/RUN ' 3.-1-2- DATE: 5-14- scf wstd 4. Percent Moisture, by Volume R - VWSW DUL/C -~ ~ V -»• V wstd mstd Bws = ^= O.Oife I.S % Ptoi4TURE ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: • / 7 - ~; j ung Location: f>/ry Static Pressure, in K,n- -,~>V jre, %: \ .-frS^ _ Molecular wt., Drv: Z«.6^ Pilot TubB^Co: . ^ Dimension, in. Diameter or Sid ulb,°F: - nrv nra* lint nter ( Is 3 V 5 V / •i. * V b ^ V.loeny H««d in. H20 ,/^, '90 rSf -3\ -90 ,93 ,/v ,/<3 _.^/ .^a ,53 .SI fip-o,vni Stock T«mp. °F /?/ /'75 /7 3 /7V /7V y7V /7V /7/ ^75 /7 V /7 Y /9V ft- 1-73 81: -l^t* Side 2: Bulb.°F: Md - (0.44 x %CO2> + (0.32 X %O2> -t- (0.28 X %l^) Md - (0.44 x ) * (0.32 X ) + (0.28 X ) M«- Z£.S>, °F- V.B3 °R(0F460) P« M Ok j. ^-" _ / -iQ Li.rv \ j. "T?-"^O 13.8 -(2&&D)+ ,38 P«- ^."H In-Hg ^-c.M-1>1 r= J Ts ^R) V.- 05.49 »CpxVAP x ^ P9XMB V. .aSdflV( T<^ )»( MH>\ )»J ,., ^»£2> V »>M • ^«.. v«-32>.»fc ft/« A.- \.Z3 ft2 Q» - VixA«xeot/m g^ Qi-jfciW^ x x80 °»- tM^^ ««n Pt ^K.0 Q« •4»Q«xi7.e47x x(t. — — ) •" T« 100 a, -n X1TMTJ1 ^M i.& «» toib '« QMd- 1^2^- d«tai~ ------- RELDDAiA^FiEET Plant Sampling Location Run Number: 9-/~ 3 Pretest Leak Rate: Date: cfm Sample Type: in- Pbar CO2: Operator: Ps: O2: — 15 in. Hg. Probe Length/Type: Pilot: - Nozzle ID: — Thermocouple #: Assumed Bws: 1.8%. Filter #: —• Meter Box #: // Y: ..^ C_AH@: Post-Test Leak Rate: .^c,g_cfm @ in Pretest Leak Check: Pilot: Mrt Orsat: - Stack Diameter: 15 As: 1.2. 3 fl-* Post-Test Leak Check: Pilot: N/3 Orsat: — Point Numto V ; Sampling Tlnw (rrtn) D /O 2* 3e> • CkxfcTbM (244iour dock) /5<^ /^5V?' /ew It/0 GaaMeUr Reading (Vm)«3 949. 7f^ 75?, 3 #** •fo. ?^» . Velocity Head (Ap) inHZO Oriica Pr«Mur« Differenlial (AH) in H20 Desired Actual Stack Temp. as) Temperature °F Probe '/////////////////////////////////S ^7 /.1 t. °) Filter knpinger Temp. °F Dry Gas Meter Temp. Inlet am in°F) Outlet (Tm out°F) Pump Vacuum (in. Hg) '///////////////////Y/////// t> * ^^ i ?# z ?g ? 1 ? ------- SAMPLE RECOVERY DATA PLANT ^-^CO DATE 5-l4--<=n SAMPLE LOCATION Sample Box No. /1/--5 OVEM q ~^c Sealed Sealed Samples Stored and Locked BACK HALF/MPTSTTTRq Container No. Liquid Level Marked Sealed IMP. NO. I 2 3 4 5 6 CONTENTS AT tfcC PT rt-,o £=-v"/?J-y £kif\ TOTAL INITIAL VOL (ml) /o o /oo • 2.00 WEIGHT (gnnii INITIAL •5&8.0 -5T7.Y yfe? 7^/o Z4o^ rL FINAL 57^,5 S&8.Z. 4^3,4 71>5.& 24113 NET • z.e o.a O.(o 4, a a. T ft ------- r=~ EPA METHOD 4 MOISTURE CALCULATIONS PLANT: Lfr.^0 _ _ SOURCE/RUN #:_iik2i_ DATE: 5-/4-f7 1 . Leakage Correction for Volume Metered Vmc=vm-(Lp-0.02)x0 Vmc=( )-( -0.02) x( * ft3 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) Pbar+(AH/13.6)N Vm = 17.64 xV_rxYx mstd mc m U4-.II8 )x(o.^t 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V... = 0.04707 x (W. - W.) std T ' Vw = 0.04707 x( a .7 ) std V.« = Q.41O set wstd 4. Percent Moisture, by Volume V WS= w wstd wstd mstd ( o.4lo ) 0.410 — l.fe % Moit>TuR.C .a ------- Date:__^ Location: Run #: Q- /- Stack I.D.: Pbar: METHOD 18 FIELD DATA SHEET Tested Analyte:_ Orifice Tank #:. Pump/Rotometer #: Pt: Pretest (mm Hal: . ceo Sample Tube Operators: Post-Test (mm Hq)> • A \ , IQ i /# r£O \ SUck Temp. °F &£ "> 0 )< OSltl •5QC .3/>O~ '99C cyj p^ •J30 9/<7^- 3/'7 r a?d; -°2: -C02L Md - (0.44 x %C02> + (0.32 X %a,) + (0.28 X %N2) Md.-(0.44x 0 ) + (0.32 X a. I )+(0.28x7^ o I / 0 Md- M. - %H2O %H,0 2 .7% '- 1&.& IH.HB .? ' i(°R) ^.^7 V« - 65.40 X < frr*??) X ( •V 28.15, A.- //ZZ;7 n Qt-VsxAaxflOi/m x0o ------- FIELDDAlAWiEET Plant Sampling Location <&.'«.» Run Number /&vL-/ Date pretest Leak Rate: .ooV cfm @ /^ in. Hg. Pretest Leak Check Ptot: A>^ Orsat: - Sample Type: A\ " V Operator: Pbar-^frfofr Ps: CO2: fe-a° Q2: Probe Length/Type: Stack Diameter: /t>x/> Nozzle ID: Thermocouple #: Assumed Bws: .2. > Filter: Meter Box i Pilot #: As:_L23-fVL AH@: ost-Test Leak Rate: gol cfm @ /T in. Hg. Post-Test Leak Check: Pitot: l-4A Orsat: ' — TravwM notnt Numb .,, * Swiping Tkm (mlrj CO fin ™0 OockThm (244tour dock) ;<9y^ /o^o /( ^ ;/ /o Gas Meter Raacfing (Vm)ft3 99^,^6 S ^63,90 ?// 10 0o Velocity Head(Ap) lnH2O Oil ca Pr«e«ur« Differential (AH) in H2O Desired Actual Stack Temp. fTs) Temperature °F Probe \| Filter s/// //////////////////////////////, A?& I ,U t'Zi Impinger Temp. °F Dry Gas Meter Temp. Inlet (Tm in°F) Outlet (Tm out°F) Pump Vacuum (in. Hg) /////////////////////////// - 1 ^ ------- SAMPLE RECOVERY DATA PLANT . DATE SAMPLE LOCATION TRAIN PREPARER T/?~ Run No. sample Box No. A/O Job No. Filter No. "A SAMPLE RECOVERY PERSON COMMENTS FRONT HALF Acetone Container No. Filter Container No. Description of Filter 4 Liquid Levei Marked Sealed Sealed Samples Stored and Locked BACK HALF/MOISTimF Container No. Liquid Levei Marked Sealed IMP. NO. 1 2 3 4 5 6 CONTENTS ®T #o -or iO ^W/ $ke« G-e.1 TOTAL INITIAL VOL (ml) )Q O /OO . £00 WEIGHT (gnnsi INITIAL 55?. £ 66V. 7 5/A ^ ^3y,6 25fc3.4 ». » i FINAL 557,2. btS.7 ftt.o e>&^ zztb.s NET • 6.7 l.o o.4 4.e> /£& . .£,- »- . >•. /•*/ ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: L^<^p _ SOURCE/RUN ' /o-M HAT& 5-14-97 1 . Leakage Correction for Volume Metered Vmc=vm-(l-p-0.02)x0. Vmc=( )-( -0.02) x( ft3 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) 'Pbar+(AH/13.6)N = 17.64 xVmcxYxx 'm /13-6)' = 17.64 x(23.-73S )x(o.itu )x ISM ,..^ (s^s } _dscf 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V ... = 0.04707 x (W, - W. ) w v std wstd Vw a 0. b07 SCf wstd 4. Percent Moisture, by Volume Vwstd mstd Bws = (o.bo7 2.1 % P\OI6TUR£ ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: LA^tO Date: 6'l^'9~) Sampling Lo cation: <9 Us A' ^/O 2xfiWs'T Clock Time: I32£ ~ / ~^ Ooerators: 73 /Mi. S . Barometric Pressure, in. Hg: ^ ? ^- Static Pressure, in. HoO: _!_^gBL -' ^ Moisture. %: 2, 3 tf ^ ii Molecular wt.. Drv: Zti.g'S Pilot Tube. CD: -93 Stack Dimension, in. Diameter or Sid Wet Bulb. °F: - Drv Travaraa Point Numbar A- 1 9 3 V 3 6 a- / 5 3 V b 6 ^••••M^BMUBMB^^MMi Valochy Haad in. H2O rQl ^.9-> ,9; ' /? <^? ^/ ,M ,/6 , / 1 ,-96 .-^9 .9 S XP.OV&' Stack T«mp. °F s>(/ 91) a ; •> J7/5 .9/ r •9ir .9/< -?t %3 / .9^0 910 3 n Tl. 9 /U B1: TV/<" Side^: — Rulh^F- — Md - (0.44 x %C02) + (0.32 X %O2) + (0.28 X %*£ Md - (0.44 x ) ••• (0.32 X ) + (0.28 X ) •"-Wf A-;/~ % H.O % H20 ' Ma • Mdx(1 - ) 18 ( — — — ) 100 100 Ma-( )x(l- tnn )>ia( > M.- Z^^ ^-2/r °F'^7f °(°r + «» SP • - fS'" 13.6 J(^8'/1) ' 13.8 - 2^85 in- HS ^p-^y^3 / T. («Q1 Va - tO>.4li x (J0 x VA^ « V "Tax Ma V.-85.48X, ,^ )<.*# ,xJ_iZ±-r 1 2#.tffi 1-) V.- ^VJ3 ft/a A.. /. 1^7 n2 Qa - VaxAaxeOa/m Qa- x xOO v,0«- l^."/ adm P« %H2° O»^- Q« X1 7.847 x — x(1- * • > •to Ts 100 Oi^- Xl7.e47X^ Xd* ) 100 ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Samplinq Location: djesJ A9 Zk4j<± Clock Time: M2t> Run #: /O - / - 3 Ooer^"^' PA^ /TO Barometric Pressure, in. Ha: $%< Zd Static Pressure, in. K,O: ^ 3 f ^ ^ • Velocity Head in. H^ ,41 '35 .33 ,33 .$3 ,3ti - 26 ..96 OP-O.tW Stack T«mp. °F 350-. 9-9 a 9^-3 ,^S>3 3&\ BSO W§ 222 Zl 333 9£>\ 33i\ Tf- 222.'^ 91: 7^'^ /5 Side 2: ^ ' pi,\|hOp- — . Md - (0.44 x %C02> •• (0.32 X % Sa 13.0 13-8 P»- 2^/73 "«-H8 ^SP- «/^7 — f Ts ^H) P~ J ' ' \ "' Ve - «5.48 x Cp x 4b? x y " "p, ,; ^8 V v«. 3^ 700 «/• Ae- \|.Xl? n2 Q»- V«xA»xeOi/m Q«- x xOO Q«- Z£7£3 «" Pfl %H?° 0* ...QiXl7.e47x x(1- * } td T, 100 ------- FIELD DA IA SHEET Plant: L.Jt->Lt? ling Location lumber: /£>~j t Leak Rate: 1 Leak Check v+^l£> i-2 Date: 5-#-f7 .•»£. cfm@ iff in. Hg. : Pitot: MA Orsat: - Sample Type: ft- 7 Pbar Zf.tf Ps: CO2: O O2: Probe Length/Type: Stack Diameter: K" Operator: 7^ 2.8.9- 2-J Pitot #: As: \|.23 ; -ft2 Nozzle ID: ~ Thermocouple #: — Assumed Bws: > -1"^ Filter #: ^- Meter Box #: /^ Y: #££, AH@ Post-Test Leak Rate: ga^ cfm @ /fa in. Hg. Post-Test Leak Check: Pitot: Nf ------- SAMPLE RECOVERY DATA PLANT /. h^L DATE 5- H-T7 Sample Box No. A/- 6 SAMPLE LOCATION 0\/£Ki * 10 ».A\A TRAIN PREPARER Run No. Job No. . CO Filter No. SAMPLE RECOVERY PERSON COMMENTS FRONT HALF Acetone Container No. Filter Container No. Description of Filter EPK NUruors 4 Liquid Level Marked ^ Sealed Sealed Samples Stored and Locked BACK HArF/MOTSTTTRF Container No. Liquid Level Marked Sealed IMP NO i 2 -3 4 ~ 5 6 TO] POKmrxTrr TXT it,o or y?o E«x?A/ V/,-c^ 66 6c/ RAL INITIAL VOL (ml) /CC) /OQ zoo INITIAL . $-9 A 9 662.3 VSSf 764/.^' 247 4, / WEIGHT (gnnui FINAL 5^5. a bb1),0 45UO 7t>J.t> 2.483,8 NET • 3.3 a7 D,b •5.1 w ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: LkSQD _ SOURCE/RUN ' /A-t-% DATE: 1 . Leakage Correction for Volume Metered Vmc=( )-( -0.02)x( 2. Volume Metered,,Standard Conditions (68 F, 29.92 in. Hg) Pbaf+(AH/13.6)N Vm = 17.64 xVmcxYx mstd . mc ... . .T m. Vm = 23.5 rterf mstd 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V = 0.04707 x (W, - W. ) std f ' Vw = 0.04707 x( ^, std Vw = 0.45-7 scf wstd 4. Percent Moisture, by Volume Vwstd V + V "' mstd ( 0,457 ) (0.4-57 ------- METHOD 18 FIELD DATASHEET i-'ianrz/'i^ Tested An^iy0' fyr*^ Date: 5Vy-T Orific0 T^ ' #T"? Location: ^v£0- \/b& Pump/Rotometer #: - , _.,, Run: toBD- / r- 7, M Nfr- I - 3 Pt: Pretest (mm Hg)- Z Stack I.D.: ^2^HaSr & t.s'x^" Post-Tflst (mm Hg); - Pbar: 2f.fr Tt: Pretest PR: Sample Tube # • fi/DB-/-St-. /UDB-I-3& Post-Te«?t fP)1 Time: StartMS'ft? Finish: H»* /i>y. ^>4«> /SS7. 09/4&> Gauge Vacuum (Hg) * / / / r / 1 / Flow Setting i/ ^\ £» ?j -i zl i\ Trovraa Point Number Velocity Head In.H^ Stick Temp. °F • • £. £ Md - (0.44X%C02) •• (0.32X%02> + (0.28x%N2) ^t- Md - (0.44 x ) + (0.32 X ) •»• (0.28 x ) 1? w Md" % HO % H20 ^ M..Mdx(l--^r> + l8(-j3-) Me - ( 'x'1 100 100 ^/ 93 "" ^ Te- °F- °R(°F4«0) SP. V P"Pb^TJ<< )+ 13.8 Pt . In. Hg J5P- V« - 6SM X Cp X VAP x ^ p,XMe Ve - «/• A.- n2 Q«- VexAexOO«/m OB- x xW Oe • aeftn Pi %H2° Q> ..» 01X17.647 x — X(1« ) •id Ti 100 <.«- ^'•fl4;x x(l' loo' Otgtd* dMfen ------- 3OQ S o /6 20 3<> ^ ^ ^ Plant: ^/^^^ Date: <-///-f7 Location: /l/D<3 «-^j/c/»/ ^ Run#: n/n/J- /- / Stack I.D.: 32." x ^" Pbar: ^fr.^2. Sample Tubi Operators: , 9- NDA-l-\Q M^fi'l-IH T* L_eak Check: Pre: ^ Post: "^ Gauge Time Vacuum (Hg) /&<:. 7V,$ i- Flow Setting 1.1 "if Zl ~?.i 11 z/ 21 Trov«r«« Point Numbar Velocity HMd In. H^O Stack T«mp. "F /k- f" ^^5 50 ^^ [?1 7 ^f 61 METHOD 18 FIELD DATA SHEET Tested Analyte: t& Pump/Rotometer #:_ Pt: Pretest (mm Hg): — Post-Test (mm Tt: Pretest fF):. Time: Start: iVXe Finish://?/ Total: W/B: D/B: O2: ^c CQ2: 2v W Md • (0,44%CQ2) + (0.32 X%02> -t- (0.28 X%^) Md - (0.44 x ) + (0.32 X ) + (0.28 X ) Md- -2.5.64- % K,0 % K,0 Mi-( Ma- ) + Pt • In. Hg Va - 65.40 x Cp X VAP X V« - 85.40 X ( ) X ( V«- fl/« p,xM§ )X i A.- . V«xA»x«0«/m Q»» Qs» ^rtd - Q«XI7.847x x(1 oeftn p. %H.O - X1- — •- ^Md- •x(1 ------- """Plant: Site: Wfrfr WET-BULB/DRY-BULB MOISTURE CALCULATION LASCC Location: _A/DO - Run #: Operators: f/ -l '3 Date: Pbar±-f3f Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw (from Table) = Pvw = (Ps - Pvw) x (AT) Pbar = Pg = Ps = Tw = Td = AT = Pvw = 7_tf.tfO 0.0\ L3.V>* 6V ID L .(,60^ in. Hg in. HLO 2 in. Hg °F °F °F in. Hg Vapor Pressure of H20 = Pva = (Pvw) - Pva=( 2800 - (1.3 x Tw) ) x ( 6 ) 2800-(1.3 x i Proportion of Water Vapor by Volume = Bws «.„._ (Pva) _ ( (Ps) T«mp. OF 0 10 20 30 40 50 60 70 60 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 0 0.0370 0.0631 0.1025 0.1047 0.2478 0.3020 0.5218 0.7392 1.032 1.422 1.932 2.590 3.440 4.525 5.681 7.569 9.652 12.20 1529 19.01 23.47 28.75 35.00 42.31 5044- 1 0.0398 0.0600 0.1080 0.1710 0.2570 0.3764 0.5407 0.7648 1.068 1.467 1.992 2.672 3.549 4.647 6.034 7.759 9.885 12.48 15.63 19.42 23.96 29.33 35.68 43.11 51.76 in. Hg ( i«.efl ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0096 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 15.96 19.84 24.46 29.92 36.37 43.92 52.70 3 0.0441 0.0728 0.1100 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.629 3.744 4.900 6.350 8.150 10.36 13.07 16.34 2027 24.97 30.52 37.07 44.74 5345 4 0.0403 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 6.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.87 5442 5 0.0469 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 0.880 8.557 10.86 13.67 17.07 21.14 26.00 31.75 38.50 46.41 5540 6 0.0517 0.0840 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 0.850 8.787 11.12 13.98 17.44 2149 26.53 3248 3924 4727 5640 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.961 11.38 14.30 17.82 2245 27.07 3342 3949 48.14 5741 8 0.0571 0.0932 0.1502 0.2292 0.3384 0.4858 0.6903 0.9666 1.335 •1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1821 22,sg 27.62 3347 40.75 4943 5843 9 0.0598 0.0982 0.1567 0.2383 0.3493 0.5035 0.7144 0.9989 1.378 1.875 2.521 3.351 4.408 5.732 7.384 9.424 11.92 14.96 1841 2249 28.18 3443 4142 4943 5947 ------- APPENDIX A. 1.3 Condition 2 (includes flows, moistures, and Method 18) ------- METHOD 18 FIELD DATA SHEET I Plant: £-}€,<> Tester Analyta- -Vw r~- Date: ^/'i/if Orificn Tank • ^17/3 - 2— - ocation: AM frl~-r Pump/Rotnmeter #: Run: / V J (^ A $ V 7. t, . I-® 0, 2.7 ^."27 . ?.. £oV3 Stack Tamp. If f =1 f 2- ^ 2- f 2— f »- 9 'Z— f / 10 (^) /^^ (/ 6 Md . (0.44 x ) + (0.32 X ) (0.28 X % HO % HO 70 M.-Mdx(1.-^-) + 18(-— ) "7 ' Ma-( )x(1- ) + 18( ) 100 100 M" 2&rf( ^^.(1)6 ^ Ta« ^2- °F- 5^2^-°R (°F-\|-4«0) 13.8 13.8 ^P- .5W3 1 T. XJB» ?= < 1 ' ' va - <».«* x up x «y- x ^ P, x Ma Va - 85.40 x ( ) x ( ) x \l /st0 C-' , 2 * " 1 ,v> / Qe • VaxAax80e/m Qa • x x80 /> j^/J ^^ °" 3j^T2^ "^ Jiil'P P«J /• VteU Qa.. -Oexi 7.647 x x(1- • ) s 6?t>~~- o >/ r / /-V^A^ - If^t^f^ it>£ 100 ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: /_,^0 ^^>r I orar,nn- ^ r ^,, Site: /^U, £>£,,,, Operators: Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Pbar + - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H20 at Tw Vapor Pressure of HoO = Pva - (Pvw) - D-°''03.^C kit PW«=/ rcm } (.2f.e/ - T^>; M- Run: Wf-t Pbar = Pg = -EL- Ps = 13.6 KS Tw = Td = AT = (from Tc^ei = Pvw = (Ps - Fvw) x (A"0 2SOO-(1.3xTw) ^£. fflx( ZY ) p -1 Date: $//#$ 7 ^0.«.Q^ in Hg £g OP f-L- Op 2-y -OF . (#£ _B£ in. Hq su u> i 0_3 ?.<-/ ------- cia GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Sampling Location: /£.«„ £yU~.tr Date: Clock Time: 2.-1-/ Barometric Pressure, in. Hg: "Z-ft sy Static Pressure, in. l-^O: Moisture, %: 0. 3 Molecular wt., Drv: ^gftV Pitot Tube, Cp:_» Stack Dimension, in. Diameter or Side 1: ' 7 £ Side 2: Wet Bulb, °F:__£/_ Drv Bulb. °F: 10 TrovcrM Point Number S V.tecity &-0.t/ffl Stack T«mp. 11 1* 91 S- ^V- Md - (0.44 x %CO2) * (0.32 x %02> + (0.28 x -Klty Md - (0.44 x ) ••• (0.32 x ) + (0.28 X ) "<- 28, % HO HO 100 ,00 P«-Pb + S.P. 13.0 ) + '3.8 J T9<°R) ^ Pa x MB V« • 65.40 x ( )»( )x ^ > • V« x A* x 60 i/m Qs« Q«- x «7aefcn Os -^=Q«x 17.847 x x(1 -- — ) 100 X 17.847 X- QHtd- 100 ------- Plant: Site: WET-BULB/DRY-BULB MOISTURE CALCULATION xfr Location: j-^c&^&^c / ^ Operators: - 13.6 Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of StacK = Pbar Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw (from Table) = Pvw = : (Ps - Fvw) x (A"H Run ff: //(T-2^2- Date: S/wfa? Pbar= 2-%W Pg = +. 0 I PS= 2-0,0 / Tw= (0( Td= 10 AT= 1? Pvw= .VO'. in. Hq in. H C in. Hg °F °F °F 7 in. Ha Vapor Pressure of H2O = Pva = Pva=( .5V07 ).(_90" .! A: 2800-(1.3xTw) )x( 2800-(1.3 x Proportion of Water Vapor by Volume = Bws = (Pva> = ( 0.7-W7 } (Ps) 2387 in. Hg 0.-00& 7.8* T«mp. °F o 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 0 0.0376 0.0631 3.1025 0.1047 0.2476 0.3626 0.5218 0.7392 1.032 1.422 1.932 2.596 3.446 4.525 5.881 7.588 9.652 1240 1549 19.01 2347 20.75 3540 4241 5044- 3.0398 0.0660 0.1060 0.1718 0.2576 0.3764 3.5407 0.7648 1.086 1.487 1.992 2.672 3.543 4.647 6.034 7.759 9.605 12.48 15.03 19.42 2340 2943 3540 43.11 51.70 ( 2e.&r ) VAPOP PPPSQI mcc r^e rA/A-rrrn #2^>,/ 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 15.90 19.04 24.40 2942 3047 49.92 52.70 In Inches of Mercury 3 0.0441 0.0728 0.1186 3.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.629 3.744 4.900 6.350 6.150 10.30 13.07 10.34 2047 2447 30.52 3747 44.74 534S 4 0.0463 3.0768 3.1248 3.1955 3.2891 3.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 9.513 8.351 1041 1347 16.70 20.70 25.40 31.13 37.70 4547 5442 5 0.0489 0.0810 3.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.860 2.243 2.995 3.954 5.165 6.680 6.557 10.80 13.07 17.07 21.14 20.00 31.75 3040 4041 5540 e 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.001 4.083 5.302 6.650 8.707 11.12 13.90 17.44 2149 2043 3240 3944 4747 5040 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 6.901 11.30 1440 17.02 2245 2747 3342 3949 40.14 5741 -2, a 3.0571 3.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.819 2.440 3.259 4.289 5.585 7.202 9400 11.65 14.02 1041 2242 2742 3347 40,75 4843 5043 72.1 9 0.0598 0.0982 0.1587 0.2383 0.3493 0.5035 0.7144 0.9969 1.370 1.075 2.521 3451 4.400 5.732 7.304 9.424 1142 1440 1041 2249 28.10 3443 4142 4843 5947 -, & ------- 3 ag i-za GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: L&CO /^J^-t - H»-~ ^ Hate: evY/* 7 S R B k S V ampling Loc un#: A atiorv A4/« gx&+~r Clock Time: 2.30 if-i-i orwatnrs' t ^,^2- Stack T«mp. °F tz- ?t> . to ]0 9o <2>% <3? g? ^f fO 90 ? . 1 •\- 17-f* Side 2: -~ nlh.Op- ^7 Md - (0.44x%CO2> •»• (0.32x%O2> + (0.28 X%f^) Md - (0.44 x 0 ) + (0.32 x 2 / ) * <°-20 x ^T ) Md - 2.&?f % HO % H20 100 1^O Mt- Z^."?^ CD 9 ^U Pl"Pb'l"3.C (M™ 13.0 P,. 2-f.f^ ln.Hg /is* 52^ x 00 t/m Qt- x x«0 0.. -1^2,7^ adm ?• %^°, Q -,-QiX 17.847 x x(1- * ) nd fs '"•• I a Lff-.fflafcRS-l? 1 Q>--3"»-'- X17.647X ^ ML^ ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: Lh$to Site: ty/lfM ^xwdUA-f- Ooerators- Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Pbar ^ - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw ..<••?• V Vapor Pressure :o1 Ho O = Pva = (Pvw) - Pva=/ «/«n . ( f.tf - • 2800 -(1.3 Location: ffltl A £•* •rtV/fJt Run #: Aie-z-3 Pbar = Pa = -^L. PS = Tw = Td = AT = (from Table) = Pvw = (Ps - Pvw) x (AT) 2800-(1.3xTw) 7l)x( 2? ) x Cel ) W^f- • Date: 5-;V-^7 Z«.^V in Mr, » ^^ in W 0 2 f. W in Hg L,\ OP rl QC ^f °F •Wl in Hg 2^ #" in. Hq Proportion of Water Vafaor by Volume = Bws Tamp. OF o 10 20 30 40 50 60 70 60 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 (Ps) 0 0.0378 0.0831 0.1025 0.1647 0.2478 0.3626 0.5216 0.7392 1.032 1.422 1.932 2.596 3.446 4.525 S.661 7.569 9.652 1240 1549 19.01 2347 28.75 3540 4241 5044- 1 0.0398 0.0880 0.1060 0.1716 0.2576 0.3764 0.5407 0.7648 1.066 1.467 1.992 2.672 3.543 4.647 6.034 7.759 9.885 12.48 15.63 1942 2346 2943 3948 49.11 51.78 ( zffV ) y- VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0896 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 15.98 1944 24.46 2942 3647 4342 5&70 3 0.0441 0.0728 0.1180 0.1876 0.2782 0.4052 0.5802 0.8163 1.138 1.581 2.114 2.629 3.744 4.900 8.350 8.150 10.36 13.07 18.34 2047 2447 30.52 3747 44.74 534S 4 0.0483 2.0766 3.1248 3.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 8.513 8.351 10.61 13.37 16.70 20.70 2548 31.13 37.78 4547 5442 5 0.0469 0.0610 0.1302 0.2035 0.3004 0.4359 0.8222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.680 6.557 10.86 13.67 17.07 21.14 2640 31.75 3840 4841 5540 & 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.850 8.767 11.12 13.98 17.44 2149 2843 3248 3944 4747 - 5840 7 0.0541 . 0.0892 0.1429 0.2203 0.3240 0.4686 0.6689 0.9352 1.293 1.765 2.379 3.189 4.174 5.442 7.024 8.981 11.38 14.30 17.82 2245 2747 3342 3949 48.14 5741 a 0.0571 3.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.819 2.449 3.2S9 4.289 5.585 7.202 9.200 11.85 14.62 1841 22.52 2742 3347 40.75 4943 5843 9 0.0596 0.0982 0.1587 0.2383 0.3493 0.5035 0.7144 0.9989 1.378 1.878 2.521 3.351 4.408 5.732 7.384 9.424 11.92 14.98 1841 2249 28.18 4142 4949 5947 ------- r METHOD 18 FIELD DATA SHEET Plant: ^^co fa^ &,<>.< Tested Ana'vte: SAyu. — C L F g F c C L o ft- " 1 Z4 r ; o ifc °* ,!K <"* r » >>&<, ~— §>5" late: 5/A//V 7 Orific« T»"i< ' '"^ '/ ocation: ^^>^ £>4u/><. Pump/Rntnmeter #: lun#: #£-T.-l Pt: Pretflst (mm Hq): tack I.D.: 2-«/ * •« v Post-Tact (mm Hg): 'bar: i.fl# Tt- Prntflst I°FV ... - >ample Tube Operators* ^- Ac--L-f Rost-T««t fF)' szX/'tff Time: Start' *** Finish: ^ zi- Total: 6 o — eak Check: Pre: i-^ Post: ,/ W/B:^I D/B:^^O0: - COr,:^ — /9, i?i?3 »y /& /?. tf#o ^r 2-" Gauge Time Vacuum (Hg) 10 X-O »»- 767f.5ifl ' lo 1 0 ^&^» 7^2.^ / 20Vt. . £$> 76>eY, 35 / 2x>* i-* • / &££> 7e~7L1 4,2-1 / Flow Setting & $ - ZSocc. *> o.l 0.3 0.2 A3 s Traverse Point Number / I. $ Y } L g t i. > V £ c> 0 ( 1 3 V > (> P 1 2, J V $ (o #I^#£ O,ol o. 07 P.Ot 0.*.o% 0. D7 O.OCe o. ?7 0.0% o.t>l b.oV, o.O 7 Q>. 0(s 6> o(e &.&( o.oie 0. 05 0, 0$ O.Ole 0. 0(e V, 740-7 Stack Temp. °F 8(* <§ D/.t/ dedm** ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: LA^o fi^JL.* Site: /$L«~ ^.C^r Operators: Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar 3 - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw Vapor Pressure of H^O - Pva - (Pvw) - P™ =<<„., 7 ) '.?** •••« Location: /^st/Vv~_, /t^ A£/^ Run #: J>£-T,-\ Date: / Pbar = 2.«. ff/ Pq = -'.66' -mT Ps = ^ 7? 13.6 Tw = 7 )X( 2-/ ) £> 32,^ '/V/ 7 in. Hg in. KLO 2 in. Hg °F °F °F in. Hg in. Hg •••"-' ' 2800-(1.3 x Proportion of Water Vapor by Volume = Bws (Ps) Tamp. OF 0 10 20 30 40 SO 60 70 60 90 100 110 120 130 14O 150 160 170 180 190 200 210 220 230 240 0 0.0370 0.0031 0.1025 0.1647 0.2478 0.3020 0.5218 0.7392 1.032 t.422 1.932 2.596 3.444 4.525 5.081 7.589 9.652 12.20 15.29 19.01 23.47 28.75 35.00 42.31 5044- 1 0.0398 0.0600 0.1080 0.1710 0.2570 0.3764 0.5407 0.7648 1.006 1.467 1.992 2.672 3.543 4.647 6.034 7.759 9.885 12.48 15.63 19.42 23.96 29.33 39.68 43.11 51.76 0.011 ( 23.7? ) i VAPOR PRESSURES OF WATER 5"? >, } In Inches of Mercury 2 0.0417 0.0096 0.1127 0.1603 0.2077 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 15.98 1944 24.46 2942 3647 4342 52.70 3 0.0441 0.0728 0.1180 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.829 3.744 4.900 8.350 8.150 10.36 13.07 16.34 2027 24.97 30.52 37.07 44.74 5345 4 0.0463 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 6.513 8.391 10.61 13.37 16.70 20.70 25.48 31.13 37.78 4847 54.62 5 0.0469 0.0810 0.1302 0.2035 0.3004 0.4359 0.0222 0.8750 1.213 1.860 2243 2.998 3.954 5.165 8.680 8.597 10.66 13.67 17.07 21.14 26.00 31.75 3840 46.41 5540 a 0.0517 0.0840 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 0.850 8.767 11.12 13.98 17.44 21.59 2643 3248 3924 4727 5640 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.981 11.38 14.30 . 17.82 2245 27.07 3342 3940 48.14 5741 — — z 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9668 1.335 1.819 2.449 3259 £289 5.585 7.202 9200 11.65 14.62 1821 2242 27.62 3347 40.75 4043 5843 7-°.7 9 0.0598 0.0982 0.1587 0.2383 0.3493 0.5035 0.7144 0.9969 1.378 1.875 2.521 3.381 4.406 5.732 7.384 9.424 1142 1446 1641 2240 28.18 3443 4142 4043 5047 .-. ve/ ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: LASCO fi^JL,.*- /?£.-&, ^ Date: //v/7 Sampling Location: fo~* exU^i- ' Clock Time: 2.205 Run #\ ft £"- 2.-Z— Onfirarors! ^X/-7> Barometric Pressure, in. Hq: 'iG.lf Static Pressure, in. HoO: -'I U» Moisture. %: / O Molecular wt. Drv- ^fteV Pilot Tube. Co: .77 Stack Dimension, in. Diameter or Side 1 : 2V '' Side 2: 'Z^ Wet Bulb. °F: £ c T. .3 V 5 fr 6 ' i. 3 V* 5 0 C 1 2. 3 V $ (, D < i. 3 V 5 b Vateety Haad !n,H2O 7 ^>.t?f ^. ^ft A ^« ^?^7 ^.0T ^.^ ^,l 0.0-J 0.0 O.o-l 0.0-7 0.0 M.- ^«-73 T:. ^>"2.«F. ^vz, °R(°P.4«» C D Pa • Pb -t- i ( ) t . 13.8 ' 13.8 P«- T&.II In. Hg ^P-/17?7 — / Ts (^R) Va-6b.4WxCpxV5P x ^ P9JCM9 V«- (f.l^ (t/t A.. ^01 ** Qs> x x60 0»- £j 'hi/ft «n - ^y ^/ x/ ^ -•..•. Pi K,O Qt .^-Qi XI 7.847 x x(1- —2—) •W !• 100 ' Q»rtd" X17.847X x(1"1oB^ ------- 30C3 - _ WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: ^Mrj> /L^s* - £ Site: /?^w ^r£* Pbar = 2-fc e«/ Pa = — . b(f Ps= ^8.7? Tw= <^ Td= e»- AT= l-l- = Pvw = A 5"2^8 ix (AT) V7 in. Hg in. HO 2 in. Hg °F °F °F in. Hg ) 2800-(1.3xTw) )x( 2.2- ) 2800 -(1. 3 x Proportion of Water Vapor by Volume = Bws (Pva) ( a in. Hg (Ps) Tamp. OF 0 10 20 30 40 so 60 70 60 90 100 110 120 130 140 ISO 160 170 180 190 200 210 220 230 240 ( 2-S.7? ) VAPOR PRESSURES OF WATER In Inches of Mercury 0 0.0370 0.0031 0.1025 0.1047 0.2470 0.3020 0.5210 0.7392 1.032 1.422 1.932 2.596 3.446 4.525 5.801 7.569 9.652 1220 1529 19.01 2347 28.75 3540 4241 5044- 1 0.0398 0.0660 0.1 080 0.1710 0.2576 0.3764 0.5407 0.7648 1.066 1.467 1.992 2.672 3.543 4.647 6.034 7.759 8.885 12.48 15.63 19.42 2346 2943 3S48 43.11 51.76 2 0.0417 0.0090 0.1127 0.1003 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 0.190 7.952 10.12 12.77 15.98 1944 24.46 2942 3647 43.92 52.70 3 0.0441 0.0728 0.1188 0.1670 0.2782 0.4052 0.5802 0.8183 1.136 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.36 13.07 16.34 2027 24.97 30.82 37.07 44.74 5348 4 0.0403 3.0760 0.1248 0.1955 0.2091 0.4203 0.0009 0.8402 1.175 1.010 2.178 2.911 3.848 5.031 0.513 0.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 4847 5442 5 0.0409 0.0810 0.1302 0.2035 0.3004 0.4359 0.0222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.680 8.557 10.86 13.67 17.07 21.14 2640 31.75 38.80 4641 33 JO 6 0.0517 0.0040 0.1370 0.2110 0.3120 0.4520 0.0442 0.9046 1.253 1.712 2.310 3.061 4.063 5.302 0.850 8.767 11.12 13.98 17.44 2149 2643 3248 3924 4727 5340 7 0.0541 0.0092 0.1429 0.2203 0.3240 0.4666 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.981 11.36 14.30 17.82 2248 27.07 33.02 3949 48.14 5741 a 0.0571 0.0932 0.1502 0.2292 0.3304 0.4858 0.6903 0.9060 1.335 1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1821 2242 27.62 3347 40.75 4949 5843 !/ £V-7 2-Tzlr- 9 0.0598 0.0982 0.1507 0.2383 0.3493 0.5035 0.7144 0.9989 1.378 1.878 2.521 3451 4.406 5.732 7.384 9.424 1142 14.98 1841 2249 28.18 3443 4142 4943 5947 ,~l ------- UfflQ CJ GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Date: Sampling Location: <£«,, £">< £«^>««- " Clock Time: 2 3$^ He-?.-** Onprators- X* /?# Barometric Pressure, in. h Moisture. %: /. / q: ^S.tY Static Pressure, in. hUO: %—^ ^'' MolprularAArt, nrv 2A firV PitOt Tube, Cp: „ T7_ ._ Stack Dimension, in. Diameter or Side Wet Bulb. °F: (no Orv F TrovtrM Point Number fl t -^ 3 V $ If 6 \ 2. 3 V 5 k £ / z, 3 V 5 (f £ \ 2. 3 V .5 (^ Vatoeny HMd in. H20 ac^ . o. o<-f C-oti o.o^ 0,0^ 0.0& D.07 r2 03 o,o<£ O,oio fr 07 tO.cl 0. If OJO 0..&1 0,01 (0.01 O.Ot o, (o 0,li> Q.O% 0,d1 0,0(0 0,0 7 Stack T«mp. °F »o &c " <&o %o Bv QO #0 ®0 ®<0 @£> <60 #0 82- 9>\ 9>l 9)1 &( &( %1 i)\ $/ 8/ 8/ Ql X- VI 1: -2-V Side 2: 2-e 5ulbTOp- «8/ Md - (0.44 x %CXlj) ••• (0.32 X %02) + (0.28 X %N2> Md - (0.44 x ) + (0.32 X ) + (0.28 X ) Md- ^'^/ % H20 % H20 M..( )X(1.___),B(___) I — ^B O __— O O v ' t-< p ~fi I Ml P ^ 4QQ1 13.8 13.8 P« - 2^^. 77 1"- Ha — I Ts i^R) V"°""^"^X V p«M- ' A»-y^7 ft2 Ott • \Jm « A* w AA »/m o«- x xeo °«" ^o? «" Pt %H,° Qi .,-QtX 17.647 X x(1 ^-) •" T IV °«td" x 17<647 "" X ( 1 ' 100 } ------- Plant: Site: WET-BULB/DRY-BULB MOISTURE CALCULATION Location: ^C^-LJ^^. , /£ -v A^c^y Operators: j Run ~ 13.6 Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Pbar Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td • Tw = . „ Saturation Vapor Pressure of H2O at Tw (from Table) = Pvw = (Ps - Pvw) x (AT) Date: 5//y/ Pbar = Pg = Ps = Tw = Td = in. Hg 01 in. Hg °F °F °F in. Hg Vapor Pressure of H2O = Pva"=: (Pvw) - Pva=( ,S"l/fc )-- 2800-(1.3xTw) ,$W )x( 2~I ) 2800-(1.3 x fro ) in. Hg Proponion of Water Vapor by Volume = Bws (Pva) w** ------- f Plant: Date: S-M-I-I METHOD 18 FIELD DATA SHEET —. Tested Analyte:_5^/ —. Orifice Tank Stack I.D.:__nf_ Sample Tube #:. Operators: *-yvt Leak Check: 10 tm. ------- FIELD DA I A SHEET Plant: Sampling Location ft Run Number: ?-.Q- I Date: g/l	5fc> •TO Clock Time (24-hour dock) ^^i.K' ocyy^> y\/> ij^~ £0$^ ,._ Gas Meter Reading (Vm)«\|3 ^^ V;3g ;©-3 , -70 A! o .- 5^ // S"» ?V7 • Velocity Head(Ap) inH20 Oriica Preoour Differential (AH) in H20 Desired Actual Stack Temp. (Ts) •:* Tempeiature Probe Fitter Impinger Temp. °F Dry Gas Meter Temp. Inlet (Tm in°F) Outlet (Tm out°F) Pump Vacuum (in. Hg) Y///////////////////M frsfiC^ )•• ?6 I &/ \ • ?£> 1-7 \ ?9 f? "SV ^T7 5s-? ------- SAMPLE RECOVERY DATA PLANT LK-SC.Q Run No. DATE 5-11- 9~1 Sample Box No. M-5 Job No. S4-QS.6QS SAMPLE LOCATION U^N °\ Filter No. M K TRAIN PREPARER SAMPLE RECOVERY PERSON COMMENTS FRONT HALF Acetone Container No. Filter Container No. Description of Filter Liquid Level Marked Sealed Sealed Samples Stored and Locked RACK HALF/MOTSTTJRE Container No. Liquid Level Marked Sealed IMP. NO. CONTENTS bX Hi.0 TOTAL INHTAL VOL (ml) /£>£> t /0O WEIGHT (grams) INITIAL FINAL NET ------- EPA METHOD 4 MOISTURE CALCULATIONS PUNT: lA<>a> _ SOURCE/RUN #: ^-2-1 DATE: 1 . Leakage Correction for Volume Metered Vmc=Vm.(Lp-La)xe Vmc=vm-(Lp-0.02)xQ vmc=< )-( -0.02) x( ) ft3 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) P-MAH/13.6)N Vmstd (548 ) •\ , dscf 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V ... = 0.04707 x (W. - W. ) wstd T ' Vw = 0.04707 X( U-0 ) wstd vw wstd 4. Percent Moisture, by Volume _ Vwstd BW8~ w TTT mstd B W8 (0.-LB2. )+(2/,52Z ) ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: ^45 Co Date: f'/^H Sampling Loc Run#: 9~C ation: DL'JSL/l1 T* 9 Clock Time: JRSft #?^O J-3L nporntnrs- /)/V\ /££> Barometric Pressure, in. H Moisture, %:/A //<7 , 99 . aa /•3 1 xfjy ^p-0,H^l Stack T«mo. °F .v^fr- 165 I&S 1 tot> \<t, Iblo 16$ /63 I(a6 J66 ibn IbO S./^'F 1: /fX/ Side 2: nlhOp - Md - (0.44 x %CO2) + (0.32 X -fcOj) (0.28 x %Nj) ; Md - (0.44 x ) + (0.32 X ) f (0.28 X ) M-- Z?.^ % HO % HO M.-MdX(1 io(j )-lB< 1QO ) ^^ M.-< ,xO--— -)18(_— -) ^ Mi- J6.?/ ^- ((/5> °F- t^ °R ("p460' Pa - Pb * S'P' = ( ) + 13.8 '3.8 - 2^.~7°l ln-H9 ^'n^ZM — ,/ Ts^R) Vi - 85.49 X Op x VAP X U - p9 x M, Vta-3l.(^2/1 « A«- \|.W> I2 O* • Va v Aa x 00 i/m Qa» x x80 Qi- 252B «n P« H»° 0-.M- Q-17.647X — x(1 • -^j- ) Oi^- X1/.84/X (l" 100 J ------- 3 BC3 C^3 GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: LASC.O Date: Sampling Location: Run: Tfl-A -' - J& Clock Time: Operators: - Barometric Pressure, in. Hg: Gp.ft, Static Pressure, in. HoO: "> Moisture, %: /./'/• Molecularwt., Drv: 23.V Pitot Tube, CD: .'99 Stack Dimension, in. Diameter or Side 1: K" Side 2: •- Wet Bulb, °F: Trav«rM Point Number A - ? ^ 3 V .< £> A- / 5 3 y f & Velocity H«M in. H20 ,// f\t r90 '92 •W '99 , 9^3 ,93 ,29 ,21 ,99 ,99 $P -, \ Ibh /fod Ibto Jb& /£>!> '/t K>¥ ft. /6^ Dry Bulb, °F: Md - 100 Md % H,O % HO M«- Mdxd • - — 1 -r 18 ( - £-) 100 ' MI- Pa - Pb s-p- I3.fl 13.0 Vt m 65.40 x Cp 1 Vi«85.40x(, PsxMs v. ft/* .2 Q« • V« x A* x CO «/m Qs- xflO «n Qs M- Q» x 1 7.847 x - x (1 p. %H-0 - x 1 - — •- ------- FIELDDAiAS&EET Plant: C/1,i>CO Sample Type: /ty- V Operalor: DSA/d'G Sampling Loo Run Number: ition lU'rT ^ 9 Pbar 9SM?/> Ps: ^'B°> ' 33-"? Date: ^"•/V'9'7 CO2: ~ Pretest Leak Rate: . CO c cfrn @ >\ ££ , V o 6 (<> , Q Vo Velocity Head (Ap) inH2O Oriioe Presaure Oiftarential (AH) in H20 Desired Actual Stack Temp. Us) Nozzle ID: /v>4 Thermocouple #: T"(i> J? Assumed Bws: AJA- Filter #: — " Meter Box #: /f Y: /^6bAH@: htfb '^ Post-Test Leak Rate: / COO cfm @ ^ in. Hg. Post-Test Leak Check: Pilot: yX" Orsat:.-- Temperature °F Probe ) Fitter Impinger Temp. °F y//////////////////////////////////////////// /gcoct f 1 '^ 1 <$ f ]/ / 1 1 . \^> , £•-} ,££. 40 '/* ,99 '3$ l.'ft) /:<£<& It %d? rs 9k' "^ 5 r7 #)jf 0? 1^ 52 ) 9 O o. Q/ C, 5??"? g»&iO ^/^ ) ^\ ^^ ,^ \ ^^^ t^ j<_ 9&0 ••«? , -J £"} £C t-1ft Dry Gas Meter Temp. Inlet (Tm in°F) Outlet (Tm out°F) Pump Vacuum (in. Hg) '////////////y///. #-y ^t? ^3- - ^.3 S^ ^"^> 3 ^ 3 s r. is ft- ------- SAMPLE RECOVERY DATA PLANT L.teCjL> Run NO. DATE 0^XT SAMPLE LOCATION TRAIN PREPARER Q sample Box No. M-l Job No. Filter No. SAMPLE RECOVERY PERSON COMMENTS FRONT HALF Acetone Container No. Filter Container No. Description of Filter 4 v^c Liquid Level Marked Sealed Sealed Samples Stored and Locked RACK HALF/MOTSTTIRF Container No. Liquid Level Marked Sealed -^- 3 IMP. NO. 1 2 3 4 5 6 CONTENTS b? ^0 bT ^0 "/•** 3/t. ic. A £f£L* TOTAL INITIAL VOL (ml) sao /(SO SL-5TO WEIGHT (grams) INITIAL btfU c,o(o,a> 4^1.5 631 .3. WHf FINAL (0/0,0 (obl.o in* B ?.f tffV-l NET • 0.7 0,T- &,1> Z,6 5.1 1,1 ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: - Lfl^c. _ SOURCE/RUN #:^i2^_ DATE: & 1 . Leakage Correction for Volume Metered Vmc=vm-(Lp-La)xe Vmc=vm-(Lp-0.02)x0 Vmc=( )•( -0.02) x( ) ft3 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) P-MAH/13.6)N m ( <«>) + < / 6U /13.8) )x dscf 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = Vw = 0.04707 x (W, - W.) wstd v f •' Vwst(j = 0.04707x( 5\ i v,. AD, 4. Percent Moisture, by Volume V,.. BWS= • wstd V w •• m wstd mstd Bws = ( . 2101 ) 0. ------- j aa L- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Sampling Location: Run #\ /O ~3 - / Date: f'H- Clock Time: =9 Operators: Barometric Pressure, in. Hg: ffg-JC _ Static Pressure, in. HUP: - Moisture, %: — — Molecular wt., Dry: _ Pitot Tube, Cp: Stack Dimension, in. Diameter or Side 1: /£' Wet Bulb. °F: — Dry Bulb,0F:. Side 2: TravcrM ^_l_.A KOfnt NumMr .4 • / V V .r Velocity Head in. H2O ,?£> ,31 r IX Stack T«mp. °F 7 9) Md - (0.44 x %CO2) + (0.32 X %Q^ + (0.28 X %Nj) Md - (0.44 x ) * (0.32 X ; • (0.28 X Md - Ms • Mdxd MS- ( 100 % H.,0 . ico 100 100 Ms Pa.Pb p.- 13.0 Vi « 65.4Q x Co X Vt • 65.48 x ( T3 (°R) Pax Ms ) x ( Q» • V« x A* x 00 «/m Of- Q,. xeo adm Ps •M^lV Ts X 17.647 X- 100 ------- METHOD 18 FIELD DATA SHEET 3lant: L/ttCO Tested Analvte: Sfy/^-t Date: 5" H -S ) Orifica Tank #• 1 ( I ?1/ '^ «3 -7S- 5Sb-^^ JVI? \ , 7^ ttH '53 >h ^' \J)6".35 ,s-^ ocation: ®tf CW£ .ct&&£')\ Gauge Time Vacuum (Hg) i^co O 3900 O »5130 ^ aa-so o &>^0 O 3£ £"° 0 3300 o STrtTKL -.'{$"3 Trtveree Point Number 4-f a ^ ^ < &> n i 3- j y Velocity Heed In.H^O //O tiL ,n . i f ,1 ? ^^>^/ ' ]<^ .S& ,9^ . Q.K . 1 / l<4 Flow Setting $& Cti/^ \ / >// Stack Temp. 917 3 /-> J)-7 ? /» 391 '4W 3>~> §^O &&0 &ac 3d/ <$dl 6 W/B:/l'.4 D/B:A;/» O«: CO0: Md - (O.WxttCCy -l- (0.32 X%02) + (0.2BX%N2) Md.(0.44x )-\|.(0.32x )-f(0.28X ) ¥&- I** ?/' %H,0 %HO ?7/j£--Md(1--!»f) + ia( — ' J •8'3'Um -1 IvH l-t-181 ) Me • ( )xn- — r=— ' f'oi » fS/S^-7 1°° ^7 2e^ Ta- OTTj °F- (c,&0 °R(°F4«0) ^VP? fc- ""•&-< ^•tD)* -rlr- P«- ^.H ln.Hg ^p . 0 .42-5D «. ^f \I T8(°R) Ve - 85.48 x Cp x VAP x W paxMe V.-3^.UfS ft* Ae- ft2 O»- VaxA«xeo«/m Q,. \|.72V x x80 08 • ^^/P^ "" p. %H,0 Q»^,-QiXl7.B47x x(1- — •-) •W te 1°O ^ud' Xir(fl dedm ./if ------- FIELD DA IA SHEET Plant: Ln5(LO Sample Type: Al- / Operator: &&&/&!> Sampling Loci Run Number: ition £>l)gUV &-JO Pbar.9$ffC Ps: Zfi.^H / /0-2-3L Date: 5"-/i''97 CO2: — — O2: -^ Pretest Leak Rate: -Oco cfm@/s in. Pretest Leak Check: Pitol I Traverse Number Sampling Time (mln) O Jc> 9Q 30 dock Time (244iour dock) '3301 a&n 333( &&3f y t"4 : A'Ar Orsat: /t Gas Meter Reading (Vmjft3 ;^x9^3 .9£ ' ^7 O 3»V >To Vd / S'/ f»= 2.3.75?' v£p= "~ AH= l,ft(j ^^Ts= • -''•»- •.»••:«./' ,^ ^? ^9 5'^ • 'V ^L 9^>" ^^ '"- '-'• ^9 56 &3 Pump Vacuum (in. Hg) ^t {.£ (,5 s> ^^ 1 x« ------- =355 SAMPLE RECOVERY DATA PLANT Run No. - 2.- DATE 5//c/7V Sample Box No. NJ-la Job No. S4QS . QO3> SAMPLE LOCATION ^"^ 1° ^V^tfA Filter No. M/A* TRAIN PREPARER SAMPLE RECOVERY PERSON COMMENTS 4- FRONT HALF Acetone Container No. Filter Container No. Description of Filter Liquid Level Marked Sealed Sealed Samples Stored and Locked BACK HALF/MOISTURE Container No. IMP. NO. 1 2 3 4 5 6 CONTENTS DX VA-2.O t>i uto eriwpry SlMCA ^EL TOTAL INITIAL VOL (ml) /> /ffO — -250 WEIGHT (grams) INfTIAL 5^6.2- Ubl).0 45b.O 7^,b ^63.8 FINAL 517.7 £6^3 ^/56// 7 75 •/ 2v\Q(b.'f NET ' 2.^ o.J o.( 3.8 •t.7" ------- 3 aa cj EPA METHOD 4 MOISTURE CALCULATIONS PUNT: ZA«Q _ SOURCE/RUN #:_/£llil_ DATE: 1 . Leakage Correction for Volume Metered vmc = V ------- Plant: Sampling Location: UN«T Run#: 19-2-3 GAS VELOCITY AND VOLUMETRIC FLOW RATE Date: Clock Time: Barometric Pressure, in. Hg: ?%. Moisture, %: \H ?6. Molecular wt., Dry:. Stack Dimension, in. Diameter or Side 1: i.V Wet Bulb, °F: Operators: £ Static Pressure, in. H2O:_ I PitotTube, Cp:. Side 2: — Dry Bulb, °F: ^ Travaraa Point Numbar A -i 2, S <-/ ^ (S e>- < 2 ? / <> L, Valocity Haad In. H2O <-V <£ /U l> . IT- •fr 2o )^2. ZO ^e ^2 ?.< ^P-O.M^MI Stack Temp. °F ^17- ^)> 2»ft J'<* Z^l 72-2, 2-»e 21 V 2-ZjC? 2-1-t 2- "2-2. i.Zo k- an Md - (0.44 X %COZ) + (0.32 X %O2> + (0.28 X %r^) Md-(0.44x J-M0.32X )-t-(0.28X ) Ma - Md x (1 - Ms- i-Pb + P.. % H-0 % HO S.P. 13.8 13.8 ,n.Hg Va - 85.49 x Cp X Va • 85.48 X ( & Va- $2rftt ft/a Aa- I-Z2LV ft2 Qa-VaxAax60a/m Qa • x 0 PsxM8 \|x( )x i x X80 adm Pa ' .-Qaxl7.847x x(1- ^—) * Ta 100 0»^- X 17.847 X- •x(1 100 ------- g_ao_c METHOD 18 FIELD DATA SHEET Plant: uflS«« C^^t/> Tsstart Analvtfi- ^A*— C L F c F c C L 0 <$ 1 5» V* 5« fo Date: s //«//« 7 Orifirp Twnk #• 7^>»e^ l/£>' \> \L»_J?. .ocation: fiJtoo-k Pump/Rntnmfiter #: lun#: x/4-2-»- pt- pretoct (mm Hg)- Stack I. D.: 3lM;t> Post-T«ct (mm Hg)- =bar: -2-».«Y Tt- Prfltnst <°FV Sample Tube Operators: #: fJOA.z-i- pc«:t.Tflet CF}- >e-A Time: Start: 22* Finish: «• Totaled -.•- .eak Check: Pre: / Post: ^ W/B: — D/B: - O0: ^ CO,,:_2 Gauge Time Vacuum (Hg) 2-^ /3J7/i / tt/^ / 3 Qtctd dtetm ------- a aa cu r=~ p D L R S P S C L O 10 I* 3o «/o k METHOD 1 8 FIELD DATA SHEET lant: LlA<>t.o fa A.** TesteH Anslyts- 5s-yu~^ ate: //v/r7 Orific° Tanu- • "xrfW» i/g ..-"3 acatiorv /J D B> Pump/Rotnnnetar #: un#: A/PB-2-3 Pt: Pretest (mm Hq): tack I. D.: 0-5" }2." Post-Test (mm Hq); bar: ^«-/ Tf Protect r°R- ample Tube Jperators: > eak Check: F O.oa #• /Vj)£-2.-Z pCct.T«ct f F) • fl4 /Ta Tim«- start:/'** Finish:/23o_Total:_i^i^ 're: ^ Post: .X W/B: - D/B: - GV,: * CO0:_2 — > ~t 11" .a ~ rtf7.it / 7A** llsMo I Mlb l-& ko 1 Wo /3^,3« / 11 to rlU.eZ f Row Setting 10 Zo ^0 2Z> ^o I O L> TrovrM Point Number Vttectty HMd In.HjO Stack T.mp. Md - <0.44x%CO2) -t- (0.32 X%02) + (0.28x%N2) £_ Llrf _ in AA w ^ ^ let 32 « ) -f (0 28 X ) 3t Md - •: 'fu ^ %H.O %HO ••• <\( M.-Mdx(1--^-) + 18(-T5r) ' ^Z M«-< )x<1 __)-.- 18 (_—-) 93 ^3 M>- ?v T.- °F- °R(°F4«0, SB ^""'^iir ( ' 13.6 Pt - In. Hg £P- S= . 1 T» <^R) vt • 99.40 x up x »ur * M Pa x Ma Vi - 65.48 x ( ) x ( ) x -U. V» • ft/a A »2 A* • R Qt - Va x As x 80 a/m Qs- x x« Q«« adm p, %K,0 Qi ..-Qi XI 7.847 x x(1- - ' ) lf ! QHtd- dMta I. ------- APPENDIX A. 1.4 Conditions (includes flows, moistures, and Method 18) ------- METHOD 18 FIELD DATA SHEET p D L R S P S C L ^25 » ^H ^7 5,j i (} j<-/5<; >£, H^t 3S) ™<* & " lant: Art5/0 TesteH Anaiyte- Vi//^^^ ate: ^-;<>'- O«: '!' CO«: O _. Gauge Time Vacuum (Hg) 226! . 3 / .3to . 31? • 33 . i^" .2.1 . ^$3^ Stack T«mp. 1L, <%& %O ?l -r/ VO 90 iij \J 4? J & t 31 5>/ 7l VO ^o ¥ C Md - (0.44 K %COZ) -t- (0.32 X %02) + (0.28 X %h^) m Mrl • (D Al v 1 -(- (0 32 X ) + (O.2B x ) % H2O % H2O f .O'f M»-( )X<1" 100 , ) + l8< 100 Ta - ^ O °p " 5^0 R ( F + «0) P. Ph t S'P- - < ) t P' Pbf 13.8 ' ' 13.8 ^SF " t) B£30 \ T. /°m r^ , \| Ta r n) ' i / -f .2 " Q> • Vt x A» x 80 «/m Qt. x X80 _ •) -> T> . »• 37/2- « ------- WET-5ULE/DHY-EULE MOISTURE CALCULATION J^chc+r _scaticn: &<£, ^ ^ oerators: Date: Pbar = Pg = Barometric Pressure, in. Hg = Static Pressure, in. M20 = Absolute Pressure of StacK = =bar •<• 3/wl x 2Boo = ( 2800- (1.3 x 57 Proportion ot Water Vaoor oy Volume = 6ws (Pvaj r ------- m^^m ^^w ^•^ ass. £3 IB- 18 FIELD DATA SHEET PlantL Date:_ Location:^ Run #:_jh Stack I.D.:. Pbar: £ - 3 - z, n. Sample Tube Operators :_u Leak Check: Pre: ^ CQ( <.f ZQ" Post: l^8 Tr«v«ra« Point Number V«iodiy H««d In. H^O &, to 0. Z( 0.11 , JZ- . >* ^ /? /(? 20 Time /fa> - 2t/0- ^ /(/to 2 T-91, '~ /<* <= t ,v /*•«. Stack Tmp. °F 77 PO too (60 00 to VO'F* Tested Anaiyte:. Orifice Tank #:_ Pt: Pretest (mm Hg): Post-Test (mm Hg)L Tt: Pretest fF):_ Time: Start: /Us Finish: JkMTotal:_£D£$L W/B:J52_D/B:^_O«:^/_ Md - <0.44x%C02) f . • -- Md - (0.44 x ) -t- (0.32 X ) + (0.28 X ) ' :Md %' %H,0 100 100 T.- 13.8 13.8 Vi - 85.40 X Cp V«« 65.48 X( / -3fc.W X^P x y- •V- > V«xAaxOOt/m Qi- Qs« xOO p. %H_0 Qi .^-QiX 17.847x x(1 •-] •ta T* 100 - ------- Plant: Site: WE7-3ULE/DRY-SULS MOISTURE CALCULATION //feo &«J? /^oJlj-j _scaucn: nerators- - : 3.6 aarometrtc Pressure, in. hg = Static Pressure, in. H20 = Absolute Pressure of Stacx = =bar Wet-Bulb Temperature. °F = Ory.8ulb Temperature. °r = Temperature Difference. Td - Tw = Saturation Vapor Pressure of H,Q at Tw itrcm fabtei = =vw = Vapor Pressure of K,G = Pva = .Pvw,. 28CXD -(1.3X Tw) 2800 - (1.3x Proporaon of Water Vaoor oy Volume m 6ws 8ws= -LPva» VAPOR PRESSURES OF WATEH In IncfiM of Mercury 3F • 3 '0 20 30 «O SO 00 70 90 00 100 110 .120 '(30 140 190 180 170 180 180 200 210 3 3.0378 3.0031 ".1023 3.1847 0.2478 0.3828 0.9218 0.7382 1.032 1.422 (.832 2488 3448 4.828 S481 7.988 9482 1240 1349 1841 2947 2841 \ ^.03841 3.0880 0.1080 0.1718 0.2378 0.3784 0.3407 0.784* t.C 1.4 2J02 2 : O4I7 -1127 0.1803 0.2877 0.3801 0.7912 1.102 1.319 2.740 4.047 7.79 19 4.772 8.180 7.088 10.12 12.77 30728 0.1188 0.1878 0.2782 0.4082 0.3802 04183 1.138 1.981 2.114 2J28 3.744 4.1 4 : 94O3 :0788 M248 3.1893 3.2881 3.1 0.1 0.1 1.179 1.810 2.178 2J11 8.180 1008 1347 1844 2OBT 2447 4841 4841 9747 9481 0419 8481 1041 1347 18JO 20JO 2948 31.19 37JI S 3.0488 C.0810 0.1302 04033 04004 0.4 0.1 04790 1.213 1.880 2449 2488 3484 9.183 a 3.0317 0.0841) 0.1370 C.312O 0.4820 0.0442 04OM 1.299 1.712 2410 3481 4J 8487 1048 1947 1747 21.14 «J 8J8T 11.12 1948 1744 2140 3149 Date: Pbar = Pg = Pa = Tw *• Td = -2-8.90 f. c2- 74. fO & eo m. Ha in. H-.Q 2 in. Hq °F °F .Z&2- m. Mg r 3.0341 3.0882 0.1428 04203 0.324O 0.4 O.J 1.289 1.789 2478 3.188 4.174 9442 7.024 8481 1148 14 17J 9 :0371 . :.OB32 :.15O2 3.2282 3.3384 0.4 0.1 OJ 1.339 1.818 2.4441 3498 4488 9488 7402 a. 0.1887 04144 1471 U 2. 3481 1148 1442 1841 tl 1 1 2747 ------- METHOD 18 FIELD DATASHEET Plant: Lfeco Date: v-/5-- 5L Trav«ra« Point Numbar Velocity Hud In.H^O Stack T«mp. °F Tested Analyte:. Orifice Tank • - Pump/Rotometer #: ^ Ft Pretest (mm Hg): Post-Test (mm Hg)L Tt: Pretest Post-Test (°F): : Time: start: ^% Finish: Total: Md « (0.44 x %C02) Md - (0.44 x ) + (0.32 X Md- %H_O 10O ) + (0.28 X ) HO 100 Mc- P«.Pb •»•-§£--( )-t- 13.0 13.0 Pt» ff" Vi • 65.48 X Cp X In. Hg JS?x^- V« - 65.48 x ( ) X ( Vs- ft/I )x ^ A>« Qs»V«xAtxflOi/m Qs« x Qa> acfcn Qt -j-QiX 17.647x —x\| ltd Tt Qi^,- x 17.647 X- xW ------- METHOD 18 FIELD DATA SHEET ,- 5 > Plant: I-HS& Date: 35 . 33 ,2.3 .2^ -» tV ,Z0 .?>o /3I •32 .3/ ^,^57 H/r-3- 3/? 3ost: ., Flow Setting / jo < - , /'•' /7* '•'- /^ f t- Stick T«mp. °F 9O -79 tfe> to 2& €° •to It 7? ^»o ••» J .. . , „ H \ , QHW-^i/Zy dtcta ,^r ------- • WET-5ULE/DRY-BULS MOISTURE CALCULATION ?lanr />fe£Q &^J? /wt^ .scanon: /=Z^« . &.A,L^ 3ite: /fa £C—^ Coerators: -ftfa =un IF- tff-3-1 Date: 5//$/? 7 Barometric Pressure, in. Hg = Pbar = 2?,/0 ,n. Hg Static Pressure, in. H20 = pg - —, z/ ,n ^Q Absojute Pressure of Stacx = =bar 3 -^- Ps = 2^f, og in. Hg Wet-Bulb Temperature. °F = Tw = 5^ o p Ory-8ulb Temperature. °F = Td _ €& o F Temperature Difference. Td • Tw = &T = 2-/ a F Saturation Vaoor Pressure of (-LQ at Tw (from Table) = 3vw = 0 £~3o£ in. Hg Vapor Pressure ot K,G = Pva = ,Pwv, - '** ' ^™ * '^ 2BCXD - (1.3 X Tw) Pv..< ^05 ) (/Zf^ ' .5^>5)x( 2,/ ) = __^J/£5__ ,„.Hg 2800- (1.3 x Proportion ot Water Vaoor oy Volume = 8ws Bwa= (Pva> = ( 0.3/05 ) _ 0.0 If * /JY. VAPOR PRESSURES OF WATER T4mo In Inches of Mercury °C ° ' ^ 3 4 5 9 7 9 9 •0 3^1 ^SS :04" 3'0441 :34M 0-°88 3-M17 :-0341 30S71 OJ 20 -ToM ^'?«~ :OM 107M :07M 3-M1° 3-084a ^O892 =-08» 0-OBB 20 ..1023 -.1MO :.,,2r anaa rJ24- ^lMa o_jaro ^UM ,_is(a W9§r tao AIM ^-, 3-84a 3744 it* '-M* «« «•»» «^«« 130 4128 4447 4.772 4800 S4B1 9.189 1392 1448 198 7988 7718 J'25 "" MM 9J8° aj98 TOM '" -_ I'!8 7-88« «.»»0 9^81 8A7 a«fT 8jm ;: :sr :^ i— ««• s ;s ;jz !J2 ;^ J1.14 21.88 27J07 3.1878 3.1899 OJ033 04118 34203 3.2282 0. 9.2782 3.2881 0.3004 OJ120 0.3240 3.3384 0.4062 3.4203 0.4388 0.4820 0.48M 3, 70 n'^ «'^T1 g-a°°1 °-MOa °-a°OB °-taa O'843 O-"8* O-"08 ""** M ,'S i^J °'79ta 0'81M °-84« °-8780 °>« OJ»» OJ»" OJi" oo .'!» ^! '•1oa '•1M '-17S '-213 ••»» '•» 1-33S 1JJ> 100 an 'p» '4ia 1'sei '-910 '-680 '-71? '•r« '•«• '• ,10 ,.«. ,!- 2 ------- METHOD 18 FIELD DATA SHEET Plant: 3ate: y . o~i .$£ . tJtr ,lO .11- .tl ,6~J .o< 06 «/? .ov .<^"7 ,05 .Ob DO /£? P, Q-7fcU» Stack T«mp. °F "? t 76 75- 7^' 75 Iv5" 76j ~ICf ~)$ If 7 ^ 7^ 76* ?<> 75 75 75 7^ T6- -j<^ -75 7-^" 7$ 75 T-S" Tested Analyte: ' Orifice Tank #: z_ Pump/Rotometer #: v^ Pt: Pretest (mm Hg)- Post-Test (mm Tt: Pretest f F): Post-Test fF): Time: Start;j±zl_Finish:.^£_Total: W/B:Jf_D/B:Jg®_O2:_i_C02:. Md - <0. Md-(0.44x 0 ) (0.32X -Z/ (0.28x % HO M. - Zfc. 13.6 Pa . ZV. Jr "> In. Hg &-o. Vt - 65.48 X Cp X V - 05.40 X I t Pax Mi Qs - V« x A* x 80 i/m 0.- xOO X 17.647 X- d-8fcn 100 ------- WE7-3ULE/DHY-6ULS MOISTURE CALCULATION ch -scaocn: oeraiors: Date: - : 3.6 3arometnc Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stacx = ~bar Wet-Bulb Temperature. °F = Dry-Bulb Temperature. °F = Temperature Oifference. Td - Tw = Saturation Vapor Pressure of H.Q at fw (from Fabte> = 3vw Pbar = _. Pg = - Ps = _ Tw = _ Td = _ £J=_ ^VW — 2$. = (O (Pa) T ' O.W&7 in. Hg 0.00% VAPOR PRESSURES OF WATER In Ineftss of Mercury - «. ice. J ^ •9 20 80 70 ao 90 100 110 .120 't30 140 -190 180 170 180 100 200 210 3 3.0378 3.0831 3.1023 3.1847 0.2478 0.3820 0.9218 0.7382 1.032 1.422 1.832 2488 \ C. 0381 3.1080 0.1718 0.2378 OJ784 0.9407 0.784 1.000 1.44J7 2 :04<7 4.828 S481 7,< flj 1240 1948 1841 2347 23JI 3441 4447 0404 7.7W 3.1127 0.1803 0.2077 0.9001 0.7012 1.102 1.913 2493 2.740 3442 4.778 8.100 7.082 10.12 12J7 3 3.0441 30728 3.1188 0.1878 0.2782 0.4082 0.9802 04183 1.138 1.981 2.114 2428 3.744 4.1 0788 3.1998 0.2881 0.4203 0.8008 04402 1.178 1.810 2.178 2411 5 3.C 3.0810 3.1302 04039 04004 0.4 0.1 04750 1.213 1.800 2443 2J a 3.0917 3.08441 0.1370 04118 04120 0.4820 04442 04048 1.293 1.712 2410 3481 II 2448) 8.180 1048 1347 1844 2047 2447 3747 5431 8413 8481 1041 1347 18JO 28JO 2948 31.13 37481 9.183 848O 8437 1043 1347 17.07 21.14 8480 8J87 11.12 1348 1744 2143 7 :.0341 3.0882 3.1428 0.2203 Q424O 04332 1.283 1.788 2478 3.188 4.174 9442 7.024 8481 1148 14 17J .3. 3.1302 3.2282 3.3384 0.4 0.1 OJ 1.333 1.818 2440 3493 4438 9488 1143 1443 1841 2747 274 a o.e 0.1887 OJ OJ144 1473 U 2. 3431 11 1 1 3149 ------- jag cza GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Sampling Location: /3 Run#:_&£^ 3 ~ 2 Date: s--/.r-?7 Clock Time: Barometric Pressure, in. Hg: Z?,/ Moisture, %: <2. ? Molecular wt., Dry:. Stack Dimension, in. Diameter or Side 1: Wet Bulb.°F: £G> Dry Bulb,°F: Operators: • V"5 Static Pressure, in. HUP: —, PitotTube^Cp: , ?? Side 2: _ TravarM Point Number / 2 ") ^ 5 0 / i "b ol ,cft ,Q(J .oG .01 JO ^P-.t7^3 Stack T«mp. °F 7^ 7^ 7^ 7-5 75 •75 7^ 7^ 75 75 75 75 7^ 75 75" •75 7JS 75 7>S 75 75" 75 75 75 S. 75 Md - Md • (0.44 x •• (0.32 X ) + (0.28 X ) Md - ^7, 0 Me - Mdxd Ma»( % H,O 100 )x(1- %H2O 100 100 100 TS. Pa.Pb 13.8 '.05" ln-H9 13.8 — TsT^fl) V..85.48xCpx^Px ^ paxM, v«-as.48x( \|cl^ )x( i^a, )XA/. ft/a A.- Q« - V« x Aa x 60 «/m x80 Q« -,-Qax 17.847 x - x(1- ——) •* T» 100 X 17.847 X- 100 ------- WET-BULE/DHY-BULS MOISTURE CALCULATION .-,««. /./rou? r*v>C Au^A -scancn: /Tfc/^a /fTT ^ 3ile: ^..i /fjjr/^,* Coeraiors: T^/^T =un «?• fie-S-t- Qafe: 5//f/r7 3arometnc Pressure, in. Hg = Static Pressure, in. H2Q = Absolute Pressure of StacK = ?bar 3 ?q Wet-Bulb Temperature. °F = Dry-Bulb Temperature. °F = Temperature Difference. Td - Tw = Pbar = 23. /Q Pq = -, £? ps = 2-?- ** Tw • £(f Td= 75- AT = ft m. Hg m. HJD 2 °F °F °F Saturation Vapor Pressure of H.Q at Tw (from Table) = =wv = /2 t-f'?2Q ,n> Hg Vanor Pressure of K,O = Pva = -Pvw, . 'Ps ' P>/W> X'^ 2300 -O 3x Tw) \ _ 0. I?i* in.Hg 2800- (1.3 x Proportion of Water Vapor oy Volume = 6ws 8w3= (Pva> = ( 0. l$W } _ G.oot-^ 0. VAPOR PRESSURES OF WATER In Inches of Mercury 9P . a ...... ..„_ ,.__.. 0.0888 '0 0.0831 3.0800 :.oeaa 3.0728 :.o788 c.oaio S.OBM o.oaaa .0.0933 o^ooi M ! 2 :'1M° :1127 a-l1M -"• 5.1302 0.1370 3.1428 0.1302 0.1987 3.1847 3.17IB -,,«. 3-1878 XJ9M Q^^ OJ\|la Q_ao3 3Ja>1 OJa§a OJ808 0.4082 n n'S! 'I!!7 °-aa°1 °-aa« °-BI" °:«» ^w5 0-"»" °-«» ««•• « ,'^ ^? °-7918 °'8IM O"8" "» 0-««« °-«« 0«" 0-«» 8O t.032 1.QOB • ••>• . ... . __ _ 1.378 1.919 1.981 1.010 1.800 1.712 1.789 1.810 1.870 2.748 •S !£ •• 3-744 'S i»^ ;T^ :rn ig-* '•« iaw "•« "•» «• i iaa !!U !nr IMB IM* 1M° "•°T «w* ^« '« » 2 IS Il± 1M M» 20JO 2t.1« ^S SS 25 2Mt 247 2M« 2MO » ™ 2? »• «« 3».M SW ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Sampling Location: #„ » gj^ Run #: ft£-3U^ Date: ?-ti Clock Time: Operators:. Barometric Pressure, in. Hg: ~_ ,o7 .0^ .o-7 JO .0% .oS .°3 . to .11 .10 .D~r .oS ,oG .(/ ,/ .10 c?1 •on .ol/ .» 7<> 76, 76, 76 76 76 76^ -?<-? -107 -7C, TO 1^ 10 76, -«/ lu* n^ S-7fcF. Md - (0.44x%CO2) f (0.32 X%O2) Md - (0.44 x ) + (0.32 X ) + (0.28 X . ) - Mdxd % H.O % HO - —) + 18 ( - i_) 100 100 )X(1.___).,8(_ P. ,-Pb+-!£_., 13.8 °R(°F460) 13.6 Vs - 65.40 x Cp : V* - 65.49 X ( A.- = Ts f R) Pax Ma )x( )x ft/a .2 O« - v« x A» x eo t/m Qg Q. XflO «" p, %HLO .»QtX 17.847 X x(1- 2_) ' ft 108 X 17.847 X- 100 ------- WET-3ULE/DHY-5ULE MOISTURE CALCULATION ?lant: l/hS(jg> £>^ A^..t Site: J60»« ^/f/C^./- Coerators: "/^/r/ Barometric Pressure, in. Hg = Static Pressure, in. H2Q = Absolute Pressure of Stacx = =bar ••• "q — 'TS ^ -ccaticn: /i =un ff1 /?£ ~ - Pbar = Pg= , P3 as a /17 in. Hq in. HO in. Hg Wet-Bulb Temperature. °F = Dry-Bulb Temperature. °r = Temperature Oifference. Td • Tw = Saturation Vaoor Pressure of H-.G at Tw (from Table) = Td = Vaoor Pressure of K,O = Pva = iPvwi - Pva=( 0. 'Ps- x (&T") 2800 - (1.3 x Tw) 2800- (1.3 x Proportion of Water Vapor oy Volume = 6ws (Pva) (Ps) VAPOR PRESSURES OF WATEH In InehM of Mercury o '0 20 30 40 SO 00 70 00 00 100 110 140 190 180 -170 180 180 200 210 3 3.0378 3.0031 M023 3.1047 0.2478 0.3828 0.3218 0.7382 1.032 1.422 1.032 2.588 4.128 5481 7.588 1249 1! i 3.03B8 3.0880 3.1080 0.1718 04378 04784 0.3407 0.7848 1.080 1.487 1.888 2472 3443 4447 2 0417 r.78» .1127 3.18O3 0.2877 0.3808 0.9001 0.7812 1.102 1.313 2432 2.748 3442 4.772 0.180 7.882 10.12 1848 2347 28JB 1! 1( 2448 3 30441 30728 3.1108 0.1878 0.2782 0.4082 04802 04183 1.138 1.981 2.114 3.744 0480 0.180 1048 1347 1844 2047 4 : 0403 :07BS :i248 3.1999 3.2881 3.4203 0.8008 0.8482 1.179 1.810 2.178 2411 3448 5431 0413 848t 1041 1347 18JO 20LJO 0 3.0317 3.0846 0.1370 04118 0412O 0.4820 04442 04048 1.233 1.712 2410 3481 9402 0480 8.787 11.12 1348 1744 2148 2843 -7 To 3847 3747 31.18 aunt 7 3.0341 3.0892 3.1429 0,2203 04240 04332 1.283 1.789 2478 3.188 4.174 1442 7.024 0481 1148 1440 1742 2248 2747 3342 1?Z? 3 :0371 .3.0932 :.1S02 3.2282 0.3384 0.4488 1.333 1.818 2448 3498 44 7J 9400 1148 1442 1841 2749 3347 m. Hg in. Hg a o.e 0.1987 04888 OJ144 04888 1471 1471 3481 7J 8484 1141 14 If ait ------- 3 aa i_3 GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: £A$e& Date: 5V<- ?7 Sampling Location: £>L>£_/I; d-ty Clock Time: /^S~~ Run: Static Pressure, in. HUO: -, &<* o MolPrnl3r\A^ Rry ^«. 6^ PitOt Tube^Co: ,<79 Stack Dimension, in. Diameter or Side 1 : / 3 Side 2: ' WetBulb.°F: -^~~~ nrvfiulb.OF: .. Travarm Point Number /H 3 3 / 5 6 A-/ a 3 V < C: • Velocity Haad in. H20 .OS x/9 ,/6 ,sa »a^ rCV?> ,/-9 ,31 ,<5T ' 9^ -52 -•/^ ^KF - o,«ran Slack T«mp. °F /fct IbU l£,-> Ibl i W ibi l<0^> lb f (0.32 X %O2> + (0.28 X %N2> Md - (0.44 x ) (0.32 x ) 1- (0.28 x ) Md- tt^&{^7•^ % H2O % H.,0 M..Mdx(1-^j-)i8(__ ) M.-( ,x(1.-_ -)>ie<— -> Ma- 2f «« Tj- /^ °F- °R(°F.460, 13.8 13.8 P«- ^S,8^ m.Hg ^P - ^ y??2- ^= \| "is (°R) Va-«5.4«xu>x JSP x y P9XM8 Va- V,!1/1/ ft/. A.- /. 13 ft2 Oa- x xeo Qa - 1 30 ^ aeftn Pa %H.O Q« ..-Qtx 17.847 x x(1- — 2—) «w Ta 100 IKS ------- ik I ,)• METHOD 1 8 FIELD DATA SHEET Plant: tASCr- Tested Analyte: JYx/ft^/'. Date: C '/<•<> 7 Orifice Tank #: ^ — Location: Q\lKAJ tt // 9 't/t4 l(oL. If- Z ~ • /^•^ 1 f.t<%- l~)fj /"?/ y -»/o y 6^ l(o7 Md - (0.44 x %Cag) + (0.32 X %Cy + (0.28 X %f^) Md - (0.44 x ) 4- (0.32 X ) +• (0.28 X ) Md - 2-7 - V * S^ ' «. » 0 « H 0 /6,'>^ 7* HjVJ 7b ~2W 'Ss^v " x<1 " 100 * 100 <££/$* * * 100 ' 100 /3A ,/ &^\j t y ^^ S P 13.8 13.0 P»- 2V,8f In.Hg ®-o.mf ==: . F Ts rR) VI • A9.4U x 3 " Q«- VexAexflO«/m Q«- x xM ^ Q§" /. 3 ' D M" Pi H,O Q§ .j-Q«x 17.047 x x(1- =— ) "™ !• 100 eta 100 OKU- //?/7^ ------- FIELD DA I A SHEET Plant: Sampling Location Run Number: ft-3- Pretest Leak Rate: '&) Pretest Leak Check: Pilot: ,/ tf <] ate: 5' t$' Date cfm Sample Type: Pbar 9 ft CO2: Operator: .P»:_ 02:. l£ in. Hg. / '5 Probe Lengthflype: Slack Diameter: / if' As: Nozzle ID: — Thermocouple X Assumed Bws: ""' Filter #: • Meier Box #: /» Y: ;?%6 AH@: /j Post-Test Leak Rate: > aco cfm (g)^' in. Hg. Post-Tesl Leak Check: Phot: ~~~ Orsat: TrcvwM Point Numbtr Sanipling Tbiw (mln) 0 y^> r9 6 // ^ /.- ^ 5? 60 61- '&t ^^ ^7 ------- iSSS If— SAMPLE RECOVERY DATA PLANT DATE Run No. SAMPLE LOCATION TRAIN PREPARER ft Sample Box No. M-l Job No. Filter No. SAMPLE RECOVERY PERSON COMMENTS M FRONT HALF Acetone Container No. Filter Container No. Description of Filter A erf 1/nainae.f Liquid Level Marked Sealed Sealed Samples Stored and Locked RACK HALF/MOISTTrRF Container No. Liquid Level Marked Sealed IMP. NO. 1 2 3 4 5 6 CONTENTS Z>£ 4O Dr f^o £#yalt/ ^HJC.A(=tfL- TOTAL INITIAL VOL (ml) /^t? /fft> - Zero WEIGHT (grams) INITIAL 5-52 US.7 S/2.0 BS14 2§7t>,3 FINAL 5&.l> t>t>5,7 511. b 845-1 j?£T83.0 NET • 0.4 o.o O.b .1 b.T ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: LAS^P _ SOURCE/RUN ' 4-3-2 DATE: 1 . Leakage Correction for Volume Metered Vmc = V (L - La) x 6 Vmc=Vm-(Lp-0.02)xe Vmc=( )-( -0.02) x( ) Vmc= JMO' ft3 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) Pbar-MAH/13.6)N V_ = 17.64xVmrxYx mstd mc m )x 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V... = 0.04707 x (W. - W.) wstd f ' Vw = 0.04707 x( fc.y wstd Vw wstd 4. Percent Moisture, by Volume V, wstd wstd mstd o.-ivs ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: LAZee? p^o- Sampling Lo Run#: nnprarnr:- flftX //?/V Barometric Pressure, in. Hg: d.1o Static Pressure, in. Ho O: '4^ Moisture. %: < — - /,/•/, MniPrM^rWT Prv -2-^ Pit«t Ti ihft>rv , \|«» rOOTI Number 4-1 ^ j ^ S £ OH 51 3 Y i /w /7<0 m /•-7I /(, $ Jt><\ - M 91: /<'' Side 2: ' 3ulb.°F: -— Md - (0.44 x %CO2) ••• (0.32 X %Q^ + (0.28 x %^42) Md - (0.44 x ) + (0.32 X ) > (0.28 X ) M«- zz&f-v?^ , %H20 %H20 fiifrSt" M« m Md x ( 1 • — — — ) •• 1 8 ( ^^— ) 100 100 1 1 M. -< )xd- — — — ) * ie<_— -_> 100 1OO Mt- 2&3&- ^M^ T~ ((>7 °p- 62-7 0R(°P«o) 4 D Pti — Pb +• ( ) +• 13.8 13.6 P"- "2-t.gr ln.Hg ^P - C?. ¥J<^ — / Tn /°R1 r— ,\| ' J ' "I V.-«b.4UxCpx^P X ^ p98M9 V« m 85.40 X ( ) X ( ) X J V v«- 3i',?6' m .•-/.«.> ^ Q«- V«xAsxOOa/m Q«- x xflO Qs-^^^^ adm p, %H,0 Q.itd-Q.xi7.847x — x(1--j^-) • X17-W7X X(1-"ST> dMn ------- METHOD 18 FIELD DATA SHEET -9V 31 Av - Plant: ff»co y Anaivte: LOcation-zLZLLj") L/C/V Pump/Bolometer: -~ Hun»: ;cu 3 -( R. p^st fmm Hal: ^ siack i.y.,_U Poct.jest (mm Ha) :x— Hbar:_^4d) Tf Prntn-rt (°R- ^ sample Tub Operators:^ \fJQ-5-M 10-3-iH Post-Test fR:- /JA /( yitt'l HL, - . <$($ Velocity HMd in.H^D , K .(/. .11 '3* ,3* .J ^ tf? -7< . pA . Off )tf ,»> ' &1 f . ¥^^ Stack T.omp. GZ& 'JJL&, #a~) Q ir< &&$ — 9& 33ft 3? 1 ^32 'J 3V :^-3'i? y^-3 • 22.* Md - (0.44 x %CO2) + (0.32 X %<%) + (0.28 X %^) Md - (0.44x ) + (0.32X ) * (0.28X ) '^. 2?.o WJ %Hn H20 ^'^ Sti, L Mt i- Md x M - . 1 -t- 1H f . ^ ii WAO 100 100 /, / / •>0/f5Z. ^y UA . ^ >/4 \i.«a/ \ ?y» I0° "" jy//?" M V/S's'm ^ °F" ^f °R<°F«.4ao) 0 D Pa . Ph °'r> » ^ ) + 13.6 13.8 - ^e.9/ \|n-Ha ^p-^yi^l r= J T8<°R> V.-05.48.CPXVSPX ^ p8xM§ V« • as AQ vf )y/ )v4f vt- 35:V33 fi/B •• /,23 «2 Qi • V« x Aa x CO a/m Q»» x xM Qi- it/5" -^ Pi K,0 Ql^j -Ql XI 7.047 X x<1- 2_) • !• 100 Md '100 0%M- /?/0 d«fc" . y ------- FIELDDAlASREET Plant Sampling Location €>£/£/,'-# 10 Run Number /0-3-1 Date: 5 • i-1 Sample Type: Pbar CO2: Operator: O2: Pretest Leak Rate: n3cr) cfrn @ /fl in. Hg. Pretest Leak Check: Pilot: Probe LengthAType: J ^ "* Stack Diameter: /«T v As: 1-2.3 PHot #: yy 3 Nozzle ID: •• * Thermocouple #: l£> ' Assumed Bws: Filter #: -^—- Meter Box #: /f Y^fedyAH®: A > cfm @ KXJn. Hg. Post-Test Leak Check: Pitot: •— Orsat: Point Number \ z~~r~~ Sampeng Time (mln) 0 ID 3O So j i OocfcTbm (244iour dock) \4Q(o /H3C W l^> /5'^4j Gas Meter Rearing ^ i 47^1 '71 / y < ^p/c ^fl, ^ q-7, - - Velocity Head(Ap) inH2O Orif oa Pressure Differential (AH) in H2O Desired Actual Stack Temp. (Ts) Temperature °F Probe Y/////Y/////////////////////////// // 56 )' ?& It $k h ?6 " Filter Impinger Temp. °F Dry Gas Meter Temp. Inlet (Tm in°F) • 5 ^? fj fc* ^& ~$~? %/ &9 &}. £-1 Outlet (Tm out°F) Pump Vacuum (in. Hg) s////////// %Q SI f^2 3 3 "3> -3 Tm= ------- SAMPLE RECOVERY DATA PLANT Run No. lo DATE 5"-/sT-9 "? Sample Box No. /V-5 Job No. SAMPLE LOCATION -# /O Ougw o^ie'T Filter No. TRAIN PREPARER SAMPLE RECOVERY PERSON COMMENTS FRONT HALF Acetone Container No. Filter Container No. Description of Filter Liquid Level Marked Sealed Sealed Samples Stored and Locked RACK HALF/MQTSTTIRF Container No. Liquid Level Marked Sealed IMP. NO. CONTENTS Dl IV TOTAL INITIAL VOL (ml) (bO 0 WEIGHT (grams) INITIAL FINAL 774 NET 7,5 ------- FIELDDAlASREET Plant i Sampling Location Run Number /0-3-J Pretest Leak Rate: rdcD 10 Date: cfrn Sample Type: Pbar C02: Operator: Ps: 02: Thermocouple #: -Filter #: /Q in. Hg. Pretest Leak Check Pitot: — — Orsat: Probe Length/Type: Stack Diameter: Ptot #: ££_3 As:_U3_ Nozzle ID: Assumed Bws: _^ Meter Box #: I1 Post-Test Uak Rate: „. Qg>-> cfm @ Post-Test Uak Check: Pilot: -— Orsat: TravwM Point Nurabw \ SmpKng Tbm (mln) 0 /£> i?t 30 /o i i Oodclbiw (244iour dock) ;v^6 /H3C W t^ /H S& i$ dt> GaMet«r Heating (Vm)ft3 £4 . 401 •7 ^OG - - Velocity Head(Ap) inH2O Oil ca Pr«Mur« DHtercntiat (AH) in H2O Desired Actual Stack Temp. (Ts) Temperature °F Probe '////////////////////////////////// /^4 },9& 1,5k \,?L «r Filter Impinger Temp. °F Dry Gas Meter Temp. Inlet am in°F) Outlet (Tm out°F) Pump Vacuum (in. Hg) '///////////////////////// '// • 5<£ V-,f 5^ 5"7 Ft £f ^ gi KQ 81 ?3 ?-> .... 3 3 •> •~3 AH= ------- SAMPLE RECOVERY DATA PLANT Lfl$£& Run No. / ® DATE S'-JS'-y 1 Sample Box No. A^-5 Job No. . SAMPLE LOCATION -# IP Oue-w o^ieT- Filter No. TRAIN PREPARER SAMPLE RECOVERY PERSON COMMENTS FRONT HALF Acetone Container No. Filter Container No. Description of Filter Liquid Level Marked Sealed Sealed Samples Stored and Locked RACK HALF/MOTSTTTRF. Container No. Liquid Level Marked Sealed IMP. NO. 1 2 3 4 5 6 CONTENTS Dl IV SZ HT? ^PV" Stf'c. (& TOTAL INFTIAL VOL (ml) /t>0 foo 0 z& WEIGHT fgrams) INrHAL <7/^g> £68.7 ^3,"& -7tf.(c Mtt:°( FINAL ' &r.f s$?.y wf,J 77^4 2H3t^ NET • 7,5 ------- 3 ap g GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Sampling Location: Run : /<3 ' 3 - 3 Clock Time: Operators : Barometric Pressure, in. Hg: 3%.3Q Static Pressure, in. HoO: "- Moisture, %: Molecular wt., Drv: -2&#" * Side 2: Wet Bulb, °F:. Number A- / A- i 2 5* Vttecrty H«ad in. H2O .19 Dry Bulb, °F:. Stock T«mp. °F 931 239- 130 ,9^3 Md • (0.44 x %CO2) + (0.32 X %O2> + (0.2B X %Fty Md - (0.44 x ) ••• (0.32 X ) + (0.28 X ) % HO % HO Mdx(1 - - — ) +• 18 ( - — ) 100 100 ) + 18 ( ) 100 100 71- - Pb S.P. 13.8 13.8 P.- ln.Hg V« • 65.40 x Cp X V> « 65.49 x ( PsxMs ) x ( )x /,2-3 «2 Q»» Qg" xOO %H_0 2- 100 X 17.847 X- ------- FIELD DA IA SHEET Plant- LAf^CLC^ Sample Type: /?- y Operator: y)AXy£xi; Sampling Location O0£/^- 1O Pbar. 9 Ps: — / § / ' Run Number: ;<9'3-3 Date: (f-fZ- 97 CO2: O2: Pretest Leak Rate: ,fyo elm @ r < in. Hg. Probe Lengthflype: / ' S Pilot* Pretest Leak Check: Phot Point Number d-( 3 V 4- 6 ift-/ 5? 3 ^ ^ ^ Sampling Time (mln) O /o :9O $ D 4-O Clock Time (244iour dock) ]")'3^ ({$ $5 iff &<. jY( $ : ^X^Orsat: — ST-3 • Stack Diameter: /5" As: \|. Z,? 4* Gas Meter Reading (Vm)«3 /^o. o/^? /^o,^o IV$"^0 /5'3r^5' ;^/ /^^o /4»«.>ir? Velocity Head (Ap) inH2O Orifice Pre»oure Diflerential (AH) in H2O Desired Actual Stack Temp. as) Nozzle ID: ••"" Thermo Assumed Meter Bo Post-Tesl Post-Test Temperature °F Probe Filter Bws:-^- Filter # <#:^i LeakRa LeakCh Impinger Temp. °F couple #'. ^ & Y: ,/te'6AH@: /- /4ii? 'e: «€fe'J eck: Pilot: cfm @/£ «^ Orsa in. Hg. t: Dry Gas Meter Temp. Inlet (Tm in°F) y/y////////////y//////////////////////////////////s \ftiotiil ' 1 "$> ,0 1 /2"? ..3S1 * ir 3 Q >£ / ,/SF ^^ / , ^C5 c» V5b8 // %b 1 s£& ] p£ i • 1 £> X Sr/? <-£.. QP^, 93 Y <3.9-3 QPO &J>/ 93 1 Q.3 <^ i>36 ^>3.f S>3 ? P3C ^JL- M> - \/5 ^ A- d^t^ JL$^~. <^a 5'cS1- ^? / s ^ 17-3 28.S7 2V.7/ l9.$ <3r Outlet (Tm out°F) y7 9~? /Cuf^i /QC> Pump Vacuum (in. Hg) 2 ^ 3 3 AVm- ------- SAMPLE RECOVERY DATA PLANT DATE Run No. -/ 91 H^O t^^ S-ftu GJ TOTAL INITIAL VOL (ml) /&£> /H> 0 IslO WEIGHT (grams) INITIAL blo.Q bo 73 ... issi.o NET • -0./ 1.0 0.2. 5.5 Afc ^f •^y • ------- 3 OP CZ3 METHOD 18 FIELD DATA SHEET Af: H /o 10 w 0 -o ^ Plant: A/?S£# Tested A«»'yt«' ^v/~"- Date: 5 - /? -•» T Orifice Tan1' ' - Location- ,VD# Pump/pntnmRter : \,-"frr 3 Run: /VD/J-3>-7 Pt: PretflSt (mm Hg): Stack I.D.: 52." \x&" Post-T«st (mm Hg): — Pbar: 2.^.\ Tt: Pretest <°R: ^ Sample Tube Operators: a#:/VDA-32* uM--)-2* Post-Test fR: ^~ •r4/^ _eak Check: Pre: /^ Post: ^" Gauge Time Vacuum (Hg) UcTL i~7 ) I Jfc £..«*' \ i3n^,SS i \?n^,^3 i 131^.31 i v^n^.^i I 3 >3 .0 ^ Tr«v«rs« Point Numb«r Flow Setting 3 \ B\ z\ si a\ 91 TL 1 Velocity Heed In. H^O Stack T«mp. °F Time: start:l5sV Finish:ii>^.Total:JjjjaiM w/R-_^0/B: - 02: 2-' C02:_ g — Md - (0.44 X fcCCty -•• (0.32 X %02) + (0.28 X %N2> ^2, Md - (0.44 x ) + (0.32 x ) •• (0.28 X ) n Md- "^ %H,0 %HO - ^^ TS- °F- °n (°Fao) SP. i Pi-pb-sr"( } i" Pt . In. Hfl ^s?- vt - as.48 x CP x VAP x ^ psxM« Vt« ft/* A.- n2 Qa»VtxAaxflOa/m Qa^ x xW Qt • acfm Pt %H2° Q§_^- Q» XI 7.647 X x(1- •) . «td T« I Q-.W- ^'-«'x (l< ,00 ' Qa^d- dacfcn /\| ------- METHOD 18 FIELD DATA SHEET Planr_L Date: : Tested Analyte:. Orifice Tank #:_ Location; ^D Run #:_ Stack I.D.; Pbar: 22 Pump/Rotometer #: V Pt: Pretest (mm Hg): Post-Test (mm Hg):' Tt: Pretest fF):^ Sample Tube #: NOB -3-3)1, i^i Operators: Post-Test fF)L Leak Check: Pre: Post: Time: Start: 113 5" Finish: tfl3& Total: faS m.^ W/B: - D/B: - O: ^' I I Time v»a.l(o l^^^.^^f v^ S"».4f L"Mo.toS t?t 3.^3 t^5. to-? v^^.oV Gauge Vacuum (Hg) 1 \ I 1 i 1 i Flow Setting 31 al •^\ 3t 3) X 3-1 tas 40 ------- APPENDIX A. 1.5 Condition 4 (includes flows, moistures, and Method 18) ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: [h^LO Date: .s-/5""1'7 Sampling Loc Run #: we ation: A\«;/> £>tav» Clock Time: "?o<.s- - -i-i Oneratonv Trt/s-5 Barometric Pressure, in. H Moisture, %: - 1 1 Stack Dimens Wet Bulb, °F TrimrM Number , 2. 3 ^y 5 0 7 tf I 2 3 4 6 \j> 1 3 • . q- z ef. Z. Static Pressure, in. F-UO: „ /i Molecular wt.. Drv: ZK:W PitOt Tube, Cp: ^_i? jion, in. Diameter or Side 5"f DrvB V«bcity in. H2O ,ii . W , 3O •^G , 51 . 31T .3S •S-/^ i3C7 , 30 , 33 . 3S .^1 V6> .11 .11 £P-,5lH Slack T«mp. °F ' '1^ .* ~>d i^ ~7^ 7? 1? ~7t 7^ ~7f ^^ "IS 1°l If T? T? If S--7J? 1- &i /TS Side 2: •$» nlh'Op. 78 Md . <0.44x%CO2) -f (0.32 X%O?) -i- (0.28x%N2) Md - (0.44 x & ) <0.32 x 5 1 ) + <0:28 x 1 ^ %H.O %H-0 M kJd M 1 ' 1 B ( ) •7V . '/\| — . -tfl <-/^-< Vt. "°'^" ft/« \ Col •, Aa« nz Qt • Vi x Aa x 80 /m 0.. t\|o.^ x 1.6 1 xoo Qt • "°5 ? acfm p. ItHjO ^itd"0*17'847 T. °" I'M ' Urto 31-»l -^ 0^- UI7.M7U s^ Jed 1QO ) ------- WE7-5ULE/DHY-SULS MOISTURE CALCULATION .„ .CU. .; 3lte: MfllM Ccerators: Barometric Pressure, m. r-tg = Static Pressure, in. H-O = Absolute Pressure ot Stacx = -bar 3 — Wet-Bulb Temoerature. °r = Ory-Sulb Temoerature. °~ = Temoerature Difference. Fd • Tw = Saturation Vaoor Pressure ot H.G at Fw .from fabie» = Vanor Pressure ot K,G = ^va = ,PVW, . ( x 2BOO-M.3xfw) 2800-n Proportion ot Water Vaoor ny Volume (Pvai (Pa) 6ws I ) VAPOR PRESSURES OF WATEH In Inerm ot Morettry '0 :o 50 00 70 oo M 100 110 .130 'l30 14O 190 iao 17B 180 108 200 210 3 .0378 .out .1023 3.1847 3.2478 0.36M o.uta 0.7382 1.031 1.42S 1.831 2JM 3.C :.ioao 3.1718 3.2970 OJ7B4 O.S407 0.7 1.C 1.4 1.1 2J 2 0417 1127 3.18O3 3.2877 0.5001 0.7012 1.102 1.913 2J40 4.1 SJM 7.! 3 30441 70728 3.11M 3.1870 3.2782 0.4082 3.3802 04183 1.138 1.981 2.114 3.744 4.1 0788 : 1248 3.1858 3.2881 3.4209 3.1 3.1 1.179 1.810 2.178 2J11 :.oaio 3.1302 0 2O35 o; 0.4 0.1 04790 1.213 2.243 2J a 30317 3.0844) 3.1370 Oil IB 04120 0.4820 04442 1.293 1.712 2410 3411 4J t: I! 1841 7.751 0.100 10.12 12J7 II II 8.180 1041 1347 II S431 9413 8481 1041 1347 18JD 5.189 2447 301 374 II 1347 174T 21.14 8JV7 11.12 1341 1744 214 in. Hg 3141 ------- oga rj METHOD 18 FIELD DATA SHEET Date: £->s-^i Orific« Tank • Location: m«;rt «=,^4- Pump/Rotnrnfiter #- ^"^ z- Run#: n&-4-z Pt: Pretest (mm Hq): Stack I.D.: n . ; Post-Tost (mm Hq); * Pbar: w.i It- Prntflst (°R: - — Sample Tube # Operators' -pr :jmir--v-zrt iie"4-5-(? Po«t-Tflst fF): ^ , ' Time: Start- Finish: Total: Leak Check: Pre: A/ Post: / W/B: ? D/B:^7J1_O,,: ^ CO0:_£ — ex/** c f1- -'3? i? 2V VO /O Iime,6 fe ^3&to j\|'7l Time 23.76 5"y -/-V7. 36' iz-^n, ^i 22^B. 5V / Gauge Vacuum (Hg) / / t t 34-ftVi.- r /-. o •> Traversa Point Number / ? 3 ^ •5 C- 7 fr ( z. •J H 5 Is 7 ? -TZrWfi 4vA V«tecrry HMd In. H^O -•27 ,3/ ,35- .37 , T7 ,38 ,59 .-// .20 .3/ .33 .36 .^7 . 3V .^0 ,vo • ^* 75 7? 77 75 78" iy 73 7* TT "7X Md - <0.44x%CO2) -i- <0.32X%02) + (0.28 X^) ^ ^^ Md - '-' > Si % H.O % HO 5, M..MdKJi--^.) + ie(-— ) -^ M«-< -?<•» ) X (1 - ' ' ° ) + 18 ( ' '® > v" l"( '•'' 10O 1CXJ M.- ?^ \°\ T8. ~?5 °F- SlS °H (°F4«0) 13.0 13-« p, . 0 "\ • 3O In. Hg £F- .S^SJ) ^= J T» "R) vt • «».4» x vp x r7 \|T-1Ti, -L^-7«> l-° , "••Id" Al7-e47x- ^ x(1 -jjj-t Q,^- ^"i> dwfcn ------- WET-5ULS/DHY-BULH MOISTURE CALCULATION •=iant: Site: 0 -scaticn: Coerators: Gate: Baromatnc Pressure, in. rig = Static Pressure, in. i-UQ = Absolute Pressure ot Stacx = =bar 3 ^ Wet-Bulb Temperature. °r = Ory-8ulb Temperature. °~ = Temperature Difference. ~d .- £w = Saturation Vappr Pressure of H-C at Tw itrom Tabtej = Vanor Pressure ot Pva t=( = ,PVW, . 'p« •" 2300 • i i .3 x 2800-,; 2 x Proportion ot Water Vaoor oy Volume = 8ws = (Pva) (Pa) VAPOR PRESSURES OF WATER In IneriN ot Mercury 0 •0 :o 30 «o so oo 70 00 90 100 MO ,120 'l» 140 190 iao 170 iao iao 3 T0378 c.oaat 3.1847 :.ioao 3.1718 2 0417 o.sata 0.7392 1.032 1.422 1.832 zjaa 1127 3.1803 3.3877 0.9407 0.7B4 t 008 1 .47 1.081 0.7812 1.102 t.913 3 3044 10728 3.tiea 3.1878 0.2782 O.I 0.! 0.8183 1.138 1.961 2.114 3JU 1748 0788 12441 3.1898 3.2881 3.4203 o.e 0.1 1.17S 1.810 2.178 2J11 3.C :.oaio 3.1302 0 2039 0.3004 0.4 0.1 0^790 1.213 1.080 2.243 a 30317 3.0«4« 0.1370 3J120 0.4820 04443 7.7W 210 tut 2SJT 2UI 4.773 9.180 10.12 12JT H II 2440 3.744 4.800 : 233 i.na 2J10 3 4J lost S.1B9 a.180 ioao 13JOT U 1041 8J07 11.12 1 2447 87JDT 18JO 2O9D 17JOT 21.14 21JH 3148 37JI Pg = - * • Pa = _ Tw = _. Td = _ ^T= _ \ ------- SOS. £3 JK -- 5 Plant: Date: ?-/j.--h • f1 T) I 2. II Trav«rM Point Number Vacuum (Hg) / / l / Velocity Head In. H^O nvw Setting : SOc-L- ! 50 < <- r-,0 tc. i-^,0 1 1' Stack Ttmp. °F ISM - (0.44 X %C02) -t- (0.32 X %O2) + (0.28 X %Nj) -^— Md - (0.44X ) + (0.32 X ) •»• (0.28X ) ?d Md - <•<> % HO % H2O ^ M.-Mdx(1--j35-)18(-j3r) M«-( )x(1 10Q ' 101 ,QO ' M«- T.- °F- °R(°F4«J) S P i h- ""•&•< ' 1" ^SP • j== J T"<°R' V«« 65.49 X Cp X VAP X \l p,xM« V»- ft/« At- ft2 Qt • V« x As x 00 «/m Qg» x xOO QB • adm _ %K,0 Qi_1J-Q«xl7.e47x — x(1- ) •id Ti 100 0. - X17.647X Ml- ) Qi«tU'" dtofcn ------- a OQ czj METHOD 18 FIELD DATA SHEET 1-2,2 Plant: L&fO TesteH AnaiytP- ^,^ Date: ^-K-n Orific« Tni< • Location: fW.n £«»,flu-;v- Pump/Rntnmeter #: VJ-H 2- Run#: fie - 4- 1 Pt: Pret««* (mm Hg): Stack I.D.: •A'/x^B' Post-Tact (mm Hg): - Pbar: 29.2-0 Tt: Pretest f°R: Sample Tube Operators: S:ftf-H-^ i^r-^-ift Poet-Tflfit fF): - rA Time: Start: -><•" Finish: -020 Total- «* Leak Check: Pre: ^ Post: ^ Gauge F)ow Time v«\|{m Setting 2.2^, • j 1^0 u. •27 5. 2& / i#7«. •>ai£ °r \ \ 10 n 129C, ^/3 ' ,314, <»/.-/ = — , 6^ Trov«rM Point Number 1 I 1 ^ .•S i, 1 1 •> 4 5 (/ / I T N } u i -J M 5 /.; V«tedty HMd In. H^3 ,J& ,05 -cr .aLf ,c~r .0~l .0? 07 ,oC 05" oi1 . 'O . »z . /o T,// .0% .0? .06 £»<• .<»-7 JO O.ZWL Stack T«mp. °F If I/ T Md - (0.44 x ttCC^) -t- (0.32 X KO^) + (0.28 X %^) -In— Md - (0.44 x v) )-t-(0.32x r», ) + (0.28 x""5 ^ ) ^ ^ M- z&e? % H.O % H,0 SG M..Mdx(i--^-)ie(~^r) -S"C u. _ / 1 '-i \ v M "^ 1 + 18 ( •' ) M«.< a-] )xd- — — ) + i«( 100 > M.. -? f.^ f T.- 7ff °F- ^"^ °fl(°F + «» s p ^- —. - ^^Y "•-^-S"'0^* 13.8 P« - ZT. & in- Hg ^P- 0.2.^^ r ^? \/ T9<°R) Vt-65.49xCpX VAP x W paxM, .j n-rin 1 "^^ lirf ^/-<1"')-/' V« - ^ r ( > «/• A - a . o?~) n2 Q«. V«xA»xflO«/m OB- i 73'l S x ^'^"7 xeo a" Stf? £ «dm p. %H_0 Q«^.- Q« XI 7.847 X x(1- • — ^-) •W T« 100 P1./S , <4C. ^rtd' ^^ J X17.047X ^ x<1'-^ QNW- L\<^Lj(j>tM>m ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: <_^-* r^cA,^, 3ile: ^or^ £^^4. Ccerators: 3arometnc Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stacx = Pbar -^ - Wet-Bulb Temperature. °r = Dry-Bulb Temperature. °" = Temperature Difference. Td - Tw = Saturation Vapor Pressure of H~Q at Tw Vapor Pressure of K,O - Pva - iPwvi - i 2°WK . U<; Pv»«< US-v, } ( IS 'b _2caticr.: ( ** <= »v\ £"< u « ^ ^-f Vr/i =un ff- $£-<•/- / Date: V, Phar= ^3 Pq= - • <^ =cf Ps= ^1.\|Q • J.b . T^= ^?^ Td. ^ AT= ^ itrnm TnhlP = =VW = • ^S^O 'Ps - P«/w» x (&T) 2800 - (i.3x Tw) '^b)x< n ) .^^ (<3/?-) in. Hq in.H.0 2 .. in- Hg °F °F °F in-H9 in. Ha 2800 '(1. 3 x Proportion of Water Vaoor oy Volume = 6ws T.me. 9P 0 '0 20 30 4O so 00 70 80 00 100 110 .120 '(30 140 -f90 180 170 180 190 200 210 VAPOR PRESSURES OF WATER In Inehas of Mercury 3 0.0370 0.0031 3.1047 04478 0.3829 0.3218 0.7392 1.032 1.422 t.032 2499 5411 7.! OJ 1240 1549 1041 2347 28L78 :.0380 o.ooeo 0.1000 0.1718 04978 04704 0.3407 0.7848 1.009 1.487 1.999 2479 3443 4447 8434 7.781 1248 1! II 2 :04«7 0.1127 0.1803 3.2877 0.3801 0.7812 1.102 1.313 2489 2.749 3448 4.772 0.190 7.889 10.12 12J7 1! II 3 0.0441 0.0728 0.1100 3.1078 04782 0.4082 0.3802 04183 1.138 1.581 2.114 2429 3.744 4.900 0490 8.180 1049 1347 184* 2047 2447 4 0409 0788 .1240 0.1959 3.2891 3.4203 1.173 1.010 2.179 2411 3449 3411 8.313 8481 1041 1347 1&70 20JB 2949 3747 31.10 37.71 9 00371 .0.0832 0.1302 3.2292 3.3384 3.4889 1.338 1.819 2449 3499 4499 3498 7409 1148 1841 2949 2749 3947 a 0.1987 0.7144 1471 1478 2481 im 2849 ------- Plant: I-fa to GAS VELOCITY AND VOLUMETRIC FLOW RATE Date: -/•-k.,,<,+ Clock Time: ^20^ ~ n-t Onerritors1 r^/5S , Barometric Pressure^ in. H Moisture, %: °!S Stack Dimeni Wet Bulb, °F TramrM P^_I_.A rOtnt Number f i 3 * -* fr 1 z 3 ^ 5 (X I 7 T V 5 ion, in. Diameter or Side ^7 DryE Vtlocny H««d in. H2O • o<* , of ,uu> '01 (si .01 ,0* .&% .ol .03 ,oLff 10 /3 .0? ,&<<> .0^ .05 Jl 'II .<4 6(* .0* Stock T«mp. °F •7V 7V 7V 7V -7V -7V 7-S 75- 7^ IS 7V 7V 75 75" 7^ 7V 7V vi 75 75 75 75 1- Zy " . Side?' 2^f^ iiilh.op- -7.^ Md - (0.44 x %CX^) -f (0.32 X nCty + (0.28 X %N2> Md - (0.44X 0 ) (0.32X .21 ) +• (0.2BX~/ T ) Md - 2'7 %HO %HO 100 tOO ^ 1 100 1 00 P,. •S0!. /^ in.Hg ^SP- ,.>Tf6 — f fs(°R) V..«b.4«xLpx^H x ^ P9JCM8 / S'?'3 v«» t^5."% "2. ft/« A.. %* n* t^ t^ Q> • V« x Aa x 60 «/m 4-tr" QC m I "=? • 1 2. X 3' • ( * / 1>V x * a, » 7^; cv •efc^r5^r>\ ------- ^lant: Site: WE7-5ULH;DRY-EULE MOISTURE CALCULATION -va = zaoo - r, .3 x 2800- (i.3x Proporaon of Water Vaoor oy Volume = Qws VAPOR PRESSURES OF WATEH In IncftM ot Mercury 9ai 210 s 3MS Oate: Vr«T pg= _ P9= ••'.* Tw = _ rd = _ in. Mq m. H^O m. Mq m. Mq m. Hg 2.0S41 3.0882 8 : 0371 0 2201 0 2J78 3.101 4.174 1443 7.084 :.isoa ^3.2282 0.3304 3.4 1.339 i.ait o.i 1471 4.2M 9JB8 7202 17 2U arjor 11 1 141 11 1 ------- 3JC3 CJ GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: LflSclc Date: <- 15 - Sampling Loc Run: ?-* :ation: CVeyt' ^9 Clock Time: 3" /-/ Dnorators: iDftA /<£• & Barometric Pressure, in. H Moisture, %: Stack Dimen; Wet Bulb, °F TravarM Q— 1— A rOinl Numbar /?- "\ :> 3 V ,r ^. A- ) P 3 ^ q: JftfO Static Pressure, in. HUO: ~- &"? Mnlpnilarwt Prv Pitot Tube, Cp: ?? sion, in. Diameter or Side • ' Drv E Vatociiy in. H20 .oy 1 />7) I") 5X Ite^ /6V 113 Wb /fo 1 I fob )&6? f<6 / Ibfr 1 &^> fj. ito^ 1: /5V Side 2: - nlh.Op • Md - (0.44 x %COZ) + (0.32 X %0Z) * (0.28 x K^) Md - (0.44 x 0 ) -i- (0.32 X 3 , ) -t- (0.28 X ~) =) ) Md - ^ S % H2O % H2O M..< .5^ )x(1.±_5_) + i6(-L5r) Ma- 3^-^^ T;. loV °F- 4=3^ °R(°F460)/ c p Pa - Pb + ' = ( ) •• 13.8 13.8 f& - , ^ ^m — / Ts^R) Ve-«S.4BxU>x Jf& x y p9xM(\| Aa- \-'P3 ft2 Qa . Va x Aa x 00 t/m Oa • #i^i x I- "5? x^O / 0»m 3^$ adm / P. ^HjO^ "3-sS x -L ------- I i •ii PlantL Date- Location :-Qil£AL-?L Run #: Pa /c pa^o £3 3o fv^^ Gauge Vacuum (Hg) O O C & O O Flow Setting 9SD ty/W-c / ^ Trovers* Point Numbar -£ 6 Vatoctty H In. •JO. Stuk T«mp. °P M ><* Pt: Pretest (mm Hg): — Post-Test (mm Hg): — Tt: Pretest fF): —-~" Post-Test fF): -^ Time: Start^225iFinish:^^OTotal:_^Q_ W/B: —D/B: —O2: CO Md - (0.44 x %CO2> -I- (0.32 X %Q$ -t- (0.28 X %h^) Md«(0.44xc? )+(0.32X'J( ) + (0.28x~~? J ) %H,O %H,O M-Mdx(1 - - —) + 18 ( - L_ 100 100 100 100 Mi. Pt - .-» 13.8 . 3 ) in. 13.8 Hg Vs - 85.49 x Cp X V« - 65.49 x ( Pax Mi A.- t-97 Qt-V«xA«xflO«/m x i, -yi xeo •dm Qaxl7.647x x(1- T. 100 \.-2) 100 , dMn ------- Plant Sampling Location Run Number: ^"V/ £. Date: Pretest Leak Rate: .pot cfm i Pretest Leak Check: Pitot: FIELD DA I A SHEET }'1 Operator: Sample Type: Pbar CO2: Ps: O2: Thermocouple Filter #: -^ in. Hg. Orsat: Probe Length/Type: / Stack Diameter: /3 v Pitot #: As: 1. Nozzle ID: --- Assumed Bws: Meter Box ___ Post-Test Leak Rate: .poo cfm @ J^ in. Hg. Post-Test Leak Check: Pitot: Orsat: Traverse Point Number Sampling (mln) £ 20 30 •30 I/O OockTime (24-hour dock) fttec £1 V0 0(50 22,00 0.9//D Gas Meter Reading (Vm)lt3 /<93,<93/ PO / '£o 96)^ / /O %S? I 9 . £> g 0r/ u?S^ Velocity Head (Ap) inH2O Orif ce Pressure Ditterential (AH) in H2O Desired Actual Stack Temp. (Ts) ;• Temperature y. op Probe Filter Impinger Temp. °F Dry Gas Meter Temp. Inlet (Tm in°F) y///////////////////////////y/////////////////////, /'?£> i f&> \ , %fa 1 < ?& ^f ^"V j^ <^»O 9^-' £6 Q^ Q- ^ 1 Outlet (Tm out°F) '////// 9v ^S 9r; AVm AH= Tm= : • ------- SAMPLE RECOVERY DATA Plant:. Date:_ Run No.: Sample Box No.: N-( Job No.: 6405 . Sample Location:. Sample Typp- EPA> Kg-ruoo 4 Sample Recovery Person: Comments: ~~ Filter No.: FRONT HALF Acetone Container No • Liquid Level Marked:. Filter Container No.: Sealed: Sealed: Description of Rlter: Samples Stored and Locked: BACK HALF/MOISTURE Container No.:. Liquid Level Marked:. Sealed: IMP. NO. 1 2 3 4 5 6 CONTENTS DX HT.O DX HLO Grv^^ ^ICI^A. £&— TOTAL INITIAL VOL (ml) /oo /ot> — ^50 WEIGHT (arams) INITIAL Ufl.1 bO&.O 496,2. 84o,? •2&Tr FINAL bU.1> ^oe.l, Wt.7 % ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: L^^ SOURCE/RUN #:±±JL PATE: 1. Leakage Correction for Volume Metered Vmc=( )-{ -0.02) x( ) Vmc= ft3 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) 'p^+tAH/iaef V_ = 17.64xV__xYxl — mstd mc V Tm )x 51U Vmstd = ^-2—dscf 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V = 0.04707 x (W. - W.) std ' Vw = 0.04707 X( -?.'J wstd 4. Percent Moisture, by Volume P wstd DWS- y ~^~T/ wstd mstd Bws = ------- /I -- i si PlantL Date: 5(10 METHOD 18 FIELD DATA SHEET Tested Analyte:. Location:_ Run #: /O Stack I.D.: Pbar: A?'9d / Sample Tuba • /£ -H/t to -f - Operators: Leak Check: Pre: rg0o Post: Time i< 36 2c ± Gauge Vacuum (Hg) 0 O O O Q Row Q0ttinr, Setting Tr«v«re« Point Numtar V«tocity H In. ^J. T Stack Tamp. °F .••^•"i .•vl-^rr Orifice Tank #: — Pump/Rotometer #: Pt: Pretest (mm Hg)f_I Post-Test (mm Hg)-,. Tt: Pretest CF):. Post-Test fF):_ Time: Stan^ge* Finish::?/^Total: ^.A W/B:"— D/B: —Q: Md - (0.44 x %CO2> -I- (0.32 X %O2> + (0.28 X %^) .Md-(0.44xO )-t-(0.32x ii ) +(0.28X •)•) f6> Md- 0^ •:•; M»-Mdx(l tH2O lob~! 100 • ) 100 100 °R (°F t-480) 13.8 13.8 P. . Vt - 05.48 x Cp X V.-85.48x( PaxMt • ar. « V«xA«xeOi/m - Q« xl 7.647 x X17.647X x(1 100 ------- FIELD DA I A SHEET Plant Sampling Location Run Number: Pretest Leak Rate: .002. Date: cfm Sample Type: Pbar: CO2: V Operator: Nozzle ID: Thermocouple Pa: O2: in. Hg. Pretest Leak Check: Pilot: "V Orsat: Probe Lengthflype: Stack Diameter: /< Pilot #: AH@: As: Assumed Bws: — Filter #: Meter Box #: )fy Y: ,?&£ Post-Test Leak Rate: Exso cfm @ /£ in. Hg. Post-Test Leak Check: Pilot: v^Orsat: —"~ TrawwM Pbht NunuM Samp** Time (mln) © /o £t) 3® lO Clock Time (24-hour dock) P£>C^ 50 /£> 5?o 9^» •j>63^ 9&'i& Gas Meter Reatfing (Vm) t\|3 /^* $ ' c^C>O /^ ^ / *£ 1 77 / yo ; ^$ / J iT / 3 3 . /^c- V«locrty Head(Ap) lnH2O Orif ce Presfture Drtterential (AH) in H2O Desired Actual Stack Temp. (7s) Temperature °F Probe \| Filter Impinger Temp. °F Dry Gas Meter Temp. Inlet (Tm in°F) CXjDet (Tm out°F) Pump Vacuum (in. Hg) Y/////y///////////w jf $£ l> %& 1 < c^ t / , ?^» — &CJ 5v~ £Q 67 0^ £r V 2'D &? «^s- f6 ------- Plant:. Date: •L SAMPLE RECOVERY DATA Run No.: -£ Job No.: Sample Box No.: Sample Location- /O Sample Type: Filter No.: Sample Recovery Person: Comments: FRONT HALF Acetone Container No. •_ Liquid Level Marked:. Filter Container No.:. Sealed: Sealed: Description of Filter: Samples Stored and Locked: BACK HALF/MOISTURE Container No.: Liquid Level Marked: Sealed: IMP. NO. 1 2 3 4 5 6 CONTENTS b fcv §) "£ ti-^0 £~<~pfy^~ 5ft<~W TOTAL INITIAL VOL (ml) foo L/^ 0 10 WEIGHT fqrams) INITIAL ^7.7 bbn ------- EPA METHOD 4 MOISTURE CALCULATIONS / PLANT: — — fr<^o V-'WjJr gni IPPF;PI IM #• to-i/-/ DATE: VrS/9"? 1 . Leakage Correction for Volume Metered vmc = V (Lp - La) x e vmc=( )-( -0.02) x( V = vmc 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) /(' 'std Vmstd 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V ... = 0.04707 x (W. - W. ) w T ' std Vw = 0.04707 x( std Vw =^_!±L_scf wstd 4. Percent Moisture, by Volume V, R wstd ws V,.. 4. V mstd Bws BWS— ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Sampling Location: OV&/V &• /O Run #: Date: 5 Clock Time: 3 ( Barometric Pressure, in. Hq: 9$<30 Static Pressure, in. h^O: '_ Moisture, %: Molecular wt., Dry; • Pitot Tube, Cp: •?? Stack Dimension, in. Diameter or Side 1: )5 Side 2: Wet Bulb, °R. Point Nurnbar 9* 3 ft- / G Velocity LJ^.-i nMH in. H2O Stack T«mp. Dry Bulb, °F: Md- r/0 93 P3I 32 °> 931 Md-(0.44x Md- )-t.(0.32xOl % H,0 % HO M« . Md x (1 - —) * 18 ( —-i- ) 100 100 Mi- °R(°F4ao) 13.B p,. ^ 13-8 m. Hg Vi • 65.40 X Cp X 1EJP x v«-as.48x( P9XM9 A.- ,.-2.1 ft2 Q»m V«xA«x60i/m Qt» Z^"? "1 acm O* .,-QiX 17.647X 100 ------- 3 OC3 CZ3 METHOD 18 FIELD DATA SHEET O aic S £< /n Plant: Ls s< -^ TesteH Analyte: xA,r^^ Date: 5 /"i •:/?-? Orific« Tank • urr *.? Location: A/Oj - A Run afc- A/D4 ~ H ~t PI imp/HrtfomsTer #: -" Pt- Prfltflst (mm Hq): Stack I.D.: 32' x (2 &" Post-Test (mm Hq): — Pbar: Zt> — • Leak Check: Pre: S Post: ^ W/B: — D/R (X,:2 i CO0: k Gauge Time Vacuum (Hg) i^fi'.^^. ' i /¥o/.^ / /#/£ •.»-, / " /¥^.^ :'V 1^0=1^3 / 1MU.O-? \ mi 2. <»* i Trav«rB« Point Number V.tecrty HMd In.H^O Flow Setting ^\ , M' -z-/ 7-1 \ ^\ -i^ Stack T«mp. °F Md - (0.44 x -SCXy + (0.32 X %02) + (0.28 X %(^) ^^ Md-(0.44x )+<0.32x )(0.28X ) :^ Md« £7 % H_0 % HO ^ M.-Mdx(1--^-)* "(-Eg-) '^ M« • < )x(1- ) + <8( ) fl" l ' * 100 100 4l fa- Ma- ft Qa«V«xAsx60«/m Qa» x xM Qt» acftn P. %K,0 Qi.a-QiKtr^Tx— -xd- -^-) Qi^- X17.847X 'X(1- 10JJ J OHM- < ------- p D U R S P S C L d\1» o Z/W '«• Ltfo * Aaoa 58 2,2. (o-K •l^ "36.30 * (to , METHOD 18 FIELD DATA SHEET lant: i-A-^o TesteH AnaiytR- ^^y^. ate: -r-x^-ri Orific« Tank • ~ acation: /w ft & Pump/Pntnmpter #: yo-W- un #: M n&- -4-2. Pt: Pretest (mm Hq): " _,. tack I. D.: £>.$"•< ?2." Post-Test (mm Hq); bar: -2^2- rt- Protect <°R- ample Tube (perators: eak Check: F #• AW-V-24 NDB-4-'2R Po«ft-T«fit CF): 55 ' Time: Start:? ijp Finish:^"o Total: 5t> re: ^^ Post: -" W/B: — D/B: - 00: ^' C00:_o — Gauge Time Vacuum (Hg) iH'S.Tf ; l¥'k.^ ( /^fl-1,/8 I '1-3-P-3"? I ^31,31 l • l C* O- • • i ^ \| Ll <^5l C ~7 i Flow Setting 27 2-( dl -ai •31 \ Travaraa Point Numbar Velocity Head In. H^O Stack Tamp. Md - (0.44 x %COZ) 4- (0.32 X %02> +• (0.28 x X^) f lr_ Md « (0 44 X ) +• (0,32 X ) +• (0.28 X ) _ Md- ^ % H20 % H20 "' 'X( " 100 100 lie iia Pt « In. Hg fi? - I y X)R> _—^ , j is r n) va - as.48 x up x iw x ^ p8 x Ma Va - 85.49 x ( ) x ( ) x A/ Va- ft/t A.. ft2 Qe » VaxAaxOOa/m Qt» x X00 Q»m adm Pa H_O aid" T« K 100 •to iw Otgm~ dacftn ------- APPENDIX A. 1.6 Condition 5 (includes flows, moistures, and Method 18) ------- OS METHOD 18 FIELD DATA SHEET k> Plant: Date: Pbar: Sample Tube Operators: - /A Leak Check: Pre: ./ Post: Travaraa Q— !_• "Olni Number i Z. T, -/ 5 6, 7 <<- / i ?> V <5 0 7 ? Valecity Head In. H^O 23 26 2.7 26, • z -32 »36 .iff .26 .30 -29 27. Zto .ZO .27 •2. -?7 Gauge Vacuum (Hg) / / / / Flow Setting / 50 /,- y £O £•!- ,40 t'-' ,4£>u T» -a- •rt 16 iS Time: Start:o?c-5 Finish: a ^>^> Total: W/B: 70 D/B: f 7 O2: ^y CO2: Md - (0.44 x %CO2> •!• (0.32 X %O2) -I- (0.28 X %Nj) Md - (0.44 x O ) + (0.32 x z/ ) + (0.28 x 7< Md. ZC.W %HO %H O M« - Mdxd - - — ) + 18 ( - — ) 100 100 Ma « ( ) x (1 - - ) + 18 ( - ) 100 100 T.- -87 °F- 5Y7 480, 13.6 13.8 Vs - 65.48 x Cp x Vs - 65.48 x ( Vs. 3£. f A.- >,G~» ft W ) X ( Ps x Ms )x I- ft/a 2 Qs-VixAxeoa/m Qi- ~ !• X17.647X' xeo %H2o 100 100 A, I) ------- ;aa c Plant: Site: WET-BULB/DRY-BULB MOISTURE CALCULATION Location: /}&;« Ft^n- Operators: .r»/,^ RUn #: Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Pbar Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw (from Table) = Pvw = (Ps - Pvw) x Vapor0"""-1 •"-* ^ - "-- '"---•- Pva = ne-s-i Date: 5-/?-.%?4 } .3 x Tw) 7 ) &5fr2« ) £?. o "7-. f> <* ' in. Ha . ^o% VAPOR PRESSURES OF WATER Tamp. OF 0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 160 190 200 210 220 230 240 0 0.0376 0.0631 0.1025 0.1647 0.2478 0.3626 0.5218 0.7392 1.032 1.422 1.932 2.596 3.446 4.525 5.881 7.569 9.652 1250 1559 19.01 23.47 28.79 35.00 4241 5044- 1 0.0398 0.0660 0.1080 0.1716 0.2576 0.3764 0.5407 0.7648 1.066 1.467 1.992 2.672 3.543 4.647 6.034 7.759 9.885 12.48 15.83 19.42 23.96 2943 35.68 43.11 51.78 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.842 4.772 6.190 7.952 10.12 12.77 15.98 19.84 24.48 29.92 36.37 43.92 52.70 3 0.0441 0.0728 0.1186 0.1878 0.2782 0.4052 0.5802 0.6183 1.138 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.36 13.07 16.34 2057 24.97 30.52 37.07 44.74 5345 4 0.0463 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 6.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.87 54.82 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.680 8.557 10.86 13.67 17.07 21.14 26.00 31.75 38.50 4041 5540 6 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.650 8.767 11.12 13.98 17.44 21.59 26.53 3248 3954 4757 5640 / 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.370 3.169 4.174 5.442 7.024 8.981 11.38 14.30 17.82 22.05 27.07 33.02 3949 48.14 5741 •V " I 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4058 0.6903 0.9666 1.335 1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.82 1841 22.52 27.82 3347 40.75 4943 9 0.0598 0.0982 0.1567 0.2383 0.3403 0.5035 0.7144 0.9989 1.378 1.679 2.521 3.351 4.408 5.732 7.384 9.424 11.92 14.98 1841 2249 28.18 3443 4142 4943 5947 ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant- Lflsto Date: s-/9-9~? Sampling Loc Run #: />te - ation: /fy «,;•/, £f\\*t!- Clock Time: /// V 5 0 •7 £ • - a:z# ^ Static Pressure, in. HUO: -'°3 MnlPr.ilar\wt nrv-2^/ PitOt Tube. CD: -^ iion, in. Diameter or Side -72. DrvB Vstocity Head in. H2O . , ,22 ,25 ,2.5 l£ ,3O ,33 i35 .3^ .26 , 3i5 ' 2-^ .Zff .^6? '2"? .21 /2^ SUck T«mp. °F fo :7^ ^ 90 10 70 Jo 90 to 90 9o ?o ^? ^^ 9* yo $F - >^i tr«- ^^c? 1- /7^S Side 2: Mih.op- TO Md - (0.4A x ) * (0.32 X ) + (0.28 X ) Md- ?"/ % HO % HO MS- MO XII 100 100 13.0 13.0 p* . 0^. "ti^ In. Hg £p -.??«.. -= / Ts(°R) V.-«5.48XCPX^P X ^ P9XM9 1 Vs - 85.48 x ( ) x ( ) x A< v.. 3C-55 m A 1 »2 A-" '-6~7 Qt — Vs x A* X 00 i/m Qs» X xOO Os • 3G(p S Acfcn p. %H,0 Qi .,-Q* XI 7.847 x x(1 ^-) •» Ti 100 •to 1w- ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: i-^co Location: w; FWi,^y- Site: /1/lfM EAtoud- Operators: Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Pbar + - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of HpO at Tw Vaoor Pressure of H-.O = Pva =''(Pwi\ • rn/jt Runs: ne-s-z. Date: .•/-/• Pbar = ^"? . Vf Pg = -^03 Pg p<5= s V- So IJ.b Tw = -T3 Td= 10 AT= 11 (frnpn T^hl») = P^W = ^ ' ^ ___ (Ps - Pvw) x (A"0 f'rfl in. Hg '. in. KLO 2 in. Hg °F °F °F in. Hg 2800 - (1.3 x Tw) Pva=( ~ G 2800 - (1.3 x Proportion of Water Vapor by Volume = Bws (Ps) T«mp. OF 0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 0 0.0378 0.0831 0.1025 0.1847 0.2478 0.3828 0.5218 0.7392 1.032 1.422 1.932 2.598 3.446 4.525 5.881 7.589 9.652 1250 1559 19.01 23.47 28.75 35.00 42.31 50.84- 1 0.0398 0.0680 0.1080 0.1718 0.2578 0.3764 0.5407 0.7648 1.066 1.467 1.992 2.672 3.543 4.647 6.034 7.759 9.665 12.48 15.63 19.42 23.96 29.33 35.68 43.11 51.78 in. Hg ( ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0698 0.1127 0.1803 0.2877 0.3906 .OJSgpi lOJSMT) 1.102 1.513 2.052 2.749 3.642 4.772 8.190 7.952 10.12 12.77 15.96 19.84 24.46 29.92 36.37 43.92 52.70 3 0.0441 0.0728 0.1188 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.829 3.744 4.900 8.350 8.150 10.38 13.07 16.34 20.27 24.97 30.52 37.07 44.74 53.65 4 0.0463 C.0768 0.1248 0.1955 3.2891 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 9.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.67 54.62 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.8222 0.6750 1.213 1.660 2.243 2.995 3.954 5.165 6.660 8.557 10.66 13.67 17.07 21.14 26.00 31.75 38.90 4641 55.60 a 0.0517 0.0846 0.1370 0.2118 0.3120 _ 0.4520 ' 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.650 8.767 11.12 13.98 17.44 21.59 26.53 32.38 3924 4757 56.60 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4688 0.8669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 6.981 11.38 14.30 17.82 22.05 27.07 33.02 3949 48.14 57.01 a 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.619 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1851 22.52 27.62 33.67 40.75 49.03 5843 9 0.0598 0.0982 0.1567 0.2383 0.3493 0.5035 0.7144 0.9969 1.378 1.878 2.521 3.351 4.406 5.732 7.364 9.424 11.92 1446 1841 2249 28.18 3443 4142 4848 5947 ------- 3 at GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: UftStO Date: >-/?-?-; Sampling Location: M»7rt (^IV,^A Clock Time: /35"~7 Run #: \|ft- ^2-- 1: i 7. -5" Side 2: — it Jib OF- ?2 Md - (0.44x%CO2) + (0.32X%02) f (0.28 X%Nj) Md - (0.44 x ) •)• (0.32 X ) •)• (0.28 X ) Md- 2-f.<9 % H.O % HO J,.Md(1 -j^-) ' 1fl< )OQ ) M.., )x(,.__->18(_j^.) M.. w.ii T:. <^2. °F- 5^2^ °n (°p4«o) e p r' ° 13.8 ' ' 13.8 ?•- 2-^^^ In-Ha ^SP - ^ ^^> — / Ts fto) V.-U5.4WXLPX JAH X \l P9XM8 A.. /.^^ n2 Q»- x xOO Q« » "?">/> / «cn ^7^/ Pt H>° Q.ttd.Q.X17.647x — «<1.-j^-> ------- WET-BULB/DRY-BULB MOISTURE CALCUU\TION Plant: Site: /\|fU,fl Operators: 7 Location: AO^..^ £->hc,^ /- Run #: Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar i ,. _ I J.U Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw (from Table) = Pvw =—Q. (Ps - Pvw) x (AT) A»e - 5- 3 Date: Pbar = "2^,^* Pq = -t- . o 1^ Ps = 'Zt. &$ Tw = 7o-V ) ) &oZ.<°$} VAPOR PRESSURES OF WATER ^/Z.Z- ^ n In Inches of Mercury 2. 7o^ 2 0.0417 0.0090 0.1127 0.1803 0.2077 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 8.190 7.952 10.12 12.77 15.98 19.84 24.46 29.92 36.37 43.02 52.70 3 0.0441 0.0728 0.1186 0.1878 0.2702 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.38 13.07 18.34 2027 2447 30.82 37.07 44.74 8348 4 0.0463 0.0708 0.1248 0.1955 0.2891 0.4203 0.0009 0.8462 1.175 1.010 2.178 2.911 3.848 5.031 0.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.87 54.62 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.0222 0.8750 1.213 1.000 2.243 2.995 3.954 5.165 8.680 8.557 10.86 13.67 17.07 21.14 26.00 31.75 38.50 4841 5540 e 0.0517 0.0848 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 0.850 8.787 11.12 13.98 17.44 21.59 26.83 3248 3924 4727 56.60 7 0.0541 0.0092 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.981 11.38 14.30 17.82 22.05 27.07 3342 3949 48.14 5741 a 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1821 2242 27.82 3347 40.73 4043 5843 I7Y? 9 0.0598 0.0982 0.1567 0.2383 0.3493 0.5035 0.7144 0.0080 1.378 1.878 2.521 3.381 4.408 5.732 7.384 9.424 11.02 14.08 1841 2240 28.18 3443 4142 4043 8947 ------- METHOD 18 FIELD DATA SHEET e'C ' 3lant: L-fe<-O Tactqd Analvte: S^/^a jate: ^-/v-«n nrifjra Tank #: .ocation: — S^^^h^t Pumr/Rotometer #: i^sT " / Sun #: Re - ~ - I p». Pr-ntest (mm Ha^: stack I.D.: 2.8v 2zv - PmMest (mm Hcrt: - JDar: ..z.fS Tt. Pretest<°R: sample Tube Operators: #:A£^-i+(Rt-<-/K Post-Test t°F): r/ Time- Start:<°-/ Rnish: <>i Total: 4^ Leak Uheck: Pre: ,/ Post- ^ Gauge Time Vacuum (H9) -7-7 f. 90 9 / n/5. ^5 ' 77/6. ^^ ^ n/y. 37 / •n/7. « / 772C7, ^£ / Trovers* Point Numbr f j •>! ^ ( ^ « $ 1 i 3 i (0 t 3 5 1 1 iNI». Valodty HMd In. H^3 §,0.5 0^ c$ • 0(t> .01 .07 ,07 • eft .05 .01 ,0* .07 ,/0 ,09 .£>$ -^ . /^ .03 06 ,65 -oV /O^ . 16 .,>«<«rv Flow Setting '5o^£. l£o^. l40 .L. /£&<- JJo^t. Slack T«mp. °F ^»^ 4t •?e §0 ?a v> vO ?£> ^o 0 1 46 96 fro to 90 \ — 2°- W/B:70 D/B: yi O2;-2^ CO2: A Md - (0.44x%CX32) -t- (0.32 X%O2) + (0.28 x%l^) T 1.' Md - :3 =) IS ' -^ %H.O %H,0 7? M«-Mdx(1- £_) + 18( — ) 100 100 " M« - ( )x(1 - ^ ' ) + 18 ( " ' ' ) fu 10° 10° M.- ^T^A 9?.-?-) T.- ^ °F- SV^ °* (°F4«0) P« - Pb SP< - ( ) + 13.0 13.0 P.- pj <<} ln.Hg ^P - -?V7-7 == J Ta (^R) V. - 85.48 « CH * V£»P * ^ p8xM§ Vi_ASAOv( )y( )KA/- vs. t^Mry n/. n.^(p A.- >4,61 ft2 Qt« VtxA>xOO«/m Q« • x x40 /- j^^ (ll~T~v---7N Qt" ']..ta' j aclm^}^^)1^.!^^!^ P« %K,0 Qi^-Qi XI 7.847 X x(1- - ) •5. I «d '100 .__,_-.- r i \t i" — ~^^ QN«- &££>««* V4L!o> A , ------- WET-BULB/DRY-BULB MOISTURE CALCUU\T!ON Plant: Lfc0 Op ^^ OP 19 °F '73^? in. Hg 2800-(1.3xTw) Pva=( 2800-(1.3 x Proportion of Water Vapor by Volume = Bws Bws= T«nnp. "F o 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 (Ps) 0 0.0376 0.0631 0.1025 0.1647 0.2478 0.3626 0.5218 QgH? 1.032 1.422 1.932 2.596 3.446 4.525 5.881 7.569 9.652 1240 1549 19.01 23.47 28.78 35.00 4241 5044- 1 0.0398 0.0660 0.1060 0.1716 0.2576 0.3764 0.5407 0.7648 1.066 1.467 1.992 2.672 3.543 4.647 6.034 7.759 9.888 12.48 15.63 19.42 2348 2943 38.88 43.11 51.78 in. Hg ( ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 15.98 19.84 24.40 29.92 36.37 43.92 52.70 3 0.0441 0.0728 0.1186 0.1878 0.2782 0.4052 0.5602 0.6183 1.138 1.561 2.114 2.629 3.744 4.300 6.350 8.150 10.36 13.07 16.34 20.27 24.97 30.82 37.07 44.74 53.88 4 0.0463 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 6.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.76 45.87 54.62 5 0.0469 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.660 8.557 10.86 13.67 17.07 21.14 28.00 31.78 38.80 4841 5840 6 0.0517 0.0646 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.850 8.767 11.12 13.96 17.44 21.59 26.53 3248 3944 4747 56.60 7 0.0541 0.0692 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.961 11.38 14.30 17.82 22.05 27.07 33.02 3949 48.14 5741 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.619 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1841 2242 27.82 33.87 40.78 4943 5843 9 ' 0.0598 0.0962 0.1567 0.2383 0.3493 0.5035 0.7144 0.9989 1.378 1478 2.821 3.351 4.408 5.732 7.384 9.424 1142 14.98 1841 2249 28.18 3449 4142 4943 8847 ------- 3 aq_ cza GAS VELOCITY AND VOLUMETRIC FLOW RATE =lant: } fao Date: ^' /v?~^7 Sampling Loc Run #: /^ ation: a,™ £•/,.. ^- Clock Time: ;/vz -5-2. Qoerators: -fr/jj Barometric Pressure, in. H Moisture, %: 1- • 3 Stack Dimens Wet Bulb, °F Point Numb«r 1 I i M .5 6 , x •» 4 5 c. f z. 3 f 5 6 i 2. •, f 5 ' 0 q- 2^ , O Static Pressure, in. hUO: ". 6 2, Molecular wt..Drv: ?e.fV Pitot Tube. Cp: ion, in. Diameter or Side "I/ DrvB V«loctty in. H2O • £>5 i ^-S ,oS -c)G ,06 .6(p .66 ,01 o5 .£>£> .11 JO &o .OS .0$ JO .Ck .& .05 >of> .05 Stack T«mp. °F 31 ^ ^i #3 %3 t^> W W <32> fi ^3 fS ^ fV ^?3 ?^ ?i f3 rs S3 T3 •• (0.28 X%Nj) Md - (0.44 x ) + (0.32 X ) + (0.28 x ) Md - IS] % H.O % HO M«-( )x • V« x A> x 00 t/m Q«- x xflO Q. . IfW^ adm P, KHjO Q«rtda °« » 7-M7 x ~ * « • -^5- > IA ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: l_te% ( rub > VAPOR PRESSURES OF WATER ^_£jL_^ ^ In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 8.190 7.952 10.12 12.77 15.98 19.84 24.46 29.92 36.37 43.92 52.70 3 0.0441 0.0728 0.1186 0.1878 0.2782 0.4052 0.5602 0.8183 1.138 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.36 13.07 16.34 2057 24.97 30.52 37.07 44.74 53.65 4 0.0463 3.0768 3.1248 0.1955 3.2891 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3,348 ,5,031 ?.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.87 54.62 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.6750 1.213 1.660 2543 2.995 3.954 5.165 6.660 8.557 10.86 13.67 17.07 21.14 26.00 31.75 38.50 46.41 55.60 6 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.850 8.767 11.12 13.98 17.44 21.59 26.53 32.36 3954 47.27 56.60 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 6.981 11.38 14.30 1742 22.05 27.07 3342 3949 48.14 5741 27^7"" a 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.619 2.448 3.259 4.289 5.565 7.202 9.200 11.65 14.62 1841 2242 27.62 33.07 40.75 4943 5843 9 0.0598 0.0982 0.1567 0.2383 0.3493 0.5035 0.7144 0.9989 1.378 1.675 2.521 3.351 4.406 5.732 7.384 9.424 11.92 14.98 1841 2249 28.18 3443 4142 4943 5947 ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Date: 5-/y-»7 Sampling Loc Run #: fi£ - atiorv &»-„, £/v ^ Clock Time: 14 to - ~\ Oner?nors: r/xx Barometric Pressure, in. H Moisture, %: 2 - 0- Stack Dimens Wet Bulb, °F: TravarM Point Number / I 2> ^ 5 L. i 1 ^ <, 5 (j , ^ 3 q ?• L — 9- 7 /<-.,- Stati^ Pressure, in. HUO: '.61 Molecular wt.. Drv: zT.^v Pitot Tube, Cp: _<_2f ion, in. Diameter or Side 1\ DrvB Valocny in. H2O ,0? ,^•1 .00 .c><- .0? i <=tf i 01 of 0Cs t Cr& &J> . 00 ;/0 •Of .0^" .cx5 . ./o •FT^ Stack T«mp. °F \fS $$ $5 Md- CH %H.O %H O '"" """" "* " 100 '00 Ma — ~)-o''~"i(j: Q O O ^ TM • cx £^ P * S if C H ' r ^ *oO\| Pa - Pb S'P' = < ) * — — 13.8 13.8 Pa- Ti'j'-Oy In. Hg ^P» ^OC.^J -;; / Ts"PR) Va - 65.48 x Cp x VAP x W "pg"x Ma , J Va - \3> - 7 I «/• A* • i i(f 1 " Qs • Va x Aa x 00 a/m a.. x xeo Q,. ^01°] adm p. "^o, Qs ..* Qa x 17.847 x — x (1 • — — - ) Qt^- X17.647X X(1'~^J"* i.u ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: '<.&<>£.& Site: j^o-x EUa4 Operators: Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Pbar 3 - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw Vapor Pressure of H^O = Pva = (Pvw) • Pvn=( ). Location: fe^ £,h<...^L :-.- £5 Run if. fy?- - "S Pbar = Pg = -£2_ Ps = 1 J.O Tw = Td = AT = (from Table) = Pvw = (Ps r.vpwv) x (AT) 2BOO-(l.3xTw) )x( ) Date: s -/ = ( (Ps) ) ( ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 o.oeoa 0.1127 0.1803 0.2877 0.3008 0.5601 0.7812 1.102 1.513 2452 2.748 3442 4.772 8.160 7.852 10.12 12.77 1848 1844 2446 2842 3847 4842 52JO 3 0.0441 0.0778 0.1188 0.1878 0.2782 0.4082 0.3802 0.6163 1.136 1.561 2.114 2.828 3.744 4.800 8450 8.160 1048 1347 1644 2047 2447 3042 3747 44.74 9348 4 3.0483 0.0788 0.1248 3.18S5 0.2881 0.4203 0.8008 0.8482 1.175 1.810 2.178 2411 3446 5.031 8.513 8451 1041 1347 16.70 2070 2548 31.18 3778 4847 5442 5 0.0460 0.081 0 3.1302 0.2035 04004 0.4358 0.6222 04750 1.213 1.860 2-243 2.988 3454 9.165 6.660 8457 1046 1347 1747 21.14 2840 31.78 3840 4841 5840 a 0.0517 3.0846 0.1370 0.2118 0.3120 0.4820 0.6442 0.8046 1.253 1.712 2410 3461 4463 5402 6490 8.767 11.12 1348 1744 2148 2849 3248'. • 3844 4747 5840 7 0.0541 0.0882 0.1428 0.2203 0.3240 0.4688 0.6688 0.8352 1.283 1.785 2478 3.168 4.174 9.442 7.024 6481 11.38 1440 1742 2248 2747 3342 3848 48.14 5741 a 0.0371 3.0832 0.1302 0.2282 0.3364 0.4888 0.8803 0.8686 1.335 1.818 2.440 3258 4.288 5.585 7202 0400 11.65 1442 1641 2242 2742 3347- 4078 ^ffftf 9848-- 0 0.0586 0.0882 0.1567 02383 04483 04938 0.7144 04888 1478 1478 2421 3481 4408 9.732 7484 8484 1142 1448 1841 2248 2848 3448 4148 4848 8847 ------- ^ag cza GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: M5^> Date: 5 -/•/-?-! Sampling Loc Run #: f\ F ation: ,W\Wv/ ^/> Clock Time: /wztf - T- 1 ' Operators- 7"#/£5 Barometric Pressure, in. H Moisture, %: ^ / Stack Dimenj Wet Bulb, °F TrivarM p— i— rOlfn Number / 2- .3 y £ 6 7 r / 7. 3 y 5 £ 7 ar • a: ^.^S Static Pressure, in. HUO: - -~l "7 Molecular wt.. Drv: SLfe.<^ PltOt Tube, Cp:^/:i sion, in. Diameter or Side /O DrvE V.tewty H«U in. H20 .^>O .^9 ^/2 ,^/2- ,^6 W • 3V ,3^> ,22> ,30 .3C, //6 '^3 > Vl .5^ ,27^ ^F-,^5^ Stock T«mp. °F tz <32> ?-L $->~ '* 93 ^3 ^3 ?Z ^2> f ^ ?3 ^3 » O ^3 IT:- ^3 1- j M.- ^f^ Zft^7 Tl. ^3 °F- ^^ °R (°F460) pn . Pb t ?-P>. - ( ) •"• — : 13.8 '3.8 P.. T.B.7-7 IO.HQ ^' ^.^ ------- Plant: L$uo Site: K flfni'kcj fu^v Operators: />/• WET-BULB/DRY-BULB MOISTURE CALCULATION Location: Run #: Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of StacK = Pbar Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw (from Table) = Pvw = Vapor Pressure of^O = Pva = (Pvw) (PS ' FVW) X ^ -r_P2_ - 13.6 "1- #i^x . 'I <"•••«/ rh « AF-S-I Pbar = Pg = Ps = Tw = Td = / Date: •:-/• 2-£t>$T -.77 28,77 -70 $1 -> in. Hg in. H00 2 in. Hg _°F °F AT= tl °F Pvw = 0.7 &1- _ in. Hg Pva=( )- 2800-(1-3xTw) ( '3 ) 2800-(1.3 x in. Hg Proportion of Water Vapor by Volume = Bws ( Ttmp. op 0 10 zo 30 40 50 00 70 80 80 100 110 120 130 140 150 160 170 180 180 200 210 220 290 240 (Ps) 0 0.0376 0.0831 0.1025 0.1847 04478 0.3826 0.5218 0.7382 1.032 1.422 1.832 2.586 3.446 4.825 5481 7.569 8.682 1240 1549 1941 2347 28.78 3540 4241 5044 1 0.0388 0.0660 0.1080 0.1716 04576 0.3764 0.5407 0.7648 1.066 1.467 1.802 2.672 3449 4.647 6.034 7.759 8.888 1248 1843 1942 2349 2949 3848 49.11 51.78 &.Q2-I ( Z8. 7? ) VAPOR PRESSURES OF WATER ^£££ ^ £>. In Inches of Mercury Z- 7° ? 2 3.0417 0.0888 0.1127 0.1803 0.2677 0.3808 0.5601 0.7812 1.102 1.513 2452 2.748 3.642 4.772 6.190 7.952 10.12 12.77 1548 1944 2446 2942 3947 4942 5&70 3 0.0441 0.0728 0.11B6 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.829 3.744 4.800 6.350 6.160 1046 13.07 1644 2047 2447 3042 3747 44.74 5348 4 . 3.0463 3.0768 3. 1248 3.1955 0.2681 0.4203 0.6008 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 0.513 8.351 10.61 1347 16.70 20.70 2948 31.13 37.78 4847 5442 5 0.0488 0.0810 3.1302 0.2035 0.3004 0.4358 0.6222 0.8750 1.213 1.660 2443 2.998 3.954 5.165 6.660 6457 1046 13.67 17.07 21.14 2840 31.78 3840 4641 5540 8 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.8046 1.253 1.712 2410 3.081 4.069 5.302 6.850 6.767 11.12 13.98 17.44 2149 2843 3249 3944 4747 5840 7 0.0541 0.0882 3.1428 0.2203 0.3240 0.4666 0.6668 0.8352 1.293 1.765 2479 3.169 4.174 5.442 7.024 6.981 11.36 14.90 1742 2245 2747 33.M 3940 46.14 5741 a 0.0371 0.0832 3.1S02 0.2282 0.3364 0.4658 0.6803 0.8666 1.335 1.618 2.448 3458 4.288 5.585 7.202 8.200 11.65 14.62 1641 2242 2742 3947 40.78 4949 5949 0 . 0.0596 0.0962 0.1567 04363 04499 0.5095 0.7144 0.9989 1.378 1.878 2421 3481 4408 5.732 7.384 9424 1142 1449 1941 2249 28.18 3449 4142 4848 5847 ------- METHOD 18 FIELD DATASHEET Plant; Date: s Location:. Stack I.D.:_i' Pbar: og. ti Sample Tube Operators:. Leak Check: Pre: Post: i/ // Time Gauge Vacuum (Hg) Flow Setting e. c Tr«v«re« Point Number V.toetty HMd In. stack T«mp. °F Tested Analyte:_l^ Orifice Tank #: Pt: Pretest (mm Hg)-_ Post-Test (mm Hg); Tt: Pretest Time: Start;//££_Finish W/B: - D/B: - O9 Md - (0.44x%CO2) + (0.32X%O2> + (0.28 X"^) •^flt- Md - (0.44 X ) -f (0.32 X ) -t- (0.28 X ) ------- jog a METHOD 18 FIELD DATA SHEET //£? o H 19 . '2# if "3S- v, Hi* no '/£« ° /4cf to /i 11 ~i 1^1 4V- f.13 ^ ^ M J PlantUJ^ Date: -s-/ Location: /J, Run#: /IP Stack I.D.: Pbar: Z. Sample Tube Operators :_: Leak Check: Time 1111. o~i 7122, LC ™\ vf nz"• :Of.L. \6Oti. t^Ot-i. )S£>LL Stack T.mp. ?i ^3 ^2. ^^? ?V ^-5 94 ^S #4 M $ w ?1 94 ?4 91 rt Tested AnaJyte: 5^^^ Orifica Tank : Pump/Rotometer #: y^sr^ \| Pt: Pretest (mm Hg): Post-Test (mm Hg): - Tt: Pretest f F): Post-Test <°F): Time: Start: nan Finish: Total: ^ W/B: "7O D/B: ?Y Q^: zi CCL: c5 ^ ^ •~-^~- Md - (0.44x%CO2) 4- (0.32 xXOj) -I- (0.28 x%Nj) — £- Md - (0.44 n ) -t- (0.32 X ) -t- (0.28 X ) * ^<* — P? % H_O % H.O <\? M«-Mdx(1- l_)-i-l8( — ) c 100 100 ^V ^- 1 9 - I ' Ma ml \ v M 1 i IB ( , \ Mt ( )X(1 10Q ) 1H( ) 15 ,„ "" ^^ ,. T.. XV ">F. S^ °fl(°F,4Ji In Ha " CT5- /y HI. ny fi? - ' S^4 ~) '»• -J O I ' 1= ,1 T"*") V.-M.4«MOpxVAP X ^ P8XM. W« « A^ Afiy/ \ • 1 \ Y + I Mm L)/0 /^-/ »/. ¥• • TV/--' / ft/I ^-i 1 ? o A* - o/ » v S n* Q«- V«xA«xOO«/m Qi- x xflO s~ t _ i 1 Q«- ? l^y adm PB S H_0 Q« .,-Q« XI 7.847 x x(1 2_) •• T« 100 QHtd- ^ ^"? "^ dMfcn ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: /_* < < ,, Site: Aut.tcttj Pi A Operators: Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Pbar 3 - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw Vapor Pressure of h^O = Pva = iPwv) - Pva - ( ) - /i < • '- Location: '/f-j'' «w -x-» «<•»• •»^ri Run ff: Af-^ • "5 Date: -. Pbar= ^-<* Pg = - - i S _PO_ ps= V?. -7V U.b Tw = -75 Td= ^^ AT= ^ ( o 10 20 30 40 50 00 70 80 90 100 110 120 130 140 150 160 170 180 190 200 210 220 290 240 (Ps) 0 0.0376 0.0631 0.1025 0.1647 04478 0.3626 ^2,jg18 ^OTMifr) 1.032 1.422 1.933 2.598 3.446 4.828 5.881 7.589 9.683 1240 1549 1941 2347 28.78 3840 4341 5044 1 0.0398 0.0660 0.1080 0.1716 0.2578 0.3764 0.5407 0.7648 1.068 1.467 1.883 2.872 3.543 4.647 6.034 7.789 8.888 13.48 1949 1843 2346 2943 3848 4S.11 81.76 ( ( ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1603 0.2677 0.3906 0.5601 0.7812 1.102 1.513 2.052 2.749 3.842 4.772 6.180 7.8S2 10.12 12.77 15.88 1844 24.48 2842 3847 4842 52.70 3 0.0441 0.0728 0.1188 0.1676 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.628 3.744 4.800 0.350 8.180 10.36 13.07 16.34 2047 2447 3042 3747 44.74 5348 4 0.0463 0.0768 0.1248 0.1955 0.2891 0.4203 0.6008 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 0.513 8.381 10.81 13.37 16.70 20.70 2548 31.19 37.78 4847 5442 5 0.0469 0.0610 0.1302 0.2035 0.3004 0.4358 0.6222 0.8750 1.213 1.660 2449 2.888 3.854 5.185 6.880 6.887 1046 19.87 17.07 21.14 2840 31.78 M.BO 48X41 5540 0 0.0517 0.0846 0.1370 0.2116 0.3120 0.4520 0.6442 0.8046 1.253 1.712 2410 3.081 4.069 5.302 8.880 8.767 11.12 1948 17.44 2148 2849 3248 3944 4747 7 0.0541 0.0692 0.1429 0.2203 0.3240 0.4666 0.6669 0.9352 1.293 1.769 2.379 3.169 4.174 5.442 7.024 8.881 11.38 14.30 17.82 22.03 2747 3342 3949 48.14 S741 a 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.819 2.448 3458 4.288 5.585 7.202 9400 11.68 14.82 1641 77,57 2742 3347 40.78 4948 5848 0 0.0588 0.0882 0.1567 04383 04483 0.8098 0.7144 0.9989 1.378 1.878 2421 3481 4408 5.732 7.984 9434 1142 1448 1841 2249 28.18 9448 41J2 4948 5847 ------- J aa eg GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Lteto Date: 5-^.^7 Sampling Location: /ju,;i,f,n, £.rt Clock Timp- ; «-7 y-7 77 ^/ ?-/ ffe ?s ft* ^4 ?^ Jt g^7 S- 8C a1: it. is Side 2: 3ulb.°F: 97 Md - (0.44 x ^COj) i- (0.32 X %O2) t- (0.28 X -JfeNj) Md » (0.44 x ) -t- (0.32 X ) + (0.28 X ) Md- ^ % HO % HO M« - Md x ( 1 • ) -t- 1 8 ( ) 100 100 Mt-< )x(i- -— — ) + ia<— __) 100 100 Mi. ^^77 T- fy °F- ^(f °R(°F4«), o p Da _ OU j. :3'r- i \ ^. 13.6 13.8 • 2 8, ^ in-Ha ^Sp - ^ 5^^ — I Ta (°R1 r^ .1 i j i iij v.-«b.4wxu>x VAP x ^ P9XM8 V v.. 37,277 n/t A.. 2. ^3 ft2 Qt- V«xA«xeo«/m Qs- x x60 • $oio "" Pa H,0 Q«^- Qi XI 7.847 X x(1- —2-) •" !• 100 •" 100 ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: / ft^o Site: Au7i(u. Date: Pbar = 2- §, k $ Pg = -. 8 > _±2_ Pfi = 1%, ^ IJ.b Tw = 7 f Td= V7 AT= «* ( ------- ooa a ^ »> i—.— i Plant: JASda Date: S-tf-T Location: Run#: METHOD 18 FIELD DATA SHEET . Tested Anaiyte:_ —. Orifice Tank #:. Stack I.P.: Pbar: , Sample Tube; Operators: Pump/Rotometer #: Pt: Pretest (mm Hg)-_rzi_ Post-Test (mm HQ): — Tt: Pretest Post-Test fF) Time: Start:oycw Finish: lew Total: 60 W/B: — D/B: "~ O~: — Time M0 (fa Its rYn l(<\ 1$ l&i j-n ting "//>i/n - i f k P. ) 1, D- D- j r^ <; fe> ,7 -7 f? AOi Md - (0.44 x %C02) ••• (0.32 X %O2) + (0.28 X %r^» Md - (0.44 x ) + (0.32 X ) + (0.28 X ) . ^I/^C '•/. Md - ?ys^ I % H.O % H.O M«-Mdx(1--l&T-)18(^o-) 7f :-^ M»-(e3r.r< ' x (1 ' — ^5~ 100^ M.- 1^,5^ T». '04 °F- 0"2-"/ °R (°F4«0) S P ~> GO P»-»*-S-W.2i > 13(J jXp - zj 'XcJ o j== J T«<°R' V.- 65.48 xcpx^x ^ paxMt V ^.20 / Zii e v/ O v« - ' ' •/ n/» Aa- 1,2-5 nz Qa- VexAaxOOa/m Qa- "il .^3) x 1,13 x«> Q.-L.'bH^ «' Qa^- , * l) dwftn ------- FIELD DA I A SHEET Plant 6/).3dQ Sampling Location Run Number: •£- 1 Sample Type: Operator: Nozzle ID: Thermocouple #: > Date: $•/TQ Post-Test Leak Rate: .peg ctm in. Hg. As: Post-Test Leak Check: PHot: — Orsal: Point Number j Sampling Tim* (rnin) o 90 LffQ Vv OockTbm (24-hour dock) . GGIO< (09/< O93s />9 '3i' &&£' O^Vfi Gaa Meter Reading Qf) 3 ' s rffl O CJ^'T,. ;ri 3V L / g^C-' ,^^ <^^T - 7fc> P60 ,V/6 Velocity Head(Ap) inH2O Oil ca Pressure Differential (AH)inH2O Desired Actual Stack Temp. (Is) Temperature °F Probe Biter Impinger Temp. °F Dry Gas Meter Temp. Inlet (Tm in°F) Outlet (Tm out°F) y///////////////////////////^^ //£"£> /• J7^ /,/^ p y ' (Of) 3 $~ £ <£>O £ f ^ $6 & 5^ ?3^ jp —y £?/ ^ ^ ^f Pump Vacuum (in. Hg) Y/Z 3 ^ ^ -7 j:i- AVm- Trn ------- SAMPLE RECOVERY DATA PLANT DATE £ ~ I °\ • °i 1 Sample Box No. Run No. Job No. SAMPLE LOCATION TRAIN PREPARER °V QQ^O Filter No. SAMPLE RECOVERY PERSON COMMENTS FRONT HALF Acetone Container No. Filter Container No. Description of Filter Liquid Level Marked Sealed Sealed Samples Stored and Locked BACK HALF/MOTSTTTflF, Container No. Liquid Level Marked Sealed o* IMP. NO. CONTENTS INITIAL VOL (ml) WEIGHT (grams) INITIAL FINAL NET Lit.* 9ft 7 TOTAL ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Mt>C 0 Date: Sampling Location: £)(,'Jf /I/ #" ,;^ r,3/^ ,.93 9P ..01 .90 £p-,VV Stack 1 T«mp. °F 160 Ibl ( (< /62 160 1 6/ tbH- jfyf* /v~> IA1 I&1 ll>« ft- /AV Md - (0.44 x %C02> f (0.32 X -KOj) + (0.28 X ^~^~ %H2°, ,Bf%H2°, /^/3* /.^"/ M.-Mdxd--^-) -ie( io(J ) M,-<.iv.w )X(i. —^5 -) 18<-^5~> MS- 2g;73 Tl. ;CV °F-6ZV °R(°F4«J) OL bw a. S-P- _. 124 15 1 r - "" '^-n. 13.8 13-a Pt- i.'j-'Z- In. Hg ^- .^S* / fa (^R) Vt « 65.48 x Cp x n2 Q«. V«xA»xeO«/m Qt. X xM ^ /40( ""^ Pt H_0 Q.ttd-Q.Xl7.647xirx(1.-^r) 12- , . i Q.^. xir.fl47x-z:I^ «n-ToT»' /A. ------- FIELD DA IA SHEET Plank LM^C.Q Sample Type: r\'li Operator: JN^/&G Sampling Loci Run Number: itk>n Qj«.irJ ^ V Pbar ly/1. Pd> Ps: ~, ££> our dock) j3£l l^fl^ 1 l /'3 "..IT £}J / *l 3 3 — Stack Diameter: /6T" As: 1.23^ 3T-3 r Gas Meter Reading (Vm)fl3 292 -9,0"^ 2>G I /5^> ^^q, \|^ l!)!") ^ / <> J?S>^ • 7 ?3 t/ftl-G£iry ' /i-l Q ••^ ^ l^ & /v / 3 n, Y ^" X Velocity Head (Ap) inH2O Orifice Pressure Differential (AH) in H20 Desired Actual Stack Temp. (Ts) Nozzle ID: ' Thermc Assumed Bws: • — Filter # Meter Box #: /^ Y: '% Post-Test Leak Rate: ,^00 Post-Test Leak Check: Pitot: Tempeiatura Op Probe Filter Impingar Temp. °F couple #: y ^ ^ AH@: A £^2. cfm @ /^ in. Hg. — Orsat: — Dry Gas Meter Temp. Inlet (Tm in°F) Outlet (Tm out°F) Pump Vacuum (in. Hg) y/////y/////////y/////////////////////////^ \|j_ 9 rf^"ii ^f . 11 , 1 '3 V.o I?O ' 2 ^ rj ^5 t d&~ 9 I . 9 1 / 1 S /' £&> 1 ' d(? I t%k >i *-< t lifP /£•<>' /^?6 /^»"7 /i>~^ /6^ /fj 3 /6 £> l& "? Its / fa C^ / fo 5 "V K&-- tf.L /U.4 - 26- Ps - 2-t Ms-- 3\|, ^c^-- X'ic/r* = <£>O Sj s<£> &# 9 3» -. ------- SAMPLE RECOVERY DATA PLANT DATE SAMPLE LOCATION TRAIN PREPARER sample Box No. Ov> ------- JOI EPA METHOD 4 MOISTURE CALCULATIONS PLANT:__J^2LQ SOURCE/RUN • ^'5-i DATE: 1. Leakage Correction for Volume Metered Vmc = V 0-p - La) x 9 vmc = V 0-p - 0.02) x 0 Vmc=( )-( -0.02)x( ) Vmc= 35-^0 ft3 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) ,'Ptar-M AH /13.6)N = 17.64 m ( 541 dscf 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V ... = 0.04707 x (Wr - W. ) wstd v f i' — SCf "sta 4. Percent Moisture, by Volume V^ Bws= — w m wstd mstd W8 [A ft Ml jJI ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: LA $(2 & Date:_5 Sampling Location: In Clock Time: Barometric Pressure, in.jHg: 99 Moisture, %: Oporatnrs- Static Pressure, in. I-^O: Molecular wt., Drv: — Pilot Tube, Stack Dimension, in. Diameter or Side 1: I5~fl Side 2: Wet Bulb.°F: TravtrM Potat Number V + (0.28 X S)^) Md - (0.44 x ) + (0.32 X ) + (0.26 X ) Md- 1.W % H,0 % HO Mt-Mdxd- i_)-18( —) 100 100 M« - ( )x(1 100 100 13.0 13.8 Vt - 65.49 x Cp x Vi • 85.40 x ( Pax Ma ) x ( )x Qs • v« x A« x 00 a/m xeo adm Pt Ta 100 X 17.047 X- 100- ------- FIELD DA IA SHEET Plant MS Sampling Lbcj Run Number: Pretest Leak R Pretest Leak C Traverse Point Numb Time (mln) /} /o 26. •Tf) i& V;>T itk>n_£ /0-5T- ate: Sample Type: /7'^ Ope XJC/l) #" /O Pbar^f3> — "" Stack Diameter: /C" As: /,Q.3 s^f-t Gas Meter Reading (Vm)«3 9&Q .faQ? 9106, 60 O"?6'$^ Q ^ !>O ol^ 0- i^^)i^ cfm @) £ in. Hg. "- Orsat: Dry Gas Meter Temp. Inlet (Tm in°F) 1 Outlet (Tm out°F) y/////y////////////////////////////////////////////////// l.ftfa h ------- a at METHOD 18 FIELD DATA SHEET • < l ?72- 6S' M<3<> •)1. 1 ^ >,>? «a,«* <\|^,-7'? Date: r-/9-9'P Orificft Tank • ocation: D\}t£A) & /O pump/pntnmRter #: Run- SO~f-3 Pt: Pretftst (r>m WG)' — Stack I.D.: /" Post-Tast (mm Hg); ^— 3bar: 3)30 y/s o.i T/ Mi-( )x(1- 10^-' + 1(" ,00 ' ^y?i — 2. ^ y^T.- ^^ °F- ^3 WF + 'W S P V p"Pb^-( >-^5- P.. 27. /^ In-Hg «P- Ot4& . ^? \l T9<°R) V« - 85.48 X Cp X VAP X ^ P8XM. v.. 3V. 0/ ft/. A.- / 23 «2 Q«- VxA»xCOi/m Q§. x xM Cfc « 'Jfd 1 cfcn p, H,0 QiJJ-OiXl7.e47x x(1 •-) •Id T« 100 ^•W" X17.647X "(^ 1fl0 ' " QNM--/ft40 ------- SAMPLE RECOVERY DATA PLANT DATE Run No. ^\ °l • cl "? Sample Box No. A/-5" Job No. SAMPLE LOCATION -44 10 Ov^\> QvV-«fc Filter No. TRAIN PREPARER " SAMPLE RECOVERY PERSON COMMENTS FRONT HALF Acetone Container No. Filter Container No. Description of Filter Liquid Level Marked _ Sealed Sealed Samples Stored and Locked BACK HALF/MQTSTTIHF Container No. Liquid Level Marked Sealed IMP. NO. 1 2 3 4 5 6 CONTENTS J#X D2 f/,o £~f+r 5;ltu, W TOTAL INITIAL VOL (ml) /av fro 0 26* WEIGHT (grams) INITIAL 5727 54 ¥ Wi 77(f - . •• - '• M • ^' >»• • ~m . . m" FrKAL Sw'.^ s:,:,-? -4^.1 -7-7^3 NET ' ?./ (•£ o 1.1 l.(e JR ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: ZJKCr- Date: $V?t-9'7 Sampling Loc Run#: /ft. ration: fr\)r) i If) Clock Time: /V«V^ >T--3 nnoratnrs: ftftt >te ~~•V r 6 /}- / 9 •3> <5V •9P^, t> a~> ?5t ^ ^5^ ^a^ Q3C o i a 5-?S ^y^ 35* -2, T-XK^ wt Dry • Pilot 1 uoe, up. Q.^. xir.e47x— x<1'-^~~ ------- Plant:. Date: Location: /NJnA METHOD 18 FIELD DATA SHEET Tested Analyte:_ Orifice Tank #:_ Run #: A/Dl - s-\ Stack I.P.: 3i" Pbar: 2.6 35 Pump/Rotometer #: iV)<;r Pt: Pretest (mm Hg): i_ Sample Tube #:. Operators:. Leak Check: Pre:. Post: Post-Test (mm Hg); Tt: Pretest f F): Post-Test Time: Start: ofo* W/B: Total: oo D/B:- O2: 2.1 CO^. o ^32. /AY-15.6 c, /'£> ^> 3o /i^ 50 6* Time IH^^.l 1 H 1 Q.1 y-/3^/ /^/^7. 5 A/ 40 . ' i /-9VZ.C? I^S.^! Travars* Point Number 1 3 z 2- Gauge Vacuum (Hg) 1 » / / / / I v«tocrty H«d In. H2O Flow Setting 3-1 a( £/ z./ TL/ ^/ Z\| Stack T«mp. °F Md - (0.44 x %C02) + (0.32 X StCty + (0.28 X Tt^) -^- Md - (0 44 x ) ••• (0.32 X ) + (0.28 X ) «l V Md- %H,O %H20 -~ll M>.Md;x(i--T^-) + i«(-jSr) M. -, )x(1- -^5-' + '•< 100 ' ^ ^ M" ^ Ts- °F- °R(°F^4flO) p,.Pb«.-i:l-=( ) + — -— ; — 13.8 13-8 JTp. ^? \l Ta(°R) Vt-a5.48xCpx VAP x ^ P8XM, . / Vc «l/« A.- nz Q»-VixAax00a/m Q«« x xOO Qfm «Cfm _ ^ u o Q« ^,-Qax 17.847 X X (1 • ) ^•td u"1'' T- 100 Q,^. X17.M7X X(1'"^T> Q0«M^ cfvopn ------- METHOD 18 FIELD DATA SHEET # Plant: L^Lo Tested Analyte: ^y^^ Date: 5"-M-n Orific« Tank jfc- ~~ Location: wn£> Pump/Rntnmeter #: y^-f -^s Run #: A/Dft - 5- Z Pt: Pretest (mm Hg)- Stack I.D.: P.S* * ?2" Post-Tact (mm Hg): - Pbar: Zf.r Tf Pretest f°FV Sample Tube Operators: 4. #• AX>£-Z-zA NDP>-S-Z& Poet.Test r°F)- S , Time: Start- ifdft Finish:rioft Total: 06 Leak Check: Pre: vX Post: v/ W/B: - D/B: - O^: ^ CO0:_a Gauge Time Vacuum (Hg) nm. M. i /^»V 7, ^5 / /•V5o. iS / IMW.ST ( W5M.1-7 \| ^5T. S3 I I5V ------- APPENDIX A. 1.7 Condition 6 (includes flows, moistures, and Method 18) ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: u&CO Date: --'•-?! Sampling Loc Run #: iv\e ation1 M / 5 (* 1 % • 9: ^?.7% Static Pressure, in. HoO: f ^ Molecular wt,. Drv: ^?.^/ Pitot Tube, Cp: , f f •ion, in. Diameter or Side "73 Drve V.looty in. H2O ,^ ,25" Z-7 ,3d 3o i 3V , 37 . ^1 -V/ ZC , 3tf . 3/ ,32) .3Z /3>2. .3/ .2^ Stack Ttmp. °F ^& $g (0.28x~l$ in. Hg £P- .560. — / Ts^R) Vl - 85.48 X Co X JhP X U p, Ms 1 I 5^^ V if TS" 27 v. . 1^. ^^ n/i A«» /.G~7 n2 Qt • Vi x A» x CO i/m Q»- -if- Of x /.6T xeo Qt • %07v/ adm Pi ^H.0 O.^Q.xi^x — .cd.— > Z.».7« •i-8' (to f t5» f 100 QHtd- ^ S O ctofcn .//I. ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plam: LKco : Location: ^^ e. ^ Site: M,N Operators: Run Date: <•_/?-* -7 Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw (from Table) = Pvw = (Ps - Fvw) x (AT) Pbar= ^-79 Pa = - o z- Ps = 1$. IV Tw= ^3 Td= « in. Ha in. HnO 2 in. Hq °F °F AT= ^ °F PVW= ;'?> in. Hq Vapor Pressure of HjO = Pva = (Pvw) - •2800-(1.3xTw) Pva=( , 2800-(1.3 x 1 Proportion of Water Vapor by Volume = Bws = JPva) (Ps) T«mp. OF 0 10 20 30 40 50 00 70 80 00 100 110 120 130 140 190 160 170 180 190 200 210 220 230 240 0 0.0376 0.0031 0.1029 0.1047 0.2478 0.3020 0.9218 0.7392 1.032 1.422 1.932 2.998 3.446 4.829 5481 7.989 0.882 1220 1929 101 2347 28.78 3940 4241 9OM 1 0.0398 0.0800 0.1080 0.1710 0.2978 0.3784 0.9407 0.7840 1.008 1.407 1.992 2.072 3443 4.647 8.034 7.7S9 9.088 12.40 1943 19.42 2348 2043 3948 43.11 91.78 ( in. Hg ( 1/1« ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0098 0.1127 0.1803 0.2877 0.3908 0.9801 0.7912 1.102 1.913 2.092 2.749 3.842 4.772 0.190 7.992 10.12 12.77 19.98 1944 24.40 2942 3047 4342 52.70 3 0.0441 0.0728 0.1100 0.1870 0.2782 0.4092 0.9802 0.8183 1.130 1.901 2.114 2.829 3.744 4.900 0.390 8.180 10.30 13.07 1044 2O27 2447 3042 3747 44.74 8348 4 3.0403 3.0700 0.1240 o.i ass 3.2891 0.4203 0.0009 0.8402 1.179 1.810 2.178 2.911 3.848 5.031 6.913 0.391 10.81 1347 16.70 20.70 2148 31.13 37.78 4847 9442 5 0.0409 0.0810 0.1302 0.2033 0.3004 0.4359 0.6222 0.8790 1.213 1.000 2243 2.998 3.994 9.189 6.600 8.997 10.80 13.07 17.07 21.14 ?flOQ 31.78 3040 4041 9840 6 0.0517 0.0040 0.1370 0.2118 0.3120 0.4520 0.0442 0.9040 1.293 1.712 2.310 3.001 4.003 5.302 0.090 0.707 11.12 13.90 17.44 2149 2043 3248 3944 4747 9840 7 0.0541 0.0092 0.1429 0.2203 0.3240 0.4000 0.8609 0.9352 1.293 1.769 2.379 3.169 4.174 5.442 7.024 8.981 11.38 . 14.30 17.82 2248 2747 3303 3940 40.14 9741 a 0.0571 0.0932 3.1502 0.2292 0.3364 0.4090 0.0903 0.9000 1.339 1.019 2.449 3.299 4.289 5.989 7.202 9.200 11.89 14.62 1841 2242 2742 3347 40.78 4943 9843 0 0.0998 0.0982 0.1507 02303 0.3493 0.9038 0.7144 0.9980 1.378 1.078 2421 3481 4.400 9.732 7.384 9.424 1142 1440 1841 2240 28.18 3448 4142 4048 8047 ------- Plant:. Date: 5- 23'-«n METHOD 18 FIELD DATASHEET Tested Analyte:_ Orifice Tank #:_ Location: A>.\- Run #: Mfig-//-?. Stack I.P.: n 5 Pbar: 1,1. Pump/Rotometer #:. Pt: Pretest (mm Hg):_ Post-Test (mm Hg): Tt: Pretest f°F): Sample Tube # Operators: r« Post-Test fF):_ Leak Check: Pre: Post- O /o t Time 77^£.L<. JCC. AUty£- -T • i^ V V Tf '// Travarsa Point Numbar Velocity H«ad in. H2O Stack Temp. °F Time: Start:/o39 Finish:/s9 Total: W/B: —D/B: —- O2: ajCO2: Md = (0.44 x %CO2) -t- (0.32 X %O2) -r (0.28 X Kt^) Md = (0.44 x O ) -t- (0.32 x «-/ ) + (0.28 x 7* Md Ms o Md x (1 • • !0( Ms = ( £ft ) xd Ms - Ts - °F = HO % HO -t_; - 18 ( * ' 100 ) -i- 18 ( I 100 100 °R<°F~460) c p Ps-Pb ^Jl-= ( 13.6 13.6 Ps in. Hg Vs. Vs Vs As Qs Qs Qa - 85.49 x Cp x JS^ x "W — - 85.49 X( .W )X( ft/8 ft2 • Vs x As x 60 s/rn • x • acftn Ts(°R) PsxMs ml ' \l x60 P, %H-0 Qs . .= Q8X17.647X x(t • — •W Ts 100 Qs x 17.647 x- dscfm •x(1 ------- a V METHOD 18 FIELD DATA SHEET Plant:. Date: Location: Run #: me.-)/- Stack I.D.:_Z2i£ Sample Tube #: /?-/>• •» . Operators: Leak Check: Pre: Post: Tested Analyte:. Orifice Tank #:_ Pump/Rotometer #:_i Pt: Pretest (mm Hg): Pest-Test (mm Hg):_ Tt: Pretest Post-Test fF): n^ Time: Start:.£LRnish:j»ff£jotal:_££. Time 2325.54 2326. f\ 7-1,26. 01 Gauge Vacuum (Hg) / / / Row Setting ISetc. ]<><.<- tSocc T» ts Md = (0.44 x %C02) - (0.32 X %O2) -r (0.28 X "/oNj) ^~ Md = (0.44x O )+(0.32X1' } * (0.28 x7* Md = Traverse Point Number 1 I 3 if 9 t, 7 r f t i V / V 7 J Velocity Head in. H,O .Z5 36 .3* .3z .35 .^e .vo .^•2. .ZT .36 . 2>l .3-2 .30 ,3/ .32 .^•z f9.^%3 Stack Temp. °F 7? •)1 7? 7f 7f •»f 7f 7* T 7? 7f 7t 7T 7? 7? ?4 7? Ms = Md xl) - MS- Pa - Pb %H O - =— ' 100 - 18( I > , 100 ' 100 100 S.P. 13.6 13.8 Ps= Z-^' J&m 0. Vs » 65.49 x Cp x i Ts(°R) Pax Ms Vs - 85.49 x( • 9f )x( Vs - 3% MX. ft/, A.- 7,6,7 «2 Qs - Vs x As x 60 s/m )x V Z. x60 Qs- acfm Qs . .= Qs x 17.647 x std Ps x (1 100 Q« std" x 17.647 x- dsclin 100 ------- METHOD 18 FIELD DATA SHEET Plant; Date: 2. Location:. Run #: ;; Tested Analyte: 5/y,~e.^ Orifice Tank #: ~ Stack I.P.: n.S" Pbar: zr. 7? Pump/Rotometer #:_ Pt: Pretest (mm Hg)L Sample Tube Operators:. Post-Test (mm Hg); r_ Tt: Pretest fF):_ Post-Test fF)L Leak Check: Pre: Post: Time: Start:fl33 Finish:'7Total: /< W/B: 73 D/B:^ O: -' CO2: & / 7 .V? Time no6.6-7 -71 31, 3S Gauge Vacuum (Hg) / / / Row Setting . ,£< /j#r^ /SO^ • 0 N" O i Md a (0.44 x Md a (0.44 x Md- Ms = ( + (0.32 X %O2) + (0.28 X %Nfe) ) •»• (0.32 X ) + (0.28 X ) % H.O % H.O IX(1 - ) -(- 18 ( 100 100 Travtra* Point Number V.tocrty H»ad In. H^O Stack Tamp. • Ma - Ts- °F- °R (°F 1-460) S P D« _ OK j. ^-r" _ / \ , 13.8 13.6 Ps = In. Hg fir* == . 1 Ta (°R) VB - (J!j.4U x Cp x VU^ x U ps x Ma Va • ft/a A.. »2 Aa • ft Qs • Va x As x 60 s/m Qa - x x 60 Q«- acfm Pa %H2° Qs.. .= Qs x 17.647 x x (1 • =— ) Q^fltd™ dscfm ------- METHOD 18 FIELD DATA SHEET Plant; Date: £_ Location:. Run #:* Stack I.D.; .1.5 Pbar: z?. 7 a Sample Tube Operators: -r Leak Check: Pre:_ Post: TV- >?» Trav«ro» Velocity Point H«ad Number In. I .26, .li 36 3,7 Stack T.mp. 10 9? 81 Tested Analyte:_j3£u Orifice Tank #:__ Pump/Rotometer #:. Pt: Pretest (mm Hg)L Post-Test (mm Hg); n Tt: Pretest fF): r_ Post-Test Time: Start: n 33Rnish:^v 3> Total: W/B:75 Time z^c^, yc 2.30?, JH 13/0. 2? Gauge Vacuum (Hg) / / / Row Setting iso-- '* "' ^o- T~ -77 'IT l^r Md - (0.44x%CX)2) -t- Md = (0.44 x ------- "Pa :—r WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: /^AsC& /^W^ Site: ,A.v, /jr/C^ Operators: Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar + - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H0O at Tw Location: flonVnCC, \|£V -70 Run??: fif-t-i- Date: 5, Pbar = 24. 7B Pq = "~. -a ? -rnr Ps = 2- 7 Tw= ?J Td= $1 AT= /£ (from Table) = Pvw = 0. 8/S3 '//I /i 7 in. Hg in. H.O 2 in. Hg °F °F °F in. Hq Vapor Pressure of H^O = Pva = (Pvw) - Pva= (Ps-Pvw) x (AT) 2800-(1.3xTw) (2B,it -,e/3 )x( /£ ) 2800 -(1.3 x 73 ) in. Hg Proportion of Water Vapor by Volume = Bws - (Pva) (Ps) T«mo. op 0 10 zo 30 40 50 00 70 00 00 100 110 120 130 140 150 180 170 180 100 200 210 220 230 240 0 0.0378 0.0831 0.1029 0.1847 0.2478 0.3828 O.S218 0.7302 1.032 1.422 1.832 2.308 3.446 4.S2S 5481 7.580 9.852 1240 1350 10.01 2147 28.78 3UO 4241 5044 i 0.0308 0.0880 0.1080 0.1718 0.2978 0.3784 0.9407 0.7848 1.088 1.487 1.003 2.872 3.949 4.847 8.034 7.780 0.889 12.48 1843 1042 2348 29.33 3848 43.11 81.78 2.3% ( 24, 7e ) Lfu 7 IS VAPOR PRESSURES OF WATER In Inches of Mercury 2'70$V 2 0.0417 0.0808 0.1127 0.1803 0.2877 0.3808 0.9601 0.7912 1.102 1.513 2.093 2.749 3.643 4.772 6.190 7.993 10.13 12.77 1948 1944 2446 2943 3647 4943 53JO 3 0.0441 0.0728 0.1188 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.581 2.114 2.829 3.744 4.900 0.390 8.180 10.36 13.07 18.34 2047 2447 3042 3747 44.74 5948 4 3.0483 0.0788 0.1248 0.1055 0.2801 0.4203 0.6009 0.8482 1.179 1.610 2.178 2411 3446 5.031 0.913 0491 1041 1347 16.70 20.70 2546 31.13 37.78 4847 5443 5 0.0480 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8790 1.213 1.660 2443 2.995 3.954 5.169 6.660 8.987 10.66 13.67 17.07 21.14 2640 31.78 3840 4641 5840 0 0.0517 0.0840 0.1370 0.2118 0.3120 0.4520 0.8442 0.9046 1.253 1.712 2410 3.061 4.069 5.302 6.850 8.767 11.12 1348 17.44 2149 2649 3348 3944 4747 5640 7 0.0541 0.0802 0.1420 0.2203 0.3240 0.4888 0.8889 0.9392 1.293 1.789 2479 3.189 4.174 5.442 7.024 8.981 11.36 14.30 1742 2348 2747 3342 3949 48.14 5741 a 0.0371 0.0032 3.1502 0.2292 0.3384 0.4858 0.6903 0.0668 1.339 1.819 2.449 3.299 4.289 5.585 7.202 0400 11.69 14.82 1841 2242 2743 3347 40.78 4943 9849 0 0.0508 0.0082 0.1987 0.2363 0.3493 0.9038 0.7144 0.9969 1.378 1.678 2431 3481 4408 5.733 7.384 0434 1143 1446 1641 2349 28.18 3448 4143 4948 8047 ------- jag cia GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: / f&CO Date: jr-/-? Sampling Loc Run #: (v\&- ation: ^-^ f^. ^ Clock Time: /f^o '• -"> Ooentors! ^/r/ Barometric Pressure, in. H Moisture, %: / 9 ? Stack Dimens Wet Bulb, °F- Traverse Point Number 1 7 ••> f 5* 6 7 7 i i 5 T* y <* 1 y • 9: z?,^ Static Pressure, in. H«O: c>^ Molecular wt Drv Zs-Sl PitOt Tube, Cp: (ff iion, in. Diameter or Side 6^ DrvE Velocity in. H20 ,21 2-1- • 2? ,29 33 •15 • >~~) • 3> ?&. yc> fll CO O- / {/ L_^ CJ ttf «-& ^6 95 ?^> ^•6» #6 76 ^6. ^G »^ • ft- ^ 1- ^7 , J Side 2: — ulh^F- ff(^ Md - (0.44 x %C02) f (0.32 X %O2> * (0.28 X KNj) Md - (0.44 x O ) ••• (0.32 X 2. / ) * (0.2B X ~* ** ) Md- Z-3--17 % H20 % H2O 100 100 " 100 100 M«- 2-6.C?3 Pn - Pb + ™P' - ( ?$• vy ) • — O.O^> 13.B ' 13.B P, . 2^ f, g / In. Hg fif - 0 5£}2~- / Ts (^R) u i S X MS v.- 3^ ^73 «/• •• /.^ n2 Q — V« x A» x CO a/m Qc« x xeo 0»- T.g/5" tdm ji/i j Pt ""2° ^ttd" * X ' 7 ------- Plant: Site: WET-BULB/DRY-BULB MOISTURE CALCULATION Location: ~,r Operators: Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of StacK = Pbar + 1 J.D Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Run if: /^f£~- 6>- 2 Pbar = pg = _: . Ps = Tw = Td = Date: . 0 3 17 Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw (from Table) = Pvw = —^ 7/yy (Ps- Fvw) x (AT) Vapor Pressure of H2O = Pva = (Pvw) Pva=( o.l (^ )-- 2800-(1.3xTw) )x( 17 ) /. 2800 - (1.3x Proportion of Water Vapor by Volume = Bws ( 0.&SO ) ) (Ps) Tamp. OF 0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 0 0.0376 0.0831 0.1025 0.1847 0.2478 0.3826 0.5218 0.7392 1.032 1.422 1.932 2.598 3.446 4.525 5.881 7.569 9.652 1220 1529 19.01 23.47 28.75 3540 4241 5044- 1 0.0398 0.0680 0.1080 0.1718 0.2578 0.3764 0.5407 0.7648 1.066 1.467 1.992 2.672 3.543 4.647 6.034 7.739 9.883 12.48 16.83 19.42 2348 2943 33.88 43.11 51.76 O. /? '• in. Hg in. 1^0 in. Hg °F in. Hg in. Hg ( ZMf ) VAPOR PRESSURES OF WATER -^TT -; o. (7W In Inches of Mercury T,?!0- 2 0.0417 0.0896 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.842 4.772 6.190 7.052 10.12 12.77 15.98 1944 24.46 2942 3847 4348 52.70 3 0.0441 0.0728 0.1188 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.629 3.744 4.900 6.330 8.150 10.38 13.07 16.34 2027 24.97 30.32 37.07 44.74 53.63 4 0.0463 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8482 1.175 1.610 2.178 2.911 3.848 5.031 6.513 8.331 10.61 13.37 16.70 20.70 25.48 31.13 37.78 4547 54.62 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.680 8.537 10.66 13.87 17.07 21.14 26.00 31.75 3840 46.41 5340 a 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.850 8.767 11.12 13.98 17.44 2149 2643 3248 3924 4727 5640 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4688 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.981 11.38 14.30 17.82 2243 27.07 3342 3949 48.14 3741 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9668 1.335 1.819 2.449 3.259 4.289 5.583 7.202 9200 11.63 14.62 1821 2242 2742 3347 40.75 4943 3843 9 0.0598 0.0962 0.1567 0.2383 0.3493 0.5035 0.7144 0.9989 1.378 1.873 2.321 3.331 4.406 5.732 7.384 9.424 11.92 1448 1841 2249 28.18 3443 4142 4943 8047 ------- a a Date: 5- Location Run#: METHOD 18 FIELD DATASHEET Tested Analyte:_ Orifice Tank #:. iY\ c.-.»•>,• ..i-.-f- Stack I.D.: Pbar: Sample Tube #; Operators: Leak Check: Pre: Post: S^t/c^- -. Trovtrea Point Number Velocity H««d .05" ,O(a OS .OS LJ L, Stack T«mp. °F 5-2. ZL # I. 3$ Pump/Rotometer #:_L Pt: Pretest (mm Hg) i Post-Test (mm Hg):_ Tt: Pretest Time -1-729.^^ 71-Vi.TL "T7 > 9^ -?-? T,3, ^7 -11 3^.03 77^5, 75 Gauge Vacuum (Hg) ^ i t , 1 Row Setting /<0^ /£(j (£, /$(><•£. ,j$f <:<- /4& r<- ,40" 37 Post-Test fF): Time: Start: /&, Hnish:'^ Total: 4-T W/B:"1/ D/B:03 O^: ^/ CQ~: & & ^^~^ <: Md-(0.44x%C02) + Md - (0.44 x O ) + (0.32 X 2./ ) + (0.28 X Md- % HO % HO Ms = Mdx(1 - £_) + 18 ( =— ) 100 100 Ma-( ^ Ms- - 100 100 13.0 13.8 \|n.Hg Vs - 85.49 x Cp x Vs-85.49x( -^ » ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: Li^LO Site: Kbav &t)(\Qut ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: Lfeoo fL^L^ Site: ^,,>«, £><•£—<./' Operators: Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Pbar ± - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw Vapor Pressure of HpO - Pva - (Pvw) • Pva=(/07/$V0 )-( ^'73 ''7** Location: rkr^Wf( £V ~7& Run #: fa- 6- 2- Date: * Pbar = 2^5. 7$ Pq = -; £ -2— -3L- PS= 27.3 Tw = 7/ Td= B3 AT= /2- (from Table) = Pvw = 0, 7b /£ (Ps - Fvw) X (AT) 2800-(1.3xTw) # )x( /Z- ) AW/1/ X/1/7 in. Hg in. HP 2 in. Hg °F °F °F in. Hg in. Hg 2800 - (1.3 x Proportion of Water Vapor by Volume = Bws (Ps) Tamp. OF 0 10 20 30 40 SO 60 70 60 90 100 110 120 130 140 ISO 160 170 160 100 200 210 220 230 240 0 0.0376 0.0631 0.1025 0.1847 0.2478 0.3626 0.5216 0.7392 1.032 1.422 1.932 2.596 3.446 4.52S 5.681 7.569 9.652 1220 1520 19.01 247 28.75 3540 42.31 50.84- 1 0.0398 0.0660 0.1060 0.1718 0.2576 0.3764 3.5407 0.7848 1.068 1.487 1.003 2.872 3.543 4.847 6.034 7.758 9.88S 12.48 15.63 19.42 2346 20.33 3548 43.11 51.78 2, ( 2-9.73 ) VAPOR PRESSURES OF WATER ^f_ „ 0 / In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.740 3.842 4.772 6.100 7.052 10.12 12.77 15.08 1044 24.46 2842 3647 4343 52.70 3 0.0441 0.0726 0.1166 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.629 3.744 4.900 6.350 6.180 10.36 13.07 16.34 2027 2447 3042 3747 44.74 5345 4 0.0463 0.0766 0.1248 3.1955 0.2691 0.4203 0.6009 0.6462 1.175 1.610 2.178 2.911 3.848 5.031 6.513 6.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 4847 54.63 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.860 2243 2.995 3.954 5.165 6.680 6.557 10.86 1347 17.07 21.14 26.00 31.78 3840 4641 5540 6 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.8442 0.0046 1.253 1.712 2.310 3,081 063 5.302 6.650 8.767 11.12 13.08 17.44 2140 2643 3248 3024 4727 5640 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4666 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 6.081 11.38 1440 17.82 2345 27.07 3342 3040 48.14 5741 1 70 7. 7 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.619 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1821 fja 27.62 3347 40.73 4043 5843 — "t < 9 0.0508 0.0082 0.1567 0.2383 0.3403 0.5035 0.7144 0.0080 1.378 1.875 2421 3.351 4.408 5.732 7.384 9.424 1143 1446 1841 2349 28.18 3443 4143 4943 5947 ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: i-$&£> Hate: J-^-fl : Sampling Loc Run#: Rg- ation: £,^ £V/v,,^f Clock Time: I7sf /--I, nporptnrs- T#/55 Barometric Pressure, in. H Moisture, %: "2- 2- Stack Dimens Wet Bulb, °F TrcvarM Point Number / -> c "> V 5 C / 1 "> ^ 5 t, i T. 5 / 5* C i 7. 3 4 5" L q: 28. 7^ Static Pressure, in. hUO: — ,CZ Molecular wt.. Drv: .^f- ^V Pitot Tube, Cp: . ion, in. Diameter or Side I/ DrvE Vvleeity H««d in. H2O lOG? .^7 ,^c^ ^>"7 ,^7 .oy .0^ .<& ol ,ou> ,oa? >>0 ,lb . ^ •y^ ^P-ft2-773 Stack T«mp. °F ^3 1 Sy3 5^> 43 f (0.28 x %^42) Md - (0.44 x ) * (0.32 X ) f (0.28 X ) Md - 2^7. o % HO % H20 Mi-Mdx(1 ioQ '°l 10Q M..( )x(,.___) + ia(-^5-) M«- ^.7^ ?;. g> °F- c5YJ °R(°F460) P» - Pb » S'P' = ( ) +• —— 13.B 13.8 Pi - 2^. 7 3 in. Hg £?- ^7^773 — J Ts (^R) V«-«b.48xU>x VA^ x )\| ~p9x"M8" v» - /f, o 3 ft/i A..- ^6-7 «2 Qt • Vi x A« x 00 i/m Qs • x XOO Q,- <3S/ «<" Pt H2° 0.-td=O.K17.B47x-?-x(1.-jS-) Qt^- X17.647X "C(1'"^T> ywto ------- jag c^a GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant:. Sampling Location: Run#: Rt-(,'^ Date: <-/t-^ Clock Time: /9so Barometric Pressure, in. Hq: ?j£, Moisture, %: X? Molecular wt., Dry:. Stack Dimension, in. Diameter or Side 1: Wet Bulb.°F: Ct Dry Bulb,°F: Static Pressure, in. HoO: -« 6V i.ti Pilot Tube, Cp: .99 Side2:_ Trover** • Point Number 1 ' V- z ^ V 5 C i 1 ^ 1 5 (j i L ^ H 5 u / 2 •} V 5" d/ Velocity H««d in. H20 .OG, ^••.^7 .0? .0? .0? .09 .a? ,/0 .0? .01- ,o« ,yo >// ./o ,c£ ,0^ -OG JO ,o-> .0 .05 .05 .0(s ,to Stack T«mp. °P £'' £> ?/ 11 l 91 VI V/ 8' / W 9/ ?/ 8/ t' y 71 VI l $/ 11 tl -si W T5-9/ Md - <0.44 x KCOg) + (0.32 X %O2) (0.28 X %l^) Md - (0.44 * ) + (0.32 X ) > (0.28 X % HO % HO M« - Mdx(1 - _) * 18 ( 1- ) 100 100 100 100 i-Pb+-i^-=( )* 13.8 13.6 P«- 2-Q. ~7f In. Hg V» • 65.40 x Cp ] V» - 85.40 x ( Vl» A«- ^\|<6T 1 Q>« V«xAax80i/m Os- x Q«. ^ xOO - Qi x 1 7.847 x— — x(1 T« 100 rtd- QNtd- X 17.847 X- •x(1 100 ------- •^a a.- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: ^feco ?„£ Z.o. Site'- Jtoov /^T'/^r^ Ooerators: Barometric Pressure, in. Hg = Static Pressure, in. HpO = Absolute Pressure of Stack = Pbar -- - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H^O at Tw Vapor Pressure of H~O = Pva = (Pvw> - >cfo Location: /% Date: ^ Pbar= 2-£0y Pa= -./ -$-- Ps= -£& 79 TW= (e Td = VI AT= /3 (from Tabled = Pvw = #, & ?<>2> (Ps - Pvw) x (&T) : /ti/r? , in. Hg in. HLO 2 in. Hq °F °F °F in. Hg 2800-(1.3xTw) Pva = 2800 -(1.3 x Proportion of Water Vapor by Volume = Bws Bws= (Pva> (Ps) Tamp. °F 0 to 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 160 190 200 210 220 230 240 0 0.0376 0.0631 0.1025 0.1047 0.2478 0.3626 0.5218 0.7392 1.032 1.422 1.932 2.596 3.446 4.525 5.681 7.568 9.652 12.20 15.29 19.01 23.47 28.75 35.00 42.31 50.84- 1 0.0398 0.0660 0.1080 0.1716 0.2576 0.3764 0.5407 0.7648 1.066 1.467 1.902 2.672 3.543 4.647 6.034 7.759 9.885 12.48 15.83 19.42 2348 2943 39.88 43.11 31.76 in. Hg ( ^W0\| ) VAPOR PRESSURES OF WATER ^^ * In Inches of Mercury 2- 7 < 1— 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.842 4.772 6.190 7.952 10.12 12.77 15.98 1944 24.48 2942 3847 4942 52.70 3 0.0441 0.0728 0.1186 0.1678 0.2782 0.4052 0.5802 0.8163 1.138 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.38 13.07 18.34 2047 24.97 30.52 3747 44.74 5345 4 0.0463 0.0768 . 0.1248 0.1955 0.2891 0.4203 0.6009 0.6462 1.175 1.610 2.178 2.911 3.848 5.031 6.513 8.351 10.61 13.37 16.70 20.70 2548 31.13 37.78 4647 5442 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.860 8.557 10.86 13.67 17.07 21.14 28.00 31.75 3840 4841 5540 6 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.083 5.302 6.650 6.787 11.12 13.98 17.44 2149 2843 3248 3944 4747 5840 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 6.981 11.38 14.30 17.82 2245 27.07 3342 3940 48.14 5741 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.619 2.440 3.259 4.289 5.555 7402 9400 11.65 14.62 1841 n «g 27.62 3347 40.75 4943 5543 9 0.0598 ' 0.0982 0.1567 0.2363 0.3493 0.5035 0.7144 0.9989 1.378 1.675 2.521 3.351 4.408 5.732 7.384 9.424 11.02 14.98 1841 2249 28.18 3443 4142 4041 9047 41 ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: / /} ^ C Date: 5 -//f f i -» / nneratnrs! ^JA /G ^ Barometric Pressure, in. H Moisture, %: 2. 2- Stack Dimenj Wet Bulb, °F Travsrsa Numbsr A- f Q 3 9 ^ £ & - / <£ 3 ^ ^~ & • ;ion, in. Dian q: i) ?.s2£"S ,3\ Stack T«mo. °F /<"/ 1 tol fJ- /4>^ 1: /«T Side 2: it. fl r~ ~~ ulb.uF: Md - (0.44 x %CO2> + (0.32 X -fcO^ + (0.28 X %l^) Md - (0.44 x ) + (0.32 X ) 1- (0.28 X ) ;jMd- HO % H20 % H2O MS- 2.8.7k P, Pb ^ S'P- M ) - 13.0 13.8 P.. Z7, 2O in. Hg ^f / ^f ' ^s / Ts(^R) Vs-«b.4Uxu»xVSP x \l P9J(MS i V«- 32, 6^> ft/8 As- /, Z3, ft2 Qs - V* x Aa x 60 s/m Qs- x x« 0.. Ol/(2^ «n Ps ^0 Qs ..-Qs XI 7.847 x x(1 -) std TS 100 •to iw All ------- METHOD 18 FIELD DATASHEET Date: <- fa . 9 7 Orific« T^ ' L F c F £ C L f,% I,? I0t>b,&> \o<& tell ^ \,& ocation: Tt: Pretest (°R; — lample Tube )perators: /I #•9/^-3/9 «to-J>A Post-Test f'R ; -^ fU .eak Check: Pre: ,oco Post: X ~) /6K /^f- >^ ^ /^£) IW Am — ' C Time: StartuZ23Finish:_L£22Totai:jc£zC_ W/B:* — D/B: — CL: ^ CO^: — Md - (0.44x%CX32) -t- (0.32 x%02) + (0.28 x!^) Md - (0.44 x ) + (0.32 X ) + (0.28 X ) ^ ™/W %H20 %H20 ^M.-Mdx(1--^-).e(_;— ) l.Zt ^V^Me-( )x(1- ) + l8( -) ------- Plant FIELD DA IA SHEET Sample Type: M' ^ Operator: Nozzle ID: Thermocouple Sampling Loci Run Number: Pretest Leak R Pretest Leak C Print Number i Sampling Time ^> to Qn 1t> H& ition &j£/l) & i Pbaro'S,'!?^) Ps: -0-Gl« 9 -£O Date: 5'/$-9'? CO2: O2: - ate: t &M> cfm @ /O in heck: Phot: Orsat: ' dock Time (244iour dock) m //£> . #£& / fr JO \| 83O . Hg. Probe Length/Type •~~ Slack Diameter: 5: / ' SS Pilol#: SF3 / 3^3 ijO t^j^.'«9^>l Velocity Head (Ap) inH2O Oriice Pressure Differential (AH) in H2O Desired Actual Stack Temp. fTs) Assumed Bws: -~ Filler # Meier Box #: /^ Y:..ty6 Posl-Tesl Leak Rate: it)O Post-Test Leak Check: Pilot: Tempeiature °F Probe Filter Impinger Temp. °F : • — L AH@: / fi1'^ cfm @^2-in. Hg. Orsal: — -^ Dry Gas Meter Temp. Inlet (Tm in°F) Outlet (Tm oul°F) Pump Vacuum (in. Hg) y///////////////////////////////////////////^^ /' S6> /, $b l( ^ / tS'Cf I1 i^yyte?/'?-xi /QM /n jnl 'lit Ilir >w /3-u /wf ill IV •Jr * 9^ /<5b •• ^S y& ^s^ /£> ------- SAMPLE RECOVERY DATA PLANT Run No. DATE £- / I- 9 9 Sample Box No. A'-fc Job No. -SV'l. SAMPLE LOCATION TRAIN PREPARER Qu7<-« Filter No. SAMPLE RECOVERY PERSON COMMENTS FRONT HALF Acetone Container No. Filter Container No. Description of Filter Liquid Level Marked Sealed Sealed Samples Stored and Locked RACK HALF/MQISTTJRK Container No. Liquid Level Marked Sealed IMP. NO. CONTENTS TOTAL INITIAL VOL (ml) -7 WEIGHT (grams > INITIAL FINAL NET a. 6 ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Sampling Location: QIJ& A' ^- S Clock Time: £ti&®9cc £ - ^> Ooerators: QI&Jd(\ Barometric Pressure, in. Ha: 3 ^ ^O Static Pressure, in. HoO: -,&& Moisture. %: — Molecular wt.. Drv: -T^ Pitot Tube. CD: •• .9^ Stack Dimension, in. Diameter or Sid Wet Bulb. °F: Drv Trov«rM ^ ^.i ^ rotnt Number fl-\ 9 3 V f , 3^ e Q^ , ^ ; JSP - ,^a Stock T«mp. °F tSX l<4 110 / 1»-'?? /6( /V^ /<^^ !<<< lte£> 1 (£. J^ 16V TS./#L nv / + (0.32 X %O2> «• (0.28 x %N2> Md-(0.44x J-M0.32X )+ (0.28.x ) Md- 1?l;0 AWSA^2 %H2°, ...%H2°, ? -L'/, M..Mdx(1--^5-)^8( 10Q » 4. 'i Ms-< )x(1 )-H8( ) Mt- 2.^7^ T« - /£ £- °P •' ^ £2^ °R (°F * «o) ^•^13.0 * ' 13.8 P,. 2?.(5' ln-H8 ^>^-7^ Ts (°R) /I- 1 V» « 85.48 x Cp X W X W p, „ M, V» - 65.49 x ( ) x ( ) * V 1 v«- 32,22- ft* A- /^ ft2 Q» - V« x A» x «0 «/m Qt. X X00 Q.. ^37^ adm Pt %H2° Qi^-Oi.!^.— «0--— ) Qi^- X17.047X •(!• 10Q ) 11 13 d«n .///ff ------- 30 £ METHOD 18 FIELD DATA SHEET d \<.* Plant: Lfttf.O TesteH Anaiyte- Slrtf^z Date: S't1'<47 Orific« Tanic • • _ocation- f9.;tv /O Pump/Potnmeter #: Run #: //O- ^ - / Pt: Pret««r* (mm Hg)- Stack I.D.: /< Post-Test fmm Hg): Pbar: 3?,20 Tf- Prfrtflst l°R: — Sample Tube Operators: 0^ #• /n<6-M J - l£ Poct-Tnet fF)' W^oc.i/n \ / ^^ WT/C1-VK2 CJ' , Trav«re« Point Number /-I -7 i "•5 ^ ^ 6 n- / a .3 Y * 6) Velocity Head In. HjO , ^ • < '//> . .Q/5 o^; .p-7 'IS ro/ .^ -tc ,5-s rP? /ao - vr?* Stack Temp. °F <3D^ r^QI <93^ ci?5/fv 55^ ^J2^ 3-3Z* 13 S> St&S 3Q 1 ,42 4 92 > • 93 7^ /^^ ,7^ %HO %HO . ^M..Mdx(1--^.) + l8(-^r) 2.,i I Me-( )x(1- )-t-18( ) 3^- ^ aj T.- 2.2-5 Ofr- L& 0R(°P-«JO) p"rbT5F ( ' i3.e p.- 27,/Y m. HO ^" ft^J^ ;== , I Ts <^R) V« « 03.48 X ^p X ------- FIELD DA I A SHEET Plant Sampling Location CA£A/ 1O Run Number: /Q»-6 / Date: 5T- cfm Sample Type: Pbar £3.90 CO2: __ Pretest Leak Rate: tCCt\ Pretest Leak Check: Prtot: // in. Hg. Orsat: Ps: 02:. Probe Length/Type: / Stack Diameter: )S Operator: -Q.B2. Nozzle ID: Assumed Bws: — Thermocouple #: Filter: — Pilot #: 5T3 As: Meter Box #: /^ Y: / Post-Test Leak Rate: ,OCO cfm @ /pin. Hg. Post-Test Leak Check: Phot: Orsat: TravwM Point NuniDfc . Sampling Tin (min) 0 /o 90 3n "Vo OoCfcrtOM (24-hour dodc) fe&o ILI& lt»£k Halt* \U> ^L Gas Meter Reading (Vm)ft3 O5<,-2>d3 333,36 SHJ .^o •^H^/^O 35-7 tl< •• »/ ^O ^ (5 ^- c:^ / JK- - Valocity Head (Ap) lnH2O Oriica Pressure Ditterential (AH) in H20 Desired \| Actual Stack Temp. (Ts) Temperature /•':"°F Probe Filter Impinger Temp. °F Dry Gas Meter Temp Inlet (Tm in°F) Outlet (Tm out°F) Y////////////////////^^^ \J&£tt£ — • i i j$b t>f$ t, & / , .%> ^ ^ <» • •- >' •. ^) ^ ^f ^0 i <•• „. /on 97 t^ ?r . /Cd> ^7 ?•-? 9^ Pump Vacuum (in. Hg) 7/7, "3 •^ '^ 3 AH= / - ------- Ir-1 SAMPLE RECOVERY DATA PLANT Run No. 10 - DATE 5~- Sample Box No. SAMPLE LOCATION TRAIN PREPARER SAMPLE RECOVERY PERSON COMMENTS FRONT HALF Acetone Container No. Filter Container No. Description of Filter Samples Stored and Locked RACK HALF/MOTSTTTRE Container No. Liquid Level Marked Liquid Level Marked ;0b No. ^ 4- Filter No. Sealed Sealed Sealed IMP. NO. CONTENTS INFTIAL VOL (ml) WEIGHT fgramsi INmAL FINAL NET Hio (o 1 0 o 0 . 3 0.3 TOTAL ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: LASCG Date: g-tf ?. o Pitot Tube, Cp:_^ Stack Dimension, in. Diameter or Side 1: I'S Side 2: Wet Bulb, °R. Tr«v«rM Point Number /; 6 A- / JT Velocity H««J in. H2O 1 / (0 Q 1 Dry Bulb, °F:. Stack T«mp. On 2-31-7 Md - (0.44 x %CO2) + (0.32 X KO?) + (0.28 x %r4j) Md - (0.44 x ) + (0.32 X ) + (0.28 X ) Md - % HO % HO /f— M«- Mdx(1 - —) -t- 18 ( — ) 100 100 P«-Pb 13.0 13.0 = .1 TS(°R) Vi • 05.4B x Co X V« • 65.40 x ( Pax Ma ) x ( xM Qs ^=0t x 17.647 x—— x(1 _) • ?• 100 X 17.047 X- 100 ------- Plant- "ty^ S^-O Sample Type: /V'9 Operator: fifK/tf/'-, Sampling Loci Run Number. itk>n diljM/ •" /O Pbar ^5?x?O Ps: "" ^ ^ 1 f0-£ 3 Date: ^ / in. Hg. Probe Length/Typi Pretest Leak Check: Pitot: • — Orsat: Stack Diameter: Point Numb* <. Sampling ThTM (mln) O 16 So •30 s^5 dock Time (24-hour dock) itf'f'3'7 \|6)X7 1^1 Od>;7 •an 32$' «=?a'9 f^^1 y && t ^9!T Stack Temp. (Ts) Nozzle ID: Thermocouple #: U "^ Assumeo Meter Bo Post-Tes PostTest Temperature °F Probe Filter Bws: niter x: /^ tUakRa LeakCh Impinger Temp. °F /////////////////////// C>t"7- • — . , Q :^HI^B^B^_^B«* M4 - Ms - p5 - i/s = H &.& j'/sy /4i? ^?^) ^~" O^ -^5 4T^ : , Y— $^fc AH@ /^AO te: 0>>0 eck: Pitot: cfm @ ID in. Hg. ££L Orsat: -^-2- Dry Gas Meter Temp. Inlet (Tm in°F) OuHet (Tm out°F) s//////////// ?Y O ^ ^ 3k ^i5 Atf_ ^ / ^ 1 ^ .A"Z ^IjCt \ TT7 / CV« y ^'Vi- /— 9 O £ flvrn™ j I ' v I j VAp= ' ~ j \| AH= 1 { OU !•= oy^~ • ^ Tm= ^ -^ ^V ?3> ^s 9S' 'r^JA Pump Vacuum (in. Hg) 9 7 ^ ------- SAMPLE RECOVERY DATA °<-V\ PLANT _ DATE SAMPLE LOCATION TRAIN PREPARER PAUL Run No. 1 Q ~ (a - Sample Box No. M~7 Job No. . oo3> QvTvlaA Filter No. NJ SAMPLE RECOVERY PERSON COMMENTS FRONT HALF Acetone Container No. Filter Container No. Description of Filter Liquid Level Marked Sealed Sealed Samples Stored and Locked BACK HALF/MOISTURE Container No. Sealed IMP. NO. I 2 3 4 5 6 CONTENTS fcT HxO T^X V^O Ewc«V«-j SIUICA. <^£l— TOTAL INITIAL VOL (ml) /to /eo — 2SD WEIGHT (grams) INITIAL »4 t,tsn sn.. ------- EPA METHOD 4 MOISTURE CALCULATIONS PUNT: !=££^0 SOURCE/RUN #: lf>U-?» DATE: 1. Leakage Correction for Volume Metered vmc=vm-(Lp-La)x6 vmc=vm-(Lp-0.02)xe Vmc = ( ) - ( - 0.02) x ( ) Vmc= 31.7.15 .ft-a 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) Phar-MAH/13.6)N oar* •' lsw- ".D«XVmcXYX V /13.6) ( 553 ) 3. Volume .Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V ^ = 0.04707 x (W - W } wstd v f i7 s scf 4. Percent Moisture, by Volume B - " Vw + Vm wstd mstd / (0.54^ ftr.- I fl ------- METHOD 18 FIELD DATASHEET Plant: U5£Q Date:_^ii±£ Location:. Run #; Noft^-\ Stack I.D.: .sr* Pbar: Zfe.ftM \ve Sample Tube #:. Operators: ss - t.-itv Leak Check: Pre: Post: V- IT- TravcrM B^la»* Kotnt Numbor Velocity H In. Stack T«mp. °F Tested Analyte: S-ki.^ Orifice Tank #'• — Pump/Rotometer #: .PJ Pt: Pretest (mm Hg)' Post-Test (mm Hg):_ Tt: Pretest fF): Post-Test f F); : Time: Start:IhftS W/B:_Z_D/B:_n Time 1 110.01 IHloZ> V<.&, ou i U / "1 / L/ ~ • T v * LA i ^10 .Z^ y ^7^,7-^ 11/15,^ Gauge Vacuum (Hg) / I / -••• • i / / i Row Setting Zj ~L\ l\ 7.1 :: Z( ^1 2.( K /(X) >2ULL_C02:>< Md • (0.44 x %CO2) + (0.32 X %O2) + (0.28 x %l^) Md » (0.44 X ) + (0.32 X ) + (0.28 X : LO %HO % 100 100 C D ' Ps- &- Vs - 65.40 X Cp X Vs » 65.40 X ( Vs- A- In. Hg Y-? Pa x Ms )x( ft/8 2 Qs - Vs x As x 60 s/m Qs - Qs - acfm Pa x 60 %H,0 - — 100 Qs X 17.847 x- dscfm •x(1 ) 100 ------- METHOD 18 FIELD DATA SHEET /•W Plant: LMtD Date: T-/-^ Location: A^DA Run#: AJDA-k-^ Stack ID.: V-H - M>* Pbar: z-s-.y-y Sample Tuba #• AJOA - inn ""• is • uu aid 100 Qsjtd™ dscfm ------- APPENDIX A. 1.8 Condition 7 (includes flows, moistures, and Method 18) ------- METHOD 18 FIELD DATA SHEET - Plant: Li&LD Date:. Location: Run #: Stack I.D.: Pbar:_ Sample Tube Operators:. Leak Check: Pre: Post: Time iiA). 5V :s//. oo 2V 1.1 1 Z3/2- 60 .= ^..32- Gauge Vacuum (Hg) / / / t Flow Setting L^Ot.c. /.-t. i£6{.(L )•/ Total: W/B: <^8 D/B: ?V O2: z./ CO2: Md - (0.44 x %CO2> -i- (0.32 x ^.O^ + (0.28 x %r^) Md - (0.44 x & ) Md- %H2°, Traversa Point Number t i 3 2. .±1 .30 •V3 .51 .2>t Stack Temp. W W 7-V ?V T^V ^•^/ ?«v 71 7H 25 ^< 5r_T >^ W ?V ?'/ Ts- Ps - 13.8 ", 92. In. Hg 13.8 Vs - 65.49 x Co x Vs - 85.40 x ( ,' V.. 3^T 10.0 Aa- ''6~7 ft Qs« VsxAsxOOa/m Q« Qa« Pax Ms )x xeo acfm p. Q« XI 7.847 X - x(1 Ti 100 X17.B47X- 100 Q«atd- ------- Plant: Site: WET-BULB/DRY-BULB MOISTURE CALCULATION Location: /^.^ £>k-. ^5^ Operators: .T/-f Run #\ Date: ~ 13.6 Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2Q at Tw (from Table) = Pvw = (Ps - Pvw) x (AT) Vapor Pressure of H2O = Pva = (Pvw) -'•- 2800 -(1.3xTw) 2800 -(1. 3 x Proportion of Water Vapor by Volume = Bws l.g (Ps) Tamp. OF 0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 0 0.0376 0.0631 0.1025 0.1847 0.2478 0.3826 0.5218 0.7392 1.032 1.422 1.932 2.598 3.448 4.525 5.881 7.589 9.652 1240 1549 1941 2347 28.75 3940 4241 5044- 1 3.0398 0.0660 0.1080 0.1718 0.2576 0.3764 0.5407 0.7648 1.068 1.467 1.992 2.672 3.943 4.647 6.034 7.799 9.885 12.48 19.63 19.42 2346 2943 3948 43.11 91.76 Pbar = Pg = Ps = Tw = Td = AT = Pvw = 2 ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Ln^LO Date: 6-zo—n Sampling LOG Run #: /A £ - atinn- ^v, .r £vU,L.t-f- • Clock Time: /7?j ~7 ^ft - "2- Onflraror?' -^/5-s Barometric Pressure, in. H Moisture, %: /. 5 Stack Dimens Wet Bulb, °F TrovarM Point Number 1 7 3 4 5 L> . 1 _ 3 /\| 3 o 7 % q: ~>%.0\~> Static Pressure, in. HUO: .02- Molprularwt. Drv: ^.<4 Pitot Tube, Cp: ., zJ t^fj ?5 5~?3 93 £2> 8"^ g-3 ?^ S7^ 3 .> ^3 ^^ ^ lb 7i fii- ?3 1: !"7 5 Side 2: - nlh,0p 9-5 Md - (0.44 x %CO2> (0.32 X %O2> f (0.28 X %N2> Md - (0.44 x G ) -f (0.32 x :v ) •(• (0.28 X 7V ) Md •• "2.^ CV % H.O % HO wa-Mdxd 100 ' '1Dl ,00 ' M.-,o.v.W )X(1- -Lu\|L_> + 18<-^S-> T;. ^0, 0F. ^^> °R(°F.460) 13.8 '3.8 Pt. 15.^);. In. Hg ^SF =• , 5C 5G — / Ts (^R) Va-«5.4gxU>x JS? x ^ p,xM8 Va • 3»-"'/ ft/a Aa«).C/l ft2 Qa • Va x Aa x 60 a/m ••tf TA / / ^ — Qt • J8,fJ x /. l> / xOO Qa • Z?0 0 \ adm i p, HH20 atd° ' T, 100 -28 fZ /.-6 aid i ' 5-f ^ 100 OHM- ------- ?lant: Site: WET-5ULE/DRY-5ULH MOISTURE CALCULATION -ccaticr.: /VV.A £h«»sS- cerators: Gate: 5- Barometric Pressure, in. rtg = Static Pressure, in. H2O = Absolute Pressure ot Stacx = =bar Wet-Bulb Tamoerature. °F = Ory-Bulb Temoerature. °r = Temoerature Difference. Td - Tw = Saturation Vaoor Pressure ot HTG at fw (from fabie» = ?bar = _Z Pg = Ps = Tw = Td = ..?.?£ ,n.Hfl ^T (j ------- METHOD 18 FIELD DATA SHEET Plant: I ocatiorv /Vw.A E, Run : ME-7-3 Stackl.D.:_ Pbar: 2^.9? . 5 Sample Tube • Mg. Operators: ?A- Leak Check: Pre: Post: I if 23 • zi j L'-n TravarM Point Number Velocity H««d In. H20 JO .vz. 1,7, Stack T«mp. °F Tested Analyte: -^ Orifice Tank #: 1 Pump/Rotometer #:_ R: Pretest (mm Hg): Post-Test (mm Hg)L Tt: Pretest Post-Test fF):_ Time: Start: , ?/3 Finish: /?* Total: W/B: 6V D/B: O2:< CO2: o 0 5 '6 $ Time 2.3i2.,fO z.3/^67 i3/V, 3^ Z3/5, /O Gauge Vacuum (Hg) / / / / Flow Setting i&O <• f- t<,2) + (0.32 X%Cy -H (0.28x%N2) •Md-(0.44x «3 )+(0.32x -' )-l-(0.28x 7?- Md - if. S^V % % HO M. Ta 13.8 13.8 in.Hg Va - 85.48 X Cp x Va-85.48X( . ^ V.. •J?.^' n/. A.- -\.U~\ n2 Qa - Va x Aa x CO a/m Q.- — I Ta(°R) Pax Ma Qt x 17.647 X- dscrin (i 100 ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: L^,b Site: jOdu^^^^,^ Operators: Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar + - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw Vapor Pressure of H/>O - Rva - (Pvw) - Pva=( ,^ } < wt •<«»' Location: n/u:* u,._.,i r.i Run ff: w^.-j-'b Date: Pbar = ^a.^-L Pq = . "'> -^- PS= T.? (Ps - Pvw) x (AT) 2SOO-(1.3xTw) * )x( , ------- as a. 3 METHOD 18 FIELD DATA SHEET __ '-s /9 Plant: L/tSCO TesteH Analyte- Si^^^_ Date: o'-lo-'n Orific« Tank • — Location: .^o/ £,)«.,, <..L Pump/Pntnmeter #: i/W* / Run: fte-T-i Pt: Pret«st (mm Hg)- Stack I.D.: z&" i ^ '' Post-Tact (mm Hg): Pbar: ?4 ?2_ Tf Pr«««t fry Sample Tube Operators: -n/ #-R6-)-lfl /?/=- 7-/A Roct.Toct CF)- H Tims: Start: ^ Finish:/^ Total: 3^>_ Leak Check: Pre: / Post: S W/B: -3 _D/FV i f 00: i/ CO0: o • Gauge Time Vacuum (Hg) mi, ^6 / -D3&91 ' 1110. -z.1 1 ilTH. L5 1 M.i0! 5^; Travaraa Point Numbar I •i -i •j .r U I 2. ~/ V 7 «. / 7 5 f S 6. I 1 •5 «f 5 o Flow Setting S£o<^^ /30d- ,30 cc. ;<,£»- - five. - N^ — j 0 5 Vatocrty Haad In. H^O ,06, .o6» oT ^7 , o;7 .0^ ,// ,01 O(f ;OS o5 ^ II .0^ .06, ,0^ •OCf • i -L •06» .07 0.5 o5 .w? .1 / f~o.cn if Stack Tamp. °F 7< 77 -77 77 7") T? -77 -)1 71 -77 -»T -77 -77 -77 •71 IT 11 TT TT 7~7 -77 -71 -7 7 11 -7-7 Md - (0.44 x %CO2) + (0.32 X %O2> + (0.28 X %lj) 7/ Md. ^=7 % H.O % HO 1\| Ma-Mdx(1 100 ' 1B( ,00 ' 17- Ma-(^)'rl" )x(1- _L_!_) + 18(-L_L) 1 ' 100 100 _,, M.- gS-S "g Ts- "J-? ^-^O °R(°F^4«)) D- DU ^ S.P. _ , -^ _ , . - "^S" P8 b HT ' S '-' . 13.0 Pa- D^.^"""? In.Hg ^P - o 5Cp-)V — J Ts ("R) Va - es.4* x ------- WE7-3ULE/DRY-5ULB MOISTURE CALCULATION Plant: (_q $> 0 3ite: ^DO^X, r^^O- Coerators: 3arometnc Pressure, in. rtg = Static Pressure, in. H2Q = Absolute Pressure of Stacx = Pbar - - Wet-Bulb Temperature. °r = Dry-Bulb Temperature. °r = Temperature Oifference. Td - Tw = Saturation Vapor Pressure of H«C at Tw Vapor Pressure of K,Q = PVa = iPvwi - Pve.=< . Q0?c; j ( 3S--S-7- So -scaticn: • ° ' ^/•rA "^n ?r '2^'^~> - 1 ?bar = Pg = -^_ Ps = ' T C 3 -^ > J.o Tw « Td = AT = drom Table) = 3vw = 'Ps - P'/w» x (^T) 2800 -X( i ^ ) ' T JV\ t.^ d Date: ?«?,.? 2. -,6.S 3^- ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: LMco Date: 5-20-41 Sampling Loc Run #: 7^ E ation: ^rrii^ Ar.i,,.llf,f Clock Time: /7/0 - 1-Z Onflrfrrni's- -rAI5S Barometric Pressure, in. H Moisture, %: "O- ft Stack Dimens Wet Bulb, °F Travaraa Point Numbar l L 3 ^ < 0 1 ^ -3 if 5 t- i 2- •? M 4 L t I <^ 1 q: Z^ 9 7 Static Pressure, in. HUO: •"",£•'?> Molpnilarwt Hrv ^? ?w PHotTube, Co: .7? . lion, in. Diameter or Side -£& Dry E Vatocny Haad in. H2O .0(9 0^? • ol 01 .07 .o« . u oy .01 .OS .06 , /O .// J/ •01 OG» OG .11 M ,°% ct* • OS Stack Tamp. °F 76. lt-^ 7G 7^ -70 -70 ^7 11 -T7 71 H 11 11 71 17 11 T7 11 7~1 11 n 7-) 1: Z5 Side 2: Z.V lnlh.Op. 11 Md - (0.44 x %CO2) ••• (0.32 X %O2> + (0.28 X %%) Md-(0.44xO ) + (0.32 x i ' ) -t- (0.20x7 V ) % HO % HO 100 k °° •&&- Jr Off M.-( 2«.^ )x(,.^_).ie(^-) « p • -•"• / , 2j 13.8 13.8 Pa - 7-$.$n In. Hg &P- •7-"'"? — 1 Ts f-'R) i «r"T"7 v«. /?,jS^1vi A«« ^iCl ft2 O« av Va « AA v rtO ft/m Q^ _ (TS'O %^ y j 'Vy ' w QQ • Qt- 'S^JS^L- «Hm 5^2.^1 X 17.847 X- 8i dadm 100 ------- WE7-5ULE/DRY-5ULS MOISTURE CALCULATION Bite: cerators: Date: ---< Barometric Pressure, in. hg = Static Pressure, in. H,O = Absolute Pressure ot Stacx = Wet-Bulb Temcerature. °r = Ory-Sutb Temoeratura. °F = Temoerature Difference. ~d • 7* = Saturation Vaoor Pressure ot H-G at Tw itrom Table) = =bar pg d = -7T Vaoor Pressure ot hUG = Pva = Pva •Ps - f=«/wi x 2800 - n.3x Fw> . 253Z 2BOO-(i.3x Proportion ot Water Vaoor oy Volume 5ws Bws = VAPOR PRESSURES OF WATER In Inenn ot Mercury 0 •o :o 30 «o so ao 70 00 00 100 MO ,120 'l30 14O 190 180 170 180 180 208 210 3 '.0378 :083t :.103S 0.1847 0.2471 o.uta 0.739S 1.032 1.422 1.032 2JM :.ioao 3.J718 OJ37B OJTB4 0^407 0.9 i.e 1. 2J7I 2 O417 .1127 a.taoa 3^877 ojeoa O.M01 0.7812 1.102 t.913 3 3.0441 3.0728 3.1186 3.1878 0.2782 0.4082 0.9802 04189 1.198 1.981 2.114 SJtl 1 2.740 3443 4.773 '0788 :.i24* 3.1898 3.2881 3.4 O.fl O.J t.178 1.810 2.178 2J11 a 3.0317 3.0844) 3.1370 3.744 4J 04120 0.4820 04443 04048 1.2S3 1.712 2410 3481 4J 7 3.0341 3.0882 3.1428 3.2203 04240 0.4 a 3 0371 7.7» 1X77 !( II 8.180 1840 1347 2X17 2UI 2447 301 3fl J4S1 9413 6481 1041 1347 18JO 20JD 9.109 8J07 11.12 1340 174* 2140 04382 1.283 1.789 2470 1180 4.174 1442 7.0M 8481 1148 \t 174 :.isoa 3.: 3.4 3.4 0.1 OJ t.a 1.810 2444) 3490 3488 1U 14 1841 2747 31.10 in. Hg in.r^Q in. Hg °F °F °F m. Hg in. Mg ------- cza GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: ut^o Date: 2-^>-^ Sampling Loc Run#: KE- ation: fy>wi ekur/- Clock Time: ' ?V ? 7-~^ Oneratorr •rt/f Barometric Pressure, in. H Moisture, %: /- * Stack Dimens Wet Bulb, °F: TrmrM Point Numb«r i ^ 3 V 5 0 / 7 -> V 1 U 1 z •5 1 5 o i i 3 M 5 0 q: ef.9z. Static Pressure, in. HUO: —.^3 Molecular wt.. Drv: 7ff ?V Pitot Tube, Cp: -2Z_ ion, in. Diameter or Side •** DrvB Velocity H.td in. H20 ,06 •o7 ,O(D ,OG ol -08 .09 8 .oCn .(^5 ,05 ./O /2> <0^ •OG ,05" ,0^ >/0 ,IO •°1 ,05 .0^ ,06> ./o «F-,Zd52 Stack T«mp. °F 17 77 ")? -)7 1U ^7G -71 77 if 11 71 1G 7^ ^70) '16» 7 * (0.32 X %O2) t- (0.28 X %N,j) Md-(0.44x 0 )> (0.32x^.1 )(0.28xTl ) Md- 2-.^ % HO % H20 Mc-M«iJi(l • 1QO ) io< 10Q I M.-(^.^ )xd- -^35- >* ie(^TS5-> M.- -i8-"13 T;. n °F- 531 °n (°p4«3) Pt - Pb + SP' - (l&tf'i. ) + 13.0 '3-8 P«- Z^.^l In. Hg ^P . , Z6 5 2- — . \| Ts (^R) Vi-«b.4«xCpx VAH x \j p,xM8 - 1 — I i>"2T V«- 85.48 x( .9? )»(.165Z. )XA i£J V T^.D A-Z.f.~»3 v« • /?.oG> ft/i Aa.^.^T ft2 Q • V« K AA v 6O ft/m Qt. ,f.OO x -V,C ' X«> 0.. ^00 .dm P« %«z°4 Q.itd=Q.Xl7.647x — x(1--^-) •«^-fl /.o 0.^.5000 xir.e47x_2T-_x(1.-jS-) ------- 200., Plant: Site: WET-BULB/DRY-BULB MOISTURE CALCULATION Location: Operators: fft. Run ~ 7 - Date: s~-- Pbar = Pg = Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of StacK = Pbar Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Td = Temperature Difference, Td - Tw = AT = Saturation Vapor Pressure of H2O at Tw (from Table) = Pvw = (Ps - Pvw) x (AT) /9 Vapor Pressure of H20 = Pva = (Pvw) - Pva=( , 2800-(1.3xTw) 2) X ( ,? ) 2800-(1.3 x Proportion of Water Vapor by Volume = Bws (Ps) Tamp. OF 0 to 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 0 0.0370 0.0631 0.1025 0.1047 0.2476 0.3626 0.5216 0.7392 1.032 1.422 1.932 2.596 3.446 4.529 5.681 7.569 9.652 12.20 1520 19.01 23.47 28.75 35X0 42.31 5044- 1 3.0398 0.0660 0.1080 0.1710 0.2576 0.3764 3.5407 0.7648 1.066 1.467 1.992 2.672 3.543 4.647 6.034 7.759 9.865 12.46 15.63 19.42 23.98 29.33 35.68 43.11 51.76 ,,0 in. Hg in. in. Hg o.- °F in. Hg in. Hg ( TJ-.tl ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 15.99 19.84 24.48 29.92 3647 43,92 52.70 3 0.0441 0.0728 0.1186 0.1 B78 0.2782 0.4052 0.5602 0.8183 1.138 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.36 13.07 16.34 2027 24.97 30.52 37.07 44.74 535 4 0.0463 0.0768 0.1248 0.1955 0.2691 0.4203 0.8009 0.6462 1.175 1:610 2.178 2.911 3.848 5.031 6.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.57 54.62 5 0.0469 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2243 2.553 3.S5& 5.SS3 6.660 8.557 10.66 13.67 17.07 21.14 26.00 31.75 38.50 48.41 5540 a 0.0517 0.0646 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.650 8.767 11.12 13.98 17.44 2149 2643 3248 3924 4727 5640 7 0.0541 0.0692 0.1429 0.2203 0.3240 0.4666 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.981 11.38 14.30 17.82 2245 27.07 33.02 3949 48.14 5741 9 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.819 2.449 3.259 4.269 5.585 7.202 9.200 11.65 14.62 1821 2242 2742 3347 40.75 4843 5843 9 0.0598 0.0962 0.1567 0.2383 0.3493 0.5035 0.7144 0.9989 1.378 1.875 2.521 3.391 4.406 5.732 7.384 9.424 11.92 14.96 1841 2249 28.18 3443 4142 4043 9947 ------- , c 3 K ?l Plant: Date: - 9 ? Location: CiMf/v1 Run : 90- I METHOD 18 FIELD DATA SHEET Tested Analyte:_ Orifice Tank #:_ Pump/Rotometer Stack I.P.: i S' Pbar:. Sample Tube r 9-7-M ir o Post: . Time IS-/} /scq IS l^ ^"IV /5'^ Gauge Vacuum (Hg) O O O O O Row Setting ^Td; ^A, \ — 7- ^ / ^ Point Number 5 V«lodty H in. ,01 Time: StartLL!i^Finish:jii£Tota!:_££_ W/B: — D/B: — O2: — CO Md - (0.44 x %CO2) + (0.32 X %O2) + (0.28 X %Nj) Md - (0.44 x ) -t- (0.32 X ) + (0.28 X %HO —- 100 100 I.- SB Stack T,mp. i(o //.. V o") V« • 65.48 x Cp X V« « 85.40 x ( fir^-lZ )x( )x I Qs- xflO QHW— - /. 2 ^ 100 Ifi. ------- Plant Sampling Location g)U (Ov Run Number: FIELD DA IA SHEET Sample Type: flj- V Operator:^ S/G fc- Nozzle ID: Pretest Leak Rate: Pretest Leak Check: Pilot: Date: cfm Ps: — 02: -^ Assumed Bws: Thermocouple #: Filter #: — - — Meter Box #: ) cfm @ ^£ in. Hg. Stack Diameter: /J' As: /.Z5-/V* Post-Test Leak Check: Pilot: — Orsat: ~ TrwwM Point Numtwr Sampling Tim (mln) r> /ft OA •1° V, dock Tim* (244iour dock) /ty^t, I$QO K/a i< 3>ft j<^n Gaa Meter Reacfing (Vm)tt3 N9I/6* ^»S.5& V^.-vs" i/K <^ <63.^i< V.locrty Head (Ap) lnH2O Orifice Pressure Differential (AH) in H20 Desiied \| Actual Stack Temp. (Ts) Tempeiature °F Ptobe Filter Impinger Temp. °F Dry Gas Meter Temp. Inlet (Tm in°F) Outlet (Tm out°F) Pump Vacuum (in. Hg) Y/////////////////////M l.fL (.$& /x§6 j, e^> '•• .-•"" .' •'. ' r: ^« srt ------- SAMPLE RECOVERY DATA PLANT DATE tMa> Run No .?-?-/ Sample Box No. loh No. SAMPLE LOCATION TRAIN PREPARER SAMPLE RECOVERY PERSON COMMENTS FRONT HALF Acetone Container No. Filter Container No. Description of Filter Samples Stored and Locked RACK HALF/MOTSTTfRF Container No. Liquid Level Marked Liquid Level Marked Filter No. Sealed Sealed Sealed IMP. NO. CONTENTS TOTAL INITIAL VOL (ml) /(> to WEIGHT fgramsi INITIAL FINAL 010.3 NET 0. S /A III ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: U<^o _ _ SOURCE/RUN #: JL2^L_ DATE: 1 . Leakage Correction for Volume Metered Vmc=( )-( -0.02) x( V = _ ft vmc - ll 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) Pbar+(AH/13.6)N Vm = 17.64 xVmrxYx std mc Tm Vm = 17.64x( mstd v v mstd 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V... = 0.04707 x (W. - W.) wstd T ' 'std rstd Vw = 0.04707 X( V =_ili§_scf 4. Percent Moisture, by Volume w wstd v , v wstd mstd - ws~ ------- 3-B.a. cia GAS VELOCITY AND VOLUMETRIC FLOW RATE Pi^nr /flWr, . Date: A-.90-?9 Sampling Loc Run#: £'7- ation1 OlfS.f\J ** <9 Clock Time: /$tPG -7 Operate"^- £)&Y/<3G , Barometric Pressure, in. H Moisture, %: "~ Stack Dimens Wet Bulb, °F: TravanM Point Number /9- \ 3 3 - Static Pressure, in. H«O: • ~£ft Molecular wt.. Drv: — Pilot Tube, Cp: , ?£. ion, in. Diameter or Side DrvB Velocity in. H2O < 11 ••19 , l'~> »• ^"t) /^ 3H , Qf5 , 1 1 , 9o Q.9 - 9o .30- . 91 Stack Temp. °F /6t iG'~) Ib^ .00 //& -t- (0.28 X S,!^) Md - (0.44 X j } ••- (0.32 X ~i\ ) f (0.28 X~l 5 ) Md » '>£•'? H % H.O % HO 4Wi 1ft/ ^ • JA V W » ^& f ^ 13.8 13-8 Pa- 7 ------- FIELD DA IA SHEET Plant: LA^db Sample Type: /V\ - M Operator: b&/C& Sampling Loci Run Number: ition OlDifA) ^ Pbar 0 ' y-")-^ Date: 5'3Cr9"7 CO2: O2: Pretest Leak Rate: , Cfin cfm @ /$ in. Pretest Leak Check: Pitot: — -Orsat: — Point Numbe Sampling Time ; (rrtn) DO /° 9C, i 0 \|c dock Time (244iour dock) /^l\ \QS\ IS '31 1^4-1 i°i5 ) Hg. Probe Length/Type • Stack Diameter: _/ j; j 's'^ Pilot #: S" 3 S'1 As: 1,23-ft2 • Gas Meter Reading (Vm) ft3 V£S. 6V<5 4^1 .1 '>7.3 ^•Q J ,4-13 •Sc.?, 4-"7_J 5^-j 9<9 Xl-i .3 .•^ V ^ n ' ^ o ^ ^ r b Velocity Head (Ap) inHZO Oriioe Pressure DirlerentuU (AH) in H2O Desired Actual Stack Temp. as) Nozzle ID: •— Thermc Assumed Bws: ' Filter # Meter Box #: / ^ Post-Test Leak Ra •couple »: VA Y:/9£kAH@: /..(7-'=i le: (SXl)'> Post-Test Leak Check: Pilot: Temperature °F Probe Fater Impinger Temp. °F cfm @ i^ in. Hg. Orsat: — • Dry Gas Meter Temp. Inlet am in°F) Outlet am out°F) y///////////////////////////////////////////^^ \}&.LC£rf ,O°i ( \ 3 r I"? ' y 4. -•~ y/f S>¥ \j --7 ^^ X J '7 ^^ i? o o 5^7 9o « Pump Vacuum (in. Hg) -/^ 3 3 3 2> AVm- Tm= JJ ------- t SAMPLE RECOVERY DATA PLANT DATE Sample Box No. SAMPLE LOCATION TRAIN PREPARER ^ T Ou SAMPLE RECOVERY PERSON COMMENTS FRONT HALF Acetone Container No. Filter Container No. Description of Filter Samples Stored and Locked RACK HALF/MOISTTTKF Container No. Liquid Level Marked Liquid Level Marked Run No. Job No. Filter No. • / Sealed Sealed Sealed IMP. NO. CONTENTS Ox H2o N TOTAL INITIAL VOL (ml) (00 WEIGHT (grams) INITIAL FINAL NET ' \ ./(I! ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: U ------- J ag GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: £/?SC°> .. 9^ , QQ ,os Stock T«mp. °F DPS' ^>£9 99^ -S' 3 ,5kO 9>9£> P9S' 3P Md - (0.44 x O ) -f (0.32 X 1,\ ) f (0.28 X "71 ) Md- ^T'^Y % HO % H.O M. -Mdxd IOQ ) 1B< IOQ ) 1,7 t>> M.-(»<.1^)x(1--T—- )l8(-j— -) Ms- 9^ -TO 71- 33n °F- l^6? 0R(°F460) Pa — Pb = ( 3 i* Q3) +• ^— ' — ™ i3.a su.q?; ,3B p.. 9^-^ in.Hg ^- .HZI — , \| Ts ^R) vi-«6.4yxcpx ^SP x ^ '"'p;;1^ V.-05.48X( TT )x(.-n\ '^35.^^ V.-^5'50 fM A.- 1-3? n2 oc. l»-^<> x \-^^ xeo Qt- ^31"? adm Pt H,° Ot^- Q« XI 7.847 X x(1- -—^-) •» j, 100 •yy.%0, V.3 Q-rtd- »?^Ki7Jir« — ^Y"'0"^ ------- ago eg METHOD 18 FIELD DATA SHEET Plant: L/)^jO T«st«H Anaivte- Srv/teA1* : D L R S P S C L 2%fS' ^0/60 3^-11 3^'93 t/ -^ 2,%'^ Hi. <° ft.b* \2^L ate: S'-^c- '-) 9 Orifico Tanir 4- acation: OUZ/U X-/0 Pump/Pntnmfiter #: - - un #: /tf - 7 - .X Pt: Pret«c (mm Hg)- - tack I. D.: JS " Post-Test (mm Hq); — bar: £S#9 Tf Pmtoct (°P)' — ample Tube Jperaiors: D #• )C -7 - 5.^ /O f-9 A Po«t-Tflst <°R • - — eak Check: Pre: -aco Post: • oco to ^L ^> 1-73^ o 11^3 O 1 ~> S"3 0 / 6 63 0 Flow Setting ?&ct/n • ' ' i y \ x ^TATI(L ~~ • PI Traverse Point Number fl-» _y ^ f c .A-; o> ^7 y <;~ ds Velocity . /^) ' / "5 I L-> 90 - £c' ^ Q ^7 ' ^ 6, , 55 C3 1 , I ^ '0O »<9V <^— WfcP X«V^ Stack Tamp. 95? l ;9^7/ .9 s? •£ .5»9V &3(3 g Si. C( 5-3O ^SS" 0 "V? ?P '? 5? J^? tf 9$'% ftSlS Time: StartLLlsi_Finish:j8o2__Total:_(46 — ^ W/B: — D/B: — O2: — CO«:— ~^ Md - (0.44 x ttCOj) + (0.32 X %O2> + (0.2B X %N2> Md-(0.44x ^ J-M0.32X Zf ) •»- (0.28 x"7? ) ^ V ^ % H-O % H20 •fe/^ -3 V'? '"^ W-T'" 39e) °fr-(i'XAI A. _ V« ^J ** Qa • Va x Aa x flO a/m •7 J JJ a-7 Qg-O'l'Q^x I- »)XflO Q_ ^.tj^-j •" P« SHjO D.<, _ ( • J . ^^•_\|gjfjaj 1 (J ^ 1 OflflVD ------- FIELD DATA Plant U\>CO i • Sampling Location duiCH & )£, Run Number: 1 C -7- 2 Date: Pretest Leak Rate: , OCO cfm @ / 1>' in. Hg. Pretest Leak Check: Pitot: - Orsat: — - Sample Type: f^\ ' I Pbar 2-&&1 Ps: CO2: O2: Probe Length/Type: / Stack Diameter: /,}' " Operator: P#ty Pilot: ST-3 As: I • M -ft* Nozzle ID: Thermocouple #: n u Assumed Bws: — Filter: Meter Box #: ; ------- SAMPLE RECOVERY DATA PLANT """^ c ° ¥f°'d v cr DATE ^-^-«!\ Sample Box No. * SAMPLE LOCATION ^\0 ^oc^ ^ ;obNo Vi'l.oo? Filter No. /VA TRAIN PREPARER SAMPLE RECOVERY PERSON COMMENTS 4 r>U FRONT HALF Acetone Container No. Filter Container No. Description of Filter Liquid Level Marked Samples Stored and Locked RACK HALF/MOTSTTIHF Container No. Liquid Level Marked Sealed Sealed Sealed IMP. NO. 1 2 3 4 5 6 CONTENTS 0* Uno or wto ^•I v~(^ S , 1 ( <"„ CjAJL TOTAL INITIAL VOL (ml) [;OW 1 OC? - 390 WEIGHT (granui INITIAL GlG^ 6o(?J 471-3 ^SU FINAL 63^-7 L^oo,6 ^.1 "l^G.y NET ' 2.1 o.g &M 573 %3 ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: Laj-'2- DATE: 1 . Leakage Correction for Volume Metered Vmc=( •)•( -0.02) x( ) V = _ ft3 vmc - ll 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) Pbar-MAH/l3.6)N Vm = 17.64xVmrxYx mstd mc m v mstd 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V w = 0.04707 x (Wf - W.) Vw = 0.04707 x( r rstd vw = - scf wstd 4. Percent Moisture, by Volume V, wstd BWS= ~ wstd mstd B - DVVS- '*—- /»» ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: _ Sampling Location: QU<£A' Run#:J^> 3> Date: $ - 9C - 9 1 Clock Time: Q&&O Operators:. Barometric Pressure, in. Hq: £>fr'.93 Static Pressure, in. HgO: Moisture, %: Molecular wt., Drv: "" Pitot Tube, CD: , 9S Stack Dimension, in. Diameter or Side 1: 15 '' Side 2: Wet Bulb, °F: Bulb,°F:. Trovara* Point Number /M •^ ^ V f & A- / .0 ^ H < 6 Velocity Head in. H2O ' /O MS M .l^ ,95' r^^ .. 3rt /- 5 i ..0) ,/<5 .9' , yH Stack Tamp. °F 35? "I 9^0 937 ST79 2.9.? 2 $7 asi atj f (0.32 X %O2> * (0.28 X %NZ) Md - (0.44 x ^ ) + (0.32 X ~~\ ) -t- (0.28 x"? T ) Md. 3-«lf % HO % HO Mt . Mdx(1 - —) •• 18 ( — ) 100 100 100 . 3-8.10 liL_ 100 °R(°F+430) oa _ «I + -i-^-^ ( >30 =Q« xi 7.647 x - x(l- - — ) T« 100 Qt-M- ?5"3? X 17.647 X- , «W 6.1-2, dwtm •xd 100 .///f ------- •3-3 Q 3 u-ac=; METHOD 1 8 FIELD DATA SHEET Plant: ^iO Tester! AnaK/t«- $A/ «.^«_ C L F S F £ C L t4So o g'S'O ;o i S ^ aft / "S 2.&> i° feo Ql _ 'y« si /5to ^\): (b.oZ. %--B% Jt )ate: ^-Zfl-'H Orific« Tani< • - .ocation: MDft Pump/Rntnmeter ^: v0^^ * a- iun #: NDA-1- 1 Pt: Prefect (mm Hg)- Jtackl.D.: 52"xi2T>11 Post-Test (mm Hg): - sbar: ^it Tt: Prfitset <°R- sample Tube Operators: •« !A;nfl-l-»fl MOA-1-/R Post.Teet (°R: ~ »-55 .eak Check: Pre: // Post: ^ Gauge Time Vacuum (Hg) 14 ^5^-7 , ' ^ -?•? . so r «?qn-7l^ ' ,^3.2, / / ^s- , ^ i •.IW.IS I \ 5oo0 t»7 1 Flow Setting 2.1 2.1 1-\ 2 / ^.i Z/ 3^ Trav«re« Point Numbar Vatocity Haad In. HjO Stack Tamp. °F Time: Start^sb Finish: Jl5& Total :J^6 W/B: — D/B: - O£: -Li CO2: ^3 Md • (0.44 x -fcCOj) -f (0.32 X %O2> + (0.28 x %^) -r / A\ u j /<» 4^ „ \ j. /rt ^9 v ^ ^ fO 5B x 1 ?3 w Md- % KLO % HO ^ M.-Mdx(1.^-).18(-i^-) ^ Ms " ( )x(1- )-i-18( ) ^ 'M 100 100 c\|/ M«- Q3 Ts- °F- °R(°F + 4flO) o p D« . DK i °'' ' -, / \ J. 13.8 13.8 Pa - In. Hg V5p- s= J Ts ^R) V» - 65.W x Cp x V^ A y p8 x Ma Va - 65.40 x ( ) x ( ) x Al Vs- ft/a A.- n2 Qa-VaxAaxeoa/m Qt- x x80 Qa - acfm Pa «2° Qa^.- Qe xl 7.047 x x(1- — -2- ) Q^rtd" xi7.e47x x(i- iflo ) • Qtttd" dacfm ------- METHOD 18 FIELD DATA SHEET PlantL Date:_ Location:_ Run #:_M Stack I.D.:_ Sample Tube ; /\/nft-i-zA~/7pfe-7-23 Operators: ^5 Leak Check: Pre: / Post: .^" Tested Analyte:_^ Orifice Tank #: Pump/Rotometer Pt: Pretest (mm Hg): Post-Test (mm Hg)L Tt: Pretest (°F):. Post-Test fF)L_r_ 13 \ •-> z* Time \ SCJO.^-JL i So 5 . 3-7 / .56 5. . Finish: ^^iTotal:. W/B: — DIB: — O2: a CO2: Md - (0.44 x %CO2) + (0.32 X %O2) + (0.28 X %N2> Md - (0.44 x Md (0.32 X (0.28 X %H20 100 100 100 e p Pa- &- Va • 65.48 x Cp x Va - 65.40 x ( Va« Aa- in. Hg Y-STsr )x( )x f ft/a Qa-VaxAaxeOa/m Qa- Qa- x00 aefm Qt ...iQex 17.647 x-^-x(1- —•-) •tn Tg 100 Q«atd" X 17.847 X- dacfm •x(1 ------- APPENDIX A. 1.9 Condition 8 (includes flows, moistures, and Method 18) ------- DQC7 Plant: L /Ud£> Date:. 5-z^-n METHOD 18 FIELD DATASHEET Tested Analyte:_ Orifice Tank #:_ <>V,/,~/v>. Location:. Run #: /vig- Stack I.D.: Pbar- Sample Tube #: Operators: fA Leak Check: Pre: Post: of «?•/ oS '3 /o Pump/Rotometer #: ./ - 18 ( i 100 100 1.2 100 100 ^y, 1 • <_ - ,o7 Travarse Point Number i 2 T V •f 6 1 1 1 I 3 H 5 /, 1 tf TSu - Velocity H«aa in. H^ -Z.-7 ^/ j,3 , ^3 . b'-f . 2~J •^ "i . / ?> 18 . 30 - 12 . 51 ,32 32 • )>3 .32- O.5>il Stack Tamp. °F -rJ -73 w "I'-f 7V "?y 7T 2-H dadm x60 %HgO 100 Z9 5 S3V i.q 100 ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: i-^(o Site: M/VIM &u>titf,r- Operators: Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Pbar ± - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw Vapor Pressure of K-.O - Pva = rPvwt - Location: . r?tjur., ME, T^ Run #:££-Date: ;'-z?-4-i 2^-5" in. Ha • * 2- in. HnC 2 zf-5 in. Ha r? °F TV Op /5 °F . -To 3 .r in. Ha 2800 - (1.3 X Tw) Pva =( 503. s ) - 2.1. S 30 2800-(1.3 x «; Proportion of Water Vapor by Volume = Bws ( .i 1-2.% VAPOR PRESSURES OF WATER In Inches of Mercury in. Hg Tamp. OF 0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 180 170 180 100 200 210 220 290 240 0 0.0378 0.0631 0.1025 0.1647 0.2478 0.3028 0.5218 0.7392 1.032 1.422 1.932 2.506 3.446 4.52S 5.881 7.560 9.652 12.20 15.29 10.01 23.47 28.75 35.00 42.31 5044- 1 0.0398 0.0660 0.1080 0.1716 0.2576 0.3764 0.5407 0.7648 1.066 1.467 1.002 2.672 3.543 4.647 6.034 7.750 0.885 12.48 15.83 10.42 23.06 20.33 39.88 49.11 51.78 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.740 3.642 4.772 6.100 7.052 10.12 12.77 15.08 10.84 24.46 20.02 36.97 49.02 52.70 3 0.0441 0.0728 0.1186 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.820 3.744 4.000 6.350 8.150 10.38 13.07 16.34 20.27 24.07 30.52 37.07 44.74 5945 4 0.0463 0.0768 0.1246 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.176 2.911 3.848 5.031 6.513 8.351 10.61 13.37 16.70 20.70 25.48 31.19 37.78 45.57 54.62 j 5 0.0489 0.0810 0:1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.005 3.054 5.165 6.680 8.557 10.86 13.67 17.07 21.14 28.00 31.75 38.50 48.41 5540 8 0.0517 0.0846 0.1370 0.2116 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.650 8.767 11.12 13.08 17.44 21.50 26.53 3248 39.24 47.27 58.80 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4666 0.6669 0.9352 1.293 1.785 2.370 3.160 4.174 5.442 7.024 8.081 11.38 14.30 17.82 2245 27.07 39.02 3040 48.14 5741 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4856 0.6003 0.9666 1.335 1.819 2.440 3.250 4.280 5.585 7.202 9.200 11.65 14.62 18.21 2242 27.62 39.67 40.75 4049 5849 9 0.0596 0.0082 0.1567 0.2383 0.3403 0.5035 0.7144 0.0080 1.378 1.875 2.521 3451 4.408 5.732 7.384 9.424 1142 1448 1841 2240 28.18 9449 4142 4043 5047.: J. ------- ^^m ^M aca GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: LA&6' Date: S-zz.-'n Sampling LOG Run #: «= ation: /v»^;/, /r-v/wA Clock Time: -"^-s- - ion, in. Diameter or Side d.3 DryE Velocity Heed in. H2O ,zy , >/ . S2 ?>/ £, -3S .Vd; ,v / ,iS .i7 17 7? 7T 71 77 77 -7 7 -7-7 •7"? ^^ 11 "77 -77 77 71 1: /7 ^ Side 2: — ulh.op- 71 Md - (0.44 x %CO2) -t- (0.32 x %O2> + (0.28 x%r^) Md»(0.44x & )-t-(0.32x^/ ) + (0.28 x ' r ) . Md - Z.S'S''' % HO % HO M< - "2^, ^0 1~3.8 13.8 Ptm 2. n2 Q> • Vs x AB x 00 s/m Q« - i+y^tS x / " "7 xOO Qt- ^5^^ aefmfttsT) P.^ %H,0 0,itd-Q.xl7.e47x — x(1.-j^-) K4,trh <^/ 2'^ . . '»-5 nd 5 3 -7 100 ------- Plant: Site: WET-BULB/DRY-BULB MOISTURE CALCULATION Location: /vie -i^L- /n<;, C^A. Operators: rA Run #: , -.S in. Hq ^\ (. -S °F -7~» 0P; AT= 1 °F Pvw = • 5t> = ( Tmp. OF o 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 160 190 200 210 220 230 240 (Ps) 0 0.0376 0.0631 0.1025 0.1647 0.2478 0.3626 0.5216 0.7392 1.032 1.422 1.932 2.596 3.446 4.525 5.881 7.569 9.852 1220 1529 19.01 23.47 28.78 35.00 4241 5044- 1 0.0398 0.0600 0.1080 0.1716 0.2576 0.3764 0.5407 0.7646 1.066 1.467 1.992 2.672 3.543 4.647 6.034 7.789 9.885 12.48 18.83 19.42 23.98 2943 35.88 43.11 51.78 in. Hg ( it.; ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1603 0.2077 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 15.98 19.84 24.46 29.92 36.37 43.92 52.70 3 0.0441 0.0728 0.1186 0.1876 0.2782 0.4052 0.5602 0.6183 1.138 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.36 13.07 16.34 2027 24.97 30.52 37.07 44.74 5345 4 0.0463 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.176 2.911 3.848 5.031 6.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 48.57 54.82 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.660 8.557 10.86 13.67 17.07 21.14 26.00 31.75 38.50 48.41 5540 8 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.650 8.767 11.12 13.98 17.44 21.59 26.53 3248 3924 4727 5840 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.981 11.38 14.30 17.82 22.05 27.07 33.02 3949 48.14 5741 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 •1.819 2.440 3259 4.289 5.585 7.202 9.200 11.65 14.62 1821 22.52 27.82 33.87 40.75 4943 5843 9 0.0598 0.0982 0.1567 0.2383 0.3493 0.5035 0.7144 0.9989 1.378 1478 2.821 3.381 4.608 £.732 7.384 9.434 1142 14.96 1841 2249 28.18 3443 4142 4043 9047 J,. ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: t-(\•"/ F ation: \ })c. ;,v r x h c, ,„ r Clock Time: y^ o 3 S '- 7 Onerator^' "?# / ss Barometric Pressure, in. H Moisture, %: 1'$ Stack Dimens Wet Bulb, °F Travara* Point Mum bar / t ^ V 5 G -7 J' / T_ i 4 5 t, 1 tf q: ~>Q, <$ Static Pressure, in. hUO: cz Molecular wt.. Drv: --W Pitot Tube, Cp: .-? .ion, in. Diameter or Side 67 DryE Vatocrty Haad in. H2O , ^2^ . ^' !>3 , i3 . 3G .i? . // .^/Z. 26 7 4 ' ^- ^5 ,26 .32. ,30 ,3>3 • ^ ,33 Stack Tamp. C^"2> 90 .50 5'0 gro 80 T^ f^) ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: L$6(J) Site: MO^ <2skfaJJr Operators: Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar ± - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of HpO at Tw Vapor Pressure of H/jO = Pva = (,Rvw) - ( 2.£ -?i S?< Pva=(,5£6i. ) — Location: M* -zt'tw Post-Test (mm Hg): Pbar: H.* Tt: Pretest fR- Sample Tube Operators: #'.AIZ--I A fir-S-l Post-Test fF): Trl- ' Time- Start: cy-sy Finish: «"# Total: 3c7 eak nherk- Pre- :/ Pnsr^X W/R- <4i n/R: •?/ On: 2 ' CCV o Gauge Time Vacuum (Hg) T7s/riy < 77^3, 2 Z / 1-1^,95 / -nnL.^0 l/;n- >/,% ^ Flow Setting / •>£><"- / !?O f <• T / 1 ,/' ,0(j> .^6 . oi .Of Stack Temp. °F ~\l T 1 Tl Tl Tl Tl 11 1 ' 70 -70 70 70 -1 / 11 -I/ T I ( -l' Tl ->/ ^> ^/ T Md = (0.44 x %C02) + (0.32 X %02) f (0.28 x roNj) ^5 ,> c^ Md = ' " V? % H,O % HO 0 ' 100 100 '/""5 Ms - ( "ifr. W ) x (1 - '• ) -r 18 ( — i ) ^ ( ' ( 100 100 Ms « T-? . -\ 3 ^^ T, . -!< °F= S-5/ °R (°F.460) _ p. S.P. , 7« £ , . ~ .^X 13.6 13.6 Ps= -z.'J.V^ in. Hg ^P = 2-6 26 -= 1 Ts <°R) Vs » 6b.49 x Cp x ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plam: Lfa£0 Location: fig - f- \ n< Operators: _> Run #: - 13.6 Site: Barometric Pressure, in. Hg = Static Pressure, in. HgO = Absolute Pressure of Stack = Pbar Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H^O at Tw (from Table) = Pvw = (Ps - Fvw) x (AT) Date: 5-&-> Pbar = 7.9. S Pg = ~,0-Z- Ps= 11. 45 Tw = _-?C Td= ' T AT = & Pvw = . VS 2-0 in. Ha in. HO 2 in. Hq °F °F °F in. Hq Vapor Pressure pf H2O = Pva = (Pvw) Pva =( _^ 2800 -(1.3xTw) - . fsu) )x( if } 2800-(1.3 x Proportion of Water Vapor by Volume = Bws ( l.O (Ps) Tamp. op 0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 0 0.0378 0.0031 0.1025 0.1047 0.2478 0.3828 O.S218 0.7392 1.032 t.422 1.932 2.598 3.444 4.525 5.881 7.589 9.852 1250 1559 19.01 23.47 28.7S 35.00 42.91 50.84- i 3.0398 0.0880 0.1080 0.1710 0.2578 0.3764 3.5407 0.7648 1.088 1.467 1.992 2.872 3.543 4.647 6.034 7.7S9 9.88S 12.48 18.83 19.42 2340 29.33 3540 43.11 51.76 in. Hg ( i.y5 ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0896 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.842 4.772 6.190 7.952 10.12 12.77 15.98 1944 24.48 2942 3647 4342 52.70 3 0.0441 0.0728 0.1160 0.1676 0.2782 0.4052 0.5802 0.8163 1.138 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.38 13.07 16.34 2047 2447 3042 3747 44.74 CT.B3 4 0.0463 3.0766 0.1248 0.1955 3.2891 0.4203 0.6009 0.6462 1.175 1.610 2.178 2.911 3.848 5.031 9.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 4547 54.62 5 3.0489 3.0810 3.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.680 6.557 10.86 13.67 17.07 21.14 26.00 31.75 38.50 4641 58.60 6 0.0517 0.0846 0.1370 0.2116 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.850 8.767 11.12 13.96 17.44 2149 2643 3248 3944 4747 5640 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6869 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 6.981 11.38 14.30 17.82 2245 2747 38.02 3949 46.14 5741 a 0.0571 3.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1841 2242 2742 3347 40.75 4948 5643 9 0.0598 0.0982 0.1 907 0.2383 0.3493 0.5035 0.7144 0.9989 1.378 1.878 2.521 3451 4.406 5.732 7.384 9.484 1142 1446 1841 2249 28.18 3449 4142 4949 5947 ------- Plant: L GAS VELOCITY AND VOLUMETRIC FLOW RATE Date: 5 - Sampling Location: E; f?/£-fr-Z. Clock Time: Moisture, %: (. o Molecular wt., Dry: zftg/ Pilot Tube, Cp: . ?? Stack Dimension, in. Diameter or Side 1: ^^1e$ if?" Side 2:. Wet Bulb, °F: Dry Bulb, °F ° Trovare* Point Numb«r \ -i •j. > y 5 i/ ; 2. * V 5 6 / 2. 3 4 5 6 ; z. 3 ^ 5 ^ Vttocity H«d in. H20 .OB -06 .01 • 0'7 «0g .0% .10 /O . oi . O(s ,06 . ./a ,'3 .09 .01 ,d>6 .ol . 11 ./i ,o -i- (0.32 x ^.O^ -t- (0.28 x %^) -V ) -t- (0.28 X 1 ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: l^U) Location: 2... ..;=./.- J Site: &.w frUurf- Operators: Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar + - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td • Tw = Saturation Vapor Pressure of H2O at Tw Vapor Pressure of H00 = Pva = fPvwi - yii. Run : ££££&-*& Phar= ^'^ Pg= ~-M _P2_ Ps = Z«.tf 13.6 Tw = $6 Td = -Tf AT= ;5" (from Tahlp) = Pvw = , 7^°_ (Ps - Pvw) x (AT) i: 5-2^-47 in. Hg in. H_O 2 in. Ha °F °F °F in. Ha Pva = ( n 5 2.0 ( « 2800-(1.3xTw) •«*)(" ,< ) 2800 -(1. 3 x S(, Proportion of Water Vapor by Volume = Bws Bws = (Pva) (Ps) Tamp. °F o 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 180 100 200 210 220 230 240 0 0.0376 0.0631 0.1025 0.1847 0.2478 0.3626 0.5218 0.7392 1.032 1.422 1.032 2.506 3.446 4.525 5.881 7.560 9.652 1220 1520 10.01 23.47 28.75 35.00 4241 50.84- 1 0.0398 0.0660 0.1080 0.1716 0.2578 0.3764 0.5407 0.7648 1.066 1.467 1.002 2.672 3.543 4.647 6.034 7.750 0.885 12.48 15.63 10.42 23.06 2843 35.68 43.11 51.76 in. Hg ( M.«f ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0096 0.1127 0.1803 0.2077 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.740 3.642 4.772 6.180 7.852 10.12 12.77 15.08 10.84 24.46 28.82 36.37 43.82 52.70 3 0.0441 0.0728 0.1180 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.629 3.744 4.000 6.350 8.150 10.36 13.07 16.34 2027 24.07 30.82 37.07 44.74 83.85 4 0.0463 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 6.513 8.351 10.61 13.37 10.70 20.70 25.48 31.13 37.78 4847 54.62 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.054 5.165 S.660 8.557 10.86 13.67 17.07 21.14 26.00 31.75 38.50 46.41 5540 a 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.083 5.302 6.850 8.787 11.12 13.08 17.44 21.50 26.53 3248 3024 4727 56.60 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.370 3.160 4.174 5.442 7.024 8.881 11.38 14.30 17.82 22.05 27.07 33.02 30.80 48.14 57.61 a 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 •1.819 2.448 3.259 4.280 5.585 7.202 0.200 11.65 14.62 1821 22.52 27.62 33.67 40.75 40.03 5843 9 0.0598 0.0982 0.1567 0.2383 0.3403 0.5035 0.7144 0.9080 1478 1.875 2.521 3.391 4.406 5.732 7.384 0.424 11.82 14.86 1641 2248 28.18 5488 4142 4043 5847 ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant:. Sampling Location: _n Run#: ,-f^- 6- Date: Clock Time: //,< Barometric Pressure, in. Hg: £? 5" Static Pressure, in. H2O:_ Moisture, %: -1 * Molecular wt., Dry: ?..$ Pilot Tube, Cp:. Stack Dimension, in. Diameter or Side 1: z e" Wet Bulb,°F: 51 Dry Bulb,°F: Side 2: Travare Point Numb«r / 7. 3 -y s Lf i 2. J 4 ^ /•» , ^ 3 .f 5 C r i •b H 5 (^ V«tocrty H««d in. H2O co> ,07 .66 .OU .0% .07 i/O ,09 ,^7 ,Ce .oT : ^>^ i/ 3 , ^o .C?Ca ,^>G ,07 , // ./o .063 0(, .oi, .^7 JO Stack T«mp. °F 7V •?«-/ 7V "7^ -7V "7-V 7V ~IL\ 7V 74 7V -7V 7V •7V 7^ 7^/ -?y -7V -7V "7V 74 -7V 74 ^P. .ai6?\|rl- IV Md - (0.44 x ttCOj) + (0.32 X %02> + Md - <0.44 x CJ ) +• (0.32 X Zt ) + (0.28 X Md - ^ ^_y Mt - P- 13.8 ) + -Av 13.0 Pa- in. Hg V« - 85.40 x Cp x Va - 85.40 X ( •'' ^ f T3(°R) Pax Ms A.. , n Q« • VsxAaxeoa/m »- Qg. aefm Pi .Qtxl7.e47x X(1 Ti X00 SHgO 100 X17.047X- •n 100 ------- Plant: Site: WET-BULB/DRY-BULB MOISTURE CALCULATION L-'J ^ •- ••* Location: P > i//\ (A "iJ Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar ^X— Operators: TA/SS RUn #: ££'$-3 Pbar = Pg = _ Ps = Tw = - 13.6 Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Td = Temperature Difference, Td - Tw = AT = Saturation Vapor Pressure of H^O at Tw (from Table) = Pvw = ,,.. (Ps-Pvw)x (AT) Date: S'/^.z/ ° 7 in. Hg in. ^0 in. Hg -.c-V \ 1 Vapor Pressure of H2O = Pva = 2800-(1.3xTw) )( O ) 2800-(1.3 x $"-7 Proportion of Water Vapor by Volume = Bws (Ps) Tamp. OF 0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 180 180 200 210 220 230 240 0 0.0376 0.0631 0.1025 0.1847 0.2478 0.3628 0.5218 0.7392 1.032 1.422 1.932 2.596 3.446 4.525 5.881 7.569 9.652 1250 1558 18.01 23.47 28.75 35.00 4241 5044- 1 0:0398 0.0660 0.1080 0.1716 0.2570 0.3764 0.5407 0.7648 1.066 1.467 1.882 2.672 3.543 4.647 6.034 7.758 8.885 12.48 15.83 18.42 23.86 2843 35.68 49.11 51.76 °F in. Hg in. Hg ( ------- i~== GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant- //><(' (^ Date: fc 5^3 - Sampling Loc Run #: 9- X ation1 OOfAr&. ? Clock Time: /T-.f7.?^ - / onerarnrs- -/Y^ /<$ Barometric Pressure, in. H Moisture, %: -- Stack Dimens Wet Bulb, °F: Trov«rM Point Number A - i Q ' •> w fir ) 3 3 f < 6 • q: ^°i. ^ Static Pressure, in. HUO: - .is>°l Molecular wt.. Drv: " Pitot Tube, Cp: r jLi ion, in. Diameter or Side '" Drv B Velocity in. H2O - l9 . ,5/ - 23 - 33 • 22 90 Slack T«mp. °F fff' ' it,"2 /&>4 Ha? j(j£ j£>'2y /(&n 1'7L? Ik a no J ' fo7 i 1: ft" Side 2: - nlh,0p- Md - (0.44 X %C02) -t- (0.32 X %O2> (0.28 X%Nj) Md - (0.44 X ) * (0.32 X ) t- (0.28 X ) M Md «1 %"2°> 18(%H2Q) 100 100 , Ma- Zfc.lrl* e p Pa - Pb * b'K = ( ) + 13.8 13.8 £P = .^° — \| Ts I^RJ V» « 85.4B X Cp X VAP x U p, x Ma , / Vi- 32.. ^^'o «/• I Z2.T- ^ A..^^, ft Qs • Va x At x 80 a/m Qs ~ J?3 \t^~~ x x * Q> • ~L-'&0?) aefm p. %HjO «W T, 100 «td .. * * too ------- a a METHOD 18 FIELD DATA SHEET ., 1 l/dvJA^ <6 34> ><>'" •(>>* 6ft •'n (0(0 A\ •6gS* X7^3 &* ^ * Plant: £/Kff Date: ^-^-9° Location- C9i' £j^ * 9 =lun#- 9-.V-.9v Stack I.D.: /> . Ou . QH ^ /•? • 9 / , y;} rQ3 ' ,9^5 O 3- )^ /4P rVVO / / Stack T«mp. °F /^/ ' t l(a L, it'j ,(t<* Tk9 //, .^r / fc / to ^ 7 /^s nn ; 6, 7 ; d>< m l&t> Time: Start;c^;( Finish:^o^iTotal:_^l. W/B:_z^D/B:^^02: — COgiJrz^. Md - (0.44X%CO2) + (0.32X%02) + (0.28 x^) Md - (0.44 x ) -I- (0.32 X ) ••• (0.28 X ) £o/ro 1 Md - .05 C-< . ^» %H,0 ,H20 p^ ^Mt-Mdxd i_) + 18 <—-£-) \- ' 3A(S3 100 100 PV u. , \»M ) + 18( ) mv' 10° 1°° ^ M,. zi-^ T«- ILU °F- I.Z.U °B(°F-K4ao) s p . - i/'i p.-pb^Il-- + — Zk — 13.8 13-8 P.. ^.H^ In. Hg fiF - o-4MO — J Ta^R) V«-«5.4QxCpX VAP X W p8xM« Va- 3Z.6?/ n/« A.- \|.2^\| n2 O«- VaxA«xoOa/m Qs- x xeo 0- 2.3H ufm Pt %H7° Qs ..»Q«x 17.647 X— x(1 • — -— • ) Qi^- X17.047X X<1« 1fl0 ) QHtd- )^iZV dMfen ------- Plant tA$£G Sampling Location ®j£rJ 9 Run Number: 7"§* ^ Date: J> Pretest Leak Rate: .«oz- cfm @ Pretest Leak Check: Pitot: -—Great: FIELDDAiASREET JjJ/_ Operator: D - Sample Type: Pbar ' CO2: Ps: O2: — Nozzle ID: -~— Assumed Bws: — Rlter #: Meter Box #: /£ Y:, Thermocouple #: V (3 in. Hg. Probe Length/Type: / ' 5 <> Ptot : Tg-^ Post-Test Leak Rate: ..-»>» cfm @ JT in. Hg. Stack Diameter: As: Post-Test Leak Check: Phot: Orsal: Point Number Sampling Tim (mln) O 10 ^tfl ^^^\ \ f} 1+ «J ^-i^— dock Time (244iour dock) 0994L B <• Q '•> 01^7^ £>y$"3- rGd> •>- /oo 5^ Gas Meter Reading (Vm)ft3 ^V9, ^7< $"£?,. ^51 S &&/ 1 O C S 73 > V o * ' 1 * Velocity Head (Ap) lnH20 Y//////// Orif ce Pressure Differential (AH) in H2O Desired '//////, I-3L 1 ft* /<$£ .•<* Actual Stack Temp. fTs) Temperature °F Probe Filter Impingei Temp. °F '///// £>Q L/6 £~Q £ 1 Dry Gas Meter Temp. Inlet (Tm in°F) '/////, ?3 ?3 ^3 ^Y Outlet (Tm out°F) Pump Vacuum (in. Hg) ///////////. 9$ S (& & ^"} ff^ ------- 355 SAMPLE RECOVERY DATA PLANT DATE Run No. HI Sample Box No. A/-O Job No. _ SAMPLE LOCATION M °\ Qu^o ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: JA^D _ SOURCE/RUN #:_L_^lL DATE: 1 . Leakage Correction for Volume Metered ( -0.02)x( ft3 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) Pbar+(AH/13.6f 17.64 xVmcxYx 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V w = 0.04707 x (Wf - Wj Vw = 0.04707 x( ii. 'std Vw = 5-?^ scf wstd 4. Percent Moisture, by Volume V, R wstd bws wstd mstd M.A ------- GAS VELOCITY AND VOLUMETr.iC FLOW RATE Plant: Samoung Location: Run #• 9 - Date: $'99>^~) CIocx Time: / ,'/ ^ Barometric Pressure, in. Hq: ^,3'Q Static Pressure, in. HgO:^ Moisture. %: Molecular wr.. Dry: Pitot Tube. Cp: Stack Dimension, m. Diameter or Side 1 • /5"' Side 2~ • — Wet Bulb. °F: .1 '/•teeny n M, 3 l'/ -«-' XT. •mo. ' a _ If. f. 4- ILL AC; Md • 10 44 K %CO.) ^ '0.32 X %CX) - (0.28 X %»,> Md»i044« : •• <0.32 x > . (0.28 X • Md i n . M,O % H,O lOO 100 i x ( i 10O ' 100 M. SP. 13.8 1 3.8 [ /• - A3.4U K Co X «AP x \ PllM V« - 09.40 I\| - 32.. < ) a ( ot. Pi %H.O Q8.M-otair.e4TK — «o- ^ •" T» tOO °--- X 17.647 X< r\|l« (M. « '^tti ^n^Kw 108 ------- f VA METHOD 1 8 FIELD DATA SHEET Plant;. Date: c - .3 /O Location: Run #: / 0 - y - / StackI.D.: If" Pbar: o«/7 <• Sample TubAe Operators:. Leak Check: Pre:_ Post: Time Trovcre* Point NumtMr -1 ± Gauge Vacuum (Hg) 0 c o o V«lodty HMd In. \ IS 9 Row Setting ,95'0 Stuk T«mp. °F Q/ V •3 ? ^t>> 9m Tested Anaiyte:. Orifice Pump/Rotometer #: • Pt: Pretest Post-Test (mm Hg)L Tt: Pretest Time: Start: Q?kvnnish:'(Qf»fe Total: S~& Md • (0.44 x %CO2) + (0.32 x XCty + (0.28 x %r^) Md - (0.44 x ) + (0.32 X ) + (0.28 X %H_0 ia(^-> llb-18'-^1 °R(°F460\| -Pb+-±l_- 13-e • ^a ^j^ In. Hg - D-H53 Vl - 85.48 X Cp X JE? X Y Vs - 65.48 X ( Vt- -SM.IM.3) W« Pax Ma )x( )x ^ xM OB.. - Qt x 17.047 x -^- x (1 - •« T« 100 Hlft .//./» ------- FIELD DA IA SHEET Plant: LA$CO Sampling Location >Q Run Number: JO-?- I Date: Pretest Leak Rate: ,OO 1 cfm Sample Type: ;) - 4- Operator: Pbar 3j 3^ Ps: -o.ftz CO2: •* O2: Pretest Leak Check: Pitot: )£ in. Hg. Orsat: ^1 Probe Length/Type: t' Stack Diameter. jlS'" Pitot #: As: Nozzle ID: ^ Assumed Bws: _ Meter Box #: \| ^ Y: ^ Post-Test Leak Rate: Post-Test Leak Check: Phot: Thermocouple #: Filter AH@: @ '7 in. Hg. Orsat: — Traverse Point Number Sampling TbiM (mln) 0 10 ao ?>0 40 la OocfcTfcns (244iour dock) ?T54- GSkrf)tf OtlM O^^ O^^ ®8T^ Gu Meter Reading (Vm)«3 rn.^sf ^.•3s /^ 5" 33 .- ^o ^^/ / 10 — ^V73'0 Vtkxaty Head (Ap) lnH2O Oriica Pressure Dtftorential (AH) in H20 Desired s //////'///////// • }.Jt> l'$b l/?b I/ ^6 j Actual Stack Temp. (Ts) Temperature °F Probe \| Filter Impinger Temp. °F ////////////////////////////// KO 51 5^ 56 Dry Gas Meter Temp. Inlet (Tm in°F) '/////, -75 oa -7r 70 .-.' '•.•.;:•'-' ' Outlet (Tm out°F) / f / / / / ~> ~> ? ------- SAMPLE RECOVERY DATA PLANT DATE Run No. 0- ?-) Sample Box No. V-/ Job No. OO3 SAMPLE LOCATION ' # IP oTi«rT Filter No. TRAIN PREPARER ___ SAMPLE RECOVERY PERSON COMMENTS MM" P\h?iUtE. FRONT HALF Acetone Container No. Filter Container No. Description of Filter Liquid Level Marked Sealed Sealed Samples Stored and Locked RACK HALF/MOISTURE Container No. Liquid Level Marked Sealed IMP. NO. 1 2 3 4 5 6 CONTENTS 03T H,C) nr J-LO •^-ip/\j / 3:/;* r~l TOTAL INFTIAL VOL (ml) ^oo ,06 • . "Z4O WEIGHT (grams) INITIAL t,3?<7 1^,1 •756,4 H^C.5 FINAL C^/.o ^•^t y t^.7 9GI.5 "i^ofz. NET • ;.; - p.f . L. r. / f6 ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: /. &._n _ SOURCE/RUN #' io -&\ DATE: 1 . Leakage Correction for Volume Metered Vmc=( )-( -0.02) x( ft3 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) = 17.64 11 iu \ ^ m )x Vmstd= '^ dscf 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V... = 0.04707 x (W. - W.) wstd f ' Vw = 0.04707 x( rstd 'std 4. Percent Moisture, by Volume B VwStd °WS- w + w wstd mstd B - ( Bws—; ------- GAS VELOCITY AND VOLUMETr.iC FLOW RATE Plant: Sampling Location: j^ Run Date: __5 Clock Time: /'QgQ Barometric Pressure, in. Hq: P9 ,• f 0 Moisture. %: Ooerators:. Molecular wt.. Dry:. Static Pressure, in. HoQ: ~ StacK Dimension, in. Diameter or Side 1: Wet Bulb. °F: • Point 0- / v.iocnv Ii Stack I/O It 9/C, '313 on Pilot Tube. Co: /9^ Side 2: Md - <0.44 • %CO.l •>• (0.32 X %O,) ~ (0. Md - <0.44 x ) 40.32 X i - (0.2B X ) Ms • Md x (1 ioo .; . ie< too iH3O 100 too S.P. 13.8 P.. ,„.«, \cm V« • 0S.40 X ( ) » ( IX V.. JHJ1 /• A.. \|.227 n2 t Qs- Q« °-dd- xM , 108 X17J47X- •\tv ------- FIELD DA IA SHEET Plant: L43G.O Sample Type: AV ll Operator: /^ )/Ci6 Sampling Location GOi£/U it- Jfi Pbartt)<^v5o Ps: -« ff ?) 7 Run Number: /0.K.3 Date: S"->7-9"7 CO2: '- O2: Pretest Leak Rate: p>? cfm @ /5 in Pretest Leak Check: Pitot: - — Orsat: — 1 Traverae Numb Sampling Time (mln) O ;0 £h '^0 /r> Clock Tfcne (24-hour dock) HMO M SC )9CO jO/fj I-1A6 Hg. Probe Length/Typ< — Stack Diameter: ) 3. / '55 Pilot .^j- ... S" As:/.2i^' ^ Gas Meter Reacting j«r A ^ ^ftdw) Ti? V f f ^rTrT^ ^^/ ,6/0 §99 - &£> too?/ H"7 CK. 5c4- /i __ I /^i . b "L 5^ &> •A 1 •3 3 £ i « XT- 1-5 1 $•/ f < ff y3 ; . '§£, ( •• &h t< 9 6 j §f/^<2 < . '"IV^Vi Z/Ci rj S ai^- >/5 i l-f 7/5 7 Jv •> lr > yj' ''U ')((, J't ? -• >/ : ^ - ^T-.O" * r^O <>& ^'t, r.s >l.^l jb^i, l&SH • •." ^S^ ps i^r^ $>± fp> «C-frH db «-.-f m. -: - Outlet (Tm out°F) ^/yT/s £& 5>.p f? C if 7 •••••• Pump Vacuum (in. Hg) ^ gf'S '£ -s- . . ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: LA-g^-b _ SOURCE/RUN #: J£JL 1 . Leakage Correction for Volume Metered Vmc=( )-( -0.02) x( ^^l - ft3 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) /Pbar+(AH/13.6)N V^ 17.64 xVmcxYx^ — Vmstd=17.64x( 3,.u^ )x( /?OW )x Vm = 2 H7_ Hsrf mstd " 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V w = 0.04707 x (Wf - W.) Vw = 0.04707 x( 34.2. wstd wstd 4. Percent Moisture, by Volume V, n _ WStd Bws- ^7 wstd mstd ------- SAMPLE RECOVERY DATA PLANT DATE "7 sample Box No. Run No. I Q - Job No. SAMPLE LOCATION TRAIN PREPARER /O o^J Filter No. SAMPLE RECOVERY PERSON COMMENTS FRONT HALF Acetone Container No. Filter Container No. Description of Filter Liquid Level Marked ' " Sealed Sealed Samples Stored and Locked BACK HALF/MQrSTTTKF Container No. Liquid Level Marked Sealed IMP. NO. CONTENTS TOTAL INFTIAL VOL (ml) WEIGHT (grams) INITIAL G57.0 FINAL NET ------- ooa METHOD 1.8 FIELD DATASHEET Plant:. Date: Tested Analyte: Orifice Tank #: Location: AJ.DA- Run #:_ Stack I.D.:. Pbar: "• Sample Tube #-. Operators: rrt Pump/Rotometer #:_ Pt: Pretest (mm Hg): n Post-Test (mm Tt: Pretest fF):_ •** Post-Test fF):_ Leak Check: Pre: Post: •• Total: CO, 0? 13 » Ji .fa Time )t\ S.$* ,s /? . 11 ifzi, ->•?- l5i-s. i-x. \ ^ 2Ce. H'? /$^q,os \/^ » J. ;o Gauge Vacuum (Hg) / , , i I / Flow Setting 11 x. r / ^l -»-i ^' X Time: Start£7_£s_ Finish:. W/B: - DIB:- O~: Md = (0.44 x %C02) 1- (0.32 X %O2) T (0 Md = (0.44 x ) -»• (0.32 X i * (0.28 X Md = 7£> Ms = Md x (1 Ms •= ( Ms- Ts- H.O £_; 1 00 % HO - — 1 00 100 °R (°F.460) S.P. Trav«rs« Point Number Velocity Head in. HjO Stack Temp. 13.6 13.6 Ps - in. Hg _ VSP = 1 T /Oai 1 Ts rn) V3 - 03.»» X >-p X ^U-- t \\| P3 X MS u Vs - ft/S AS • n Qs - Vs x As x 60 s/m Q( m X X 60 Qft — acfm Ps HiO Q$ .= Qs X 1 7.647 X x (1 • ) 8td T. 1 QO ""• IS i uw Q«ttd" dsdm ------- METHOD 18 FIELD DATA SHEET Plant: t-"5<& Kr.Jv/cA Date: waa/ Run #: /s/D^-9-7. A^ Stack I.D.: 0 .5" >2" Pbar: zi.3 Sample Tube #: AiDA '-z^, /i/afl .s-2& Operators: H / r/\ Leak Check: Pre: ./ Post: iX Tested Analyte: Siyj-f^ Orifire Tank • - Pump/Rotometer #: t^st rt" Pt- Pretest (mm Hg): - Post-Test (mm Hg): Tt- Pretest <°R: Pnst-Test rF): — Time: Start: of 2* Finish:/^-' Total:_ W/B: — D/B: - O«: ^ CO^: > oo o O 100« 1 « V\| »<» ~L° 40 Time IS^ iH ------- APPENDIX A. 1.10 Condition 9 (includes flows, moistures, and Method 18) ------- METHOD 18 FIELD DATA SHEET Plant:j Date- -2z-C(_ ,J0S<- ^ 6« Gf' li 13 Time: Start:'€os Finish: '<# Total: ^ W/B: CC, D/B: ff )-t-(0.28x7? ) Md = 2-2 Mdx(1 100 x(1 • )00 % H2O 100 •) •- 18( Ms «= ( Ts- Ps - Pb +-1L. = &. zf, )+ •c~i- 13.6 13.6 100 Ps= 29. m.Hg Vs- Vs - 85.49 x ( . ^ t ) x ( )x ^ Af Qs » Vs x As x 60 s/m Q» - Ps Q»..j= Qs x 17.847 x 8td Ts x 60 %H20 100 X 17.847 x- 3k) ------- Plant: Site: WET-BULB/DRY-BULB MOISTURE CALCULATION . Location: \|Mftm t Operators: TA Run #: 13.6 Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Pbar t Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H20 at Tw (from Table) = Pvw = (Ps - Pvw) x (AT) Date: ,^-A-< Pbar= M-2-B Pg = O.tl Ps= 2Llt Tw = UC> TH= ^ AT= IS Pvw = v>. u^2_ in. Ha ''in. H,0 in. Hg °F >p. • °F in. Ha Vapor Pressure of H2O = Pva = (Pvw) - ,2800-(1.3xTw) Pva =( )- ( & ^'13 2800 -(1. 3 x Proportion of Water Vapor by Volume = Bws in. Hg 0 I • 6/0 (Ps) VAPOR PRESSURES OF WATER Tamp. °F 0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 0 0.0378 0.0631 0.1025 0.1847 0.2478 0.3826 0.5218 0.7392 1.032 1.422 1.932 2.596 3.448 4.525 5.881 7.569 9.652 1220 1529 19.01 23.47 28.75 35.00 4241 5044- 1 0.0398 0.0860 0.1080 0.1716 0.2578 0.3764 0.5407 0.7648 1.066 1.467 1.992 2.672 3.543 4.847 6.034 7.759 9.885 12.48 18.83 19.42 2348 2943 35.88 43.11 51.78 2 0.0417 0.0698 0.1127 0.1803 0.2877 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.842 4.772 8.190 7.952 10.12 12.77 15.98 19.84 24.48 2942 3847 43.92 52.70 3 0.0441 0.0728 0.1188 0.1878 0.2782 0.4052 0.5802 0.6183 1.138 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.38 13.07 16.34 2027 24.97 30.52 37.07 44.74 53.65 4 0.0463 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 6.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.57 54.82 IQIWUI y 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.660 8.557 10.86 13.67 17.07 21.14 26.00 31.75 38.50 46.41 5540 6 0.0517 0.0848 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.083 5.302 6.850 8.787 11.12 13.98 17.44 21.59 28.53 3248 3924 47.27 58.80 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.981 11.38 14.30 17.82 22.05 27.07 33.02 3949 48.14 5741 8 0.0571 0.0932 0.1502 0.2292 0.3384 0.4858 0.6903 0.9666 1.335 1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1821 22,52 27.82 33.87 40.75 4943 5843 g 0.0598 0.0982 0.1567 0.2363 0.3483 0.5035 0.7144 0.9989 1.378 1.875 2.521 3.351 4.408 5.732 7.384 9.424 11.92 14.98 1841 2249 28.18 3443 4142 4943 ------- '6 3 METHOD 18 FIELD DATA SHEET Plant:. Date: f>-2z-n Tested Analyte:. Orifice Tank #:_ Location: (Voc,/n /? Run #: ftc- 3- i Stack I.D.: Pbar: '^, ZQ z-6" .< -2.^ ••' Sample Tube Operators: Pump/Rotometer #:_ Pt: Pretest (mm Hg): Post-Test (mm Hg):_ Tt: Pretest fF):. H -- Leak Check: Pre: Post: Time -?n%,L,6 1^7, 15 77V?, 2/ 77^o. ^V Gauge Vacuum (Hg) , i / l Flow Setting '^c<_ / •€£? ^ ^_ /.«» ^ iSdrt. MlG? /(-. I/ Traverse Point Number i -L 1 H <, V / Z- 1 H S (j . ^ •> n A it 1 1 •} 1 f u Velocity Head in. HzO . ^T • &~1 •OG . O& . oC. . ^o .0-7 0-7 OC/ .O^J X5C oY .;i .9 79 T* Post-Test f°F):_ Time: Start:,*3 Finish: ^J2_Total:. W/B: g7 D/B: 1? O~: z/ CO .02:^ 2'- Md = (0.44 x %C02) f (0.32 X %O2) -r (0.28 X "/oN^ •^" Md = (0.44x O ) + (0.32X1-1 ) +• (0.28 X 7 7 Md = .&• * % H2O 100 100 % H2O 100 18 ( 100 Q_ _ QL_ ^ S.P. (^ A J I \ . ^C^ O r9 • rD -f ««<^^ •= ( c'i -v } + «••_—«« 13.6 13.6 ^Px\| Ts(°R) vs - 85.49 x ( . yy ) x ( )x I- M.bT- ft2 Qs • Vs x As x 60 s/m Qs X 60 Q« w= Q« x 17.647 x -^— x (1 Ps %H20 x(1- —-f-) •x(1- c^ : Si^, 100 dsdm ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: Site: Operators: Location: Run #: - 13.6 Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of StacK = Pbar Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of HpO at Tw (from Table) = Pvw = (Ps - Pvw) x (AT) R£.-q-\ Date: 5"-Z2 -«1 Pbar = Pg = Ps = Tw = Td = AT = Pvw = JM.2P -0 £ Jl £>-MU>fcU in. Hq in. H O in. Hg °P °F °F in. Hg Vapor Pressure of H2O = Pva = (Pvw) - 2800-(1.3xTw) )x( X.) ) Proportion of Water Vapor by Volume = Bws ( . (Ps) T«mp. °F 0 10 20 30 40 50 60 70 60 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 0 0.0378 0.0631 0.1025 0.1647 0.2478 0.3826 0.5218 0.7392 1.032 1.422 1.932 2.596 3.446 4.525 5.881 7.569 9.652 12.20 13.29 19.01 23.47 28.75 35.00 42.31 5044- 1 0.0398 0.0660 0.1080 0.1716 0.2570 0.3764 0.5407 0.7648 1.066 1.467 1.992 2.672 3.543 4.647 6.034 7.759 9.885 12.48 15.63 19.42 23.96 29.33 35.68 43.11 51.76 in. Hg ( 2<\.2-> ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1803 0.2877 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 8.190 7.952 10.12 12.77 15.96 19.84 24.46 29.92 36.37 43.02 52.70 3 0.0441 0.0728 0.1186 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.36 13.07 16.34 2027 24.97 30.52 37.07 44.74 53.65 4 0.0463 0.0768. 0.1248 0.1955 0.2091 0.4203 0.6009 0.8462 1.175 1.610 2.178 • 2.911 3.848 5.031 6.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.57 54.62 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.680 6.557 10.66 13.67 17.07 21.14 26.00 31.75 38.50 46.41 5540 e 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.850 8.767 11.12 13.98 17.44 21.59 26.53 32.38 3924 47.27 56.60 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.981 1 1 .38 14.30 17.82 22.05 27.07 33.02 39.99 48.14 57.61 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1821 22.52 27.62 33.67 40.75 48.03 5643 9 0.0598 0.0982 0.1567 0.2383 0.3493 0.5035 0.7144 0.9989 1.378 1.875 2.521 3.351 4.406 5.732 7.384 9.424 11.02 14.96 18.61 2249 28.18 3443 4142 4848 5847 ------- METHOD 18 FIELD DATA SHEET Date: $~-,93-<3p nrifjre Tank #• -OcatiorvO^ew • ^ P.-mp/Rotometer : Run#: °-V~; Pt- Pretest fmm Ha): — Stack I.D.: )S" Pnsr-TesUmm Ha): — Pbar: 39, 0 r «••? ,«9 ^/-7 .,a/^ ,l\ ,91 &' ;V* ='^rl Flow Setting 194; r-e/^ ] / Y ,/ i/. «a /^a //* o /^Q i4 &/?„-, ,,„ ^ , .,, -i-s , fK '" '" $r- J8 ^ Ts- \U>T> °F- ^2^ °H(°F.460) ^•^ . 0 _ _. S.P. . oa - . -. tofe p9-PbT5T^2^ ^^Ta- Ps- ^.MS' in.Hg ^p - DM2 n2 Qa • Vs x As x 60 t/m # 0« - g x x 60 o.-^2.n «" Ps %H-0 Qt^^-QmxiT^Tx x(l i-) •» T« 100 0.^- X17.847X «(1--lo7^ QHW--\®^ d-to ------- FIELD DA IA SHEET Plant IfclXlO Sampling Location _ Run Number: ?~9 Sample Type: Date: 9 3 • Pretest Leak Rate: iQo [_ cfm @ /< in. Hg. Pretest Leak Check: Pitot: —Orsat: —' Nozzle ID: Thermocouple #: ~\ f} Assumed Bws: — • Filter #: Probe Length/Type: Stack Diameter: Pitot #: 5T- 3 As: /• 23 A Meter Box #: /^ Y: Post-Test Leak Rate: .ex.to cfm @ j_^"i Post-Test Leak Check: Pitot: — -6rsat: Hg. TravwM Point Number . ; ; Sampling TbiM (mln) ^ /G 56 ft> frfc OockTkm (24-hour dock) It&f /f/V /^^ ^3^ /<•#' Gas Metar Reatfing (Vm)ft3 £/5''£? f-7 ?f W Pf £ 9< Pump Vacuum (in. Hg) 7/7, ^ 3 S _3_ AH Tm ------- a DC PlantL Date: <0 r- a a- SAMPLE RECOVERY DATA Run No.: ^"k Job No.: Sample Box No. : Sample Location:. ov7t«r Sample Type; m - Filter No.: Sample Recovery Person: Comments: FRONT HALF Acetone Container No. L Liquid Level Marked:. Filter Container No.:_ Sealed: Sealed: Description of Filter: Samples Stored and Locked: BACK HALF/MOISTURE Container No.:. Liquid Level Marked: Sealed: 9-1- IMP. NO. 1 2 3 4 5 6 CONTENTS WLO Hv0 ^PTt S/L TOTAL INITIAL VOL (ml) loo ID* — $„ WEIGHT farams) INITIAL v i / 7 V «J l\| \M^ ^i ^^ 7^;.i n A.14 S? /T ()• v FINAL 6I/,? G>.5 1-J-C.o 7^-0 ^W.f NET i ^ x^ •— >-\ «> Description of Impinqer Catch- -— - ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: LfVaCD _ SOURCE/RUN #:_3l3lL DATE: S'ZZ'T7 1 . Leakage Correction for Volume Metered vmc = V (Lp - 0.02) x 0 Vmc=( )-( -0.02) x( 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) 'Pbar-MAH/13.6)N rnstd Vmstd 'm = 17.64 x (31. oo-v )X(o/loV, )X 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V w = 0.04707 x (W. - W. ) . wstd ' ' Vw = 0.04707 X ( 2B. std - Vw = MF- sef wstd 4. Percent Moisture, by Volume wstd w w wstd mstd B ------- P'ant: Samonna Location: J ' Run x-fQ-^' J GAS VELOCITY AND VOLUMETr.iC FLOW RATE Date: m g-29-9i CIocK Time: Barometric Pressure, in. Hg:_o Moisture. %: -^ Molecular wi.. Cry: StacK Dimension, in. Diameter or Side r Wet Bulb. °F:^ Static Pressure, in. l-^O: x' ««MI W. III. 1 O ^^« _^^^^^^_ Pilot Tube. CQ: ,?9 Side 2: Md • 10.44 • %CO,J » iO.32 X %CW » (0.28 X %M,> Md • IO.44 • ! «• (0.32 X < « (0.28 X . M,O S H,O 100 100 100 Ml • Md 111 • 100 P« - Pb »-!£_-.< I* 13.0 13.0 »• - -n. H. •/• . «s.«o K Co « Ma ^ Q« 0%^- «• «17.84T X «^— « O °«-d- xoo %H.O Ti tOO Kt7J«y« Ki- ^ ------- ODCZJ METHOD 18 FIELD DATA SHEE1 0 - fe =lant: ^HSCtf Tested Analyte: S' -1 v ->--< Date: s-zz-tft Orifice Tank #: 7- _ocation: WA Pump/Rotometer #: ^^-^/ ? =lun#: NDfl-1-l Pt: Pretest ; -rim Hg): - Stack I.D.: ^-6^^ £2V 12.0" Post-Test (mm Hg): ' 3bar: 2-1 -3D Tt: Pretest <°R: Sample Tube # Operators: fA/ • /vOfl-l-i Post-Test (°F): ^ , Time: Start: «B02L Finish: ife^Z Total: 3O _eak Check: Pre: ^ Post: ^ W/B: — D/B: - O0:^> CO0: <=> Time , 5f •$>, Gauge Vacuum (Hg) / / i i Row Setting ./ it il 2-! Traversa Point Number Velocity in. H2O Stack Temp. °F Md = (0.44 x %CO2) 1- (0.32 X %O2) -r (0.28 x "/oNj) J^~y Md - (0 44 x ) -t- (0 32 x } • (0 28 x ) ------- APPENDIX A. 1.11 Condition 10 (includes flows, moistures, and Method 18) ------- METHOD 18 FIELD DATA SHEET Plant: LfeCO TestPri Analvte: 5A/^,~a C L F S F c C L ?fc/o ul/5- \L l;o V l.j )ate: 5-iz--^'' Qrificp Tank #• — ocation: /vui~ c-au^f Pump/Rotometer #: U9«,f- • -i- un #• /riif- /o-< Pf Prefpst (mm Hg): tackl.D.: I-" Post-Tpst (mm Hg): - 'bar: IA.I Tt: Pretest (°R: — >amp!e Tube Dperators: #:AI.->. ••-»-/ •» Post-Test (=F): - fKl- Time: Start: /?£ Finish: '?r/ Total: •• r eak Check: Pre:_4^_ Post:_tx^__ W/B: 6^ D/B:^2- O0:_2j_CO0:_j2_ Gauge Time Vacuum (Hg) 2->2/,S7 / ^^2. b' / z'b-ig.1?!- . / 11,13,^-5 / -h >03 Traversa Point Number ; 2 5 4 5 u 1 fi 1 1- 3 <.<. l$o<^ . 50 'V_ ,>«. M(y\- Stack Temp. °F 77 S^ ft g-z. ?^ S^- fft ^t- ^2- ^2. #2- 9-2- ^2. ?2- ^2. ?~2~ ft1,«p ,,/ c^m »ift ^ fc Md = (0.44 x %C02) (0.32 X %O2) -r (0.28 x "/oNj) — KJ — in AA V ,-• ^ J. (f) "V3 t 2.1 1 4- (O ?S K ~7^ 1 Md = -^ ^ ^ ~\ ' Ms = Md x ( 1 • — ) - 1 8 ( i 1 00 1 00 "»* M.«. )X(1 ''4 ).18( ''M-) 1 00 1 00 70 Ms » ^^- ^^ Ts- °F- °R (°F 460) c p Q_ — OL- . J-r- i \ . 13.6 13.8 PS = "23 2?> '"• ^ J&P ~ 0 ^jU~ya VS - 03.<»» X UP X «jr X ^ ps x Ms Vs - 85.49 x ( ) X ( ) X A I A. , . 1 2 1 L 1 " Qs - Vs x As x 60 s/m Q«« x X60 Qs • yo 7 » acfrn Ps ^ V2 Q* . .= Qs x 1 7.847 x — - x (1 • ) Std T_ 1fM .. aid 100 ^•>0l(J y^K^^v 8iIIII ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: L/\S<_c? Site: ^A/H&) GxkAtt^ Operators: Barometric Pressure, in. Hg = Static Pressure, in. H20 - Absolute Pressure of Stack - Pbar + - Wet-Bulb Temperature, °F - Dry-Bulb Temperature, °F = Temperature Difference, Td • Tw - Saturation Vapor Pressure of H2O at Tw V/annr Procci iro r\i W C"\ — Dwa — /D\AA/\ Pva-/ h i,tc4 \ , .^"2J, "ruc"q Location: MAH-* ddi-^Au-^T" TA Run #: rue-to-^ Date: 5-2 Pbar= >??.^ft Pa = +o.t3 -SSL, Ps= Z«.fc . Tw = 04 Td= &2. AT= \3 (frnmTflhlP)= PVW = D-UOo^ (Ps - Pvw) x (AT) 2800 - (1 .3 x Tw) in. Hg in. H20 in. Hg °F °F °F in. Hg in. Hg 2800-(1.3 x Proportion of Water Vapor by Volume = Bws _ (Pva) (Ps) Tamp. op 0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 180 170 160 190 200 210 220 230 240 0 0.0370 0.0631 0.1025 0.1647 0.2478 0.3026 0.5218 0.7392 1.032 1.422 1.932 2.596 3.440 4.529 5.881 7.569 9.652 1220 1529 19.01 23.47 28.75 35.00 42.31 50.84- 1 0.0398 0.0660 0.1080 0.1716 0.2576 0.3764 0.5407 0.7648 1.066 1.467 1.992 2.672 3.543 4.647 6.094 7.759 9.865 12.48 15.63 19.42 23.96 29.33 3S.68 43.11 51.78 ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 15.98 19.84 24.46 29.92 36.37 43.92 52.70 3 0.0441 0.0728 0.1186 0.1878 0.2782 0.4052 0.5802 0.8183 1.136 1.561 2.114 2.629 3.744 4.900 6.350 8.150 10.36 13.07 16.34 2027 24.97 30.82 37.07 44.74 53.88 4 0.0463 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 6.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.87 54.62 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.660 8.557 10.66 13.67 17.07 21.14 26.00 31.75 36.50 46.41 5540 6 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4,063 5.302 6.850 8.767 11.12 13.98 17.44 21.59 20.53 3248 3924 4727 56.80 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 6.981 11.38 14.30 17.82 22.05 27.07 3942 39.99 48.14 5741 a 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1821 2242 27.82 3347 40.75 4949 5849 9 0.0598 0.0982 0.1567 0.2383 0.3403 0.5035 0.7144 0.9989 1.378 1.875 2.521 3.351 4.408 5.732 7.384 9.424 11.92 14.96 1841 2249 28.18 9449 4142 4049 5047 ------- METHOD 18 FIELD DATA SHEET Plant:. Date:_ Tested Analyte:_ Orifice Tank #:_ Location:. Run #: fte'-fo-i Stack I.P.: 2g" / Pbar: 2.< Sample Tube #• e -/* $>=.-'<>-> Operators: rA- Pump/Rotometer #: Pt: Pretest (mm Hg): Post-Test (mm Hg): Tt: Pretest Total: Leak Check: Pre: Post: Time 77SO.?(, 1752. 3Z. ->1^^ -7 -) 55 ^ 3, Gauge Vacuum (Hg) 1 , f 1 Flow Setting /soco /So« /5rc. .^.-^ ArVJU" Md = (0.44 Md = 1i ~[l Ms = Md x •) _ i Ms - / Ts- Post-Test (°F): Time: Start:_i£ W/B: sV p/B: Md = (0.44 x %C02) -t- (0.32 X %O2) -r (0.28 x "/oNj) Md = (0.44 x o ) + (0.32 X 1 6 <, 1 i !> H 1 i. i z. 3 ^ 5 t> Velocity Head in. H^ , 3G -0(j> ,o5 . o^- .OCa •0~T . °e ,01 d?5 .o5 .05 • 01 . // •07 .0-5 ,04 .00 o<7 ,/o .05 ;t?5 .05 lOT , /o Stack Temp. °F '10 -((a 10 ni. -76 -It. -J6, ~>6 ~l(/ If -)<* 10 -,U !(!> 10 Ifr -I* -7£/ -\|U l^ 11 1(J -16 To Ps - Pb +. 13.' 13.6 Vs « 85.49 x Cp X Vs - 85.49 x ( Vs- \|>- ll/ AS - M. vrv n Qs • Vs x As x 60 s/m Ts(°R) PsxMs ) X ( 4 ft/s 2 x60 acfm Qs . .= Qs X 17.847 X Ps H,0 x(1- —2- 100 X 17.647 x- dscfm 100 ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: LAf>cr? _ Location: fc.^ g; Site: Operators: —^ Run #: £e-.o-s Date: .5- Barometric Pressure, in. Hg = Static Pressure, in. HgO = Absolute Pressure of Stack = Pbar i —r=~s I J.O Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw (from Table) = Pvw = (Ps - Pvw) x (AT) Pbar= 23.23 Pg = -0. ^^ PS = ^<^.23 TW = 54 Td= >c» AT= zz Pvw = oH"i^ in. Ha in. HLO in. Hq °F °F °F in. Ha Vapor Pressure of H2O = Pva = ''il, Pva = ( 2800-(1.3xTw) 0. 2800-(1.3 x Proportion of Water Vapor by Volume = Bws Bws = Tamp. °F 0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 (Ps) 0 0.0376 0.0031 0.1025 0.1047 0.2478 0.3020 0.5218 0.7392 1.032 1.422 1.932 2.596 3.446 4.525 5.881 7.569 9.652 1220 1529 19.01 23.47 28.75 35.00 4241 5044- 1 0.0398 0.0600 0.1080 0.1710 0.2570 0.3764 0.5407 0.7648 1.066 1.467 1.992 2.672 3.543 4.647 6.034 7.759 9.885 12.48 18.63 19.42 2346 2943 35.68 43.11 51.76 in. Hg ( 2li ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0096 0.1127 0.1803 0.2077 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 15.96 19.84 24.46 2942 36.37 43,82 52.70 3 0.0441 0.0728 0.1186 0.1878 0.2782 0.4052 0.5802 0.8183 1.136 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.36 13.07 16.34 20.27 24.97 30.82 37.07 44.74 5345 4 0.0403 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.176 2.911 3.848 5.031 0.513 8.391 10.61 13.37 16.70 20.70 25.48 31.13 37.78 48.87 54.62 5 0.0469 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.660 6.557 10.66 13.67 17.07 21.14 26.00 31.75 38.50 46.41 5540 6 0.0517 0.0646 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.850 8.787 11.12 13.98 17.44 . 21.59 28.53 32.38 3924 47.27 56.60 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 6.981 11.38 14.30 17.82 22.05 27.07 33.02 39.99 46.14 57.61 8 0.0571 0.0932 0.1502 0.2292 0.3304 0.4858 0.6903 0.9666 1.335 1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1821 2242 27.82 3347 40.75 4949 5843 9 0.0598 0.0962 0.1567 0.2383 0.3493 0.5035 0.7144 0.9969 1.378 1.875 2.521 3.381 4.408 5.732 7.384 9.424 11.92 14.96 1841 2249 28.18 3443 4142 4843 5847 ------- Plant: Samoima Location: Run: < -JO ^ GAS VELOCITY AND VOLUMETRIC FLOW RATE Date: 5^-9? CIocx Time: /dA Ooerators:. Barometric Pressure, in. Hq: 5>?.fTo Static Pressure, in. HpQ: ~, Moisture. %: Molecular wt.. Grv; —" Pilot Tube. Cp:^; Stack Dimension, in. Diameter or Side 1 • IS'/f Side 2: Wet Bulb. °F: 3otm. A- ( 6 ,30 O/'i o_ UL 1(0$ Md - (0.44 i %CO.) » i0.32 X %CUi * (0.28 X %N) Md • to.44 • ! - (0.32 x : . ------- METHOD 18 FIELD DATA SHEET Plant: C74SHG Date: ^-oia-q-/ Location: &V & ^ <• 1 n Run#: /0-/t?-/ Stack I.D.: ;esv^A Leak Check: Pre: , got' Post: Gauge Time Vacuum (Hg) 3onn rj £b Je> 0 sfcac 0 Stoic* f) 2c 3. OS aia :3 ^W ^ k?^ - Oj^330 Time: Start:0 Qi^-QiX 17.847 X x(1- 2_) •» T« 100 tf- °NW- f-70^ ------- FIELDDAlAWlEET Plant Cx/jS^O Sample Type: fl\-^ Qpeia[oi:(^/d& Sampling Location Ct)C^ f> /C Pbar £^.^>O Ps: — , 3) Run Number: ft -16- Date: 5'92-9d CO2: O2: Pretest Leak Rate: ,£#£ cfm@/<" in Pretest Leak Check: Pilot: -~ Orsat: — TMMMM Point Numb Sampling Time (mln) On 9C 3& iO dock Tim (24-hour dock) 8000 Hg. Probe Length/Typ Stack Diameter: K I 'S^ Pta*:Sf'3 }^'' As: 1 23- rji Gaa Meter Reading^ £?V4 • £3& k?&>£ . ^6 6> 70,' .^o (j,^ ^ . 35(i Velocity Head (Ap) inH2O Oriice PrMOura Diflwential (AH) in H2O Desired Actual Stack Temp. (Ts) Nozzle ID: " Thermocouple #: Y /3 Assumed Bws: - — • Filter #: " Meter Box #: /fr Y: . 9<^ Post-Test Leak Rate: 6(it> Post-Test Leak Check: Phot: Temperature °F Probe Filter Impinger Temp. °F 6 AH@: 1-S-&3 cfm @ g" in. Hg. - — Orsat: — — Dry Gas Meter Temp. Inlet (Tm in°F) Outlet (Tm out°F) '////////////////////////////////////////////////////////s 1 F6. /,$>£, /<-"¥£, \ t S& ^0 3"? 5"-^ 5"r^> .$"4^ £6 ^^ ^ "^ &"3 S^^> ^'3 PV ------- OD a Planti Date: SAMPLE RECOVERY DATA . Run No.: Sample Box No.: ^^ Job No.: Sample I oration- Sample Typfl- Rlter No. Sample Recovery Person: Comments: l"n- FRONT HALF Acetone Container No.: Liquid Level Marked:. Filter Container NO.L Sealed: Sealed: Description of Rlter: Samples Stored and Locked: BACK HALF/MOISTURE Container No.: Liquid Level Marked: Sealed: IMP. NO. 1 2 3 4 5 6 CONTENTS flto W^o CrtiPry 5/6 TOTAL INITIAL VOL (ml) (Oo > oo ~~ Mu WEIGHT (arams) INITIAL 6;, / C/&-9 4"oG. I )/t.3 35 (bQ.<^ FINAL W?.5l 6^G,& •ToC^ 7-^-7 r^on NET /, I - .5 - ,/ fy^ ll,3 Description of Impinqer Catch- . — " ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: L/V5£p _ SOURCE/RUN #: J2l/i±. DATE: 1 . Leakage Correction for Volume Metered vmc=vm-(Lp-La)xe vmc=( )-( -0.02) x( 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) 'Pbar-MAH/13.6)N = 17.64 xVxYx me- v T 'm vrrw = 17-64 (et"«H ) x ( .%<• ) x dscf 3, Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V ... = 0.04707 x (W. - W. ) ' ' Vw wstd 4. Percent Moisture, by Volume R - VWSW DW/C — - Vw 4- Vm wstd mstd B ( ) °ws—/ • .- D.OOL 31 ------- aaci METHOD 18 FIELD DATA SHEET !<»?") I 1 /- Plant: t-^-»cy Date: /i-/-/7 Location: ^0,9-4 Run: VPA -•/«-/ Stack I.D.: 3&"MM>" Pbar: 29-. is Sample Tube #• Operators: S^/TA Leak Check: Pre: \/ Post: ^ Tested Analyte: ?H'- Md = (0.44 x %CO2) * (0.32 x %O2) T (0.28 x Md = (0.44 x ) •• (0.32 x ) + (0.28 x ?'» HO HO , fn 2o ^0 . r - ^ gO TrfT ^ ' /r^5, 7~ i^1^^, 3C Traverse Point Number 7 / t Velocity Head in. H;>O 1J C M(A* Stack Temp. °F ' ' ~ 100 100 Ms » ( )x(1- )^18( ) 100 100 Ms - Ts- °F- 0R(°F.460) ^ P O. _ OU j. -J-r. ^ » _ 13.6 13.6 Ps = in. Hg jfip = V Vs - 85.49 x ( ) x ( ) x \l Vs * ft/8 A.. ft2 Qs - Vs x As x 60 s/m Q« • x x 60 Qs - acfrn Ps %H,0 Q, -0.x 17.647 X x(1. ) , Qsgfcj* dscfrn ------- APPENDIX A. 1.12 Condition 11 (includes flows, moistures, and Method 18) ------- r I o? /tf 0f- / METHOD 18 FIELD DATA SHEET Tested Analyte: Orifice Tank #: Pump/Rotometer ?/y/"<- Stack I.P.: H. S Pbar: 2j Sample Tube #:. Operators: -rA Leak Check: Pre: Post- Pt: Pretest (mm Hg): — Post-Test (mm Hg): ZL. Tt: Pretest fF):_ 0 S /* Time 232?. 5=7 iS2v. }- n-zv. 7-z- •2-375-. V3 Gauge Vacuum (Hg) / / I , Flow Setting /'<• /«rd /f«- /&><- 7 sc, SI Post-Test (°R: Time: Start: ov* Finish: <? Total: /« W/B: Ji£^ D/B: J?J_O2:_2_L_ CO2:_d_ Md = (0.44 x %C02) i- (0.32 x %O2) * (0.28 x "/oN^ Md = (0.44x O )+(0.32 X?' ) •(• (0.28x7* ) Md = ~Z ••', H,O % HO Ms = Md x 1 1 - - i— ', - 1 8 ( - '.00 ' '00 Traverse Point Number I 1 3 ^ 4 V 7 / i i 3 V ^ c, 1 f Velocity Head in. H^ . 25 31 3-1 . 23 .£ ?/ • Vd W .71 .»o .21 .31 .31 JZ .VL ,3O ID. 57f)f Stack Tamp. °F 77 77 77 77 .,-7 "77 •7 7 7-7 77 •77 77 77 77 Tt 77 77 77 Ms- Ms- TS- Ps - Pb + Jl -. 13.6 100 - 18 100 ) + — 13.6 Ps«» •e.4/'' in. Hg s^. O- Ts(°n) Vs-85.49 xCpxv'AP x \l pgxMs Vs - 65.49 x ( Vs- As- ft/8 Qs - Vs x As x 60 s/m Qs - x /• 6 "7 x 60 Qs- aefm Ps Qs . .= Qsx 17.647x —— x(1 «W TS 100 Qs x 17.847 x- •""•-sr* JW ------- WET-BULB/DRY-BULB MOISTURE CALCUU\TION Plant: LAs><^> VLvJ? ^t^JLjrr Location: f%^~c^ fc^- Site: A^ £xL~- Operators: -^/^ Run #: Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar + PV l o.b Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H20 at Tw (from Table) = (Ps - Pvw) v. < Vapor Pressure of K-.O - Pva - (P\w\ fa -II- I Date: ^ Phar= 14. ft Pg = '+ ><> - ' Ps= 14,«ft Tw= ^"2- Td= 77 AT= /£ Pvw = 0' Zkol :AT) fiV/V7 in. Hq in. HP 2 in. Hg °F °F °F in. Hq 2800-(1.3xTw) O. 2800-(1.3 x ^ Proportion of Water Vapor by Volume = Bws (Pva) _ ( 0, ------- 3 a Plant: Site: WET-BULB/DRY-BULB MOISTURE CALCULATION /./fe&? fi~J? .^uJL/r-Locati - Operators: -f^-fa Run 4 Date: ~ 13.6 Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Pbar + Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H^O at Tw (from Table) = Pbar = % ye Pg= r6.03 PS = 27. VB Tw= &(e Td= 7? in. Ha in. HnO 2 in. Hg °F °F AT= /3 °F Pvw = £>,£, V2_ in. Ha Vapor Pressure of H2O = Pva = Pva =i (Ps - Pvw) x (AT) 2800 - (1.3 x Tw) x( (3 ) 2800 -(1. 3 x in. Hg Proportion of Water Vapor by Volume = Bws «,...._ (Pva) _ ( C (Ps) Tamp. °F 0 to 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 180 100 200 210 220 230 240 0 0.0376 0.0631 0.1025 0.1647 0.2478 0.3626 0.5218 0.7392 1.032 1.422 1.032 2.506 3.448 4.525 5.881 7.560 9.652 1220 15.20 10.01 23.47 28.75 35.00 4241 5044- 1 0.0398 0.0660 0.1080 0.1716 0.2576 0.3764 0.5407 0.7648 1.068 1.467 1.092 2.872 3.543 4.647 6.034 7.759 9.885 12.48 15.63 19.42 2346 2943 35.88 43.11 51.78 &> 0 (1 in * ( isw* ) VAPOR PRESSURES OF WATER * V 37+1 ,_ ^ In Inches of Mercury IT) ( i{ ^' 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 15.98 19.84 24.46 2942 3647 49.92 52.70 3 0.0441 0.0728 0.1186 0.1878 0.2782 0.4052 0.5802 0.8183 1.136 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.38 13.07 16.34 2027 24.97 30.52 37.07 44.74 53.65 4 0.0463 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 6.513 8.331 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.87 54.62 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.680 8.557 10.86 13.67 17.07 21.14 26.00 31.75 38.50 46.41 5540 6 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.850 8.767 11.12 13.98 17.44 21.59 28.53 3248 39.24 4727 58.60 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.370 3.160 4.174 5.442 7.024 8.081 11.38 14.30 17.82 22.05 27.07 33.02 30.99 48.14 5741 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1821 22.52 27.62 3347 40.75 4943 5843 9 0.0598 0.0982 0.1567 0.2383 0.3493 0.5035 0.7144 0.9989 1.378 1.875 2.521 3.351 4.408 5.732 7.384 0.424 11.92 14.98 1841 2249 28.18 3449 4142 4943 5947 ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Date: Sampling Loc Run#: t<\&- :ation: AU,;, Fv/^W Clock Time: /t<»5- - I/-"* Onnrators: T^/55 Barometric Pressure, in. H Moisture, %: ^ U Stack Dimenj Wet Bulb, °F Travaree Point , Number (• .?_. ••-.. ; "b V ' 5 c, 7 ^ f i 3 ion, in. Diameter or Side £5* DrvE Velocity Head in. H2O •IS .11 .-3/ /,! 35 ,31 ."M / Stack Temp. °F f; ft ti V fl $1 ?r r/ ?i 21 tl / 10 n d tl 1: /7-<5 Side 2: ulb.op f/ Md_(0.44x O)+(0.32X11 )-t-(0.28x "Jf ) Md - Z* ^'/ %HO %HO Me-Mdxd ,00 ' ' 100 ' Ma - /^V ^ Pa • pb -t- = ( ^' ^ ) •»• 13.8 ' 13-8 Pa . 2 f. 2 f in. Hg fip = D ,^>6^^ — \| T3f1R) Va - 85.49 x Cp x ^P x W Rs x Ma — f Vs- 85.49 X( . f f )x( ) X A! ° Aa- /,(,-? n2 da • Ve x Aa x 60 a/m Q.. X l.(,-\ X80 Qt-^RV2) acfm "° X17.B47X- ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: / ASCh s'te: 1Aflf** i^h^,/- Operators: Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar + - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw Vapor Pressure of HoO = Pva = (Pvwi - Location: MAIM £"* MAIA^-I- T//s& Run # Pg 13.6 (from Table) = (Ps - Pvw) x : ME -f .05 .»<• .«1 00 e-T .«6 .t>S OU .«1 .// .4* • s OS ,o .11 .tA .01, QS .s .Off .11 6,1f«( Stack Tamp. °F 7Z 7r 7T 7t •»• Tt 7t 7t T7 •?•»• 7« tt. 72 7? •7t 7t 71 7* 7* Tt It 7t 11 -n 71 Ms = Ms - Ts- P9 - Pb t- -^. = 13.6 1 00 1 00 13.6 Ps in.Hg = Vs - 85.49 x Cp x VAp (°R)" PsxMs Vs - 85.49 x ( ) x ( \ ) x Qs - Vs x As x 60 s/m Q.- Q« - X60 l\<% $0 Ps Qs x 17.847 x - x (1 Ta 100 Q»atd- '^"l / efscftn 100 IB' ------- go F Plant: \| Site: E-atAvx WET-BULB/DRY-BULB MOISTURE CALCULATION Location: r< Run #: Operators: Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar i Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw (from Table) = Pvw = (Ps - Pvw) x (AT) fce-u-i Date: £/??/?-? Pbar = ^T.^ Pg = — n 6-Z Ps= ^7 13 Tw = ^ TH= ^ in. Ha in. HO 2 in. Hg °F °F AT= '<~7 °F PVW = <• 4 3 S ~ > in. Hg Vapor Pressure of H20 = Pva = (Pvw) - (->,., . UK Pva=( .^5=, ) A 2800 - (1 .3 x Tw) ) x ( '. 7 ) 2800 - (1.3 x $^- Proportion of Water Vapor by Volume = Bws (Pva) _ ( ^5? ) ) Tamp. °F o 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 160 190 200 210 220 230 240 (Ps) 0 0.0376 0.0631 0.1025 0.1647 0.2478 0.3626 0.5218 0.7392 1.032 1.422 1.932 2.596 3.448 4.525 5.881 7.569 9.652 1220 1529 19.01 23.47 28.75 35.00 4241 5044- 1 0.0398 0.0660 0.1080 0.1716 0.2576 0.3764 0.5407 0.7648 1.066 1.467 1.992 2.672 3.543 4.647 6.034 7.759 9.885 12.48 15.63 19.42 23.98 2943 35.68 43.11 51.76 in. Hg ( ?i.M ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 15.98 19.84 24.48 2042 36.37 43.02 52.70 3 0.0441 0.0728 0.1186 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.629 3.744 4.900 6.350 8.150 10.38 13.07 16.34 2027 24.97 30.52 37.07 44.74 53.65 4 0.0463 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.6462 1.175 1.610 2.178 2.911 3.848 5.031 6.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.57 54.62 5 0.0489 0.0810 0.1302 0.2035 Ji.3004^ (1X4359^) 08222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.660 8.557 10.86 13.67 17.07 21.14 26.00 31.75 38.50 4641 55.60 6 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.850 8.767 11.12 13.98 17.44 21.59 26.53 3248 3924 4727 56.80 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.981 11.38 14.30 17.82 22.05 27.07 3342 3940 48.14 5741 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 •1.819 2.449 3259 4.289 5.565 7.202 9.200 11.65 14.62 1821 2242 27.62 33.67 40.75 4943 5843 9 0.0598 0.0982 0.1567 0.2383 0.3493 0.5035 0.7144 0.9989 1.378 1.875 2.521 3.351 4.406 5.732 7.384 9.424 11.92 14.96 1641 2249 28.18 3443 4142 4049 5047 ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: L(\y$ Date: 5-7l-'fl Sampling Loc Run#: $6 ation: ^.-v £,h^y.Z Clock Time: f&v4 -»/-?_ Dnfirators: 7^/5 Barometric Pressure, in. H Moisture, %: 6. 1 % Stack Dimens Wet Bulb, °F TravarM Point Numbar ,' T V H 5 i. 1 ^ --, ^ 5 c. i - * H j o 1 Z. 3 H 5 0. q: z?. ^ Static Pressure, in. HoO: -. Cl Molpnilarwt Hrv ^Wl Pitot Tube, Cp: ,- ? >ion, in. Diameter or Side 5iC. Dry E Vatocrty in. H2O .Ots .01 .•< oL, .61 .«7 ,6 ^JO O^T' ,0« tf-T .ott • ^F ^T .05 .0* .6t .61+ .«$ -06 .6£ -01 1 A fi ^ O £llf •/w^ •* y i,^ \ t Stack T«mp. °F 7L 7V 7V 11 •»v 7V 7V 7V iy ^' -"/ 7V 1^/ 7V 7V 7^ 7V 7V 7V ^Y 7f 7V 7V 7«\| fi. "?4 1: 28 Side 2: ^' nlh.OF- 7V Md - (0.44 x %CO2) + (0.32 X %O2) -t- (0.28 X %N^) Md - (0.44 x ° ) •• (0.32 X c^ i ) (0.28 X~) '5 ) Md- P'sVf'r %H20 %H20 100 100 Nfc-O-?.'^ )xd- 10Q > 18( 10o ' 13.8 '^l-HJ' 13.8 Pa. Z^V4/ in-H8 VSp- 39,( — 1 Ts (^R) vt-as^BxCox^Hx )\| P9XM8 \| Vs - 85.49 x ( ' ^1 ) x ( . 35 (Q., ) X V V.- llo-S}- ft/i A- V.6~i n2 Qs » Vt x Aa x 60 a/m Q\|v X ' ,(j\ XOO Ot- HW- achn p, %H-0 Qs . .= Q« x 17.847 x x (1 • — •- ) •td Tt 100 ^rtd" XI7.847X K(l- 1QO ) //ft ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: U.?/?-> 2 "7 ^r in. Ha — .61 in. HO 22 ^ in. Hg £b °F /V °F /8 °F 0. WD in. Hq 2800-(1.3xTw) Pva =i ' ' ' 2800-(1.3 x Proportion of Water Vapor by Volume = Bws = _J?ya) (Ps) T«mp. °F 0 10 20 30 40 50 60 70 60 90 100 110 120 130 140 150 180 170 180 100 -200 210 220 230 240 0 0.0370 0.0031 0.1025 0.1047 0.2478 0.3020 0.5218 0.7392 1.032 1.422 1.032 2.508 3.446 4.525 5.881 7.588 0.852 12.20 1550 10.01 23.47 28.75 35.00 42.31 50.84- 1 0.0398 o.oeeo 0.1060 0.1710 0.2570 0.3704 0.5407 0.7848 1.086 1.487 1.002 2.872 3.543 4.847 8.034 7.759 9.885 12.48 15.63 19.42 23.06 29.33 35.68 43.11 51.76 0.6 >o? -i in. Hg ( Z«.Vy ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0090 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 15.98 19.84 24.46 2942 36.37 4342 52,70 3 0.0441 0.0726 0.1166 0.1878 . 0.2762 0.4052 0.5602 0.8163 1.138 1.581 2.114 2.829 3.744 4.900 6.350 8.150 10.38 13.07 16.34 2057 24.97 30.82 37.07 44.74 53.68 4 0.0463 0.0768 0.1248 0.1955 0.2691 0.4203 0.0009 0.6402 1.175 1.010 2.178 2.911 3.848 5.031 6.513 8.351 10.61 13.37 18.70 20.70 25.48 31.13 37.78 45.87 54.62 5 0.0469 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2543 2.995 3.954 5.185 0.080 8.557 10.88 13.67 17.07 21.14 26.00 31.75 38.50 4641 55.60 6 0.0517 0.0846 0.1370 0.2116 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.850 8.787 11.12 13.98 17.44 21.59 26.53 32.38 3954 4757 56.60 ^LL^Jt £7-Z7. 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.785 2.379 3.169 4.174 5.442 7.024 8.981 11.38 14.30 17.82 22.05 27.07 33.02 39.00 48.14 57.61 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.819 2.449 3559 4.289 5.585 7.202 9500 11.65 14.62 1851 22.52 27.62 33.67 40.75 4043 58.63 9 0.0598 0.0962 0.1567 05383 0.3493 0.5035 0.7144 0.9980 1.378 1.875 2.521 3.351 4.406 5.732 7.384 0.424 11.02 14.06 16.61 2240 28.18 . 3443 41.82 4043 8047 ------- METHOD 18 FIELD DATA SHEET Plant:. Date:_ Location: ^.~ ,S> Run #:_ Stack I. Pbar: Sample Tube #• Operators:_jol Leak Check: Pre: Post- Traversa Point Number Velocity Head in. H,O Stack Tamp. Tested Analyte:. Orifice Tank #:_ Pump/Rotometer #:_ Pt: Pretest (mm Hg): Post-Test (mm Hg):_ Tt: Pretest Post-Test fF):_ Time i^zfl'e t_ 132^. /3 2.3.30. 0* i-b^i. ^•L Gauge Vacuum (Hg) / / 1 1 Flow Setting l&c. >>«. .•'(- ,40tt. ^ 95 fV Time: Start:/-/ Finish:/?>/ Total: J' W/B: —B/B: — O2: •> CO2:..Q_ Md = (0.44x%C02) • (0.32 x%O2) -r (O^Bx0/.,^) Md = (0.44 x & } •>• (0.32 x Z.« ) t- (0.28 x T^ ) Md = "•' % HO % HO f«/ Ms = Md x 11 - =— i - 18 ( • 00 1 00 Ms o ( 2.1 Ms = Ts- Ps- Pb 100 _ F ™ 100 °R (°F 460) 13.6 13.6 in. Hg Vs - 65.49 x Cp x Vs - 65.49 x ( Vs« As- Ts(°R) PsxMs )x ft/8 Qs » Vs x As x 60 s/m Q« Qs Qs x60 acfm Ps . . Q8X17.047X - x<1 •W Ta 100 X17.847X- dscfm >x(1 100 ------- METHOD 18 FIELD DATA SHEET Plant: Date: Location:. Run #:&•• Stack l.D.:. Pbar: Leak Check: Pre: Post: Tested Analyte: Orifice Tank #: Sample Tube #•&•»-, Time T76Z. f ^ llLV. iS •—> — > / IT t/1 7 ' C -X • I TlU,. (,3 Gauge Vacuum (Hg) ; f 1 / Flow Setting /$£«. !«. ,6ffct. ,4'* T. 7J -ic 7^ tr Traverse Point Number i Z ^• y i (. r c 3 V .* V / t 3 » 4 V f 1 3 ft > U Velocity Htad in. H^ .tf' .ot «6 . ffC .01 Ofi .df .09 .oT • oc .46 .Of .10 • «f ,ftO .^5 .oC/ .10 .»1 ------- Plant: Site: WET-BULB/DRY-BULB MOISTURE CALCULATION LA'S Co Location: '&=>», Operators: TA Run #: £F - H-5 Date: :5^5-?> 13.6 Barometric Pressure, in. Hg = Pbar = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar i Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td • Tw = Saturation Vapor Pressure of H2O at Tw (from Table) = Pvw = (Ps - Pvw) x (AT) Ps= 2.1.20 Tw = _ Td = Vapor Pressure of H2O = Pva = (Pvw) - Pva =i 2800-(1.3xTw) X Z. _ £'• 2800 -(1. 3 x Proportion of Water Vapor by Volume = Bws - ------- - jaa ca GAS VELOCITY AND VOLUMETr.iC FLOW RATE Plant: _ Samonng Location: _0CMLAJ # Run #• ~* ' - n — i Date: .S"-33«n CIocx Time: ) o / Barometric Pressure, in. Hg: Moisture. %: Ooeratars: Static Pressure, in. HpO: ', 69 .vt.. Cry: - Pilot Tube. Co: t H StacK Dimension, in. Diameter or Side 1 • IS>" Side 2: Wet Bulb. °F: ?ofcn NumMr L -••a n. M.Q SIAUC "•mo. ^ ,0.28 1 %N> Md - iO.44 • : - (0.32 x - (0.28 X ) ^ M,O S M,O 100 100 too 100 13.8 "* '3.8 P. - 65.49 « Co « i cm i «* 2 QB.M-Oai17.e47X — i<1 •• 117^71 100 Pt H.O ------- METHOD 18 FIELD DATA SHEET Plant: Date- Run #;9-//-3 Stack I.D.: it" Pbar:_b Sample Tube: 4 -/I-. a/1 - 9- ,1-3 A Operators: Leak Check: Pre: .000 Post: J5TT Time /03^ /.Qit IOZ8- not n \s I I 80 Gauge Vacuum (Hg) CD O > O O O Row Setting 3SO CC/W \ f <\>3f 1$ fn>ri d €J Traverse Point Number A ' L 3 + (0.28 X ^h^) Md - (0.44 x ) + (0.32 X ) -•• (0.28 X Md- IK M % H0 100 %H_O 'H3- 100 Te. P.. . HO V« - v« - es.49 x < Pax Ma ft/I Qe- VaxAaxflOa/m Oe- -0. K17.B47X x00 %K,0 X 17.847 X- 100 ------- Plant Sam\| Runl Prete Prete Tr«vr4 Mnl NumbM \| : b~pfaGb - — r Ifivc^vt «-.i San ilingLoc ^umbflr: si Leak F si Leak C Sampling Tkm (rrtn) <96 -ifl_ PO 30 abbn 0(5 fi' it- Ji ^ Pba 9-/y-^- Data: S-Z^-^7 CO; late: ,OOlP cfm @ )L in Hg Prol Jheck: Phot: — - Orsal: Slac dock Tim (24-hour dodi) GM M«l«r Rcadng -9/0. PH 3- 7/) inH2O X/X ^'' ^ Nozile ID: - Assumed Bws: Meter Box #: Thermocouple Filter #: ^^ Y: Pilot #: ST- 3 Post Test Leak Rale: /coo cfm @^y in. Hg. As: — Posl Test Leak Check: Pilol: Orsal: Oi6c« Pr«»Aui« Oitt»«nliaJ (AH) in ICO D«s»d \| ActjaJ Stack Temp 01 lampeiatur* °F Piobe \| Fdtec knpingai T»mp °F Dry Gas Metal Temp (TnT^F) OuBei (Tm oul°F) Pump Vacuum (in.Hg) '•'V//''//////////////// ",• • v/////// ///////. 'V//////,y, Iff (& / f ^Typ / 1 ?£> _.. &J) H (o ^£ ------- SAMPLE RECOVERY DATA PLAiNT DATE SAMPLE LOCATION TRAIN PREPARER Sample Box No. °] Run No. . Job No. _ Filter No. SAMPLE RECOVERY PERSON COMMENTS FRONT HALF Acetone Container No. Filter Container No. Description of Filter Samples Stored and Locked BACK HALF/MOISTTJKE Container No. Liquid Level Marked Sealed \ Liquid \ Level Marked \ \ Sealed Sealed IMP. NO. CONTENTS INITIAL VOL (ml) WEIGHT (gramsi INITIAL FINAL NET Co\|.4- 130 TOTAL ------- 3 at EPA METHOD 4 MOISTURE CALCULATIONS PLANT: LA^rJZ _ SOURCE/RUN #:.2l/tL_ HATE: 5 -ZV.37 1 . Leakage Correction for Volume Metered vmc=vm-(Lp-0.02)xQ Vmc=( )-( -0.02)x( ft3 ,, 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) Pbar-MAH/13.6)N Vm =17.64 xVmcxYx std = 17.64 x ( j\flia )x(0fltb )x i.at,/13.6V •"std ^^^•..~ , i~.,v, , y ^ 545 V"std = ^'UZ dSCf 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V... = 0.04707 x (W. - W.} wstd f ' Vw = 0.04707x( 3.0 ) wstd Vw • Q.I4I wstd 4. Percent Moisture, by Volume V, BWS= rr- wstd wstd mstd j - _ ( 0-l4f ) 'W8 7^ gwO.5% Hbid'We ' A ------- GAS VELOCITY AND VOLUMETr.-C FLOW RATE Plant: £f\^<-> • Date: 5^3-?-? Rm ^ ?C'C/T°n: ^U^^q CIOCK Time: 'SO^ Static Pressure, in. HpQ: —, Barometrjc Pressure, in. Hq: d<$. Moisture. %:^=^_ Molecularwt.. Crv: Pilot TubeTCo: ,99 Slack Dimension, in. Diameter or Side 1: JS " Side 2: Wet Bulb. °F: Md • I0.4A • %CO..) -r .0.32 x %O.> « - <0.28X fft . ------- METHOD 18 FIELD DATA SHEET Plant: ^-s «• Date: ,r-> - Location:_ Run #: /J Stack I.D.: Sample Tube Operators: /0-M- Leak Check: Pre: >^«/ Post: 1^,36 / CO , to • o-y <^ ™OC:^ Tested Anaiyte: $''T/X£JiL Orifice TanK #: :. Pump/Rotometer #: Pt: Pretest (mm Ho^: Post-Test (mm Hg): Tt: Pretest fF):. Post-Test fF):_ Time: Start:c>9/3Ftnisn:/gyg Total: £?o W/B> D/B: -— O,.: — Gauge \| FIow (H^ Settin9 ffit-3 0 l-xo/itf/j OS 9? 1 o 1 ^^7'?P- 1 (9 1 1 f,QH'^ 10 \| I #5'2 C 0$OA 0 \| /6JO O 1 V rl flw TrovcrM Point Number A / 2. 5 f f & ft 1 > i f / (i Velocity H«M m.H^J . i-3 /q ./sr HH ,9 .Q3'3 .^Jiy 9'?':5 ^y-3/ A,^ S3 1 Md - 10.44 x %CO,) - (0.32 x %O,J ^ Md = i0.44 x ) - (0.32 x ; (0.28 x '» Md - MS - Md x ( fr i H,O % H,O 1_. - 18 ( i— 1 i00 i00 xd- _£!_»-,8(_2! 100 100 2i\ F- bll R ( F»460) Pb +-IL.- ( ^.Ufe ) * '-&' 13.8 ' 13.8 p.- ;i,( Vs - 85.49 x Co x V$P~ x '\ Vs • 65.49 x I Vi- 3- )x( )x i- ft/» Q« • VsxAaxeOs/m Q« - xflO Pa l Q>.M=lQlxt7-847x «« — ) •W T« 100 ------- FIELD DA I A SHEET Plant: c"* S c 6 Sampling Location -ft /O oo«~» Run Number: \|0~M\ Date: Sample Type: Pbar 3M CO2: Ps: - 02: Thermocouple it: Filter #: Pretest Leak Rate: .^p I cfrni® \s in. Hg. Pretest Leak Check: Pilot: _J/Orsat: •••% Probe Length/Type: /X Stack Diameter: ^ $ " Pilot #: Sr- 3 As: Nozzle ID: Assumed Bws: — Meier Box #: y 4- Post-Tesl Leak Rate: . Ope cfm @ _/& in. Hg. Post-Test Leak Check: Pilot: Orsat: AH@: / TravwM Nurnbe Sampling Time (mln) no 3# ^£> -lO OodcTime (24-hour dock) &9/Q W93 ^^f2 ^f ^^ ^^ * j""^\ f_J "1 , j ^ Goa Meter Reading f 1tt ^^ I ^* Q v ' 9 1 ~^ ^^. 7^ 011 , ^03 /QiQ "71 C . OH * Velocity Head (Ap) lnH2O Orif ce Pressure Difterential (AH) in H2O Desired Actual Stack Temp. (Ts) Temperature °F Probe Fdter Impinger Temp. °F Dry Gas Meter Temp. Inlet (Tm in°F) y/////////////////////////////////////////////////. If $b /'? ? - 6> ° ^/ 5=3 57 s >•• <^o ?"3 $ ^ ^ ^ — ^ ->- . . Outlet (Tm out°F) S9 $ S" ^^ O' Pump Vacuum (in. Hg) y 4 t-f fy ~jn/" ------- PlantL Date: SAMPLE RECOVERY DATA Run No.: ^~^_ Job No.: Sample Box No.: Sample Location:. Sample Type: 2 Filter No.: Sample Recovery Person: Comments: FRONT HALF Acetone Container No.; Filter Container No.: Liquid Level Marked:. Sealed: Sealed: Description of Rlter: Samples Stored and Locked: BACK HALF/MOISTURE Container No.: Liquid Level Marked: Sealed: IMP. NO. 1 2 3 4 5 6 CONTENTS IKo VKo l«W (^o WEIGHT farams) INITIAL 6a? t^^-s t^-O 7^o 9-^.f FINAL c/u C^^ t^.t -7JT/.4 >^.t NET -,i 0,3 ,t U Z «7. Description of Impinger Catch- ,. \|vl\ ------- .3 ai EPA METHOD 4 MOISTURE CALCULATIONS PLANT: LAACO _ SOURCE/RUN #: IQ-U-l PATE: 1 . Leakage Correction for Volume Metered Vmc = V (Lp - La) x 9 Vmc=Vm-(Lp-0.02)xG vmc=< )•( -0.02) x( ) ft3 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) Pbar-MAH/13.6)N = 17.64 xVxYx mc )x dscf 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V... = 0.04707 x (W - W. wstd f ' Vw = 0.04707 x( 2 2_ wstd •'- V,« = O.\o4 4. Percent Moisture, by Volume V, wstd R - WsW °ws Vw -K Vm wstd mstd BWS = ------- GAS VELOCITY AND VOLUMET-C FLOW RATE Plant:_LflSCO Date: 5^33-97 CIocx Time: // o o Samoung Location: ffite Run : IO-\\ -Z Ooerators:. Barometric Pressure, in. Hq: 8ft ,<1% Static Pressure, in. HpQ: -, g/ Moisture. %: Molecular wt.. Crv: Pilot Tube. Cp:^_~ " StacK Dimension, m. Diameter or Side i • JS'' Side 2' Wet Bulb. °F: 'oint Nuowr /?'/* Dry Bulb. °F: V.toOTV n M_Q n StAcic "•mo. a_ 91 A ~( \ .if. \ Md - <0.44 H %CC,> » '0.32 x %CU - .0.28 X %H,» Md - 10 4* H ) - (0.32 x - (0.28 1 ) • Md id iM.O too ,H,0 100 100 100 P«-Pb - S P" - i 13.8 ,3.8 P,. -n.H« V« • 65.40 It v«. •f w. 2 Q«" o.. xflO %H.O °»-d- X17J47K" Ml- a'/, O \L A .. ------- FIELD DATA SHEET & lO Plant: Sampling Location Run Number: ,/> Ps: -', gj CO2 O2: Noule ID: --- Thermocouple #: V/3 Assumed Bws: ~ Filler #: - Meter Box »: ]\ Y: Probe Lenglh/Type: J7$3 Pilot : $7^J5 Post Test Leak Rale: cfm Slack Diameler: " As: -2$ -ft Posl Test Leak Check: Pilol /^in. Hg rsal: Trav«rM Pobt Numb Sampling TVm Mn) <90 At) 90 no 1O Ooc* Tim* doe) IQo\ 1^1 1 O5\| I P ^/ /^-1l Gu Meter Beating (Vm)ft3 ^VP/VSO ^0,55^ ^^,30 •?££ /3o 973,^70 /I ' 1 9 3 ^^ 5^ ^^ £) " / ^ 3 V Y 333 53 0 23-> Q3V 4^7 >?30 ii3\| Te-^f> & Deratui °F \| Filter Impingai Temp °F Dry Gas Maler Temp Omin0F) Oudel (Im outcF) Pump Vacuum (in.Hg) : '///////////////• '/////////, v.io 3%^5t •j& yi^5 J^^. 60 ^ ^ ^ t -**- -fft> ftciivi l<. 4 rh fS" 96 ^ J&-- &S ?0 ££ £g~ ^ Y _i.... B lm = . ! ------- Plant: Date: SAMPLE RECOVERY DATA Run No.: Sample Box No.: W -Co Job No.: Sample Location- Sample Type: \0 Oocj Filter No.: Sample Recovery Person: Comments: FRONT HALF Acetone Container No.: Filter Container No.: Liquid Level Marked:. Sealed: Sealed: Description of Rlter: Samples Stored and Locked: BACK HALF/MOISTURE Container No.: Liquid Level Marked: Sealed: IMP. NO. 1 2 3 4 5 6 CONTENTS Hn> VHo £fTr /c- TOTAL INITIAL VOL (ml) 100 Ue? ^ 3^0 WEIGHT faramsl INITIAL 6(U G37.^ t^-fe "?3^3 >-q<^G.3 FINAL f2>' GVf 6>>.y 4^3.C NET 1,4 D.O o.s s.-t -?- 3 Description of Impinger Catch- ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: LAS Co _ SOURCE/RUN #' IQ-H-? DATE: 1 . Leakage Correction for Volume Metered , W °-02) x 0 . Vmc=( )-( -0.02) x( - V_ -^ <^ •"" t-i A * me" '-r 7.^11) ft 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) Pbar-MAH/13.6) V = 17.64 xVxYx m . mr mstd Vmstd= 17.64 std 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V ... = 0.04707 x (W. - W. ) std ' ' = 0.04707 x( >>) 4. Percent Moisture, by Volume _scf 'std f 4. W wstd mstd Bws = ------- ana 100 METHOD 18 FIELD DATA SHEET Plant:. Date:_ >e o Tested Analyte:. Orifice Tank #:_ /v»fl-4 Location:_ Run #• A/M-n Pump/Rotometer #: v/* Pbar: Zr/g Pt: Pretest (mm Hg): n. Post-Test (mmHg):_^ Tt: Pretest f F):_ Sample Tube #: Operators: Si M4 Post-Test fF): n. Leak Check: Pre: >/ Post: ,X Time: Start:04H Finish:n>H Total: m W/B: - D/B:— O2:_^ .C02:_ Md = (0.44 K %CO2) 1- (0.32 X. %O2) -r (0.28 x % Md = (0.44 t. ) +• (0.32 X ) •)• (0.28 x Md = /5 ------- APPENDIX A. 1.13 Condition 12 (includes flows, moistures, and Method 18) ------- a at METHOD 18 FIELD DATA SHEET Plant:. Date- Location- ^V./i Run #;ttE- a-' Stack I.D.: Sample Tube #:. Operators: iP> - tfe Leak Check: Pre: Post- Tested Analyte:. Orifice Tank #:_ Pump/Rotometer #: Pt: Pretest (mm HQ): Post-Test (mm Ha): - Tt: Pretest fF):_ Post-Test fF): n. Time 733/, JO X3^/- 3^. /^ Gauge Vacuum (Hg) i / / / Flow Setting i£a ct- /Soff. iSC><.C- /5S W/B:_££_D/B:^_02:_ZJ_C02:_a_ Md = (0.44 x %CO2) i- (0.32 x %02) -r (0.28 x "/oN^ Travarsa Point Number / r 3 y 5 L 7 f i I, H f (, 1 4 rp Velocity Head in. H^ .^T> .ZT . 3° ,3/ .3-? .03 .1 18 . ?(. "71 77 .2ft •2-r .-ZT 21 .21 D.^B Stack Temp. °F 7 9 •79 11 Tf 7f ->^ i? 7^ 1 f "7? -?1 7? 77 7^5 7^ 11 Ti> W •Md = (0.44 x Md = 2.^ Ms = Md x11 (0.32 X •i- (0.28 x 100 100 100 100 Ma .b^ r,. 71 13.6 13.6 Vs - 6S.49 x Cp x Vs - 85.49 x ( , v* - Ts(°R) PsxMs ) X ( )x AS- . Qs - Vs x As x 60 s/m Qs» Qs» Q».td ^rtd3 Qsatd- x60 adni Ps %H-0 Qs x 17.647 x - x (1 - - £- ^ 100 X17.847X- 100 ------- i acn WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: / /V^-O Site: /V\4j^, ^rvW^u«J\~ Operators: Barometric Pressure, in. Hg = Static Pressure, in. HoO - Absolute Pressure of Stack - Pbar + - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td • Tw = Saturation Vapor Pressure of H2O at Tw Vaoor Pressur@ of HoO — Pva — (Pvwi - i „ .i« . fi\ r Location. j'lAiAJ z,x ^MU.^T' 7$ Run #: fle-ii-i Date: 5 Pbar= 21 $O Pg = . Z> -?- -^ PS= ^13/ I3.b Tw = U U> Td= 9 ? AT= /^ (from Tahlp) - Pvw = ^/. ^H ^'L (Ps - Pvw) x (AT) . 2800-(1.3xTw) -ll'l in. Ha in. HLC 2 in. Hg °F °F °F in. Hg in. Hq * >~n L ' 2800-(1.3 x ^ Proportion of Water Vapor by Volume = Bws '0....- (P^) uvvo Tamp. OF 0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 180 100 200 210 220 230 240 0 0.0376 0.0831 0.1025 0.1647 0.2478 0.3626 0.5218 0.7392 1.032 1.422 1.032 2.598 3.446 4.525 5.681 7.569 9.652 1220 1529 10.01 23.47 28.75 35.00 4241 5044- >S) 1 0.0398 0.0680 0.1080 0.1716 0.2576 0.3764 0.5407 0.7648 1.066 1.467 1.002 2.672 3.543 4.647 6.034 7.750 9.685 12.46 15.63 10.42 2346 2043 35.88 43.11 51.76 ( ^.?» ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1603 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.180 7.952 10.12 12.77 15.98 19.84 24.48 29.02 38.37 43.92 52.70 3 0.0441 0.0728 0.1186 0.1876 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.38 13.07 16.34 20.27 24.07 30.52 37.07 44.74 53.65 4 0.0463 0.0768 0.1248 0.1955 0.2S91 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 6.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.57 54.82 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.1 65 6.880 8.557 10.68 13.67 17.07 21.14 26.00 31.75 38.50 46.41 5540 e 0.0517 0.0846 0.1370 0.2118 0.3120 0.4S20 0.6442 0.9046 1.253 1.712 2.310 3.081 4.083 5.302 6.650 8.787 11.12 13.98 17.44 21.59 26.53 32.38 39.24 47.27 56.60 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4688 0.8669 0.9352 i.293 1.765 2.379 3.169 4.174 5.442 7.024 8.981 11.38 14.30 17.82 22.05 27.07 33.02 39.09 46.14 57.61 8 0.0571 0.0932 0.1502 0.2292 0.3304 0.4858 0.6903 0.9666 1.335 1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1821 22.52 27.62 33.67 40.78 4949 5843 9 0.0598 0.0982 0.1567 0.2383 0.3403 0.5035 0.7144 0.9989 1.378 1.675 2.521 3.351 4.406 5.732 7.384 9.424 11.02 14.06 1841 2X09 28.18 3443 41.62 4043 5847 ------- Plant:. Date:_ METHOD 18 FIELD DATA SHEET Tested Analyte: ^/^^ Orifice Location: Run #: Stack I.P.: 'i. s Pump/Rotometer #: Pt: Pretest (mm Hg):. Tt- Post-Test (mm Hg):. Sample Tube #:. Operators:. Leak Check: Pre: ' Time: Start:^&££_ Finish :_id££_Total:_&£ Post: V£>ft? W/B: 60j o H> lt> x> •"> so t Time ->->-! °.^1 •012.37 Gauge Vacuum (Hg) / / Flow Setting \0c^ -S o f.<- ,> \ V \ Stack . Temp. °F Md = (0.44 x %CO2) -t- (0.32 X %O2) -r (0 Md = (0.44 x ) -i- (0.32 X ) -t- (0.28 Md = % HO % HO Ms = Mdxd • — '• - 18 ( i 100 'CO Ms = ( ) x(1 Ms- T,. °F = Ps - Pb + -§^- = ( I - 18( ) 100 ' 100 ) •• 13.6 Pa in. Hg Vs " 85.49 X Cp x JEF ' Vs - 85.49 x ( ) X ( Vs - It/8 As » " . Qs » Vs x As x 60 s/m Ms )x i Ga- ds- Acfm Ps x 60 %H0 Q»std=Q« 17.647X — XO 1QO X 17.847 X- dseftn ------- METHOD 18 FIELD DATA SHEET Plant:. Date: 5-zq-r Tested Analyte:. Orifice Tank #:_ Location:. Run #: A Stack I.D.:_iLJL Sample Tube #:» Operators: rW- Pump/Rotometer #: Pt: Pretest (mm Hg): Post-Test (mm Hg): Tt: Pretest fF):_ Post-Test i°F): '— Leak Check: Pre: Ibif Time: Start: '6v Finish: "_*_ Total:. Post:_^2iD W/B:lj^D/B: 76. O2: "^ 0 A u lo 4» # (A Time 2-333. /-z 2 V3^/, ^o Gauge Vacuum (Hg) / j Flow Setting ISO £.<- ISa <, ISO ^ /So e-e. /SotC /£0 ------- METHOD 18 FIELD DATA SHEET Date: 2 Location: Run #: Tested Analyte:. Orifice Tank #:_ Stack I.D.:_jjLJL Pbar: ^."b Sample Tube :ihg5-/z-3/3, Operators: rA- Pump/Rotometer #: Pt: Pretest (mm Hg): Post-Test (mm Hg): Tt: Pretest fF):_ Post-Test ff=)- Time: Start: £LZ_Finish:_ Total: ex? Leak Check: Pre: Post: CO2: o // i\i5 'TOf Time -nil. fV 1Z •nf/. 73 Gauge Vacuum (Hg) Traversa Point Number Velocity Head in. H^O Flow Setting ISO C<- W/B: — DIB: — Q2: . Md = (0.44x%CO2) +• (0.32 X%O2) i- (0.28 x%Nj) 60 Stack Temp. Md = (0.44 x ) -i- (0.32 x Md Mdxd - —\ • 18 ( =- 100 100 (0.28 X ) Ms « I 100 100 "F- Ps - Pb -t- S.P. 13.6 13.6 in. Hg Vs • 65.49 x CD x Vs - 85.49 X ( Vs- As- Ts(°R) sxMs )x ft/s .2 Qs - Vs x As x 60 s/m x60 Qs- acfm Ps Qs . .= Qs x 17.047 x — x (1 • - — ) »W T, 100 x 17.847 x- dscdn ------- METHOD 18 FIELD DATA SHEET Plant:. Date:_ Tested Analyte:. Orifice Location: A/U-.^ g.i Run #:_rv\e-_f7-^ Stack I.P.: n, 5 Pbar: -z^. 3 Pump/Rotometer #\ \JOST Jt'Z- Pt: Pretest (mm Hg): ~~ Post-Test (mm Hg): Tt: Pretest fF): 1_ Sample Tube #:. Operators: rft A Leak Check: Pre: Post: Time: Start:_/i2£. W/B:_6ll_D/B:J Finish:/zojf Total: Lo g_02:^_C02: 6 •' '5 /o 74 If 35 Time Z33 7, 73 1/rs Gauge Vacuum (Hg) / Flow Setting . 60 6C Md = (0.44x%C02) •" (0.32 X%O2) T (0.28x%N2) 65 66 Traverse Point Number i Z 3 •^ 5 (. 1 t 1 ^ T, / J 6 7 ? Velocity Head in. H^ t3 . 2-J • Z.~? .7.") 3,; 35 ^^ .3-7 .2.5 . •< .7.^ ,-i.l 2-S . ^^ .?(• .20 Stack Temp. yo FO ffl ?' ^/ ^ ' yo to ?6 fO 9° no <%0 g0 $° 1i --W Md = (0.44 x ) + (0.32 x Md = ~L<\ (0.28 x Mdx(1 % HO - £_ ) 1 00 % HO - 1 00 Ms - Ts. * 13.6 Ps = Z«. -> in. Hg °R(°F-460) 13.8 — J Ts <°R) Vs - 85.49 x Co x VAP J ps X MS Vs - 85.49 x ( , ix< . « AS- , , .-x n' J /b T Qs • Vs x As x 60 s/m Qs- Qs- x 60 acfm Ps Qs . .= Qs x 17.647 x -^- x (1 • — ) •W Ts '00 X 17.647 X- •(1'—> QflAftWeW "WQ ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: Site: rators: rft Location: Run #: fl Date: Pbar + Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of HpO at Tw (from Table) = Pvw = (Ps - Pvw) x (AT) Pbar = Pg = Ps = Tw = Td = ;? ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Date: _s Clock Time: i2n Operators:. Sampling Location: Run#: BaromeirTcTPressure, in. Hq: 213 Static Pressure, in. HoO: .« Moisture, %: i,??^ Molecular wt., Drv: zf Pitot Tube, Cp:_i Stack Dimension, in. Diameter or Side 1: /-?. s Side 2: Wet Bulb. °F: 6g Dry Bulb, °F:. Travtm Point Number v • c Z •5 V 5 £ ? f / z 3 V 5 (, 7 f V.locrty Hud In. H2O ,t3 . 2-0 "•• .^-}. .2-1 .•« .3 I .33 .36 ,zy .-2-5 .ZLO • Zl .25 .2^ >23 .23 ^KP-.5/ftc» Stack T«mp. °F .9 * f2- ?«• S-z_ 92_ J^ ff-z- 5T- 9T- 71 SI 11 ?z. ?7L §2. S-''- T.- P2. Md - (0.44 x %CO2) 4- (0.32 x %O2) + (0.28 x %^) Md«(0.44x o )+(0.32x ?/ ) + (0.23x7f Md - 2- "? - Mdxd • % H,0 % HO '\j_1A* Pa. Pb +J£^=( 2-- 13.8 Pa. ^».3 in. Hg 13.0 Y-5 (°R) V«-»b.4UxCpx AP x V»-85.48 X( ,?7 )x( ,5/00 )X ^rt Q«-VixA«x60a/m Qs- Qs« Q». actm p. %K20 .= Q«X 17.647 x x(1- — !• 100 X 17.647 X- 21 • -x(1 100 ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: L/feo Site: MAio ^U£4u<4— Operators: ,A\|c£ Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Pbar + — ^L- 13.6 Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H0O at Tw (from T Location: 1Y\<^^^J Run #: f^t-ii- 1 Pbar = Pg = Ps = Tw = _ Td = AT = _ able) = Pvw = Fx v-VAuST Date: -^ir-S-Zfi'il ^•3 in. Ha ^ in. H2O tf. ^ in. Ha Uti °F fo °F H °F b. ulv£ in. Ha Vapor Pressure of H2O = Pva = (Pvw) - (Ps - Pvw) x (AT) 2800-(1.3xTw) Pva=( )- ( 2.S-3 2800-(1.3 x ( Proportion of Water Vapor by Volume = Bws (Ps) Temp. OF 0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 100 170 180 190 200 210 220 230 240 0 0.0370 0.0031 0.1025 0.1047 0.2478 0.3020 0.5218 0.7392 1.032 1.422 1.932 2.596 3.446 4.525 5.881 7.569 9.652 1220 1529 19.01 23.47 26.75 35.00 4241 5044- 1 0.0398 0.0660 0.1080 0.1716 0.2576 0.3764 0.5407 0.7648 1.066 1.487 1.992 2.672 3.543 4.647 6.034 7.759 9.885 12.46 15.63 19.42 23.86 2843 35.68 43.11 51.76 in. Hg ( Z1-3 ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1603 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 15.98 19.84 24.46 2942 36.37 43.82 52.70 3 0.0441 0.0728 0.1186 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.36 13.07 16.34 2027 24.97 30.52 37.07 44.74 53.65 4 0.0463 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2,178 2.911 3.848 5.031 9.513 6.351 10.61 13.37 16.70 20.70 25.46 31.13 37.78 45.57 54.62 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.680 8.557 10.86 13.67 17.07 21.14 26.00 31.75 38.50 46.41 5540 6 0.0517 0.0848 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.850 8.767 11.12 13.98 17.44 21.59 26.53 3248 39.24 4727 56.60 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.981 11.38 14.30 17.82 22.05 27.07 33.02 3949 48.14 57.61 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1821 22.52 27.62 33.67 40.75 4843 5643 9 0.0598 0.0982 0.1587 0.2383 0.3493 0.5035 0.7144 0.9888 1.378 1.875 2.521 3.351 4.406 5.732 7.384 9.424 11.82 14.86 1641 2248 28.18 3443 4142 4843 5047 ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Date: Sampling Loc Run #: K& ation: ^ ad^s-A- Clock Time: £> /./, / V«-85.49x< .99 )< )x<\\| Vt« \f. ^ ft/t A.- <-\.\|/^ R2 Qt • Vi x AM x 60 t/m Q«- x xOO Q.. t,\^Vl »«" P. "HjO, Q.ttd-Q.xl7.847x ^ x(1- iflo ) ^tW" X17.647X— X(1'~!5~> ------- r WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: LASrr> Site: {^a^ "^p^y^^ Operators: Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar + - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td • Tw = Saturation Vapor Pressure of H^O at Tw Vapor Pressure of H20 = Pva - (Pvw) - " '\ Pva=( ^, ,.(«:« - .« Location: fco^ FxM/v^r ~rHJfZS Tw = 0? 3 Td = H AT= II Pvw = D'^^l- :AT):< Tw) ) . D.H . in. Hg . in. r-LO 2 . in. Hg °F °F °F . in. Hg in. Hg 2800-(1.3 x Proportion of Water Vapor by Volume = Bws (Ps) Tamp. °F 0 10 20 30 40 50 60 70 60 90 100 110 120 130 140 150 160 170 160 _ 190 -200 210 220 230 240 0 0.0376 0.0631 0.1025 0.1647 0.2478 0.3626 0.5216 0.7392 1.032 1.422 1.932 2.500 3.440 4.525 5.881 7.569 9.652 12.20 15.29 19.01 23.47 26.78 35.00 4241 5044- 1 0.0398 0.0660 0.1060 0.1716 0.2576 0.3764 0.5407 0.7648 1.066 1.467 1.992 2.672 3.543 4.647 6.034 7.759 9.685 12.48 15.63 19.42 23.96 29.33 35.68 43.11 51.76 ------- oacu METHOD 18 FIELD DATASHEET Plant: / AttO Tested Analyte: Vv^^<. Date: -5-z-«-i Orifice Tank #: Location: &>«. £,^s+ Pump/Rotometer #: \/o^:3±'2- Run #: K£- ii-z, Pt: Pretest (mm Hg): Stack I.D.: zg".iV" Post-Test (mm Hg): Pbar: Tt: Pretest (°R: Sample Tube Operators: - #-R£'K-2.ae-r2-Zfl Post-Test PR: -i4- Time: Start: Finish: Total: Leak Check: Pre: Post: W/B: D/B: O«: ?/ CO«: o Gauge Time Vacuum (Hg) /v // f / \ ( v > Flow Setting / SO ec /^Wt t~£a(- V Jt-- \ £u,.'c- Traverse Voint NlJlpber (\ l \ 5 \ $ it i i * «/ * • (0.32 x%O2) -r (0.28x%N2) ^*/ MJ _ in M v 1 (O 12 x i +• (0 28 X ) I •: Md = ^4 \ . j % HO % HO \ ^j _ \|y)(J jj/^ ' < 1 8 ( • 'r \ "" - :^" ,co -' ,00 x Mr^(2^ )x(i- 1-18( ) \-^ 100 100 Ms - Ts » °F » °R (°F * 460) 13.6 13.6 Ps = in. Hg ^Jp" = — I isTR) vs = oa.ta x «-p x vu-- x ^ ps x Ms Vs - 85.49 x( )x( ) x \l U Vs « ft/s A»- rt2 Qs » Vs x As x 60 s/m Qi - x x 60 Qft * acfin p, %H_O Qs . .= Qs X 17.847 X — — x (1 • ) std T« 100 std 100 QS0f^w QlCnll ------- 3 aca cia GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Sampling Location: Run#:_M-_ ------- 3 Ql—' WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: Site: Operators: 7 Location: _ Run #: Q6- \z- Date: Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = _. Pbar = ~ 13.6 PS = __2> Tw= AT= M Saturation Vapor Pressure of H2O at Tw (from Table) = Pvw = Q. ^ (Ps - Pvw) x (AT) Vapor Pressure of H2O = P.va = (Pvw) - Pva=( 2800-(1.3xTw) 2800 -(1. 3 x Proportion of Water Vapor by Volume = Bws (Ps) T«mp. °F 0 10 20 30 40 50 60 70 60 90 100 110 120 130 140 150 100 170 180 190 200 210 220 230 240 0 0.0378 0.0631 0.1025 0.1847 0.2478 0.3620 0.5218 0.7392 1.032 1.422 1.932 2.598 3.448 4.525 5.881 7.569 9.652 12.20 15.29 19.01 23.47 28.75 35.00 42.31 50.84- 1 0.0398 0.0660 0.1080 0.1710 0.2570 0.3764 0.5407 0.7848 1.088 1.467 1.992 2.872 3.543 4.847 6.034 7.759 9.885 12.48 15.83 19.42 23.98 29.33 35.68 43.11 51.76 in. Hg in. H20 in. Hg °F °F °F in. Hg in. Hg ( Z ------- ^ GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Sampling Location: foe Run* Date: 5 Clock Time: /^-vz- Barometric Pressure, in. Hg:_ Moisture, %:_J_2l Molecular wt., Dry: Stack Dimension, in. Diameter or Side 1: Wet Bulb, °F: 6Y Dry Bulb,0F:. Operators:. Static Pressure, in. -,C 2 Pitot Tube, Cp:_iH_ Side 2: •75- TravirM Point Number 1 1 •} t s c / I T V J 0 » 7 1 4 3 C / 1 1 9 5 6 • Vtlocrty Ha«d in. H2O .0* .00 .0^ oO .oc, .0 n OG .0^ .05 .0^ .65 .06 .C78 .07 .05 ,0V 05 .0<* . 01 .06, ,« Md - 1.1 %H,0 %H,O M« - Mdx(1 - —) * 18 ( — ) 100 100 ' T ) + 18( '" 100 100 Ma- Ta« ' Pa-I Pa- 13.8 13.8 In.Hg Vs - 65.48 x Cp x Vl-85.49x( . Pax Ma «i I V ft/I AI- f.e- \ ft' Qi-VixAix60i/m Qa- x xeo ftcffn Pi H,0 -Qixl7.847x x(1 2_) Ti 100 X 17.047 X- d«n 2.1. 100 ------- Plant: Site: WET-BULB/DRY-BULB MOISTURE CALCULATION Location: /ft' Run #: Sy WvrQperators: Barometric Pressure, in. Hg = Pbar = < Static Pressure, in. H20 = Pg = — Absolute Pressure of Stack = Pbar + ; 9 Ps = —* 1 J.o Wet-Bulb Temperature, °F = Tw = : Dry-Bulb Temperature, °F = Td = Temperature Difference, Td - Tw = AT = Saturation Vapor Pressure of H2O at Tw (from Table) = Pvw = _IL (Ps - Pvw) x (AT) Date: 5-21-ft ;3 in. Hg iii in. HLO in. Hg >S n Vapor Pressure of H20 = Pva = (Pvw) - Pva=( 2800-(1.3xTw) 2800-(1.3 x Proportion of Water Vapor by Volume = Bws Bws= Tamp. OF 0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 180 190 ' 200 ~ 210 220 230 240 (Ps) 0 0.0378 0.0831 0.1025 0.1647 0.2478 0.3020 0.5218 0.7392 1.032 1.422 1.932 2.596 3.446 4.525 5.681 7.569 9.652 1220 1529 19.01 23.47 28.75 38.00 4241 5044- 1 0.0398 0.0660 0.1080 0.1718 0.2578 0.3764 0.5407 0.7848 1.066 1.467 1.992 2.672 3.843 4.647 6.034 7.759 9.885 12.48 15.63 19.42 23.96 29.33 38.68 43.11 51.76 °F °F in. Hg in. Hg ( -2^.1^ ) VAPOR PRESSURES OF WATER 1 fc In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.982 10.12 12.77 18.96 19.84 24.46 29.82 38.37 43.92 82.70 3 0.0441 0.0728 0.1186 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.829 3.744 4.900 6.350 8.180 10.38 13.07 16.34 2027 24.97 30.82 37.07 44.74 5345 4 0.0483 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 6.313 8.381 10.61 13.37 16.70 20.70 25.48 31.13 37.78 48.87 54.82 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.660 8.557 10.66 13.67 17.07 21.14 26.00 31.75 38.50 46.41 55.60 6 0.0517 0.0646 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.850 8.767 11.12 13.98 17.44 21.89 26.83 3248 39.24 47.27 56.80 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 6.981 11.38 14.30 17.82 22.05 27.07 3342 3949 48.14 5741 8 0.0571 0.0932 0.1502 0.2292 0.3304 0.4858 0.6903 0.9666 '.338 1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.82 1821 2242 27.62 3347 40.75 4943 5843 9 0.0598 0.0982 0.1587 0.2383 0.3493 0.5035 0.7144 0.9989 1.378 1.878 2.821 3.381 4.408 5.732 7.384 9.424 11.92 14.98 1841 2249 28.18 3443 4142 4943 5947 ------- ^F7^ F C L F v^ F c C L 0 V37 o «-> » 09 3 1 20 U 101 SO mtot--rt METHOD 18 FIELD DATA SHEET lant: Lf&tD TesteH Anaiyte: 5/v^-^ late: £-£4-^ Orifice Tank #• ~- ocation: A;-. Ih.^/ fc-K«i^^ Pump/Potometer #: \) «^ Traverse Point Number 1 t ^ O .^1 .28 .-W f ^i ••p > 37 «ft ,"2>8 .-p .'V'/ ••Jo b .S9 .-« > .bl .-§5 .y> 20 ^o . 33 . 38 .38 jj Stack Temp. °F 7 JL 72- 7i 7^ 7f. -j^_ -7-t Tic -77_ •7 3 72. 1H 7^ 72. •7Z. ^72. ~i> -"f"t- Md = (0.44x%C02) f (0.32 x%O2) -r (0.28x%N2> Ls_-Md -> (0 44 X ^ ) +• (0 32 X 3 f ) +• (0 28 x 7 '.' ) % H20 % H20 ^2- Ms - ( 2^ )X(1 . '• T ) . i8( ^' ^ ) 1 00 1 00 Ts - -) Z. ^P = <"2o R ( F i- 460) S P •» ^" • Q^^ - 13.6 13.6 Ps » 'Z') • Vt in. Hg ^5?= .tn-v^ f T- /Op\ Vs - 85.49 x (. W )X( )XAJ 1 W Vs « 2«D c/\ Ws x» ^ 2 As - % , / = n Qs - Vs x As x 60 s/m Qe - x x 60 _ UflOJ _._ Qs - "Ti acfm Ps %H,0 Qs . .= Qs x 17.047 x x (1 - ) °std~ XI7.847X (l 100 ' Qs«td~ HU^f dsefm ./.I.I ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: L/^fecO Site: Aocili'iLj ,-61 Operators: Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar + - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H20 at Tw Vapor Pressure of HpO - Pva - (Pvw) - - w' ' Pva=( ,-,», ,.<2Vi'-..S8 Location: Aw^il/o^ £/i TM Run #: 4F-\i.-< Date: Pbar = L-i • 3 Pa = ^3(0 -He" Ps= Z^ 13.C - Tw= u>3 Td= >X AT= ^ (from Table) = Pvw = D- "S'BU'Z (Ps - Pvw) x (AT) 2800-(1.3xTw) 4^ )(. ^? ) 7>4^S3 I^AU^T fT-ZI-i'-f in. Hq in. HO 2 in. Hg °F °F °F in. Hg in. Hq 2800-(1.3 x (j^ Proportion of Water Vapor by Volume = Bws Tamp. OF o 10 20 30 40 so 60 70 80 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 (Ps) 0 0.0376 0.0631 0.1025 0.1647 0.2478 0.3626 0.5218 0.7392 1.032 1.422 1.932 2.596 3.446 4.525 5.881 7.569 9.652 1220 1529 19.01 23.47 28.75 35.00 42.31 5044- 1 0.0398 0.0660 0.1080 0.1716 0.2576 0.3764 0.5407 0.7648 1.066 1.487 1.992 2.672 3.843 4.647 6.034 7.759 9.885 12.48 15.63 19.42 23.96 2943 35.68 43.11 51.76 ( Ll.iH ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 15.98 19.84 24.46 29.92 36.37 43.92 52.70 3 0.0441 0.0728 0.1186 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.36 13.07 16.34 20.27 24.97 30.52 37.07 44.74 53.65 4 0.0463 3.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.176 2.911 3.848 5.031 6.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.87 54.62 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.680 8.557 10.66 13.67 17.07 21.14 26.00 31.75 38.50 46.41 5540 6 0.0517 0.0846 0.1370 0.2118 0.3120 0.4S20 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.650 8.767 11.12 13.98 17.44 21.59 26.53 32.38 39.24 47.27 56.60 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.981 11.38 14.30 17.82 22.05 27.07 33.02 39.99 48.14 57.61 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1821 2242 27.62 33.67 40.75 49.03 5843 9 0.0596 0.0982 0.1567 0.2383 0.3403 0.5035 0.7144 0.9989 1.378 1.87S 2.521 3.351 4.406 5.732 7.384 9.424 11.92 14.96 18.61 229 28.18 3443 41.82 4949 5947 ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: L Date: Sampling Location: Run #: Clock Time: uzo Operators:. rW / Barometric Pressure, in. Hg: 2.?, 3 Static Pressure, in. HUO: -.9-5 Moisture, %: /-L Molecular wt., Dry: ? Pitot Tube, Cp: .99 Stack Dimension, in. Diameter or Side 1 t^.-ts Side 2: Wet Bulb, °R. Dry Travsrss Point Mum bar ' z 3 y 3 ^ 7 / / 2. 3 V .5 fc 7 r Vstocrty Hssd In. H20 . 2? •-. 3V 30 > Q LJ~) 36 • 2.«/ ,28 1^ % 3/ . 3/ •3^ .^9 . 33 . 3. . ^^ /,/ $p-D/oH& Stock T«mp. °F 70 10 1O T> 13 "75 75" 7^ 7^ -73 13 13 13 -73 13 -73 Ts"->j Md « Md . (0.44 x Md - Z f ) + (0.32 X + (0.28 X %H 0 Ms- Mdx(1 - —) + % HO T«. Pa-Pb 13.8 13.8 — T9(°R) Vs - 85.48 x ( )»( )X )F AS- ^.J^ n: Qs - VsxAsxeos/m Qs- x x80 Qt-w-Q.xl7.e47x X 17.847 X- ------- iOCJ WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: ^ / .A5io Site: Operators: rA Location: Run #: Date: 13.6 Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar + Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H20 at Tw (from Table) = Pvw = (Ps - Pvw) x (AT) Pbar = Pg = Ps = Tw = Td = Vapor Pressure of H20 = Pva = (Pvw) Pva= 2800-(1.3xTw) )( /O ) 2800 -(1. 3 x Proportion of Water Vapor by Volume = Bws (Ps) Tamp. °F 0 10 20 30 40 50 60 70 60 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 0 0.0376 0.0631 0.1025 0.1647 0.2476 0.3626 0.5216 0.7392 1.032 1.422 1.832 2.596 3.444 4.525 5.681 7.568 9.652 12.20 15.28 18.01 23.47 28.75 35.00 42.31 50.84- 1 0.0396 0.0660 0.1080 0.1716 0.2576 0.3764 0.5407 0.7648 1.066 1.467 1.882 2.672 3.543 4.647 6.034 7.758 8.885 12.48 15.83 18.42 23.88 29.33 35.88 43.11 51.78 in. Hg in. H20 in. Hg °F in. Hg in. Hg ' Z' " ' v& VAPOR PRESSURES OF WATER S^ In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.180 7.852 10.12 12.77 15.88 18.84 24.46 2942 3847 4342 52.70 3 0.0441 0.0728 0.1186 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.628 3.744 4.900 6.350 8.150 10.38 13.07 16.34 2027 24.97 30.82 37.07 44.74 5345 4 0.0463 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 0.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.87 54.82 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.680 8.557 10.86 13.67 17.07 21.14 26.00 31.75 38.80 46.41 5540 6 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.083 5.302 6.850 8.767 11.12 13.98 17.44 21.89 26.83 3248 3924 4727 56.60 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.981 11.38 14.30 17.82 2245 27.07 3342 3948 48.14 5741 8 0.0571 0.0932 0.1502 0.2292 0.3364 0.4858 0.6903 0.9666 1.335 •1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1821 22.52 27.62 33.87 40.78 4943 58.83 9 0.0598 0.0982 0.1567 0.2383 0.3493 0.5035 0.7144 0.9989 1.378 1.875 2.521 3451 4.408 5.732 7.384 9.424 11.92 14.98 1841 2249 28.18 3443 4142 4948 5047 ------- METHOD 18 FIELD DATA SHEET Plant: I Date: S-z^-vt L F c F c C L •m o 211 /o •ZS/ V> '301 30 i 3 ii Ht> '»' 60 ocation: AwnllU^y r ------- a D F umi^m ^mmm &9 Date: £ Location:. Run #:_? METHOD 18 FIELD DATA SHEET Tested Analyte:_ Orifice Tank #:. Stack I.P.: «? Pbar: 7.SV, ./^ Gauge Vacuum (Hg) i / I / , \ , Flow Setting / i* ,c /S^cc. /5«^<-' <a^ •^o e<_ ,io^c '^oct- T, Ti •\s -11 Traversa Point Number i 1 ^ V 5 (, 7 ? J 1 ^ «y 5 ^ 7 & ^ ift Valocity Htad in. H^ . zz , 3 / ,3V .36 .3? .31 . 3 \ , 28 , 23 t6 .2? .3/ 36 . i3 . 30 .21 <3£D Stack Tamp. °F Ti 13 13 IV 76 76 76 70 "70 1C 16 16 16 10 16 10 %^ ^?<> Md = (0.44 x %C02) i- (0.32 x %O2) -r (0.28 x :Md = (0.44X0 )f(0.32xz/ )* Md = Z °l •>.', HO % HO Ms = Mdxd • —} ~ 18 ( =— i00 100 Ts Ps R ( F «-460) ' .80 13.6 . 2V in. Hg SSSO 13.6 "\\|- Ts(°R) Vs " 85.49 x Cp x Vs - 85.49 x ( . \ Vs- 5 1 Ae - 1, / 3 «t' Qs » Vs x As x 60 s/m Qt- x Z.'3 < i «^ acfm PsxMs ft/a 2 x 60 P, %H,0 Qa .^= Q« x 17.647 x x (1 • £— std T§ 100 dadm 5-3 e. /( ------- f WET-BULB/DRY-BULB MOISTURE CALCUU\TION Plant: LASCL) Location: /-luYi/'^c, ^ Site: AiAlcdiOu^^ £#•* Operators: TA/ Run #: Barometric Pressure, in. Hg = Static Pressure, in. H0O = d. Absolute Pressure of Stack = Pbar + 9 13.6 Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of HpO at Tw (from Table) = (Ps - Pvw) x Vannr Prpeicnre nf H~O — Pun — lP\ntj\ $F-I2-^ Date: ^ Ph3r= Z ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: User, Samonng Location: Run #: ^ j l-> [ Date: S~^°) <* 7 CJTLT CIocx Time: Ooerators: Cfr/<7 Barometric Pressure, in. Hq: 3 «,. 3 6 Static Pressure, in. HpQ: -.fel Moisture. %: _J.L? Molecular wt.. Crv: Z^.SH Pilot Tube. CQ: «9<; Stacx Dimension, in. Diameter or Side 1: /5 Side 2: Wet Bulb. °F Dry Bulb. °F: Md • 00 too ' ' too p«->b -!£_..< 13.0 1 3.8 . f -»r-R) y PIXMI * Q«- o.. xOO ------- 300.: U4-4- uf-fe ; METHOD 18 FIELD DATA SHEE1 Plant: Lf>co Date: <& -5" -3i.^i Location- &°\ ct/«?o o^-vu) Run #: ^ - PumD/Rotometer #: Pt: Pretest (mm Hq): — Post-Test (mm Ha): Tt: Pretest (°R: — Post-Test (°F): Time: Start: "«* Finisn: l-2'-^ Total: 8 W/B: — D/B: - O«: >« CQ,:_Q r«/> 2 " 2 — Time o HoS 10 ii » <: >« \( 3-3 V (l b5 -» I! f-5 ^ H5s <<> \>ov Gauge Vacuum (HaL f>" 0 ' 0 & b 0 0 Flow j Setting \| g^rv-^l as. 1 5rt >-So 0-5o "V^o 'V- Md - (0.44 K%CO,) (0.32X%0,1 * (0.28 »%H-,\ WO Md » 10 44 x ^ (0.32 x (0.28 x "a H,0 100 too -2'5'1 Trav«n« Point Number A 1 Z 9. / h v«ioeny H««0 'n. H^O ' fa . ^ ^1 . fcl , (1 . ------- FIELD DATA SHEET Plant: MS °t> Sampling Location # Ps: -0.fc.fc «?-;l-3 Date: ^"-^'?-c»7 CO2 rf O2: > v Pretest Leak Rate: . oo\ cftn @ I/ in Pretest Leak Check: Pitol: I/ Orsat: " TlOWM Point Nwnta Sampling Tlrm (mln) O \|0 "Jo it> A.D OochTirm doe) V\\o<> ML5 \\7> V.lb5 \V^3 . Hg Probe Lenglh/Typ "•J Slack Diameler: e: ^-^ Pitol # \3" As: l.2<; '& Gaa MaUr %Y\ ^\°T V>i.°\ ^i^^ <2 Vo °\ ,gv«\ .<\^ Velocity rtoadlAp) inH2O s Oific* PIOCUI« Orft>i«nlial (AH) vi ftZO D«sii»d \| Actjal •'••'///''///Y//// 1 ^3 \^ Vvi H 1-3 \ J v.-l Stock Temp Pio '/////, •'/•" .... - Noule ID: Assumed Bws: _j Meter Box Thermocouple Filter #: Y: ^_.f/ Post Test Leak Rate: ^ cfm@ 3 in. Hg Post Test Leak Check. Pitol: >^Orsal: oVm= . . ------- no: Plant: Date: 5~- SAMPLE RECOVERY DATA Run No.: Sample Box No.: k/~ ^ Job No.: Sample Location: Sample Type: A Filter No.: Sample Recovery Person: Comments: FRONT HALF Acetone Container No.: Liquid Level Marked:. Filter Container No. L Sealed: Sealed: Description of Filter: Samples Stored and Locked: SACK HALF/MOISTURE Container No.: Liquid Level Marked:' Sealed: Ci?>.a IMP. NO. 1 2 3 4 5 6 CONTENTS Hio HID £»rT? Vt TOTAL Description of Impinger Catch: . INITIAL VOL (ml) Uo I Oo — ^b WEIGHT farams) INITIAL ecf/3< G3«.-y f^7. \| 7437 U^.7 FINAL } C^;.^ <IS f57,3 "7^0,$- O-VAJ- NET 4Z. 3.t , i- G.^ if? ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: id^o _ SOURCE/RUN #\JLl2^2- DATE: <-;?? "? ?- 1 . Leakage Correction for Volume Metered Vmc=( )-( -0.02) x( 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) 'Pbar-MAH/13.6)N vm^ = 17.64 xVmcxYx m mstd 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V.... = 0.04707 x (W. - W.) wstd r ' Vw = 0.04707 x( Iff. fl wstd Vwstd 4. Percent Moisture, by Volume V R wstd bws v + v wstd mstd BWS = . /fl ft ------- GAS VELOCITY AND VOLUMET-iC FLOW RATE Plant: Samoung Lccatton: Run Ooerators: G-C-J Date: f •Ji>n Clacx Time: /2 9-7 Barometric Pressure, in. Hq: l^.^p static Pressure, in. HoQ: — , 71 Moisture. %:_J^_ Molecular wt.. Crv: z.B^ Pilot Tube. CD: • 9 7 Stack Dimension, in. Diameter or Side i • I«S Side 2~ —» Wet Bulb. °F: £ v.tootv -••a n M.Q fcC, Dry Bulb. °F: Stack "•mo. 113 C7J- ici n/ I 1 I i • i0.44 Md • iO * • • tO.32 x %Ou) * ,0 28 x M,> (0.32 x ; - (0.28 X } - i H,O 100 • IB ( 100 P«-Pb +-!Z_-< 13.8 13. irw i»( IX ^ rt/( Q« Q8 •rf-- O« • 17.847 X —• «\| «B \|.g •^j- xirj4?>- xeo %H,O 100 m- 108 fiR ------- FIELD DATA SHEET Plant: L^co ^ ^bO.,--1? Sample Type: W-4- Operator: ££-» Sampling Location VV VO b««o oj<^«^ Pbar: ^.30 Run Number: \0-\1-\ Data: 5-}o,.<\1 CO2 b Ps: ^- t ^5 02: a \ Pretest Leak Rate: xt>oN cfm@ \J in. Hg Probe Length/Type: S_s Pilot fr^v^ Pretest Leak Check: Phot: (/ Orsal: jv TiavwM PoM NuntM fc lo 1-O ->o (0 ; 1 2. y 4. r $ i, * 5 ^ Sampling TbM (mlnj _5'^« ^^ V3^ 40(0 4lt» OochTirm (24-hcMjr dock) Gaa Metei JVm)«3 )"74 » 3 f^S -JSJ^b >> 1^0.^ O^f%. L. ^0(o,t^<\ >(\ Slack Diameter: Velocity inK2O 7/7^-" •>• i^ • i? , \|0 , "2-0 "^ i ~L] i ^-T- » ~ i-' , \ "> "^> IS As: t.23£f' Oillc« PieMuie OiHeiential Oasiied \| Actual Stack Temp fTs) nozzle ID: A"» Thernv Assumed Bws: J_ Meter Box #: (4- Filter 3couple (f : F . j'Lf ^ vc> s AH@: / X(> L Post Test Leak Rate: cfm @ 3 in. Hg. Post Test Leak Check: Pilot. //Orsat: "'-i lempeiabJie °F Prob« ] Filler Impingei T»mp °F • ''// S/-'/ /r/////// ''/'// //// ' ' //////•''/''/ 1 ^ l.V v.\ l.«i £e. 1.1 \-4 v.a u u- ^ ^>J" O-J-S _iio_ "> bl. ^3t >^n •v^ >i>3 --- _... . _.. ^0 4^y 51. T^> Dry Gas Meter Terry tilel Oudat (Tm out°F) '///// ''/////, ^0 ^0 ^ V <\V <\0 lvt) CVG ^^> Pump Vacuum Jin Hg 3 3 i ^" M \ 1.8 !• lm= - ------- PlantL Date: ' a SAMPLE RECOVERY DATA ; Run No.: k>~-^ Job No.: r\ c. - ' Sample Box No.: Sample Location: Sample Type: Filter No.: Sample Recovery Person: ^o Comments: FRONT HALF Acetone Container No.; Filter Container No.: Liquid Level Marked:. Sealed: Sealed: Description of Filter: Samples Stored and Locked: BACK HALF/MOISTURE Container No.: Liquid Level Marked: Sealed: IMP. NO. 1 2 3 4 5 6 CONTENTS fHo Hzo ^K ^(r TOTAL INITIAL VOL (ml) (0.0 \ 00 s. WEIGHT (aramsl INITIAL Co/.^ '^7 tfs ) mi i^« FINAL ^cO^o.T J?C,^ T^^f 7tio ^1.-, NET f« 2.; ,. "1-7 i,o Description of Impinqer Catch- ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: _Ljfe£ _ : _ SOURCE/RUN • ro-n-i DATE: <~ 1 . Leakage Correction for Volume Metered vmc=VO-p-La)xe Vmc=Vm-(Lp-0.02)x9 vmc=( )•( -0.02) x( ) w _ 5, Vfj ft3 vmc •'•'in - n 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) Pbar+(AH/13.6) /13.6) = 17.64 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V ... = 0.04707 x (W. - W. ) wstd f ' std std V = 0.04707 x( $ vw wstd 4. Percent Moisture, by Volume B - Vw5td BWS v ^T\T wstd mstd B - ws" (.I.IIIL )+( ------- go ko tf METHOD 18 FIELD DATA SHEET Plant: LASCQ Peppery Date: r-j<». o o Flow Setting 05 o% T-io Ho >So o-ro >-i 0 - ,^o Trovcra Point Numbar A / L 3 - J> 9 i %l • %> , >5 • » Y . >i . w AS ¥0 Stack T.mp. l^^ i-) \ t-\ > vl>J TV^ »0 Vix. » V %st 0--M VI ' >--s >b> 5 J Md - (0.44x%CO2) •)• Md - (O.4x ) + (0.32X + (0.28X ) Md- % H-0 % HO - — ) + 18 ( - — ) ,00 100 100 100 . ,28.71 T.- Pt-Pb+-±i^-( ) + 13.6 13.8 P«- ^9.J ------- GAS VELCcrry AND VGLUMET=;C FLOW RATE Plant: Usco p£f.Q..cT » Oate: j-.^o. 77 Sampling Location: jr /o Run #• I O I 1 - } CIocx Time: // / 2 & Barometric Pressure, in. Hg: ^ 3 o Ooerators:. ^Molecular wt.. Cry:. Moisture. %: StacK Oimensio'n. in. Di&ieter or Side 1 • /_$" Wet Bulb. °F: Static Pressure, in. HpQ: '— » Pilot Tube. Co: • Md • H.O x, H,O '00 i00 100 loo p«-?b JLL.-.< 1 3.8 1 3.8 -n.M« f A«. {. 3^. n2 x80 if °«-d- T« 100 X17«7K • ------- METHOD 18 FIELD DATA SHEET \(S, 9 \|\|C.O f Plant:. Date: Pbar: LAS v5"-Pq-l)7 Orific Tank • tiorv \O' 00^ QjtLT Pump/PntnmPter #: #: \Q-l-L-ii Pt: Pretest ( mm Hq): "" (I.D.: If ' Post-Test fmmHg): -~_ >1.3r> ^ Tt: Pretest <°FV ole Tube ators: e-WFtiii- mr\ Poct.Tp^t^R' — ^•. 7 Check: Pre: (/ Post:_L/ Time: Start: JJJ/ Finish: Ibi Total: Gft^ W/R n/R- — . 0^: P-/ CO~: O Gauge Time Vacuum (Hq) 1 6 0 H r. ° \ 9o D 1 %t 0 I +o 0 ^ + 0 / iti o • «!•» rav«r>« Point Jumb»r \| ? } f S 4 » » i * J i velocity H««d in. H^O . I«L ' 'T . id , 1 ? . M" . C , 1.4- . !--?_ . 1 V • ' ? . 1^ , -Li. x V^VW Flow Setting ^5b c t »• 9S0 OSc. 7^6 >.STv K 5-^6 — i K4- Stack T«mp. °F 73 y 3-3^ '^34 ">5^ >i6 ass ^3-«, 1-35 »& >31 »7 ^>1 "1-sa Md - <0.44x%CO2) * (0.32 x%02) -r (0.28x%^42) . .i, Md » (0.44 x )-f(0.32x )-t-(0.28x ) »„"••>••» ".HO "4 HO j^^l, - Mdx(l - -J-.) -18( -j^j- ) ^>3 Ma-Cl^ou )x(i • Z'^".. > - '6( Z"^" ) VW5»' a l ^toj 100 100 '4* Th^C' jSiyM-- ^B.05 W^Ts - ) !«»- °F ' Cl<- °R <°F * 460) c p 13.8 13.8 Ps- 1«\.>^ in-Hg — ^SP = F= il 'S(VR) V9 " 03.<»S X >-p X VA^ X U p, x Ms v.. ^yi-tf .t/. . A«- V» "2 Q« • Vs x Ai x 60 t/m Q»m x X 00 •2-5\2. Qa - f\jf ^ c. 1&,- acfm ^^^P, %M,0 °«.td= °* * ' 7-847 x T" x ° ' "T^" ' °%n- fI7-M7x x(1'"^ Q.^^HrJL.n, At ------- FIELD DATA SHEET Plant: Sampling Location & \fc k>o«o u.nu'C' Sample Type: /H - «)- Operator: Run Number: \O-\>" i.^ (,j< v.< • — • ... •>• — f 6 •> H J-i- ^3 y«= ^^ /S' ^c. Jt y.y J^6 Sr7 ? JS 3 3 ------- i Plant: SAMPLE RECOVERY DATA Run No.: "-^ Job No.: /O - Sample Box No.: Sample Location- Sample Type: 10 Filter No.: Sample Recovery Person: GC Comments: FRONT HALF Acetone Container NO.L Liquid Level Marked:. Rlter Container NO.L Sealed: Sealed: Description of Rlter: Samples Stored and Locked: BACK HALF/MOISTURE Container No.: Liquid Level Marked: Sealed: IMP. NO. 1 2 3 4 5 6 CONTENTS frUo MLO £/>?«< s/t TOTAL INITIAL VOL (ml) (oo '00 — >^0 WEIGHT tarams) INITIAL kok.Z- J?c.y ^1 7^3,0 ^ViV\ FINAL ^/Co or 7 t^c^ ^9-6 'VV^M NET ii « 1 v£ r.fc U-i Description erf Impinqer Catch- war ------- EPA METHOD 4 MOISTURE CALCULATIONS PUNT: U/fer D _ SOURCE/RUN #:_j£li^ DATE: 6-2<\-ci"} 1 . Leakage Correction for Volume Metered vmc=( )-( -0.02)x( ft3 2. Volume lyietered, Standard Conditions (68 F, 29.92 in. Hg) P+(AH/13.6)N = 17.64 Vm = 17.64 x(a.Mifc )x( ^U )x st sta dscf 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V ... = 0.04707 x (Wr - W. ) w f ' std Vw = 0.04707 x( std vw wstd 4. Percent Moisture, by Volume V -4- V wstd mstd B = ------- a DC METHOD 18 FIELD DATA SHEET Plant:. Date- - «-«»-» Tested Analyte:. Orifice Tank #:_ Location: Run#: Stack I.D.:_ Pbar: it. 32-" lio" Pump/Rotometer #:_ Pt: Pretest (mm Hg): n Sample Tube Operators: $• Post-Test (mm Hg): ;_ Tt: Pretest fF): L. Post-Test Leak Check: Pre: Post: Time: Start:o<^ Finish: o^scTotal: W/B: - D/B: - O9:j2/ Time 5. 03 177.1$ Gauge Vacuum (Hg) Vnr Trav«rs« Point Number Velocity Head in. H20 Flow Setting z./ Z-l CO2:_ o Md = (0.44 x %CO2) -i- (0.32 X %O2) -r (0.28 x %f^) Md = (0.44 x ) i- (0.32 x ) -i- (0.28 x ) % HO % HO Ms = Md x(1 • _) - 18 ( — 100 100 ^ Ms Ts- 100 100 Stack Temp. °F 7- SO S P JL^—" ps-Pb-i:l-=( 13.6 ) + 13.0 Ps = in. Hg — .IfTpRT Vs - 85.49 x Cp : Va - 85.49 x ( Vs- Aa- JSPx ^ MS ix( )x )f ft/8 Qs - Vs x As x 60 s/m Qa- x Qa - acfm Pa Qa . .= Qaxi7.647x atd T, x 00 too Qa X 17.647 X- dacfen • x (1 - ) ioa- ------- METHOD 18 FIELD DATA SHEET Date: £/ Location:_ Run #-. !&>- Tested Analyte:. Orifice Tank #:_ - R Stack I.P.: o-y Pbar:_z^i^_ Sample Tube #\ Operators:. " Pump/Rotometer #:_ Pt: Pretest (mm Hg): i_ Post-Test (mm Hg): ; Tt: Pretest fF): Post-Test fF)L Time: Start:/ ?s/ Finish: "" Total: Leak Check: Pre: Post: W/B: - D/B: J2- CO lo To 13 i\ Time i4oc> . oc Gauge Vacuum (Hg) Traverse Point Number Velocity Head Row Setting Zl SS Md = (0.44 x %CO2) -t- (0.32 X %O2) -r (0.28 x ' Md = (0.44 x ) -i- (0.32 x ) -t- (0.28 x ) C.C 30 Ms = Md x 1 1 r1o. HO %H2° — ) - 1 8 ( - 1 00 1 00 °IT_ Stack Temp. °F Ms = i TS- Ps = Pb Ps i x (1 l 00 100 13.6 13.6 in. Hg Ps x Ms Vs - 85.49 x ( ) x ( ) x Vs. ft/s AS- ft2 Qs » Vs x As x 60 s/m i Qs- Qs« x 60 acfrn Ps Qs .= Qs x 17.647 x -— x (1 8ld Ts 100 x 17.847 x- dsefm •x(1- ------- APPENDIX A. 1.14 Condition 13 (includes flows, moistures, and Method 18) ------- •j ag da GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Lt\S(.o Sampling Location: Run:, Date: -ZA-~I Clock Time: / J-T- Operators:. Barometric Pressure, in. Hg: 21 zo Static Pressure, in. HoO: .a Moisture, %: id Molecular wt., Drv: 27 7^ ^7 7i >7 "?7 ~77 "M 11 11 •)7 ?T 77 77 T) T) p- 11 Md - (0.44 x %CO.j) -I- (0.32 X %O2> Md - (0.44 x ) •)• (0.32 x ) + (0.28 x 10 Md- ^ 1 % HO % HO Ms- Mdx(1 • —) + 18 ( —) 100 100 M.-( )X,1.___)^,8(_^5- TS- 13.8 13-8 P.- '"-"a = J fsW X Vs - 85.48 x ( A«- /. Q« - Vt x As x 60 a/m o«- Pax Ms )M )x ^ xeo X 17.847 X- , d«dm :(1 100 ------- 3CC3 WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: L A °F )5 °F O.-Sw^V m. Ha 2800-(1.3xTw) Pva=( 2800-(1.3 x Proportion of Water Vapor by Volume = Bws (Ps) Tamp. OF 0 10 20 30 40 50 60 70 60 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 0 0.0378 0.0631 0.1025 0.1047 0.2478 0.3020 0.5218 0.7392 1.032 1.422 1.932 2.598 3.446 4.52S 5.681 7.569 9.652 1220 1529 19.01 23.47 28.75 35.00 4241 5044- 1 0.0398 0.0660 0.1080 0.1716 0.2578 0.3764 0.5407 0.7648 1.006 1.407 1.992 2.672 3.543 4.647 8.034 7.759 9.885 12.48 15.63 19.42 2346 2943 35.68 43.11 51.76 0.0133^ in. Hg ( ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0096 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.740 3.642 4.772 6.100 7.052 10.12 12.77 15.98 19.84 24.46 29.92 3647 43.92 52.70 3 0.0441 0.0728 0.1166 0.1878 0.2782 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.829 3.744 4.000 6.350 6.150 10.36 13.07 16.34 2027 24.97 30.52 37.07 44.74 534S 4 0.0463 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 0.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.87 54.62 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.8222 0.8750 1.213 1.000 2243 2.995 3.954 5.165 6.680 8.557 10.86 13.67 17.07 21.14 26.00 31.75 38.50 46.41 55.60 6 0.0517 0.0846 0.1370 0.2116 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.650 8.767 11.12 13.98 17.44 21.59 26.53 3248 3924 4727 56.60 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4688 0.0609 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 6.981 11.38 14.30 17.82 . 22.05 27.07 3342 3949 48.14 5741 a 0.0571 0.0932 0.1502 0.2292 0.3384 0.4858 0.6903 0.9686 1.335 1.810 2.440 3.259 4.289 5.565 7.202 9.200 11.65 14.62 1821 2242 27.62 3347 40.75 4943 5843 9 0.0598 0.0982 0.1567 0.2383 0.3403 0.5035 0.7144 0.9989 1.378 1.875 2.521 3.351 4.406 5.732 7.364 9.424 11.92 14.98 1841 2249 28.18 3443 4142 4943 5047 ------- Plant:. Date: >-7.-«7 METHOD 18 FIELD DATA SHEET Tested Analyte:__^t Orifice Tank #: Location- Au.w Run #' ME- il-v- Stack I.P.: /7.5 Pbar: 11.- Sample Tube #• e-/3~2A) Operators: T"fr Leak Check: Pre: Post: ' C-V7 /!• i;;; t- Pump/Rotometer #:_&£! Pt: Pretest (mm Hg): Post-Test (mm Hg):_ Tt: Pretest fF):_ Post-Test fF):_ /o je & Jb Time 7f C>«. /5 -)<30I ^7 1 ^02, :-1 'T & A iJ 7"1 1705. Tl ") yo-j, ci ") sol, zy Gauge Vacuum (Hg) I 1 I 1 1 1 I Flow Setting ,^t /rf»c /50« / 5»«- /S<> ^c. /fete /^»cc r^ 1C 10 12 •n Time: Start:/?? Finish:-7>7. Total: W/B: (,(. D/B: ?/ O2: -z./ C02: < Md = (0.44 x %C02) * (0.32 x %O2) T (0.28 x "/oN^ -Md = (0.44xc ) + (0.32X ( ) •>• (0.28 x 7 <5 ) Ms "I '2-7 Ms- Ts- ?/ :i H20 100 ) x(1 • % HO - — 100 ' ^j ) - 18 ( 100 100 °R(°F460) Traverse Point Number 1 t. > Y 5 & r 7 f j. 9 4f 5 fr 7 1 Velocity Head in. H;jO .zs . 20 .z 5 •2-f . 31 . 3 1 . JV .3T • U .25 .20 .•2.0 2."! • «fc. .J.T .25 Stack Temp. °F ^/ tl Si ft tl s\ fl 90 yo tl ?, f/ ti 10 // tl Ps - Pb f ^^- = (t9. L ) + __Jl 13.6 13.6 Ps- Z ------- Plant: Site: WET-BULB/DRY-BULB MOISTURE CALCULATION Location: h/f&tti Operators: - 13.6 Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw (from Table) = Pvw = (Ps - Pvw) x (AT) Vapor Pressure of H2O = Pva = (Pvw) • 2800-(1.3xTw) Pva =( )- ( 2800-(1.3 x Proportion of Water Vapor by Volume = Bws Ql__ (Pva) _ ( ; (Ps) T«mp. OF 0 10 20 30 40 50 60 70 80 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 0 . 0.0376 0.0631 0.1025 0.1647 0.2478 0.3026 0.5218 0.7392 1.032 1.422 1.932 2.596 3.446 4.525 5.881 7.569 9.652 1250 1559 19.01 23.47 28.75 3540 4241 5044- 1 0.0398 0.0660 0.1080 0.1716 0.2576 0.3764 0.5407 0.7648 1.066 1.467 1.992 2.672 3.543 4.647 6.034 7.759 9.885 12.48 15.63 19.42 23.96 2943 35.68 43.11 51.76 = Q.t>i^ ^ in. Hg ( ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1803 0.2077 0.3900 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 15.98 19.84 24.46 2942 3647 4942 52.70 3 0.0441 0.0728 0.1186 0.1878 0.27B2 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.629 3.744 4.900 6.350 8.150 10.36 13.07 16.34 2057 24.97 30.52 37.07 44.74 5345 4 0.0463 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 1031 9.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.57 54.62 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.680 8.557 10.66 13.87 17.07 21.14 26.00 31.75 38.50 48.41 55.60 6 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 44442 0.9040 1.253 1.712 2.310 3.081 4.063 5.302 6.850 8.767 11.12 13.98 17.44 21.59 2643 3248 3944 47.27 5640 7 0.0541 0.0692 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.785 2.379 3.169 4.174 5.442 7.024 8.981 11.38 14.30 17.82 22.05 27.07 33.02 3949 48.14 5741 8 0.0571 0.0932 0.1502 0.2292 0.3304 0.4858 0.6903 0.9666 1.335 1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1851 22.52 27.62 33.67 40.75 4943 5843 9 0.0596 0.0982 0.1567 0.2383 0.3403 0.5035 0.7144 0.9989 1.378 1.675 2.521 3.351 4.408 5.732 7.384 9.424 11.92 14.06 1841 2240 28.18 3483 4142 4043 5047 ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Sampling Location: /-');,, /3y^..--r Run #: <)£-'.V3 Date: - ^-c< 7 Clock Time: Operators : Barometric Pressure, in. Hg: 7-^- - Moisture, %: '-^ Molecular wt., Dry: 3? Static Pressure, in. HoQ: . Stack Dimension, in. Diameter or Side 1: »7. r • Wet Bulb. °F: 6# Dry Bulb, ° F: __ Pitot Tube, Cp: Side 2: TravcrM Point Number I 2 ->, 1 ? ir 7 r / 7 •v T 5 U ^7 t Velocity H««d in. H20 LZ- ,2C . Z.1 i-7 .30 - ^2. .W . 3>1 2.V .Z5 . 2_«S 16 15 ^: -2-1 .2.6 ^SF -.5220 Stack Tamp. °F S"2 cz S Z- £-2- ?z- fz. 1r^- f «- y. STi_ sz_ S'Z-- ^^ ^z. 9 a. S^^ S- ^ Md - (0.44 x %CO2) + (0.32 x %O2> + (0.28 x ntty Md - (0.44 x ^ ) ••• (0.32 x £/ ) + (0.28 x 7 ? ) Md - 2. V %HO M« - ( -? ? ) x (1 %H° 100 13.0 13.8 In. Hg — Ts Vt - 85.40 x Cp x Vs< A.- Pax Ms «/• .2 Q« - V«xA8XOO«/m C3»- x X80 p. — X 17.647 X- d«dm 7.2. A 100 ------- Plant: -:. Site: WET-BULB/DRY-BULB MOISTURE CALCULATION Loc^ion: /^Ar £A Operators: T&h< Run #: ^, ^ Date; Pbar = Pg = Ps = Tw = Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Pbar Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw (from Table) = Pw = (Ps - Pvw) x (AT) 0 . Vapor Pressure of H2O = Pva = (Pvw) - 2800 -(1.3xTw) Pva = ( j . (_ ; }_ 2800 -(1.3 x Proportion of Water Vapor by Volume = Bws Bws = T«m0. OF o 10 20 30 40 50 60 70 80 90 100 110 120 130 140 190 160 170 160 _190 200 210 229 290 240 0 0.0376 0.0631 0.1025 0.1647 0.2476 0.3626 0.5218 0.7392 1.032 1.422 1.032 2.596 3.446 4.525 5.881 7.569 9.852 12.20 15.28 19.01 23.47 28.75 35.00 42.31 5084- 1 0.0398 0.0660 0.1060 0.1718 0.2576 0.3764 0.5407 0.7648 1.066 1.487 1.992 2.072 3.543 4.647 6.034 7.7S9 9.885 12.48 15.63 19.42 23.86 29.33 35.68 43,11 51.76 in. Hg in. H20 in. Hg °F in. Hg in. Hg : : = _v_« — J_L- •• . i-- VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3906 0.5601 071 i ~ .75', .•: 1.1C2 1.513 2.052 2.740 3.S4? 4.772 0.1 60 7.982 10.12 12.77 15.98 1944 24.46 2942 3647 AM O4 4342 52.70 3 0.0441 0.0728 0.1186 0.1878 0.2762 0.4052 0.5802 0.8183 1.136 1.561 2.114 2.829 3.744 4.900 0.350 8.150 10.36 13.07 16.34 2027 24.97 30.82 37.07 44.74 5348 4 0.0463 0.0768 0.1248 0.1955 0.2891 0.4203 0.6009 0.8462 1.175 1.010 2.1.78 2.911 3.848 5.031 0.513 8.381 10.61 13.37 16.70 20.70 25.48 31.13 37.78 48.87 5442 5 0.0489 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2243 2.995 3.954 5.165 6.680 6.557 10.66 13.67 17.07 21.14 26.00 31.78 '38.50 4641 8840 8 0.0517 0.0646 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.083 5.302 6.650 8.767 11.12 13.98 17.44 21.59 26.53 3248 3924 4727 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4688 0.6669 0.9352 1.293 1.765 2.379 3.189 4.174 5.442 7.024 8.981 11.38 14.30 17.82 2245 27.07 33.02 3949 46.14 5741 g 0.0571 3.0932 0.1502 0.2292 0.3384 0.4858 0.6903 0.9666 1.335 1.819 2.440 3.259 4.289 5.585 7.202 9200 11.68 14.62 1821 2242 27.62 3347 40.78 4943 5843 g 0.0598 0.0982 0.1587 0.2383 0.3493 0.5038 0.7144 0.9989 1.378 1.878 2.821 3.381 4408 5.732 7.384 9424 1142 1446 1841 2240 28.18 3443 4142 404* 8047 ------- GBGJ METHOD 18 FIELD DATA SHEET Plant: t-Aito TesteH AnaiytP- A^_. Date: 5-n-«i Orificn Tank #• — ocation: «« »•.+ Pump/Rntnmeter #• t/os-f *J- Run #: te - i»— » R: Prefect (mm Hg); — Stack I.D.: 2 '«. ^ Vslocity H«ad in. HjO . «£ .»<• . .•<• 00 . 6"! -0T ,T .00 .* .0* .** ,01 .10 .+» .OS] .t>3 .OS ./o .60 • A3 75 7f 75 rr ?r -7^ 7* •»3 if 73 7* •7* 7V If •}£ 7f if 7t 7T IS 71 -^—^— e. f- Md - (0.44 x %CO2> + (0.32 X "fcOj) + (0.28 x %Nj) m utft _ in AA. » i j. (n a? x ) + <0 28 x ) Md - (f $1 % HO % HO j6 Mt.Mdx(1.-^r) + l8(-jS-) ^ Ma-< )x(1- '"^ )-H6(— — ) (7 ;. ^^ 100 100 J5^5' n0 Ma- ^B.b^ 7^> Ts- T-S' °F= 5!)^ °R(°F460) SP "~.0,^- D- _ nh I °'r' i / 1 i. 13.8 13.8 Ps- - 1\.l In. Hg JSp- -Mlb ^= J Ts <°R) vs - 09.4W x up x ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: Site: fcyry £ykitcsrt—Operators: Location: Run #: Date: Pbar + 1 3.6 Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw (from Table) = Pvw = —H (Ps - Pvw) x (AT) Pbar = Pg = Ps = Tw = Td = /D ZZz Vapor Pressure of H2O = Pva = (Pvw) - 2800-(1.3xTw) \rn- 2800.-(1.3 x Proportion of Water Vapor by Volume = Bws Q,.,_ (pva) _ ( .^» (PS) Temp. OF 0 10 20 30 40 50 60 70 60 90 100 110 120 130 140 1.50 160 170 180 190 200 210 220 230 240 0 0.0376 0.0631 0.1025 0.1647 0.2478 0.3626 0.5218 0.7392 1.032 1.422 1.932 2.596 3.440 4.525 5.881 7.569 9.652 12.20 15.29 19.01 23.47 28.75 35.00 42.31 50.04- 1 0.039S 0.0660 0.1060 0.1716 0.2578 0.3764 0.5407 0.7648 1.066 1.467 1.992 2.672 3.543 4.647 6.034 7.759 9.805 12.40 15.63 19.42 2346 29.33 35.08 43.11 51.76 in. Hg in. H20 :in. Hg °F in. Hg in. Hg ( ~l.&' ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 6.190 7.952 10.12 12.77 15.96 19.04 24.40 29.02 30.37 43.02 52.70 3 0.0441 0.0728 0.1186 0.1878 0.2782 0.4052 0.5802 0.6183 1.138 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.30 13.07 16.34 2047 24.97 30.52 37.07 44.74 53.65 4 0.0463 0.0768 0.1248 0.1955 0.2891 .£.4203 0.6009 0.8462 1.175 1.610 2.178 2.911 3.848 5.031 9.513 6.351 10.01 13.37 16.70 20.70 25.48 31.13 37.78 4547 54.62 5 0.0469 0.0810 0.1302 0.2035 0.3004 0^80 (Q&M. STSTSO 1.213 1.660 2.243 2.995 3.954 5.165 6.600 8.557 10.86 13.07 17.07 21.14 20.00 31.75 30.50 46.41 5540 6 0.0517 0.0646 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 6.850 8.707 11.12 13.98 17.44 21.50, 26.53* 3248 3944 4747 5640 7 0.0541 0,0892 0.1429 0.2203 0.3240 0.4686 0.6669 0.9352 1.293 1.705 2.379 3.169 4,174 £.442 ••".024 3.981 11.30 14.30 17.02 22.05 27.07 3342 3949 48.14 5741 8 0.0571 0.0932 0.1502 0.2292 0.3384 0.4858 0.6903 0.9660 1.335 •1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.02 1041 22.52 27.02 3347 40.75 4943 58.63 9 0.0598 0.0982 0.1507 0.2303 0.3493 0.5035 0.7144 0.9900 1.370 1.075 2.521 3.351 4.400 5.732 7.384 9.424 11.92 14.06 1841 2240 28.16 3443 4142 4043 5047 ------- 3BC3 ( GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: LfiM.o Date: 5-e.<»-c»n ling Location: A, fix,^ Clock Time: t^ * f. RB-/3-2. Operators: r«-/^X netric Pressure, in. h ure. %: 1.® q: j -T. ^ Static Pressure, in. HoO: — -. ^ 1 Molerularxwt Hrv- 29 Pilot Tube. CD: .99 Dimension, in. Diameter or Side 1 : 2 % " Side 2: 2v - 5ulb.°F: 6^ DrvBulb.Op. 7 <: v«rM olnt mb«r ( ? > V r 0 / X. I V f V ( X > f T V c i i V r c. Velocity H«ad in. H20 ^5 / o S o5 OS oO .& Is .01 0~7 ,0? .o5 o5 -oS , 08 o-I , oO .c>^ u£ • 0? .0* ,ol .0^ ,^5 ,<• .^f IT— --»/i. Stock T«mp. °F TT ^ ; + 1fl ( ... . 1 Ms- ( C-Y )X(1 ..^ I io( IQO i Mi- TS. ~>7 °F- S3S" °R (0F + 460) Po - Pb t S-P- , i 29. •» ) t- "' U 13.8 ' 13.8 Pa - 21./C- In. Hg JSP- .^G3 — / Ts (^R) . V«-(t».4UxUpx^P x \l P8XM8 Vn-nido-rr 991 )x( i^O-^txAl -^-JS V «. '6 « V« - / (, . 6r 8 ft/« A.. ^.6i n2 o«- x y.C~( xeo Q,. ^/&7/ cfm p, %K,0 Q.ftd-Q.xl7.e47x — x(1--j^-) •2^./Q 100 ONW- ------- WET-BULB/DRY-BULB MOISTURE CALCUU\TION Plant: L#3_o Site: &VM ^c^omj^r- Operators: Barometric Pressure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar + - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td • Tw = Saturation Vapor Pressure of H^O at Tw Vapor Pressure of H^O ~ Pva — (Pvw) • Pva={ }.( 1 Location: fof\ £vhaa TAfa Run #: 6E-&-2, Date: ; Phar= 2^-2, Pq= -a.u-i pg Pe= 2«-u< 13.b ,- T«/= lt» TH = ^S AT= 10 (fr«m Tahl°) = Pvw = ^ZZT- (Ps - Pvw) x (AT) 2800-(1.3xTw) .•5 ) x ( ) _arfT ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Date: 5 -z9-/>„> r- Clock Time: / -?? /:U7, nnoratnrs- 74/5.5 Barometric Pressure, in. H Moisture, %: \--» Stack Dimens Wet Bulb, °F: TrsvtrM Point Number i ^ V fj $ (j ( 2 } H 5 G I 2. "i H £• 6 i T- 5 ^ 5 6 q: Z^.Z. static Pressure, in. hUO: -.63 Molecular wt.. Drv: 2 V Pitot Tube, Cp: , If — •ion, in. Diameter or Side tii Dry E Vttooty H««d in. H20 - t>7 6'7 oG . 01 • 0T ,07 • 06. . 05 • oO .05 .05 ,c~> ,Cfe ,07 0^ G5 ;o5 .0? ,ofe .05" .C75 . OS .oS .Q0 ^F-,ZH6I Stack Tamp. °F 7L ~7U 70 7^ "> 0 "1C 7(, 7c 7lx ?C l_ 1C •76 -70 1C, ~?0 "7(/ 16 7C. 7^ 7c 7k ?(. 76 7i/ T:- 76 1- 2.8" Side 2: if " nlh,0p 7L Md - (0.44x%CO2) + (0.32X%02> -i- (0.28 X%^) Md-(0.44x<7 ) -t-(0.32x-I/ (+(0.28x7^ ) Md - Zf % H_O % HO M.-MUX(1 ' 10Q » ' 101 100 ' M.-e=L ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: I^A&t) Location: Site: &^ Date: 5--^ Pbar = 2A •* Pa = -• US -^2_ ps _ i. 15 1 T r ro— ' -^ 1 J.b Tw= UH Td= >^ AT= ^2. (from Table) = Pvw = O.^OOf (Ps - Pvw) x (AT) '-.?- in. Hg _ in. H.O 2 _ in. Hg °F °F °F in. Hg Pva=( ( 2800-(1.3 x Proportion of Water Vapor by Volume = Bws Bws = Tamp. "F 0 10 20 30 40 50 60 70 60 90 100 110 120 130 140 150 160 170 180 190 200 210 220 230 240 (Ps) 0 0.0378 0.0631 0.1025 0.1647 0.2478 0.3826 0.5218 0.7392 1.032 1.422 1.932 2.598 3.446 4.525 5.881 7.569 9.652 1250 1559 19.01 23.47 28.75 35.00 4241 5044- 1 0.0398 0.0660 0.1080 0.1716 0.2576 0.3764 0.5407 0.7648 1.066 1.467 1.992 2.872 3.543 4.647 6.034 7.759 9.685 12.48 15.63 19.42 2346 2943 35.68 43.11 51.76 in. Hg ( ) VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0696 0.1127 0.1803 0.2877 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 8.190 7.952 10.12 12.77 15.98 19.64 24.46 29.92 36.37 43.02 52.70 3 0.0441 0.0728 0.1188 0.1878 0.2762 0.4052 0.5802 0.8183 1.138 1.561 2.114 2.829 3.744 4.900 6.350 8.150 10.36 13.07 16.34 20.27 24.97 30.52 37.07 44.74 5345 4 0.0463 0.0768 0.1248 0.1955 02891 0.4203 0.6009 0.8482 1.175 1.610 2.178 2.911 3.848 5.031 6.513 8.351 10.61 13.37 16.70 20.70 25.48 31.13 37.78 45.87 54.62 5 0.0469 0.0810 0.1302 0.2035 0.3004 0.4359 0.6222 0.8750 1.213 1.660 2.243 2.995 3.954 5.165 6.680 8.557 10.86 13.67 17.07 21.14 26.00 31 .75 38.50 46.41 55.60 6 0.0517 0.0846 0.1370 0.2118 0.3120 0.4520 0.6442 0.9046 1.253 1.712 2.310 3.081 4.063 5.302 8.850 8.767 11.12 13.98 17.44 21.59 26.93 32.38 39.24 4757 56.60 7 0.0541 0.0892 0.1429 0.2203 0.3240 0.4680 0.8669 0.9352 1.293 1.765 2.379 3.169 4.174 5.442 7.024 8.981 11.36 14.30 17.82 22.05 27.07 33-02, 3949 48.14 5741 a 0.0571 0.0932 0.1502 0.2292 0.3384 0.4856 0.6903 0.9666 1.335 1.819 2.449 3.259 4.289 5.585 7.202 9.200 11.65 14.62 1851 2242 27.62 3347 40.75 4943 5643 9 0.0598 0.0962 0.1567 0.2383 0.3493 0.5035 0.7144 0.9989 1.378 1.875 2.521 3.351 4.406 5.732 7.364 9.424 11.92 14.96 1841 2249 28.18 3449 4142 4849 5947 ------- METHOD 18 FIELD DATA SHEET Plant: Lftsco C L F c F c C L &t£> o /»» ye iW > f&o id /»•• LJO A'° 7 •* Date: S-*- .ocation: fa Run #• rtF- Tested Analyte: vv ,.«. ?T Orificp Tank : — • //A- /TSI Pump/Rntometer #: ^»1 * "i- n-l' Pt: Pretp^T rmm Ha^: — Jtackl.D.: /17S Post-Test ( mm Ha^: — 3bar: 2* 20 Sample Tube Operators: 7 Tt: Pretest I°R: - -A .eak Check: Pre Time 2,5. OT> i^Cff, y$ 2362, /fl ^ / « 1 f Velocity Head in. H2O .23 Jf . J5 .3C. i 39 . 37 .35 ,t.1 ./ .1 3 21 . 31 . 3 Y .31 .JO . 2^/ • Stack Temp. °F 7t 7Z 73 73 76 76 •76. 7C. 76 •76 76 7C 76 7C 79 76 Vs • 85.49 x Cp x Vs - 85.49 x ( .77 ) X Vs- j7,^ tt/s As- 2. /3 ft2 Qs - Vs x As x 60 s/m Qa • x Qs» ^7^ 7 acfn1 Qa . ,= Qa x 17.647 x std T8 x 60 100 •atd- x 17.847 x- • x < 1 ) 100 ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: \| J^ffc Location: /Uvi' Site: /cvXfAW P^AJ Operators:-^ Run #: ArP-ftrt Barometric Pressure, in. Hg = Pbar = Static Pressure, in. H20 = Pg = - Absolute Pressure of StacK = Pbar + 3 Ps = Wet-Bulb Temperature, °F - Tw = ' Dry-Bulb Temperature, °F = Td = Temperature Difference Td - Tw = AT = Saturation Vapor Pressure of H~O at Tw (from Table) = Pvw = __D (Ps - Fvw) x (AT) 2 ' ' jy. 2800- (1.3 xTw) Pva=< ,-' .„...' "< } = ^ /AAx £«1U Date: 5"'Z1-^ ZA- 2- in. Hq ".QO in. HO ^•tq m. Ha J4 °F % °F 1 2. °F ,UO ------- 3 oca c=a GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: Sampling Location: Run# Date: Clock Time: /7/f Operators: Barometric Pressure, in. Hg: ^f. 20 Static Pressure, in. h^O: Moisture, %: !•> Molecular wt., Dry: 7* Pilot Tube, Stack Dimension, in. Diameter or Side 1: / ?. 7-5 Side 2: Wet Bulb, °F:___0_5_ TravarM Point Number 2'' DryBulb,°F: T{. Velocity H««d in. H2O .51 35 .3,1 Stack T«mp. °F •76 Ic 17 76 •76, •7C Md - (0.44 x %CQ2) + (0.32 X Md-(0.44xO )(0.32X + (0.28 X %Wj) •t-(0.28x7>' % H-O % HO P.. 13.8 13-8 2i i."f ft/t A.- , Qt - v« x A» x ao «/m 0.- x 2. /3 xeo .rf •to Qi xl 7.847 X %K,0 •• ^ 100 X 17.847 X- dtcfm 100 ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: LtS^^ Slte: AgXLLtoy.EAri Operators: Barometric Pressure, in. Hg = Static Pressure, in. H2O = Absolute Pressure of Stack = Pbar + Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H20 at Tw Vapor Pressure of H~O = pva = (Pvw) - Pva=( \ ( 2800 -1 1.3 Location: Aw/ft I//AL* Pi TAlys Run:.AP-tflu> Date:: Pbar= ^-2_ Pa= -O.fel HO -73-5- . Ps= 2-MH Tw = (D S Td = V^- AT= \~L- (from Table) = Pvw = £>• ^oi^Z. (Ps - Pvw) x (AT) 2SOO-(1.3xTw) )x( ) 0.44(02, x \ 5y» 5"-23- ------- J am da GAS VELOCITY AND VOLUMETRIC FLOW RATE Date: Clock Time: Plant: Sampling Location: A,A.\ Run #: PtP - 'V. Operators:^ Barometric Pressure, in. Hq: '.vi..i Static Pressure, in. H^O:^ Moisture, %:_±3- Molecular wt., Dry:^ Pitot Tube, Cp:. Stack Dimension, in. Diameter or Side 1: /•?• 7-5 Side 2: Wet Bulb. °F: C5" Dry Bulb, °F:. Trav«rM Point Number I 1 3 •Y 5 6 •7 7 / t. ^ f 5 6 "7 5 Velocity H«md In. H2O -IV ,3>j , 55 , 16 .3? ,S5 . 3^ , ^ «Z7 .2L5- ,25 -«,3 ,35" . 33 . iO i^l «P-.^% Stack T«mp. °F 7V -It 16 75 76 1-1 •?-? n -?6 75" 7C "76 nc 76, 16 ~>6 IS- 16 Md - (0.44 x %CO2) i- (0.32 X %O2) + (0.28 X %^) Md-(0.44xc )+(0.32xe/ )+ (0.28x77 'Md- 2. - Mdx(1 % HO - i-) 100 18 100 %H,0 '-^- .) + 18 ( 100 Ma- Tl- Ps - Pb •»• Pa- "F- S.P. 13.0 ) -t- 13.0 = .I fs(°R) Va - 85.40 x Cp x Vs - 85.40 x ( .77 ) x ( Va- PsxMa )x Q« - Vs x Aa x 00 a/m Qa- x 2. / 3 xeo 'Qaxl7.647x-^-x(1- _ ) Ta 100 °Vtd- OHM- X 17.047 X- 100 ------- WET-BULB/DRY-BULB MOISTURE CALCULATION Plant: LA^D Site: A(A~{ fa, £^, OoerarorR- Barometric Pres/ure, in. Hg = Static Pressure, in. H20 = Absolute Pressure of Stack = Pbar + - Wet-Bulb Temperature, °F = Dry-Bulb Temperature, °F = Temperature Difference, Td - Tw = Saturation Vapor Pressure of H2O at Tw Vapor Pressure of H~O = pva = /PWV, . Pva = t \ ( " Location: Au^llar^ (~i rate Run #: Af~ 15- b uate: j Pbar= 2.4.^ Pa= -D.^2. -±2_ PS- Z4 H 136 KS ~ l' Tw = ^ Td= >^ AT= U (from Table) = Pvw = O.UZ/i-l' (Ps - Fvw) x (AT) 2800-(1.3xTw) )< ) 0/5Qi,q- = ( ) (Ps) Tamp. OF o 10 20 30 40 50 60 70 00 90 100 110 120 130 140 150 160 170 180 _190 200 210 229 230 240 0 0.0376 0.0631 0.1025 0.1847 0.2478 0.3626 0.5216 0.7392 1.032 1.422 1.932 2.596 3.446 4.525 5.881 7.569 9.652 1240 1549 19.01 2X47 28.75 3540 4241 5044- 0.0398 0.0660 0.1080 0.1718 0.2576 0.3764 0.5407 0.7648 1.066 1.467 1.092 2.672 3.543 4.647 6.034 7.759 9.865 12.48 15.63 19.42 23.96 29.33 35.68 49.11 51.76 • . : = ^ » — v i ro VAPOR PRESSURES OF WATER In Inches of Mercury 2 0.0417 0.0696 0.1127 0. 1 803 0.2677 0.3906 0.5601 0.7912 1.102 1.513 2.052 2.749 3.642 4.772 040V* • 190 7.952 10.12 12.77 15.98 19.84 24.46 2942 ------- GAS VELOCITY AND VOLL'METr.iC FLOW RATE Plant: L Samoung LC Run #: 1 - cation: # \ ^utu C^T«.T COCK Time: ^P^ -* ~ 1 nnRrarors- Cr C* r Barometric Pressure, in. H Moisture. %: \| StacK Oimen Wet Bulb. °F T'«viM 3olm Numoac 1 1 3 3 _T t, I * > * s V. •^^— ^— -^^— . ^^•"•^•^••^B™ lg: 1 «r. Zp Static Pressure, in. HoO: — • 7Z. Molecular wt.. Drv: 'Z-^.MH Pilot Tube. Co: . 7 1 sion. in. Diameter or Side 1 : /£" Side 2: — • QrvHulhOc. — v«toeBv [ - — . -i ,H,Q 1 3tACk 1 "•mo. " • i I 6€ 1 /t.«J : . fci i no ! , c-7 1 H>- 1 , fy 1 Ur I7.T I?A — •— — «^« —— — — — s-n-o- Md - (0.44 I %CO,) » .0.32 X %O,) -r (0.28 X %hi,» Md • iO.4Ai ; » (0.32 X > - (0.20 « ) •«-?». 8 f ^ M,O S H,O Ml • Md 1 ( 1 . ^— — _ . - 1 fl ( _^_ ^ . 100 100 M««. ix(l. — ___..iai __-^ 10O 1OO M.. 3»'1l 71 - I-?T- °F- U3; °««°p-«a SD 13.8 iTi ?«- ">^,^ -"-HO VS? - _^ f "i fRl >..«a.4»Mua«<6P> .] p,^. V v«- 5<^. ------- METHOD 18 FIELD DATA SHEET Plant:. Date- c c Tested Anatyte:. Orifice TanK #:_ Location:_ Run #:__3_- c x n. « 7 Pump/Rotometer #: Pt: Pretest (mm Hg):. Stack I.D.: Pbar: TV Post-Test (mm Hg):_ Sample Tube #:jfe2±J Operators: Cc- Leak Check: Pre: Post: Time: Start: /£-v Finish: H3? Total: W/B: ^ D/B: ~ O2: » COC:1 GAS /««T<«- m, (o 1. HI — Time /bn Kf -7 'CJ~7 > 116? "s fill f nai nk nvl ^ ^~ Tr«v«r«« Point Numbvr A 1 > • •} 4. ^- fe A 1 > 3 4. j- 4> Gauge Vacuum (Hg) o 0 0 o 0 0 D <9 o ) 0 Velocity H«M m. H$,> ! >-o •^.^ - .no- Slack T«mp. °F M \l 1 £ C! \T J> 114- l 1J i T f 1 & ^ k'j ' It »T < VI V \ T n \T \ Vld • 10 44 x ) - (0 3 / % H O Kti Mt., )x<1- — ^^ ^ ilf%* M< " 7^^ •I^T,-!-)! °F-t> T '-$* S P ^r] p, — p)., ^ J'r- - ( 13.8 Vjp" = Vs • 6S 49 x Co x JAP x V« • 85.48 x ( V« • fSL^-^r f P nit fa flf ->!• V ' As » \ > V ft2 Qs » v« x As x 60 «/m Qs « x Qs » iJr'f^" ac* ^ p Qs ..-Osx 17.847 X — Q«.j- X17^ „... ^,-n... , _J,_ . .--!. .• ' ' - (0.32x%0.,) -. (0.28 (0.28 X 13.8 -s i^-R) )x( i xOO p, %H-0 -^— x(l • ^ 100: ------- FIELD DAT/WHEET Plant UK^CQ Sampling Location ^ °V Run Number: <\-\V> Date: S- ^=\-S1 Pretest Leak Rate: _.6«>l elm @ \5 in. Hg. Pretest Leak Check: Pitot: U Orsat: WN Sample Type: yn ~ \- Pbar:_ C02: Operator: O2: > I Probe Length/Type: Slack Diameter: \ Nozzle ID: K><^ Thermocouple #: Assumed Bws: _J Filter #: A<^ Meter Box #: ) <. Y:.%x AH@: I. %(>, Post-Test Leak Rate: Q cfm @ ^ in. Hg. As: Post-Test Leak Check: Pilot: Orsat: TNWWM Wnl Numtoi Samplm Thw (min) 0 IO 70 30 vo CkxdcFim* (244iour doc) lfci-7 It VI itn Hoi \1\T Goa Meter Readmg (Vm)tt3 <\Vl.^o ^^oA ^>lo °(^i ^4-3, CGt Velocity Head (Apl tnH2O Oifica Piesoute Oittorenttol (AH) in H2O Desired Actual Stack Temp. as) Temperature °F Probe Fitter Impinger Temp. °F Dry Gas Meter Temp Inlet (Tmin°F) Outlet (Tm out°F) Pump Vacuum (in. Hg) y////////y//////////////////////^^^^ - 14 v. i.tf u \.s \.H) /.^ I.* ^ " /— -^ — — - — - — "™ "" — <-Tr SI J~J. S3 Sf »f Xt % ------- Plant: l/laco Date: -T SAMPLE RECOVERY DATA ; Run No.: Sample Box No.: >°--5 Job No.: 3 fo-$"-«o3 Sample Location:. Sample Type: Filter No.: Sample Recovery Person: Comments: H6«97 FRONT HALF Acetone Container No.: Liquid Marked:. Filter/ ' Container No.: Sealed: Sealed: Description of Rlter: Samples Stored and Locked: BACK HALF/MOISTURE Container No.: Liquid Level Marked: Sealed: IMP. NO. 1 2 3 4 5 6 CONTENTS Mlo Hu> 6«,T-r ^/(r TOTAL INITIAL VOL (ml) «* \to — >.0 WEIGHT (arams) INITIAL GrC-o 07.7 4^t> 11?. <• WH.T FINAL tffil 07^ f9C£ 7^"f>-r \M« NET 3,7 , I ,-u j-.^ ^•\ Description of Impinqar Catch- • ------- J3OE3 EPA METHOD 4 MOISTURE CALCULATIONS PLANT: /.XfoO _ SOURCE/RUN #' °\-HJL DATE:_£lHlll 1 . Leakage Correction for Volume Metered vmc=sV(Lp-0.02)x0. Vmc=( )-( -0.02) x( 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) Pbar-MAH/13.6)N = 17.64 xVmcxYx 13.6V Vm mstd 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V ... = 0.04707 x (W. - W. ) wstd T ' Vw = 0.04707 x( ------- GAS VELOCITY AND VOLUMETriC FLOW RATE Plant: L/>5e^ Harp- T- ^P- » .0 20 X%N-,> Md - 10.44 • i - (0.32 X : - (0.2B X ) •»- )b^4- S M^O S H,O M« • Md > 1 1 • ' . - ' fl ( — — . IOO 100 M« - » ) K(I . . « IB ( , lOO 100 M.. >1--1^ ^. (I !> °F- S.i3 °a(°P.«OI e p 1 3.8 1 3-8 "•••'M.vv in-M9 ^. V..«5.4W«CO«^P « >J p,KM. V V. . S • ^> IM A.. V§OP> n2 Qt« vciAaieOMn Q«- x xeo Oa M • * ^k Aj^nt* 01 " o<(\d- •"•" __ %M_Q M W ?>** o« _-as«ir.64Tx— — « ------- METHOD 18 FIELD DATA SHEET Plant:. Date: Sc o Location- =» to OC.CA/ Run at: / 0- I b-l Stack I.D.: L Pbar: Sample Tube Operators: Leak Check: Pre: Post: n.oil i.1* 0 Gauge \/>0 Jii. 0 /G» 0 j-o H FIow Tested Analyte: ST? e'-lf Total: S_S W/B: - D/B: - O0: 2r vrrm^ pTv o^ Trev«ri« Point Number 1 ) ^ 4- J- fe I J> "i 4- J" L Velocity H««d •n.H^O . 1^ . 1 (, . fv , Isf . 1T^ , 7.3 . 1^ , T-O . ^-"L. , zo . i* , 'L'T- . ^riVU Slack T.mp. °P ^^^ ->-30 >5» 5--^ / T-3J" >e> 4 >3Z- •^^c >i£. 3 % 7 -"Sj7 T-T-O ^>>o Md - «0.44 x %CO=) - (0.32 X %02) - (0.28 X VoN;;) Md - 10.44 x j - (0.32 X . * (0.2B x ) 7$lu 'S H,0 "' H0 P8 in.Ha Vs - 65.49 x Co x Vs - 85.48 x ( =, x Ms )x( )x i A.- \.>> n Qi • V» x As x 60 t/m Q« . x Os- 1fl0 ------- FIELD DATA SHEET Plant: Lt\* c O Sa Samf Run^ Prete rfingLoc 4umber: si Leak P ation fl It) Ouu OuT4"^ Pb. io-13-1 Dale: 5" •>«* 9 "7 CO ate: , d0 / cfm @ l-S\n Pretest Leak Check: Pilot: / Oral: h :_ ^ ! i ;! >. 4". Tiav«rM Pofcil Numb* J Sampling Tbra 0 (0 «.o 3> 0 to OockTim. (24-houi dock) \^>0 IJT30 (S'fO U-fo \fet)0 Hg Prc .1 Sla GajMoUf Ftoadng JT^O ,7 O 9 5>58>5^> Q0C «A- cj^v , y> Q \| ^ 0"1 C V.kjcrty '///.'/• Sample Type: yv\-d Operator: Q C Ps: ^ , VS Noule ID: Assumed Bws: 02 Thermocouple Filler: AM Probe Length/Type: Stack Diameter: \| Meier Box: J4- Y: .'' Post Test Leak Rate: ° cftn @ ^ in. Hg Post Test Leak Check: Pilot: X'Orsal: t/«l OiiSc* Pl«»sur« Orttoicnbal (&H)inH2O Dasiid \| Actual Stack T«mp a»i lempeiatLirt °F Piob« \| Filur Impingai T»mp °F Dry Gas Metof Tamp kilat amin°F) Outlet (Tm out°F) Pump Vacuum (in.Hg) ''-'''//''////////////////•''/ : '///////////////. '////A •'///, i ^ l-T) !•» VI 1-^ _L-Z_ — _;-- 5-5 s* J- »- •i^ «t Pf i^_ ------- Plant; <-/>s c o Date: Z-W- t G.Q li-7 Description of Impinqer Catch! — ------- og EPA METHOD 4 MOISTURE .CALCULATIONS PLANT: l^Co _ SOURCE/RUN #:_ili£li_ DATE: 1 . Leakage Correction for Volume Metered vmc = Vmc=( )-{ -0.02) x( ft3 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) Pbar+(AH/13.6)\ Vmst(j= 17.64 xVmcxYx Vm = risrf mstd 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = VW = 0.04707 x (W.-W. ) wstd T ' V = 0.04707 x( std fstd 4. Percent Moisture, by Volume V,.. R °ws w / B WS" wstd mstd ( - ------- GAS VELOCITY AND VQLUMETF.iC FLOW RATE Plant: L * s c ^_ Samonng Location: a IQ ntitf, Date: j"-0 static Pressure, in. HpQ: —. 70 Moisture. %: /^2.-j2, Molecular wt.. Dry; ze.en Ptteat Tube. Co: .97 StacK Dimension, in. Diameter or Side i: Lf Side 2: — Wet Bulb. °F: Dry Bulb. °F: — M4-I0.44M '),-<0.32X >0.2B I %N,» -(0.20K - 78-^4- 100 too S H,O 100 • is r too P"PbTn- ------- GAS VELOCITY AND VOLUMETRIC FLOW RATE Plant: LA.S c Samoiing Location: j /n Ouet, „.,-, .T r io-tY. •». Date: CIocK Time: / .'/CT Ooerators: Cfc >.? static Pressure, in. Barometric Pressi^e. in. Hq: Moisture. %: /^, i.g Molecular wt.. Crv: 1Z.W Pilot Tube CD: .97 Stack Dimension, in. Diameter or Side 1 • / f _ Side 2' — _ Wet Bulb. °F: Dry Bulb. Qc. Md • io.44 • %CO.) * <0.32 X %O-l » i0.28 X %H,> Md • <0.44 • ; «• (0.32 X . . 40.28 X ) M« • Md K 1 1 M.O S H,O " i . I a ( ' 100 100 too 100 13.8 t3.8 • 05.481 Co * • 05.48 • I . I ~rm y PIKM« ) a I v • v > xflO %H;O too . K17JM7X' TRiu 103 ------- Plant Sampling Location H lo Run Number: lb-13^ 'Pretest Leak Rate: .cot Date elm Pretest Leak Check: Phot: 15 in. Hg. Orsat: rj> FIELD DATASHEET Sample Type: rn CO2: O O2: 1 I Probe Length/Type: Pilot Stack Diameter: If As: <. 2,j Nozzle ID: N» Assumed Bws: Meter Box #: >4- Post Test Leak Rate: Post-Test Leak Check: Pilot: // Orsat: Thermocouple Filter #: Y: A/I .AH@: O cfm in. TrawwM Point Numbw Sampling TbTM (mln) 0 10 7A ao 1* 1 OocfcTiriM (24-hour dock) Uo?- l«\|7- m>- V91>V \v^v Gas Mel«f Reading (Vm)«3 cf^s.i^ ^vu ^?.J o^.-b c\n^,\>s V.locrty HMd (Ap) inH2O Orifice Pr«Mur« Orfterantial (AH) in H20 Desired Actual Stack Temp. (Ts) Temperature °F Probe Filter Impinger Temp. °F Dry Gas Meter Temp. Wei (Tmin°F) Outlet (Tm out°F) Pump Vacuum (in. Hg) '//////// //////////////////y///////^/////////////// y//// •'///,-. u \ X l-?s \X l« (4 1.* l.W — brA lot C^ S-4- 3-^ S4- q.i M \0 ^0 9J ------- PlantL Date: SAMPLE RECOVERY DATA . Run No.: Job No.: - 3 Sample Box No.:. Sample Location- "^ >o. Sample Type: !ZL Filter No.: Sample Recovery Person: Comments: FRONT HALF Acetone Container No.; Liquid Level Marked:. Filter Container Sealed: Sealed: Description of Filter: Samples Stored and Locked: BACK HALF/MOISTURE Container No.: Liquid Level Marked:. Sealed: IMP. NO. 1 2 3 4 5 6 CONTENTS to a Ho £lpTMf * TOTAL INITIAL VOL (ml) (d<» I'o — . S& WEIGHT (arams) INITIAL e? 7 Gf34 f -T7. C, "&& .-r >A«s.> FINAL 6i3. t C4ij fJ"?7 7G3.^ >4-^l-t NET > '1 •\ ")> li-4- Description of Impinger Catch: ------- EPA METHOD 4 MOISTURE CALCULATIONS PLANT: MftO _ SOURCE/RUN #: JL±J_ DATE: 5-tf- 1 . Leakage Correction for Volume Metered Vmc=( )-( -0.02) x( 2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg) Pbar+(AH/13.6)N 17.64 xVmcxYx 2/4.2 Vm = - risrf mstd 3. Volume Water Vapor Collected, Standard Conditions Impingers & Silica Gel = V ... = 0.04707 x (W, - W. ) wstd T ' Vw = 0.04707 x( rstd rstd 4. Percent Moisture, by Volume R - UtAIC — ' Vwstd+ Vmstd o _ °WS" ------- Plant: LAS<-Q Date: £: - fl METHOD 18 FIELD DATA SHEET Tested Analyte: SViv Orifice Tank #: Location:. Run #: MDA- 13-1 Stack I.D.: Pbar: " i« Pump/Rotometer #: VQST Pt: Pretest (mm Hg): : Post-Test (mm Hg): ; Tt: Pretest (°F):_ Sample Tube #:. Operators: - i A B Post-Test fF):_ Leak Check: Pre: V Post: \/_ Time: StartifcB Finish: W/B: w D/B: - O2: CO Time 1 laoa.^ \|(oO-M ^ J /<,6 7. z$ 1too°! "S^ Uo/i ,S£ u/ s - n iudS-iM Gauge Vacuum (Hg) \ i { \ , 1 1 Flow Setting 2.1 TL\ "2 i •2-1 "2_! 2-1 -2.1 AO&, Traverse Point Number - Velocity Head in. HjO Stack Tamp. °F "JJ" ^ Jf ^^ Md = (0.44 x %C02) -t- (0.32 X %02) ^ (0.28 x Md - 10.44 x (0.32 X (0.28 : :'oH,0 %HO Ms = Md x ( 1 • - ^— ) - 1 8 ( - '. 1 00 1 00 Ms = ( Ms i x(1 • ) - 18 ( 100 100- Ts - F » y SP 1 p, = Pb + -±:i-=( 13.6 Ps = in. Hg .460) ) + 13.6 Vs- e Vs - 85.49 x I Vs- As- Ts(°R) ix( )x ^f ft/8 2 Qs - Vs x As x 60 s/m Qs- Qs- x 60 acfrn Qs std Qsx 17.647 x Ps Ts x(1 100 X 17.847 X- dsedn ------- APPENDIX A. 1.15 NDO Summary Data ------- PACIFIC ENVIRONMENTAL SERVICES, INC. Prepared By 3 3_ f Date Checked By ProiectN° Page of Client Location Date Sheet Title 500-70 400-500 £00 -lit) .£&?- -',?; : ------- O PACIFIC ENVIRONMENTAL SERVICES, INC. Project No. Client Location Page of / / Prepared By Date Checked By Date Sheet Title M&o-B ' 1130 - 3 x> -30 1733- ------- VCIFIC ENVIRONMENTAL SERVICES, INC. Project No. Page of Client ' LA sco Location /%. Drepared By 2 K. tJt Date Checked By Date Sheet Title V 0-2- Wi 30 j / //-/"". f-i. f 7 ^w P ------- E7 PACIFIC ENVIRONMENTAL SERVICES, INC. Project No. Page of i i Client Location Prepared By Date Checked By Date Sheet Title A/Do /% „/ ?* L* 7-1 7 VJb-A A/Do- B A/fio-c 7-3 2*0-130 ------- TECHNICAL REPORT DATA Please read instructions on the reverse before completing 1. REPORT NO. EPA-454/R-99-024a 4. TITLE AND SUBTITLE Air Emissions From Reinforced Plastics M Products: Volume I /i Volume I of III 2. anufacturing Process, LASCO Panel posJ-Vc 7. AUTHOR(S) Franklin Meadows Daniel F. Scheffel 9. PERFORMING ORGANIZATION NAME AND ADDRESS Pacific Environmental Services, Inc. Post Office Box 12077 Research Triangle Park, North Carolina 27709-2077 12. SPONSORING AGENCY NAME AND ADDRESS U.S. Environmental Protection Agency Office of Air Quality Planning and Standards Emissions, Monitoring and Analysis Division Research Triangle Park, North Carolina 277 1 1 3. RECIPIENT'S ACCESSION NO. 5. REPORT DATE August 1999 6. PERFORMING ORGANIZATION CODE 8. PERFORMING ORGANIZATION REPORT NO. 10. PROGRAM ELEMENT NO. 11. CONTRACT/GRANT NO. 68-D-70069 13. TYPE OF REPORT AND PERIOD COVERED Final 14. SPONSORING AGENCY CODE 15. SUPPLEMENTARY NOTES 16. ABSTRACT The United States Environmental Protection Agency (EPA) Emission Standards Division (BSD) requested that the EPA's Emissions Monitoring and Analysis Division (EMAD), Emission Measurement Center (EMC) provide testing support in the investigation of the reinforced plastics composite manufacturing source category to properly set the Maximum Achievable Control Technology (MACT) standards as required by the Clean Air Act Amendments of 1990. The reinforced plastics composite manufacturing process located at LASCO Panel Products in Florence, Kentucky was selected by the BSD as the host facility for this emissions testing program. The sampling program was designed to support the following ESD objectives: 1) Identify and quantify the hazardous air pollutants (HAPs) emitted by reinforced plastic manufacturing, 2) Identify the sources of HAPs and the total HAPs mass emission rates from the wet application area and the oven area, 3) Evaluate three ventilation scenarios, 4) Depending on the effectiveness of the industry proposed "closed" system, develope a performance-based emission limitation achieved by the use of a wet area enclosed table system, 5) Assess the existing emission factors for volatile organic compound emissions from a continuous lamination process for the purposes of updating the information in AP-42 and determining cost effectiveness for MACT options involving emissions abatement, and 6) Determine the effect of various process paramenters such as line speed, laminate thickness, HAP content of raw material and the addition of a gel coat layer on the emission factor. Sampling was performed during 13 process operating conditions. Measurements were made of the total hydrocarbons (THC), styrene, cumene, and methyl methacrylate (MMA), and the air flow rate at all enclosure exhausts. A secondary objective of the sampling program was to obtain the emissions of HAPs from the oven stacks. This volume (Volume I) is comprised of 464 pages and consists of the report text and Appendix A.I (Manual Methods Raw Field Data). 1 7. KEY WORDS AND DOCUMENT ANALYSIS a. DESCRIPTIONS Cumene Emission Measurements Hazardous Air Pollutants Lamination Process Methyl Methacrylate Reinforced Plastics Manufacturing Styrene Total Hydrocarbons Volatile Organic Compounds 18. DISTRIBUTION STATEMENT Unlimited b. IDENTIFIERS/OPEN ENDED TERMS 19. SECURITY CLASS (This Report) Unclassified 20. SECURITY CLASS (This page) Unclassified c. COASTI Field/Group 21. NO. OF PAGES -l^W-l/loH 22. PRICE EPA Form 2220-1 (Rev. 4-77) PREVIOUS EDITION IS OBSOLETE F:\U\FMeadows\TRD.Frm\WP 6.1 -------


United States
Environmental Protection
Agency
Office of Air Quality
Planning and Standards
Research Triangle Park, NC 27711
EPA-454/R-99-024a
August 1999
AIR
   ©EPA
   Air Emissions From
   Reinforced Plastics Composite
   Manufacturing Process
   LASCO Panel Products: Volume I
            •v^n^

-------
            FINAL REPORT

         AIR EMISSIONS FROM
  REINFORCED PLASTICS COMPOSITE
      MANUFACTURING PROCESS
       LASCO PANEL PRODUCTS

           VOLUME I OF III
            REPORT TEXT
            APPENDIX A.I
       EPA Contract No. 68D70069
        Work Assignment No. 2-10


              Prepared for:

       Mr. Solomon Ricks (MD-19)
        Work Assignment Manager
       SMTG, EMC, EMAD, OAQPS
    U.S. Environmental Protection Agency
     Research Triangle Park, NC 27711
              August 1999
               P:\i530\finrpt

              Submitted by

PACIFIC ENVIRONMENTAL SERVICES, INC.
      5001 South Miami Blvd., Suite 300
             PO Box 12077
      Research Triangle Park, NC 27709
             (919)941-0333
           Fax: (919)941-0234

-------
                                DISCLAIMER

      This document was prepared by Pacific Environmental Services, Inc. (PES) under
EPA Contract No. 68D70069, Work Assignment No. 2-10. This document has passed
PES' internal quality assurance review and has been approved for distribution.  The
contents of this document do not necessarily reflect the views and policies of the U.S.
EPA.  Mention of trade names does not constitute endorsement by the EPA or PES.
                                      n

-------
                     TABLE OF CONTENTS


VOLUME I                                               Page

1.0   INTRODUCTION	1-1

2.0   SUMMARY OF TEST RESULTS 	2-1

     2.1   EMISSIONS TEST LOG	2-1
     2.2   PROCESS LINE RESULTS	2-4
     2.3   TOTAL TEMPORARY ENCLOSURE - METHOD 25A
           TOTAL HYDROCARBON RESULTS 	2-5
     2.4   TOTAL TEMPORARY ENCLOSURE - VOLUMETRIC AIR
           FLOW RATE RESULTS 	2-5
     2.5   TOTAL TEMPORARY ENCLOSURE - METHOD 18 RESULTS . . 2-5
     2.6   OVEN NOS. 9 AND 10 - METHOD 25A TOTAL
           HYDROCARBON RESULTS  	2-23
     2.7   OVEN NOS. 9 AND 10 - VOLUMETRIC FLOW RATE
           RESULTS 	2-23
     2.8   OVEN NOS. 9 AND 10 - METHOD 18 HAP RESULTS 	2-23
     2.9   UNCATALYZED RESIN (UCR) AND GEL COAT
           SAMPLE RESULTS	2-23
     2.10  RESPONSE FACTOR RESULTS  	2-41
     2.11  METHOD 204 TOTAL TEMPORARY ENCLOSURE
           VERIFICATION	2-41

3.0   PROCESS DESCRIPTION	3-1

4.0   SAMPLING LOCATIONS	4-1

     4.1   MAIN EXHAUST STACK	4-1
     4.2   ROOM EXHAUST STACK	4-1
     4.3   AUXILIARY EXHAUST STACK	4-4
     4.4   NATURAL DRAFT OPENINGS	4-4
     4.5   OVEN EXHAUST NO. 9 AND NO. 10	4-4
                             in

-------
                   TABLE OF CONTENTS (Continued)
5.0    SAMPLING AND ANALYTICAL PROCEDURES 	5-1

      5.1    LOCATION OF MEASUREMENT SAMPLE/VELOCITY
            TRAVERSE POINTS 	5-1
      5.2    DETERMINATION OF STACK GAS VOLUMETRIC
          •  FLOW RATE	5-1
      5.3    DETERMINATION OF DRY MOLECULAR WEIGHT 	5-4
      5.4    EXHAUST GAS MOISTURE CONTENT	 5-4
      5.5    DETERMINATION OF HAZARDOUS AIR POLLUTANTS 	5-4
      5.6    DETERMINATION OF TOTAL HYDROCARBONS 	5-6
      5.7    DETERMINATION OF VOLATILE MATTER CONTENT,
            DENSITY, VOLUME OF SOLIDS, WEIGHT OF SOLIDS,
            WATER CONTENT, AND HAPS BY DISTILLATION	5-6
      5.8    RESPONSE FACTORS FOR FLAME IONIZATION
            ANALYZERS 	5-10

6.0    QUALITY ASSURANCE/QUALITY CONTROL  	6-1

      6.1    CALIBRATION OF APPARATUS	6-1
      6.2    ONSITE QA/QC 	6-3

      APPENDIX A - RAW FIELD DATA

           Appendix A.I Manual Methods Raw Field Data

           A. 1.1  Method 1 Field Data Sheets (includes flows, moistures, and
                 Method 18)
           A. 1.2  Condition 1 (includes flows, moistures, and Method 18)
           A. 1.3  Condition 2 (includes flows, moistures, and Method 18)
           A. 1.4  Condition 3 (includes flows, moistures, and Method 18)
           A. 1.5  Condition 4 (includes flows, moistures, and Method 18)
           A. 1.6  Condition 5 (includes flows, moistures, and Method 18)
           A. 1.7  Condition 6 (includes flows, moistures, and Method 18)
           A. 1.8  Condition 7 (includes flows, moistures, and Method 18)
           A. 1.9  Condition 8 (includes flows, moistures, and Method 18)
           A. 1.10 Condition 9 (includes flows, moistures, and Method 18)
           A. 1.11 Condition 10 (includes flows, moistures, and Method 18)
           A. 1.12 Condition 11 (includes flows, moistures, and Method 18)
           A. 1.13 Condition 12 (includes flows, moistures, and Method 18)
           A. 1.14 Condition 13 (includes flows, moistures, and Method 18)
           A. 1.15 NDO Summary Data

                                 iv

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                    TABLE OF CONTENTS (Continued)


VOLUME II

            Appendix A.2 Instrumental Methods Raw Field Data

            A.2.1  TTE Static Pressures
            A.2.2  Method 25A Calibration Data
            A.2.3  Condition 1 Method 25A
            A.2.4  Condition 2 Method 25A
            A.2.5  Condition 3 Method 25A
            A.2.6  Condition 4 Method 25A
            A.2.7  Condition 5 Method 25A
            A.2.8  Condition 6 Method 25A
            A.2.9  Condition 7 Method 25A
            A.2.10 Condition 8 Method 25A
            A.2.11 Condition 9 and 10 Method 25A
            A.2.12 Condition 11 Method 25A
            A.2.13 Condition 12 Method 25A
            A.2.14 Condition 13 Method 25A
            A.2.15 Conditions 1-13 Method 25A Strip Charts
            A.2.16 Oven Nos. 9 and 10 Method 25A

VOLUMEIII

      APPENDIX B - ANALYTICAL DATA

            B. 1   Method 18 Analytical Data
            B.2   Method 18 GC Chromatograms

      APPENDIX C - CALCULATIONS

      APPENDIX D - QA/QC DATA

      APPENDIX E - PROJECT PARTICIPANTS

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                             LIST OF TABLES


VOLUME I                                                            Page

Table 1.1     LASCO Panel Products Test Matrix	1-6

Table 2.1     Emission Test Log, LASCO Panel Products, Florence, Kentucky ....  2-2
Table 2.2     TTE Total Hydrocarbon Mass Emission Rate Summary	2-6
Table 2.3     Summary of TTE Stack Gas Conditions, and THC Concentrations
             and Mass Emission Rates, Condition 1 - May 14,1997  	2-8
Table 2.4     Summary of TTE Stack Gas Conditions and THC Concentrations -
             Condition 2 - May 14,1997	2-9
Table 2.5     Summary of TTE Stack Gas Conditions and THC Concentrations -
             Condition 3 - May 15,1997	2-10
Table 2.6     Summary of TTE Stack Gas Conditions and THC Concentrations -
             Condition 4 - May 15,1997	2-11
Table 2.7     Summary of TTE Stack Gas Conditions and THC Concentrations -
             Condition 5 - May 19,1997	2-12
Table 2.8     Summary of TTE Stack Gas Conditions and THC Concentrations -
             Condition 6 - May 19,1997	2-13
Table 2.9     Summary of TTE Stack Gas Conditions and THC Concentrations -
             Condition 7 - May 20,1997	2-14
Table 2.10   Summary of TTE Stack Gas Conditions and THC Concentrations -
             Condition 8 - May 22,1997	2-15
Table 2.11   Summary of TTE Stack Gas Conditions and THC Concentrations -
             Condition 9 - May 22,1997	2-16
Table 2.12   Summary of TTE Stack Gas Conditions and THC Concentrations -
             Condition 10 - May 22, 1997	2-17
Table 2.13   Summary of TTE Stack Gas Conditions and THC Concentrations -
             Condition 11 - May 23,1997	2-18
Table 2.14   Summary of TTE Stack Gas Conditions and THC Concentrations -
             Condition 12 - May 29,1997	2-19
Table 2.15   Summary of TTE Stack Gas Conditions and THC Concentrations -
             Condition 13 - May 29,1997	2-20,
Table 2.16   TTE Mass Rate Summary - Styrene, Methyl Methacrylate, and
             Cumene by EPA Method 18 	2-21
Table 2.17   Ovens 9 and 10 THC Mass Emission Rate Summary	2-24
                                     VI

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                        LIST OF TABLES (Concluded)

Table 2.18    Summary of Oven Stack Gas Conditions and THC Concentrations
              and Mass Emission Rates, Condition 1 - May 14,1997  	2-26
Table 2.19    Summary of Oven Stack Gas Conditions and THC Concentrations
              and Mass Emission Rates, Condition 2 - May 14,1997  	2-27
Table 2.20    Summary of Oven Stack Gas Conditions and THC Concentrations
              and Mass Emission Rates, Condition 3 - May 15,1997  	2-28
Table 2.21    Summary of Oven Stack Gas Conditions and THC Concentrations
              and Mass Emission Rates, Condition 4 - May 15,1997  	2-29
Table 2.22    Summary of Oven Stack Gas Conditions and THC Concentrations
              and Mass Emission Rates, Condition 5 - May 19,1997  	2-30
Table 2.23    Summary of Oven Stack Gas Conditions and THC Concentrations
              and Mass Emission Rates, Condition 6 - May 19, 1997  	2-31
Table 2.24    Summary of Oven Stack Gas Conditions and THC Concentrations
              and Mass Emission Rates, Condition 7 - May 20,1997  	2-32
Table 2.25    Summary of Oven Stack Gas Conditions and THC Concentrations
              and Mass Emission Rates, Condition 8 - May 22,1997  	2-33
Table 2.26    Summary of Oven Stack Gas Conditions and THC Concentrations
              and Mass Emission Rates, Condition 9 - May 22,1997  	2-34
Table 2.27    Summary of Oven Stack Gas Conditions and THC Concentrations
              and Mass Emission Rates, Condition 10 - May 22, 1997 	2-35
Table 2.28    Summary of Oven Stack Gas Conditions and THC Concentrations
              and Mass Emission Rates, Condition 11 - May 23,1997		2-36
Table 2.29    Summary of Oven Stack Gas Conditions and THC Concentrations
              and Mass Emission Rates, Condition 12 - May 29,1997 	2-37
Table 2.30    Summary of Oven Stack Gas Conditions and THC Concentrations
              and Mass Emission Rates, Condition 13 - May 29,1997 	2-38
Table 2.31    Ovens 9 and 10 Mass  Emission Rate Summary - Styrene,
             Methyl Methacrylate,  and Cumene by EPA Method 18 	2-39
Table 2.32    Summary of Response Factor Results - Styrene Bag Standards	2-42

Table 5.1     Sources, Test Parameters, and Methods Summary
             LASCO Panel Products - Florence, Kentucky	5-2

Table 6.1     Summary of Temperature Sensors Calibration Requirements	6-2
Table 6.2     Summary of Calibration Results for THC Analyzers
             Condition Nos. 1-13,  LASCO Panel Products	6-5
Table 6.3     Summary of EPA Method 18 Quality Assurance Results
             Styrene Recovery Efficiencies	6-7
Table 6.4     Summary of Desorption Efficiencies	6-7
                                     vn

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                              LIST OF FIGURES
VOLUME I                                                              Page

Figure 1.1     Key Personnel and Responsibility for Testing at LASCO
             Panel Products	1-2
Figure 1.2     Overview of Sampling Locations 	1-5

Figure 2.1     Diagram of Temporary Total Enclosure	2-43

Figure 4.1     Main Exhaust Sample Location	4-2
Figure 4.2     Room Exhaust Sample Location	4-3
Figure 4.3     Auxiliary Exhaust Sampling Location	:	4-5
Figure 4.4     Natural Draft Opening Sampling Location	4-6
Figure 4.5     Oven No. 9 Schematic of Sampling Location	4-7
Figure 4.6     Oven No. 10  Schematic of Sampling Location	4-8

Figure 5.1     Schematic of EPA Method 4 Sampling Train	5-5
Figure 5.2     Schematic of EPA Method 18 Sampling System -
             Sorbent Tube Method  	5-7
Figure 5.3     Schematic of Methane/Ethane Sampling System	5-8
Figure 5.4     EPA Method 25A Total Gaseous Organic Analyzer and
              Sample System	5-9
Figure 5.5     Schematic of Bag Standard Preparation System	5-13
                                     vm

-------
                              1.0 INTRODUCTION
       The U.S. Environmental Protection Agency (EPA) Emission Standards Division
(ESD) requested that the EPA's Emissions Monitoring and Analysis Division (EMAD),
Emission Measurement Center (EMC) provide testing support in the investigation of the
reinforced plastics composite manufacturing source category to properly set the
maximum achievable control technology (MACT) standards as required by the Clean Air
Act Amendments of 1990.  The sampling program was conducted through EPA Contract
No. 68D20162, Work Assignment No. 4-05. Figure 1.1 represents the test program
organization and major lines of communication.

       The reinforced plastics composite manufacturing process located at LAS CO Panel
Products in Florence, Kentucky was selected by the ESD for this emissions testing
program for the following reasons:

       1.      The lamination process (resin and gel coat application areas) is contained
              in a single room. This room can be treated as a total enclosure with slight
              modifications.

       2.      The process line can accommodate a wide variety of operating conditions
              to simulate worst case production plus the gel coating conditions.

       3.      The facility was willing to assist with the sampling effort.  The "Wide
              Line" lamination table currently has an enclosure around the wet
              application areas (resin and gel coat) which controls organic emissions and
              vents to the roof exhaust.

       4.      The facility was willing to conduct a careful mass balance (using special
              scales to weigh raw materials and final product) to determine emissions
              during the tests so that the mass balance technique could be compared
              against stack measurements.
                                       1-1

-------
LASCO Panel Products

    Hilary North
   (606)371-7720
        PES
    QA/QC Officer

  Jeffrey L. Van Atten
    (703) 471-8383
 Pretest Site
  Survey

   PES
Site Specific
 Test Plan

   PES
                       EPA/EMC
                Work Assignment Manager

                     Solomon Ricks
                     (919) 541-5242
                                                 PES
                                           Program Manager

                                             John Chehaske
                                             (703) 471-8383
                         PES
                    Project Manager

                      Dan Scheffel
                     (513)489-6611
Field Testing
                                                  PES
                                             Subcontractors

                                                DEECO
Analyses
                                                                            PES
                                              EPA/ESD
                                           Work Assignment

                                        Madeleine L. Strum, PhD
                                            (919)541-2383
                                                                  ESD Contractor
                                                                      PES
                                                                  Project Manager
                                                              Kenneth R.Meardon, PhD
                                                                  (919)941-0333
  Report
Preparation

   PES
                                                    Subcontractors

                                                       DEECO
                                                Enthalpy Analytical. Inc.
  Figure 1.1 Key Personnel and Responsibility for Testing at LASCO Panel Products

-------
The sampling program was designed to support the following BSD objectives:

1. Identify and quantify the hazardous air pollutants (HAPs) emitted by
reinforced plastic manufacturing.

2. Identify the sources of HAPs and the total HAPs mass emission rates from
the wet application area and the oven area.

3. Evaluate the following ventilation scenarios:

• The current enclosure of the wet application area which is referred
to as "current."

• The current enclosure disconnected and turned off, where there is
no capture of emissions in the wet application areas. This is
referred to as "open."

• Enclosure of all wet application areas, or as much as is possible,
with the current exhaust fan disconnected. This is referred to as
"closed." (In the original test plan, this condition was referred to
as WAE.)

4. Depending on the effectiveness of the industry proposed "closed" system,
develop a performance-based emission limitation achieved by the use of a
wet area enclosed table system.

5. Assess the existing factors for volatile organic compound emissions from
a continuous lamination process for the purposes of updating the
information in AP-42 and determining cost effectiveness for MACT
options involving emissions abatement.

6. Determine the effect of various process parameters such as line speed,
laminate thickness, hazardous air pollutant content of raw material and the
addition of a gel coat layer on the emission factor. Monitor and record
related process and operating information to support the establishment of
the emission limit and the assessment and development of emission
factors.

The primary objective of the testing program was to obtain total HAPs emitted
from the lamination line and resin/gel coat usage rates to develop emission factors. The
emission factors (pounds of HAPs emitted per pound of HAP used) were developed for a
variety of process conditions. Sampling was performed during 13 process operating
conditions. Measurements were made of the total hydrocarbons (THC), styrene, cumene,
1-3

-------
and methyl methacrylate (MMA), and the air flow rate at all enclosure exhausts. It should
be noted that styrene and cumene were originally expected to account for more than 99
percent (%) of the total HAP emissions and were the compounds of primary interest. The
measurement of MMA was not part of the original test plan, but was added while onsite,
after it was discovered that MMA may account for higher percentages of the HAP content
depending on the type of product produced. The secondary objective of the sampling
program was to obtain data on the emissions of HAPs from the oven area.

      PES utilized the support services of two subcontractors to provide sampling and
analytical support for this test program. Enthalpy Analytical, Inc. performed EPA
Method 24 analyses on resin samples, analysis of HAP content of resin samples and
vacuum distillations of several different resin samples. DEECO provided onsite gas
chromatography HAP analysis of sorbent tube samples, spike tube preparations,
ethane/methane analysis of oven bag samples and continuous measurements of total
hydrocarbons on the oven exhausts and natural draft openings (NDOs). Figure 1.2
presents an overview of the sample locations at the LASCO site. Included in the diagram
are the following locations: main exhaust, room exhaust, auxiliary exhaust, natural draft
openings (A, B, C, and D) and ovens 9 and 10. Sample locations are described in detail
in Section 4.0.

      Table 1.1 summarizes the test matrix for the test program.

      In addition to this introduction, this report contains the following sections:

      2.0    SUMMARY OF RESULTS
      3.0    PROCESS DESCRIPTION
      4.0    SAMPLING LOCATIONS
      5.0    SAMPLING AND ANALYTICAL PROCEDURES
      6.0    QUALITY ASSURANCE/QUALITY CONTROL PROCEDURES AND
             RESULTS

      APPENDICES
             A.   RAW FIELD DATA
             B.   ANALYTICAL DATA
             C.   CALCULATIONS
             D.   QA/QC DATA
             E.   PARTICIPANTS
                                    1-4

-------
                 Flow
                 Out
                  i
                o
          Oven 10
                 (    J Oven 9

                   t
      NDO-B
Flow In
NDO-C
I
                 Flow
                 Out
             Flow
              In
                      NDO-A
                I  Flow In
                        Process
                          Line
              Temporary Total Enclosure
                               Flow Out
                                  Flow In

                                  NDO-D
                                               Auxiliary Exhaust
                                                Flow Out
                                               Room Exhaust
                                 Main Exhaust
              Figure 1.2 Overview of Sampling Locations
                              1-5

-------
            TABLE 1.1
LASCO PANEL PRODUCTS TEST MATRIX
Sample Location
Main Wide Line
Exhaust
Room Exhaust
Auxiliary Exhaust
Natural Draft
Openings A, B, C, D
Oven Exhaust No. 9
Oven Exhaust No. 10
Resin Holding Tanks
Number of Test
Conditions
13
13
2
13
13
13
13
Sample Type
THC
Styrene, Cumene, MMA
THC
Styrene, Cumene, MMA
THC
Styrene, Cumene, MMA
THC
Styrene, Cumene, MMA
THC
Styrene, Cumene, MMA
Methane/Ethane
THC
Styrene, Cumene, MMA
Methane/Ethane
Volatile content, solids,
water, density
HAPS
Sampling Method
EPA 25A
EPA 18
EPA 25A
EPA 18
EPA 25A
EPA 18
EPA 25A
EPA18
EPA 25A
EPA 18
EPA 18
EPA 25A
EPA 18
EPA 18
EPA 24
EPA 18
Analytical Method
FIA
GC/FID
FIA
GC/FID
FIA
GC/FID
FIA
GC/FID
FIA
GC/FID
GC/FID
FIA
GC/FID
GC/FID
Gravimetric
GC/MS
Contractor (Subcontractor)
PES
PES (DEECO)
PES
PES (DEECO)
PES
PES (DEECO)
DEECO
PES (DEECO)
DEECO
PES (DEECO)
(DEECO)
(DEECO)
PES (DEECO)
(DEECO)
(Enthalpy)
(Enthalpy)

-------
2.0 SUMMARY OF TEST RESULTS
This section provides summaries of the test results obtained from the testing
program at LASCO Panel Products. The primary focus of the sampling effort was to
measure THC concentrations and calculate mass emission rates from the temporary total
enclosure (TTE). Also included are the results of the tests conducted for styrene, MMA,
cumene, ethane and methane. The ethane and methane data was only collected from the
oven areas to account for emissions as a result of poor burner efficiency. The oven data is
included and was a secondary objective of this field effort to evaluate HAP emissions
from the oven area. The resin analysis for VOC, water, solids, density and HAPs are not
included in this report. The resin results and process data are contained in the ESD Test
Reports.
2.1 EMISSIONS TEST LOG

Sampling was conducted during the period of May 14 through May 29,1997.
Table 2.1 summarizes the emissions test log. Presented in the table are the condition
numbers, test runs, dates, sample locations, pollutants and process conditions. Each
condition number correlates to a variation in process conditions, which included
CURRENT, OPEN, CLOSED, and variations in product, line speed, and panel thickness.
The following is a general description of the three room conditions that were examined
during this sampling program. For each of the three conditions, the process room was
treated as a TTE with all the access doors closed and NDOs minimized. The negative
static pressure in the room was maintained at -0.004 inches of water or greater.

The current condition was the operation of the process line the normal way it
operates each production day. The main exhaust system is exhausting air emissions from
the table area to the main roof exhaust stack. The table area is covered partially. Most
top areas of the table are covered with panels and side areas mostly open. The initial
resin application area is partially closed, with some panels open. The sampling areas
consisted of the Main Exhaust which normally draws emission directly from the wet
application area, the Room Exhaust which draws fugitive emission from floor level in
one corner of the room, four natural draft openings (NDOs), and Ovens 9 and 10 exhaust
stacks.
2-1

-------
                                          TABLE 2.1
                                     EMISSION TEST LOG
                                   LASCO PANEL PRODUCTS
                                    FLORENCE, KENTUCKY
Condition No.
1
2
3
4
5
6
Run No.
1,2,3
1,2,3
1,2,3
1,2
1,2,3
1,2,3
Date
5/14/97
5/14/97
5/15/97
5/15/97
5/19/97
5/19/97
Sample Location
Main Exhaust
Room Exhaust
NDOs
Oven 9 & 10
Resin Tank
Main Exhaust
Room Exhaust
NDOs
Oven 9 & 10
Resin Tank
Main Exhaust
Room Exhaust
NDOs
Oven 9 & 10
Resin Tank
Main Exhaust
Room Exhaust
NDOs
Oven 9 & 10
Resin Tank
Main Exhaust
Room Exhaust
NDOs
Oven 9 & 10
Auxiliary
Main Exhaust
Room Exhaust
NDOs
Oven 9 & 10
Pollutant
THCa, C8H8b,
THC, C8H8,
THC, C8H8,
THC, CH4C, C2H6d,C8H8
HAPS, Solvent, Moisture, Density
THC, C8H8,
THC, C8H8,
THC, C8H8,
THC, CH4, C2H6, C8H8
THC, C8H8,
THC, C8H8,
THC, C8H8,
THC, CH4, C2H6, C8H8
THC, C8H8,
THC, C8H8,
THC, C8H8,
THC, CH4, C2H6, C8H8
THC, C8H8,
THC, C8H8,
THC, C8H8,
THC, CH4, C2H6, C8H8
THC, C8H8,
THC, C8H8,
THC, C8H8,
THC, CH4, C2H6, C8H8
Process Condition
Current
+Gelcoat Application
Tank Supplied
0.06" panel
38.5% HAP with MMA
Current
+ Gelcoat Application
Used totes
0.045" panel
38.8% HAP with MMA
Current
No Gelcoat
0.09" panel
45.2% HAP without MMA
Current
No Gelcoat
Increased line speed to 18 fpm
0.09" panel
45.2% HAP without MMA
Open
No Gelcoat
Removed metal panels and one glass
panel.
Disconnected exhaust line on table.
84 minute samples
0.06" panel
40.5% HAP with MMA
Current
No Gelcoat
0.06" panel
40.5% HAP with MMA
N)
to

-------
                                                                  Table 2.1 (Concluded)
Condition No.
7
8
9
10
11
12
13
Run No.
1,2,3
1,2,3
1
1
1,2,3
1,2,3,4
Void No. 2
1,2,3
Date
5/20/97
5/22/97
5/22/97
5/22/97
5/23/97
5/29/97
5/29/97
Sample Location
Main Exhaust
Room Exhaust
NDOs
Oven 9 & 10
Main Exhaust
Room Exhaust
NDOs
Oven 9 & 10
Main Exhaust
Room Exhaust
NDOs
Oven 9 & 10
Main Exhaust
Room Exhaust
NDOs
Oven 9 & 10
Main Exhaust
Room Exhaust
NDOs
Oven 9 & 10
Main Exhaust
Room Exhaust
NDOs
Oven 9 & 10
Auxiliary Exhaust
Main Exhaust
Room Exhaust
NDOs
Oven 9 & 10
Auxiliary Exhaust
Pollutant
THC,CgH8,
THC, C8H8,
THC, C8H8,
THC, CH4, C2H6, C8H8
THC, C8H8,
THC, C8H8,
THC, C8H8,
THC, CH4, CjH^, C8H8
THC, C,H8,
THC, C8H8,
THC, C8H8,
THC, CH4, C2H6, C8H8
THC, C8H8,
THC, C8H8,
THC, C8H8,
THC, CH4, C2H6, C8H8
THC, C8H8,
THC, C8H8,
THC, C8H8,
THC,CH4,C2H6,C8H8
THC, C8H8)
THC,C8H8,
THC, C8H8,
THC, CH4, C2H6, C8H8
THC,C8H8,
THC, C8H8,
THC, C8H8,
THC, C8H8,
THC, CH4, C2H6, C8H8
THC, C8H8,
Process Condition
Current
No Gelcoat
0.075" panel
40.5% HAP with MMA
Current
No Gelcoat
0.06" panel
42.4% HAP without MMA
Current
No Gelcoat
0.09" panel
42.4% HAP without MMA
Current
No Gelcoat
0.1 29" panel
39.5% HAP without MMA
Current
No Gelcoat
0.09" panel
39.5% HAP without MMA
Open
No Gelcoat
Panels removed
System opened up
Auxiliary fan on
0.09" panel
45.2% HAP without MMA
Closed
No Gelcoat
Panels all in place
Additional panels + plastic used to
enclose all table "wet" areas
Auxiliary Fan on
0.09" panel
45.2% HAP without MMA
to
U)
          • Total hydrocarbon concentration measured by EPA Method 25A.
          bStyrene concentration measured by EPA Method 18.
          'Methane concentration measured by EPA Method 18.
          d Ethane concentration measured by EPA Method 18.

-------
       The open condition involved the removal of panels and enclosures covering the
wet application area of the line. The top panels and hinged access panels were removed
or opened where possible. The Main Exhaust duct was disconnected so there was no air
being pulled directly from the table area. The Main Exhaust pickup lines were all closed
(knife dampers closed) and the pickup lines disconnected and taped off. The Main
Exhaust fan continued to draw fugitive emissions from above the table area. Thejorjen
condition was to simulate uncontrolled emissions from the table area. The Auxiliary
Exhaust was operated during the open condition so that pressure negativity could be
maintained in the room. The sampling areas consisted of the Main Exhaust, Room
Exhaust, Auxiliary Exhaust, three NDOs, and Ovens 9 and 10 exhaust stacks.

       The closed condition was the operation of the line with everything covered and
panels in place on the process line.  The Main Exhaust line was disconnected so there was
no air flow being pulled directly from the table area. The Main Exhaust pickup lines
were all closed (knife dampers closed), and the pickup lines disconnected and taped off.
Additional rigid panels were placed on any open areas on the top and sides of the table
area. The rigid panels were taped closed where possible. Areas where rigid panels could
not be used were covered with foil-faced foam insulation board and taped shut.  The table
area was estimated to be 98% covered. The Auxiliary Exhaust was operated during the
closed condition so that pressure negativity could be maintained in the room. The
sampling areas consisted of the Main Exhaust, Room Exhaust, three NDOs, and Ovens 9
and 10 exhaust stacks.

       During all process conditions (current, open, and closed), the production room
was treated as a TTE. All air THC concentrations entering the room enclosure and
exiting the room enclosure were measured continuously by EPA Method 25A. A more
detailed description of the process conditions is presented in Section 3, Process
Description.
2.2    PROCESS LINE RESULTS

       The room containing the process line was treated as a TTE. The TTE enabled
sampling all HAP concentrations entering and leaving the enclosure for the purpose of
determining total HAPs emitted from the process line. The TTE is described in detail at
the end of this section. The emission points sampled were the following:  main exhaust,
room exhaust, auxiliary exhaust, and NDOs A, B, C and D.  Sampling at the emission
points was conducted using EPA Methods 1-4,18 and 25A to determine stack gas
velocity, temperature, molecular weight, moisture content, styrene/MMA/cumene
concentrations and THC concentrations. Typically, three 60-minute sample runs were
conducted for each process condition sampled. Sample run times were modified
dependent on process material production rates.
                                       2-4

-------
2.3 TOTAL TEMPORARY ENCLOSURE - METHOD 25A TOTAL
HYDROCARBON RESULTS

Table 2.2 presents the THC mass emission rate summary for data collected at the
TTE locations. The THC mass rate data represents emissions collected using EPA
Method 25 A. The THC mass rate data was calculated using styrene response factors to
adjust all data to a styrene basis. The calculated overall THC mass emission rate from the
TTE exhaust was determined by adding the THC mass emission rates from the Main
Exhaust, Room Exhaust and Auxiliary Exhaust, and subtracting the THC mass emission
rates from NDOs A, B, C and D. Conditions 1 and 2 showed the highest THC mass
emission rates which represented a "current" condition with the gel coat line in operation.
The gel coat line was expected to increase THC mass emission rates. The lowest THC
mass emission rates were measured during Condition 13 which was the "closed"
condition. Concentrations and mass emission rates were consistent during each sample
condition.
2.4 TOTAL TEMPORARY ENCLOSURE - VOLUMETRIC AIR FLOW RATE
RESULTS

Tables 2.3 through 2.15 present volumetric flow rate data and THC concentration
and mass emission rate data collected at the TTE sites. Each table of results represents a
sample condition, 13 total conditions were sampled. The sampling sites consisted of the
main exhaust, room exhaust, auxiliary exhaust and NDOs A, B, C and D. One
volumetric flow rate was performed for each sample run at each location. Flow
conditions were very consistent over the sample program.
2.5 TOTAL TEMPORARY ENCLOSURE - METHOD 18 RESULTS

Table 2.16 presents the Method 18 results measured at the TTE sample locations.
One sample run for styrene, cumene, and MMA was performed for each sample condition
(or 1 run per 3 Method 25 A sample runs). The Method 18 data was collected as support
for the THC results and as an indicator of the amount of styrene and cumene present at
each sample location. The measurement of MMA was not part of the original test plan
but was added while onsite. Initial estimates of the HAPs present was that the MMA
would account for less than 0.2% of the total HAP content from the process line and was
not a compound of concern. While onsite, it was discovered that MMA may account for
higher percentages of the HAP content depending on type of product produced. At this
point it was decided to measure MMA along with the styrene and cumene HAPs being
measured. It should be noted that recovery efficiencies for the MMA were consistently at
70% (70 -130% were the acceptable ranges). The Method 18 laboratory results were
adjusted for recovery efficiencies.
2-5

-------
                     TABLE 2.2
TTE TOTAL HYDROCARBON MASS EMISSION RATE SUMMARY"
                                           LASCO Panel Products
Condition
No.
1
1
1
Run
No.
1
2
3
Average
2
2
2
1
2.
3
Average
3
3
3
1
2
3
Average
4
4
4
1
2
3
Average
5
5
5
1
2
3
Average
6
6
6
1
2
3
Average
NDO Total,
Ib/hr*
0.38
0.34
0.34
0.35
0.64
0.66
0.69
0.66
0.65
0.64
0.64
0.64
0.80
0.80
NA
0.80
0.18
0.18
0.18
0.18
0.20
0.20
0.20
0.20
Main Exhaust,
Ib/hi*
70.44
59.32
56.62
62.13
56.92
55.50
55.34
55.92
18.22
17.59
16.74
17.52
18.34
18.37
NA
18.35
11.24
10.00
9.70
10.31
21.40
21.20
21.59
21.40
Room
Exhaust,
Ib/hr"
13.11
11.13
11.47
11.91
10.51
15.11
14.85
13.49
3.88
4.50
4.42
4.27
3.69
4.04
NA
3.87
3.53
3.98
4.02
3.85
5.42
5.03
3.94
4.80
Auxiliary
Exhaust,
Ib/hr"
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
NA
5.02
4.70
4.79
4.84
NA
NA
NA
NA
NA
Total Overall
Enclosure Exhaust,
lb/hrd
83.17
70.11
67.75
73.68
66.79
69.95
69.50
68.75
21.45
21.45
20.52
21.14
21.23
21.61
NA
21.42
19.61
18.51
18.32
18.81
26.62
26.03
25.33
25.99
                         2-6

-------
                                  TABLE 2.2 (Concluded)
Condition
No.
7
7
7
Run
No.
1
2
3
Average
8
8
8
1
2
3
Average
9

10

11
11
11
1

1

1
2
3
Average
12
12
12
1
2
3
Average
13
13
13
1
2
3
Average
NDO Total,
Ib/hr"
0.14
0.14
0.14
0.14
0.47
0.47
0.46
0.47
0.18

0.21

0.28
0.27
0.28
0.28
0.88
0.88
0.85
0.87
0.77
0.76
0.77
0.77
Main Exhaust,
Ib/hi*
18.12
21.69
22.20
20.67
15.98
16.08
17.18
16.41
15.53

15.28

14.11
14.35
14.13
14.20
8.96
7.42
7.05
7.81
4.59
4.34
4.42
4:45
Room
Exhaust,
Ib/hi*
3.28
3.63
3.38.
3.43
6.65
6.44
5.01
6.04
2.61

2.12

3.81
3.03
2.99
3.28
4.86
4.32
3.97
4.38
3.16
3.25
3.34
3.25
Auxiliary
Exhaust,
Ib/hr"
NA
NA
NA
NA
NA
NA
NA
NA
NA

NA

NA
NA
NA
NA
6.05
4.89
4.71
5.22
4.11
3.89
4.11
4.04
Total Overall
Enclosure Exhaust,
Ib/hr4
21.26
25.18
25.44
23.96
22.17
22.06
21.73
21.99
17.96

17.19

17.64
17.11
16.84
17.20
18.98
15.75
14.88
16.54
11.08
10.72
11.11
10.97
a Oven emissions are not included in this table.
b Pound per hour, total of four natural draft openings as styrene equivalent.
c Pound per hour, as styrene equivalent.
d Pound per hour, Enclosure exhaust adjusted for NDO contribution as styrene equivalent.
                                                2-7

-------
                                                            TABLE 2.3
     SUMMARY OF TTE STACK GAS CONDITIONS, AND THC CONCENTRATIONS AND MASS EMISSION RATES
                                                  CONDITION 1 - MAY 14,1997
                                                                                                                    LASCO Panel Products
to
00
Run No.
Time
Stack Gas
Velocity,
fps>
Volumetric Flow Rate
acfmb
dscfm"
Temperature,
op
Moisture,
%
THC Concentration
ppm, wef1
ppm
.dry"
ppm, as styrenef
Mass Rate,
Ib/hr"
Main Exhaust
1
2
3
1034-1134
1225-1325
1546-1646
Average
37.22
33.83
31.62
34.22
3729
3390
3168
3429
3378
3030
2804
3071
92
91
93
92
1.6
3.5
4.1
3.1
2965.4
2730.4
2798.6
2831.5
3013.6
2829.4
2918.2
2921.0
1284.7
1206.2
1244.0
1245.0
70.44
59.32
56.62
62.13
Room Exhaust
1
2
3
1034-1134
1225-1325
1546-1646
Average
Run No.
1
2
3
Average
18.86
17.28
17.82
17.99
5281
4838
4993
5037
NDO-A(-)
Velocity,
fpm"
275
235
230
247
Flow Rate,
cfm1
7334
6267
6134
6578
Cone,
ppm wetd
6.1
5.0
6.9
6.0
4886
4483
4644
4671
78
81
79
79
1.9
1.6
1.6
1.7
NDO-B (-)
Velocity,
fpmh
550
600
600
583
Flow Rate,
cfin'
138
150
150
146
Cone,
ppm wef1
NA
6.0
6.0
6.0
380.5
353.2
351.3
361.7
387.9
358.9
357.0
367.9
165.3
153.0
152.2
156.9
NDO-C (+) Forced Makeup Air
Velocity,
fpmh
263
230
240
244
Flow Rate,
cfm1
665
582
607
618
Cone,
ppm
wef1
15.9
NA
3.0
9.5
13.11
11.13
11.47
11.91
NDO-D (+) Forced Makeup Air
Velocity, Flow Rate,
fpmh cfm1
210 531
200 506
200 506
203 514
Cone,
ppm
wef1
15.9
NA
3.0
9.5
1 Feet per second.
b Actual cubic feet per minute.
c Dry standard cubic feet per minute.
d Part per million, wet basis as propane equivalent.
e Part per million, dry basis as propane equivalent.
' Part per million as styrene equivalent based on styrene response factor.
B Pound per hour.
k Feet per minute.
1 Cubic feet per minute.

-------
                                                                   TABLE 2.4
to
                             SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                                         CONDITION 2 - MAY 14,1997
                                                                                                                           LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps"
Volumetric Flow Rate
acfmb
dscfrtf
Temperature,
op
Moisture,
THC Concentration
ppm, wet*
ppm, dry*
ppm, as
styrenef
Mass Rate,
Ib/hr8
Main Exhaust
1
2
3
2020-2125
2155-2255
2337-0038
Average
34.87
33.70
36.20
34.92
3494
3377
3628
3500
3173
3105
3333
3204
92
89
89
90
1.5
0.8
0.9
1.1
2553.6
2562.8
2378.0
2498.1
2592.5
2583.5
2399.6
2525.1
1105.2
1101.3
1022.9
1076.5
56.
55.
55.
92
50
34
55.92
Room Exhaust
1
2
3
2020-2125
2155-2255
2337-0038
Average
Run No.
1
2
3
Average
17.86
19.16
19.45
18.82
5001
5369
5450
5273
NDO-A (-)
Velocity,
fpmh
225
235
225
228
Flow Rate,
cfiri
6000
6267
6000
6089
Cone,
ppm
wef1
5.7
4.5
30.1
13.4
4637
4983
5062
4894
82
82
81
82
1.1
1.0
1.1
1.1
NDO-B (-)
Velocity,
fpm"
450
350
550
450
Flow Rate,
cfm1
113
88
138
113
Cone,
ppm
wef1
NA
NA
4.4
4.4
324.1
433.9
419.4
392.5
327.7
438.3
424.1
396.7
139.7
186.8
180.8
169.1
NDO-C (+) Forced Makeup Air
Velocity,
fpmh
265
260
260
262
Flow Rate,
cfiri
670
658
658
662
Cone,
ppm wetd
1.6
2.9
5.4
3.3
10.
15.
14.
51
11
85
13.49
NDO-D (+) Forced Makeup Air
„ . .. Flow
Velocity, _ .
fpm" Rf?
v cfm1
200 506
210 531
260 658
223 565
Cone,
ppm wetd
1.6
2.9
5.4
3.3
      • Feet per second.
      b Actual cubic feet per minute.
      c Dry standard cubic feet per minute.
      d Part per million, wet basis as propane equivalent.
      * Part per million, dry basis as propane equivalent.
f Part per million as styrene equivalent based on styrene response factor.
8 Pound per hour.
h Feet per minute.
1 Cubic feet per minute.

-------
                                                             TABLE 2.5
                       SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                                   CONDITION 3 - MAY 15,1997
                                                                                                                     LASCO Panel Products
(0
o
Run No.
Time
Stack Gas
Velocity,
fps8
Volumetric Flow Rate
acfmb
dscflnc
Temperature,
op
Moisture,
%
THC Concentration
ppm, wef1
ppm, dry"
ppm, as
styrene'
Mass Rate,
Ib/hr*
Room Exhaust
1
2
3
1425-1525
1559-1659
1735-1836
Average
37.65
36.41
36.36
36.81
3772
3648
3643
3688
3526
3414
3424
3455
80
80
80
80
1.0
0.9
1.1
1.0
739.2
738.1
698.6
725.3
746.7
744.8
706.4
732.6
318.3
317.5
301.1
312.3
18.22
17.59
16.74
17.52
Room Exhaust
1
2
3
1425-1525
1559-1659
1735-1836
Average
Run No.
1
2
3
Average
18.76
18.60
18.71
18.69
5255
5213
5241
5236
NDO-A (-)
Velocity, Flow Rate,
fpmh cfm'
225 6000
240 6400
230 6134
232 6178
Cone,
ppm wef1
12.0
15.1
11.3.
12.8
4961
4950
4974
4962
75
75
76
75
0.8
0.9
0.8
0.8
NDO-B (-)
Velocity,
fpmh
650
650
650
650
Flow Rate,
cfiri
163
163
163
163
Cone,
ppm wef1
12.3
1.8
8.3
7.5
112.2
130.1
127.5
123.3
113.1
131.3
128.5
124.3
48.2
56.0
54.8
53.0
NDO-C (+) Forced Makeup Air
Velocity, Flow Rate, Cone,
fpmh cfin1 ppm wef1
245 620 0.6
240 607 1.8
240 607 2.8
242 611 1.7
3.88
4.50
4.42
4.27
NDO-D (+) Forced Makeup Air
Velocity,
fprn"
260
250
260
257
Flow Rate,
cfnY
658
633
658
650
Cone,
ppm
wef1
0.6
1.8
2.8
1.7
* Feet per second.
k Actual cubic feet per minute.
c Dry standard cubic feet per minute.
d Part per million, wet basis as propane equivalent.
c Part per million, dry basis as propane equivalent
f Part per million as styrene equivalent based on styrene response factor.
' Pound per hour.
h Feet per minute.
' Cubic feet per minute.

-------
                                                                   TABLE 2.6
10
                             SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                                        CONDITION 4 - MAY 15,1997
                                                                                                                          LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps°
Volumetric Flow Rate
acfmb
dscfm0
Temperature,
op
Moisture,
%
THC Concentration
ppm, wef;1
ppm, dry"
ppm, as
styrenef
Mass Rate,
lb/hi*
Main Exhaust
1
2
3
2005-2105
2130-2230
NA
Average
40.44
40.23
NA
40.34
4053
4032
NA
4043
3846
3823
NA
3835
78
78
NA
78
0.9
1.0
NA
1.0
682.8
687.6
NA
685.2
689.0
694.5
NA
691.8
293.7
296.1
NA
294.9
18.34
18.37
NA
18.35
Room Exhaust
1
2
3
2005-2105
2130-2230
NA
Average
Run No.
1
2
3
Average
18.15
18.32
NA
18.24
5083
5129
NA
5106
NDO-A (-)
Velocity,
fprn"
250
275
NA
263
Flow Rate,
cfrri
6668
7334
NA
7000
Cone,
ppm wef1
12.8
18.3
NA
15.6
4846
4886
NA
4866
75
75
NA
75
0.9
0.9
NA
0.9
NDO-B (-)
Velocity,
fpmh
700
700
NA
700
Flow Rate,
cfhv
175
175
NA
175
Cone,
ppm wef1
1.6
NA
NA
1.6
109.2
118.4
NA
113.8
110.2
119.5
NA
114.8.
NDO-C (+) Forced Makeup Air
Velocity, Flow Rate, Conc>
w cw 55
250 633 1.7
300 759 1.6
NA NA NA
275 696 1.7
47.0
50.9
NA
49.0
3.69
4.04
NA
3.87
NDO-D (+) Forced Makeup Air
Velocity,
fpm"
275
275
NA
275
~ 5
696 1.7
696 1.6
NA NA
696 1.7
     1 Feet per second.
     b Actual cubic feet per minute.
     c Dry standard cubic feet per minute.
     d Part per million, wet basis as propane equivalent.
     c Part per million, dry basis as propane equivalent
f Part per million as styrene equivalent based on styrene response factor.
g Pound per hour.
h Feet per minute.
' Cubic feet per minute.

-------
                                                              TABLE 2.7
                       SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                                   CONDITION 5 - MAY 19,1997
                                                                                                                       LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps'
Volumetric Flow Rate
acfinb
dscfmc
Temperature,
°F
Moisture,
%
THC Concentration
ppm, wet;1
ppm, dry"
ppm, as
styrener
Mass Rate,
Ib/hr8
Main Exhaust
1
2
3
0903-1027
1106-1231
1357-1521
Average
36.59
36.55
36.94
36.69
3667
3663
3701
3677
3345
3314
3308
3322
87
90
92
90
2.0
2.1
2.4
2.2
476.0
426.9
413.5
438.8
485.7
436.1
423.7
448.5
207.1
185.9
180.6
191.2
11.24
10.00
9.70
10.31
Room Exhaust
1
2
3
0903-1027
1106-1231
1357-1521
Average
17.06
17.28
18.21
17.52
4777
4842
5099
4906
4402
4297
4619
4439
80
83
85
83
2.1
2.3
2.2
2.2
113.5
130.9
123.1
122.5
115.9
134.0
125.9
125.3
49.4
57.1
53.7
53.4
3.53
3.98
4.02
3.85
Auxiliary Exhaust
1
2
3
0903-1027
1106-1231
1357-1521
Average
Run No.
1
2
3
Average
40.84
40.14
39.28
40.09
5219
5124
5020
5121
NDO-A (-)
Velocity,
fpmh
325
325
325
325
Flow Rate,
cfnV
8668
8668
8668
8668
Cone,
ppm
wet?1
1.1
4.7
1.1
2.3
4780
4677
4541
4666

Velocity,
fpmh
500
400
500
467
83
84
86
84
2.1
2.1
2.1
2.1
148.7
142.3
149.1
146.7
151.9
145.4
152.3
149.8
NDO-B (-) NDO-C (+) Forced Makeup Air
Flow Rate,
cfhV
125
100
125
117
Conc' Velocity, Flow Rate, Conc'
55 *mh cfini 55
0.0 300 759 0.0
0.5 275 696 0.9
3.3 275 696 0.8
1.3 283 717 0.6
64.8
62.0
64.9
63.9
5.02
4.70
4.79
4.84
NDO-D (+) Forced Makeup Air
Velocity,
fpmh
350
250
250
283
Flow Rate, Conc'
55
886 0.0
633 0.9
633 0.8
717 0.6
" Feet per second.
b Actual cubic feet per minute.
c Dry standard cubic feet per minute.
d Part per million, wet basis as propane equivalent.
c Part per million, dry basis as propane equivalent.
f Part per million as styrene equivalent based on styrene response factor.
8 Pound per hour.
h Feet per minute.
1 Cubic feet per minute.

-------
                                                                 TABLE 2.8
                            SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                                       CONDITION 6 - MAY 19,1997
                                                                                                                       LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps°
Volumetric Flow Rate
acfmb
dscfinc
Temperature,
op
Moisture,
%
THC Concentration
ppm, wef1
ppm, dry*
ppm, as
styrenef
Mass Rate,
Ib/hi*
Main Exhaust
1
2
3
1605-1706
1734-1855
1936-2018
Average
38.68
38.09
38.07
38.28
3876
3817
3815
3836
3513
3449
3488
3483
88
89
86
88
2.2
2.3
1.9
2.1
861.0
868.0
877.6
868.9
880.4
888.4
894.6
887.8
375.3
378.7
381.4
378.5
21.40
21.20
21.59
21.40
Room Exhaust
1
2
3
1605-1706
1734-1855
1936-2018
Average
Run No.
1
2
3
Average
18.23
19.03
19.06
18.77
5107
5331
5341
5260
NDO-A (-)
Velocity,
fpmh
300
250
275
275
Flow Rate,
cfrrf
8001
6668
7334
7334
Cone,
ppm
wef1
3.9
3.8
2.4
3.4
4663
4868
4920
4817
83
83
81
82
NDO-B (-)
Velocity,
fpmh
250
250
200
233
Flow Rate,
cfm'
62.5
62.5
50
58
Cone,
ppm
wef1
3.0
9.7
29.6
14.1
2.2
2.2
1.9
2.1
164.2
146.0
113.6
141.3
167.9
149.3
115.8
144.3
NDO-C (+) Forced Makeup Air
Velocity, Flow Rate, Conc'
** - 5
250 633 2.7
250 633 5.6
250 633 1.9
250 633 3.4
71.6
63.6
49.4
61.5
5.42
5.03
3.94
4.80
NDO-D (+) Forced Makeup Air
Velocity,
fpmh
250
250
350
283
Flow Rate,
cfm'
633
633
886
717
Conc,
ppm
wef1
2.7
5.6
1.9
3.4
to
u>
     a Feet per second.
     b Actual cubic feet per minute.
     c Dry standard cubic feet per minute.
     d Part per million, wet basis as propane equivalent
     ' Part per million, dry basis as propane equivalent.
f Part per million as styrene equivalent based on styrene response factor.
8 Pound per hour.
h Feet per minute.
1 Cubic feet per minute.

-------
                                                                   TABLE 2.9
                             SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                                         CONDITION 7 - MAY 20,1997
                                                                                                                            LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps"
Volumetric Flow Rate
acfinb
dscfm"
Temperature,
op
Moisture,
%
THC Concentration
ppm, wet?1
ppm, dry"
ppm, as
styrenef
Mass Rate,
Ib/hr8
Main Exhaust
1
2
3
1449-1613
1705-1828
1913-2036
Average
38.82
38.73
38.86
38.59
3891
3881
3893
3866
3585
3593
3608
3575
84
83
83
83
1.8
1.5
1.4
1.6
717.5
859.4
876.6
817.9
730.7
872.5
889.0
830.8
311.5
371.9
379.0
354.1
18.12
21.69
22.20
20.67
Room Exhaust
1
2
3
1449-1613
1705-1828
1913-2036
Average
Run No.
1
2
3
Average
18.16
18.86
18.06
18.36
5085
5291
5060
5145
NDO-A (-)
Velocity, Flow Rate,
fpmh cfm1
250 6668
250 6668
300 8001
267 7112
Cone,
ppm
wetd
3.4
2.0
1.9
2.4
4772
4979
4753
4835
77
77
77
77
1.1
0.8
1.0
1.0
NDO-B (-)
Velocity,
fpmh
200
200
300
233
Flow Rate,
cfm1
50
50
75
58
Cone,
ppm wet*
3.5
3.8
1.4
2.9
98.1
104.4
101.7
101.4
99.2
105.2
102.7
102.4
NDO-C (+) Forced Makeup Air
Velocity, Flow Rate, Conc>
f -' S
250 633 2.2
250 633 1.5
300 759 1.0
267 675 1.6
42.3
44.9
43.8
43.6
3.28
3.63
3.38
3.43
NDO-D (+) Forced Makeup Air
Velocity,
fpmh
300
300
300
300
Flow Rate,
cfm'
759
759
759
759
Cone,
ppm
wef1
2.2
1.5
1.0
1.6
to
      " Feet per second.
      b Actual cubic feet per minute.
      c Dry standard cubic feet per minute.
      d Part per million, wet basis as propane equivalent.
      c Part per million, dry basis as propane equivalent.
 Part per million as styrene equivalent based on styrene response factor.
8 Pound per hour.
h Feet per minute.
' Cubic feet per minute.

-------
                                                                 TABLE 2.10
N>
                            SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                                       CONDITION 8 - MAY 22,1997
                                                                                                                        LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
rps"
Volumetric Flow Rate
acfmb
dscfmc
Temperature,
op
Moisture,
THC Concentration
ppm, wef1
ppm, dry*
ppm, as
styrenef
Mass Rate,
Ib/hr8
Main Exhaust
1
2
3
0752-0844
091-9-1049
1139-1309
Average
38.58
38.45
38.47
38.50
3866
3853
3855
3858
3724
3679
3661
3688
74
77
80
77
1.2
1.5
1.5
1.4
612.8
622.3
667.9
634.3
620.2
631.8
678.1
643.3
264.4
269.3
289.1
274.3
15.98
16.08
17.18
16.41
Room Exhaust
1
2
3
0752-0844
0919-1049
1139-1309
Average
Run No.
1
2
3
Average
18.95
19.42
18.58
18.98
5309
5441
5202
5317
NDO-A (-)
Velocity,
fpm"
275
300
300
292
Flow Rate,
cfhV
7334
8001
8001
7779
Cone,
ppm wef1
11.0
5.6
NA
8.3
5144
5272
5013
5143
71
71
74
72
1.0
1.0
1.0
1.0
NDO-B (-)
Velocity,
fpmh
550
400
400
450
Flow Rate,
cfm'
138
100
100
113
Cone,
ppm wef1
NA
2.5
NA
2.5
185.0
174.9
143.1
167.7
186.9
176.7
144.5
169.4
79.7
75.3
61.6
72.2
NDO-C (+) Forced Makeup Air
Velocity, Flow Rate, Conc>
^ h f i ppm
fpnr cfm1 vv *
e wer
550 1392 6.2
350 886 3.0
300 759 NA
400 1012 4.6
6.65
6.44
5.01
6.04
NDQ-D (+) Forced Makeup Air
Velocity, Flow Rate,
fpmh cfm'
450 1139
400 1012
400 1012
417 1054
Cone,
ppm
wef1
6.2
3.0
NA
4.6
     " Feet per second.
     b Actual cubic feet per minute.
     c Dry standard cubic feet per minute.
     A Part per million, wet basis as propane equivalent
     * Part per million, dry basis as propane equivalent.
f Part per million as styrene equivalent based on styrene response factor.
g Pound per hour.
h Feet per minute.
' Cubic feet per minute

-------
                                                                  TABLE 2.11
to
                             SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                                        CONDITION 9 - MAY 22,1997
                                                                                                                            LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps1
Volumetric Flow Rate
acfm"
dscfmc
Temperature,
op
Moisture,
THC Concentration
ppm, wef1
ppm, dry*
ppm, as
styrenef
Mass Rate,
Ib/hr*
Main Exhaust
1
2
3
1802-1844
NA
NA
Average
38.69
NA
NA
38.69
3877
NA
NA
3877
3624
NA
NA
3624
84
NA
NA
84
1.6
NA
NA
1.6
609.3
NA
NA
609:3
619.2
NA
NA
619.2
264.0
NA
NA
264.0
15.53
NA
NA
15.53
Room Exhaust
1
2
3
1802-1844
NA
NA
Average
Run No.
1
2
3
Average
17.74
NA
NA
17.74
4971
NA
NA
4971
NDO-A (-)
Velocity,
fpmh
250
NA
NA
250
Flow Rate,
cfm1
6668
NA
NA
6668
Cone,
ppm wef1
3.2
NA
NA
3.2
4728
NA
NA
4728
78
NA
NA
78
0.8
NA
NA
0.8
NDO-B (-)
Velocity,
fpmh
300
NA
NA
300
Flow Rate,
cfm'
75
NA
NA
75
Cone,
ppm wef1
2.7
NA
NA
2.7
79.2
NA
NA
79.2
79.8
NA
NA
79.8
34.0
NA
NA
34.0
NDO-C (+) Forced Makeup Air
Velocity, Flow Rate, Conc>
fpmh cfm! ppm
\VCIT
300 759 2.7
NA NA NA
NA NA NA
300 759 2.7
2.61
NA
NA
2.61
NDO-D (+) Forced Makeup Air
Velocity,
fpmh
400
NA
NA
400
Flow Rate, Conc'
, i ppm
Cfm wef
1012 2.7
NA NA
NA NA
1012 2.7
      " Feet per second.
      b Actual cubic feet per minute.
      c Dry standard cubic feet per minute.
      d Part per million, wet basis as propane equivalent.
      e Part per million, dry basis as propane equivalent.
f Part per million as styrene equivalent based on styrene response factor.
g Pound per hour.
h Feet per minute.
' Cubic feet per minute.

-------
                                                                   TABLE 2.12
                             SUMMARY OF TIE STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                                         CONDITION 10 - MAY 22,1997
                                                                                                                            LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps"
Volumetric Flow Rate
acfin"
dscfm"
Temperature,
op
Moisture,
%
THC Concentration
ppm, wetd
ppm, dry"
ppm, as
styrenef
Mass Rate,
Ib/hr8
Main Exhaust
1
2
3
1959-2050
NA
NA
Average
38.45
NA
NA
38.45
3854
NA
NA
3854
3623
NA
NA
3623
82
NA
NA
82
1.4
NA
NA
1.4
600.9
NA
NA
600.9
609.4
NA
NA
609.4
259.8
NA
NA
259.8
15.28
NA
NA
15.28
Room Exhaust
1
2
3
1959-2050
NA
NA
Average
Run No.
1
2
3
Average
17.16
NA
NA
17.16
4806
NA
NA
4806
NDO-A (-)
Velocity,
fpmh
300
NA
NA
300
Flow Rate, Conc'
-_ : ppm
cfm wef
8001 3.8
NA NA
NA NA
8001 3.8
4597
NA
NA
4597
76
NA
NA
76
0.6
NA
NA
0.6
NDO-B (-)
Velocity,
fpm"
550
NA
NA
550
Flow Rate,
cfnV
138
NA
NA
138
Conc,
ppm wef1
2.6
NA
NA
2.6
66.1
NA
NA
66.1
66.5
NA
NA
66.5
NDO-C (+) Forced Makeup Air
Velocity, Flow Rate, Conc>
e h f i Ppm
fpm- cfm' ^
400 1012 2.6
NA NA NA
NA NA NA
400 1012 2.6
28.3
NA
NA
28.3
2.12
NA
NA
2.12
NDO-D (+) Forced Makeup Air
Velocity,
fpmh
400
NA
NA
400
Flow Rate, Conc'
«* S
1012 2.6
NA NA
NA NA
1012 2.6
to
-J
      * Feet per second.
      b Actual cubic feet per minute.
      c Dry standard cubic feet per minute.
      d Part per million, wet basis as propane equivalent
      e Part per million, dry basis as propane equivalent
f Part per million as styrene equivalent based on styrene response factor.
8 Pound per hour.
h Feet per minute.
1 Cubic feet per minute.

-------
                                                             TABLE 2.13
                       SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                                  CONDITION 11 - MAY 23,1997
                                                                                                                      LASCO Panel Products
to
00
Run No.
Time
Stack Gas
Velocity,
fpf
Volumetric Flow Rate
acfmb
dscfinc
Temperature,
op
Moisture,
%
THC Concentration
ppm, wef1
ppm, dry0
ppm,asstyrenef
Mass Rate,
Ib/hr8
Main Exhaust
1
2
3
0912-1015
1040-1121
1200-1242
Average
38.36
38.42
38.06
38.28
3844
3849
3813
3835
3672
3652
3581
3635
77
79
81
79
1.4
1.7
1.6
1.6
547.5
558.3
561.2
555.7
555.3
568.0
570.3
564.5
236.7
242.1
243.1
240.7
14.11
14.35
14.13
14.20
Room Exhaust
1
2
3
0912-1015
1040-1121
1200-1242
Average
Run No.
1
2
3
Average
17.32
16.87
18.24
17.48
4850
4727
5107
4895
NDO-A (-)
Velocity,
fpm"
300
300
200
267
Flow Rate,
cfirf
8001
8001
5334
7112
Cone,
ppm
wetd
8.0
5.0
3.9
5.6
4694
4557
4863
4705
72
74
77
74
0.9
0.9
0.8
0.9
NDO-B (-)
Velocity,
fpmh
525
525
525
525
Flow Rate,
cfnV
131
131
131
131
Cone,
ppm wef1
1.5
0.9
3.1
1.8
116.3
95.2
88.2
99.9
117.4
96.1
88.9
100.8
NDO-C (+) Forced Makeup Air
Velocity,
fpmh
400
. 400
400
400
Flow Rate,
cfin'
1012
1012
1012
1012
Cone,
ppm
wef1
3.3
1.0
0.8
1.7
50.0
41.0
37.9
43.0
3.81
3.03
2.99
3.28
NDO-D (+) Forced Makeup Air
Velocity,
fpmh
400
400
400
400
Flow Rate,
cfnV
1012
1012
1012
1012
Cone,
ppm
wef1
3.3
1.0
0.8
1.7
* Feet per second.
b Actual cubic feet per minute.
c Dry standard cubic feet per minute.
d Part per million, wet basis as propane equivalent.
" Part per million, dry basis as propane equivalent.
f Part per million as styrene equivalent based on styrene response factor
8 Pound per hour.
h Feet per minute.
1 Cubic feet per minute.

-------
                                                                     2.11
                       SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                                  CONDITION 12 - MAY 29,1997
                                                                                                                    LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps>
Volumetric Flow Rate
acfm"
dscfmc
Temperature,
op
Moisture,
%
THC Concentration
ppm, wef1
ppm, dry"
ppm, as
styrenef
Mass Rate,
Ib/hr8
Main Exhaust
1
3
4
0835-0935
1104-1202
1230-1330
Average
36.60
35.63
35.24
35.82
3667
3571
3531
3590
3459
3364
3305
3376
79
80
82
80
1.7
1.6
1.9
1.7
368.0
313.5
304.9
328.8
374.4
318.6
308.3
333.7
159.6
135.8
131.4
142.3
8.96
7.42
7.05
7.81
Room Exhaust
1
3
4
0835-0935
1104-1202
1230-1330
Average
17.05
17.30
16.37
16.91
4774
4846
4587
4736
4541
4610
4350
4500
74
74
75
74
1.6
1.6
1.7
1.6
152.1
133.2
129.6
138.3
154.6
135.4
131.8
140.6
65.9
57.7
56.2
59.9
4.86
4.32
3.97
4.38
Auxiliary Exhaust
1
3
4
0835-0935
1104-1202
1230-1330
. Average
Run No.
1
3
4
Average

Velocity,
fpmh
450
450
450
450
38.53
38.91
37.56
38.33
NDO-A (-)
Flow Rate,
cfhV
12,002
12,002
12,002
12,002
4924
4967
4800
4897

Cone,
ppm wet1
10.8
12.0
11.2
11.3
4694
4731
4547
4657

Velocity,
fpmh
1000
950
850
933
72
73
76
74
NDO-B (-)
Flow Rate,
cfiri
250
238
213
234
1.7
1.6
1.6
1.6
183.0
147.1
147.4
159.2
186.2
149.5
149.8
161.8
NDO-C (+) Forced Makeup Air
Cone, Velocity, Flow Rate,
ppm wet? fpmh cfrn'
1.4 250 633
0.2 300 759
0.2 300 759
0.6 283 717
Cone,
ppm wet1
1.5
0.3
0.4
0.7
79.4
63.7
63.9
69.0
6.05
4.89
4.71
5.22
NDO-D (+) Forced Makeup Air
Velocity,
rpmh
350
450
400
400
Flow Rate,
cfm1
886
1139
1012
1012
Cone,
ppm wetd
1.5
0.3
0.4
0.7
* Feet per second.
b Actual cubic feet per minute.
c Dry standard cubic feet per minute.
d Part per million, wet basis as propane equivalent.
e Part per million, dry basis as propane equivalent
f Part per million as styrene equivalent based on styrene response factor
8 Pound per hour.
h Feet per minute.
' Cubic feet per minute.

-------
                                                                   TABLE 2.15
                             SUMMARY OF TTE STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                                         CONDITION 13 - MAY 29,1997
                                                                                                                             LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps-
Volumetric Flow Rate
acfmb
dscfmc
Temperature,
op
Moisture,
%
THC Concentration
ppm, wetd
ppm, dry"
ppm, as
styrenef

Mass
lb/
Rate,
hi*
Main Exhaust
1
2
3
1518-1614
1637-1737
1801-1901
Average
35.46
35.77
35.56
35.60
3553
3585
3565
3568
3362
3358
3325
3348
77
81
82
80
1.4
1.7
1.9
1.7
194.4
183.8
188.5
188.9
197.2
187.0
192.2
192.1
84.0
79.7
81.9
81.9
4.59
4.34
4.42
4.45
Room Exhaust
1
2
3
1518-1614
1637-1737
1801-1901
Average
16.89
16.68
16.82
16.80
4729
4671
4708
4703
4465
4412
4447
4441
75
75
76
75
1.8
1.8
1.6
1.7
100.3
104.5
106.9
103.9
102.1
106.4
108.6
105.7
43.5
45.4
46.3
45.1
3.16
3.25
3.34
3.25
Auxiliary Exhaust
1
2
3
1518-1614
1637-1737
1801-1901
Average
37.58
37.14
37.59
37.44
NDO-A (-)
Run No. velocity, Flow Rate,
fpmh cfhV
1 450 12,002
2 450 12,002
3 450 12,002
Average 450 12,002
4797
4741
4799
4779

Cone,
ppm wet*
11.7
10.1
8.4
10.1
4536
4471
4529
4512

Velocity,
fpmh
950
950
950
950
75
76
76
76
1.6
1.7
1.7
1.7
128.8
123.6
129.0
127.1
130.9
125.7
131.2
129.3
NDO-B (-) NDO-C (+) Forced Makeup Air
Flow Rate, Cone, Velocity, Flow Rate,
cfhV ppm wef1 fpmh cfm1
238 4.2 300 759
238 1.5 400 1012
238 3.1 400 1012
238 2.9 367 928
Cone,
ppm wef1
1.8
1.9
1.8
1.8
55.8
53.6
55.9
55.1
4.11
3.89
4.11
4.04
NDO-D (+) Forced Makeup Air
Velocity,
fpmh
400
400
400
400
Flow Rate,
cfm'
1012
1012
1012
1012
Cone,
ppm wef1
1.8
1.9
1.8
1.8
to
to
o
      "Feet per second.
      bActual cubic feet per minute.
      T)ry standard cubic feet per minute.
      dPart per million, wet basis as propane equivalent.
      Tart per million, dry basis as propane equivalent.
Tart per million as styrene equivalent based on styrene response factor.
*Pound per hour.
hFeet per minute.
'Cubic feet per minute.

-------
                              TABLE 2.16 (Concluded)
Condition
No.
7
7
7
Run
No.
1
2
3
Average
8
8
8
1
2
3
Average
9

10

11
11
11
1

1

1
2
3
Average
12
12
12
1
2
3
Average
13
13
13
1
2
3
Average
NDO" Total,
Ib/hi*
ND
ND
-

ND
ND
-

ND

ND

ND
-
-

ND
ND
-

0.36
-
-
0.36
Main Exhaust,
Ib/hr*
11.25
-
14.33
12.79
10.11
-
-
10.11
10.47

VOID

7.97
7.36
-
7.67
5.29
-
4.87
5.08
-
2.80
-
2.80
Room
Exhaust,
Ib/hi*
1.20
-
-
1.20
3.39
-
-
3.39
2.08

0.44

1.4J
-
0.71
1.09
-
-
-
-
1.781
-
-
1.81
Auxiliary
Exhaust,
Ib/hi*
NA
NA
NA
NA
NA
NA
NA
NA
NA

NA

NA
NA
NA
NA
4.03
-
3.19
3.61
2.43
-
-
2.43
Total Overall
Enclosure
Exhaust,
Ib/hr"
13.99
13.50
12.15

0.44f

8.76
8.69
7.04
• Note: NDO-Aflowrates and concentrations were used to calculate mass rates.
b Ib/hr = Pound per hour, total pounds of styrene and MMA measured.
0 ND = Detection limit of analytical instrument.
d - = Sample not collected in this test condition.
* NA = Not applicable - auxiliary fan not in operation.
f Result is not valid due to a voided main exhaust sample.
                                               2-22

-------
      The Method 18 analysis showed MMA, styrene and cumene at detection limit
(± 1 ppm) values for most of the runs conducted at the NDO sites. If compounds were
detected, the TTE results were adjusted based on HAP content at the NDO sites.
2.6   OVEN NOS. 9 AND 10 - METHOD 25A TOTAL HYDROCARBON RESULTS

      Table 2.17 presents the THC mass emission rate summary for the Oven Nos. 9
and 10 locations. The THC mass emission rate data represents emissions collected using
EPA Method 25A and corrected for methane and ethane mass emission rates measured by
Method 18.  The methane and ethane concentrations were a result of inefficient natural
gas dryers; these concentrations were measured and subtracted from the Method 25A
total.  The final THC mass emission rate data was calculated using styrene response
factors to adjust all data to a styrene basis. The oven sampling program was performed
simultaneously with the TTE sampling.
2.7   OVEN NOS. 9 AND 10 - VOLUMETRIC FLOW RATE RESULTS

      Tables 2.18 through 2.30 present flow rate data and THC concentration data
collected at the Oven Nos. 9 and 10 sample sites. Each table of results represents a
sample condition, 13 total conditions.  One volumetric flow rate was performed for each
sample run at each location.  Flow conditions were very consistent during the sample
program.


2.8   OVEN NOS. 9 AND 10 - METHOD 18 HAP RESULTS

      Table 2.31 presents the Method 18 results measured at the Oven Nos. 9 and 10
sample locations. One sample run for styrene, cumene and MMA was performed for each
sample condition. As mentioned in Section 2.5, the Method 18 data was collected as
support for the THC results and as an indicator of the amount of styrene, cumene and
MMA present at each sample location. The Method 18 results were adjusted for
recovery efficiencies.


 2.9   UNCATALYZED RESIN (UCR) AND GEL COAT SAMPLE RESULTS

      Process samples of the UCR and gel coat (gel coat was only used during
Conditions 1 and 2) were collected at the beginning and end of each sample run. The
process  samples were analyzed by EPA Method 24 to determine volatile matter content,
water content, density and weight of solids. Analysis was also performed to determine
HAP content. Results of the analysis are contained in the ESD Test Report.
                                    2-23

-------
         TABLE 2.17
     OVENS 9 AND 10 THC
MASS EMISSION RATE SUMMARY
                               LASCO Panel Products
Condition No.
1
1
1
Run
No.
1
2
3
Average
2
2
2
1
2
3
Average
3
3
3
1
2
3
Average
4
4
4
1
2
3
Average
5
5
5
1
2
3
Average
6
6
6
1
2
3
Average
Oven No. 9 Exhaust,
Ib/hr"
0.27
0.31
0.28
0.28
0.00
0.00
0.22
0.07
0.43
0.29
0.29
0.34
0.26
0.33
NA
0.29
0.40
0.72
0.60
0.57
1.11
0.85
0.95
0.97
Oven No. 10 Exhaust,
Ib/hr"
0.18
0.12
0.11
0.14
0.18
0.07
0.05
0.10
2.24
2.21
2.45
2.30
2.80
2.66
NA
2.73
1.46
1.35
1.43
1.41
1.26
1.54
1.46
1.42
Total Oven Exhaust,
Ib/hr"
0.45
0.43
0.39
0.42
0.18
0.07
0.27
0.17
2.67
2.50
2.74
2.64
3.06
2.99
NA
3.02
1.86
2.07
2.03
1.98
2.37
2.39
2.41
2.39
             2-24

-------
                            TABLE 2.17 (Concluded)
Condition No.
7
7
7
Run
No.
1
2
3
Average
8
8
8
1
2
3
Average
9

10

11
11
11
1

1

1
2
3
Average
12
12
12
1
2
3
Average
13
13
13
1
2
3
Average
Oven No. 9 Exhaust,
lb/hi*
0.53
0.68
0.61
0.61
0.00
0.23
0.12
0.12
0.32

0.58

0.03
0.20
0.17
0.13
0.75
0.78
0.55
0.69
0.74
0.69
0.96
0.80
Oven No. 10 Exhaust,
Ib/hi*
1.81
1.96
1.89
1.89
0.55
0.56
1.10
0.74
2.68

2.16

3.18
3.39
3.23
3.27
2.95
3.40
3.39
3.25
3.94
4.11
4.09
4.05
Total Oven Exhaust,
Ib/hr"
2.34
2.64
2.50
2.50
0.55
0.79
1.22
0.86
3.00

2.74

3.21
3.59
3.40
3.40
3.70
4.18
3.94
3.94
4.68
4.80
5.05
4.85
" Pound per hour, as styrene equivalent, excluding methane and ethane.
                                        2-25

-------
                                                               TABLE 2.18
                          SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                     AND MASS EMISSION RATES, CONDITION 1 - MAY 14,1997
                                                                                                                    LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps*
Volumetric Flow Rate
acfmb
dscfm0
Temperature,
op
Moisture,
%
THC Concentration
ppm, wetd
Adjusted
ppm, wetf
ppm, dr/
ppm, as
styrene5
Mass Rate,
Ib/hr"
Oven 9
1
2
3
1034-1134
1225-1325
1546-1646
Average
32.44
32.80
33.18
32.81
2394
2420
2449
2421
1907
1924
1927
1919
169
169
173
170
1.8
1.8
1.8
1.8
118.7
132.3
128.2
126.4
19.7
22.7
20.5
21.0
20.1
23.2
20.9
21.4
8.6
9.9
8.9
9.1
0.27
0.31
0.28
0.28
Oven 10
1
2
3
1034-1134
1225-1325
1546-1646
Average
34.25
34.83
34.98
34.69
2522
2564
2575
2554
1836
1893
1878
1869
218
214
222
218
2.7
2.3
1.9
2.3
43.5
41.7
39.5
41.6
13.7
9.1
8.4
10.4
14.1
9.3
8.6
10.7
6.0
4.0
3.7
4.5
Ovens 9 and 1 0 Total Mass Rate, Ib/hi*
0.18
0.12
0.11
0.14
0.42
to
to
      "Feet per second.
      b Actual cubic feet per minute.
      c Dry standard cubic feet per minute.
      d Part per million, wet basis as propane equivalent.
e Part per million, wet basis adjusted for NDO contributions.
f Part per million, dry basis.
8 Part per million as styrene equivalent based on styrene response factor.
h Pound per hour.

-------
                                                                TABLE 2.19
                           SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                     AND MASS EMISSION RATES, CONDITION 2 - MAY 14,1997
                                                                                                                       LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps"
Volumetric Flow Rate
acfmb
dscfinc
Temperature,
op
Moisture,
%
THC Concentration
ppm, wetd
Adjusted
ppm, wef
ppm, dr/
ppm, as
styrene8

Mass Rate,
Ib/hr11
Oven 9
1
2
3
2020-2125
2155-2255
2337-0038
Average
32.52
31.62
33.15
32.43
2394
2328
2446
2389
1905
1870
1964
1913
172
165
165
167
1.3
1.2
1.1
1.2
50.4
71.9
108.0
76.8
0.0
0.0
15.7
5.2
0.0
0.0
15.8
5.3
0.0
0.0
6.8
2.3
0.00
0.00
0.22
0.07
Oven 10
1
2
3
2020-2125
'2155-2255
2337-0038
Average
33.66
32.67
33.25
33.19
2478
2405
2454
2446
1825
1769
1807
1800
219
220
219
219
1.4
1.4
1.4
1.4
43.5
38.1
34.6
38.7
14.4
5.8
4.1
8.1
14.6
5.9
4.2
8.2
6.2
2.5
1.8
3.5
Ovens 9 and 10 Total Mass Rate, Ib/hi*
0.18
0.07
0.05
0.10
0.17
to
to
-J
      " Feet per second.
      b Actual cubic feet per minute.
      c Dry standard cubic feet per minute.
      d Part per million, wet basis as propane equivalent.
e Part per million, wet basis adjusted for.NDO contributions.
f Part per million, dry basis.
8 Part per million as styrene equivalent based on styrene response factor.
h Pound per hour.

-------
                                                             TABLE 2.20
                         SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                   AND MASS EMISSION RATES, CONDITION 3 - MAY 15,1997
                                                                                                                LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps1
Volumetric Flow Rate
acfmb
dscfmc
Temperature,
Of
Moisture,
%
THC Concentration
ppm, wetd
Adjusted
ppm, wet"
ppm, dr/
ppm, as
styrene8
Mass Rate,
Ib/hr*
Oven 9
1
2
3
1425-1525
1559-1659
1735-1836
Average
31.24
31.82
31.96
31.67
2306
2348
2359
2338
1855
1886
1894
1878
167
167
167
167
1.1
1.1
1.1
1.1
87.9
118.9
106.4
104.4
33.5
22.3
22.2
26.0
33.8
22.6
22.4
26.3
14.4
9.6
9.6
11.2
0.43
0.29
0.29
0.34
Oven 10
1
2
3
1425-1525
1559-1659
1735-1836
Average
35.43
34.49
34.71
34.88
2615
2545
2561
2574
1910
1852
1871
1878
229
232
229
230
1.1
1.1
1.1
1.1
185.7
189.1
204.7
193.2
167.3
170.9
186.8
175.0
169.1
172.8
188.9
176.9
72.1
73.7
80.5
75.4
Ovens 9 and 10 Total Mass Rate, Ib/hi*
2.24
2.21
2.45
2.30
2.64
to
to
oo
     0 Feet per second.
     b Actual cubic feet per minute.
     c Dry standard cubic feet per minute.
     d Part per million, wet basis as propane equivalent.
c Part per million, wet basis adjusted forNDO contributions.
f Part per million, dry basis.
8 Part per million as styrene equivalent based on styrene response factor.
h Pound per hour.

-------
                                                                TABLE 2.21
                           SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                     AND MASS EMISSION RATES, CONDITION 4 - MAY 15,1997
                                                                                                                      LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps*
Volumetric Flow Rate
acfmb
dscfrrf
Temperature,
Of
Moisture,
%
THC Concentration
ppm, wetd
Adjusted
ppm, wet"
ppm, dr/
ppm, as
styrene8
Mass Rate,
lb/hi*
Oven 9
1
2
3
2005-2105
2130-2230
NA
Average
31.85
32.22
NA
32.03
2345
2372
NA
2359
1890
1917
NA
1904
164
163
NA
164
1.2
1.2
NA
1.2
110.1
113.4
NA
111.8
19.5
24.3
NA
21.9
19.7
24.6
NA
22.1
8.4
10.5
NA
9.4
0.26
0.33
NA
0.29
Oven 10
1
2
3
2005-2105
2130-2230
NA
Average
35.29
34.46
NA
34.88
2599
2537
NA
2568
1897
1850
NA
1874
229
230
NA
230
1.1
1.2
NA
1.2
231.0
226.6
NA
228.8
210.8
205.0
NA
207.9
213.1
207.5
NA
210.3
90.8
88.4
NA
89.6
Ovens 9 and 10 Total Mass Rate, Ib/hi* |
2.80
2.66
NA
2.73
3.02
to
      " Feet per second.
      b Actual cubic feet per minute.
      c Dry standard cubic feet per minute.
      d Part per million, wet basis as propane equivalent.
e Part per million, wet basis adjusted for NDO contributions.
f Part per million, dry basis.
8 Part per million as styrene equivalent based on styrene response factor.
h Pound per hour.

-------
                                                              TABLE 2.22
                          SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                    AND MASS EMISSION RATES, CONDITION 5 - MAY 19,1997
                                                                                                                   LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps"
Volumetric Flow Rate
acfmb
dscfmc
Temperature,
op
Moisture,
%
THC Concentration
ppm, wef1
Adjusted
ppm, wef
ppm, dr/
ppm, as
styrene8
Mass Rate,
lb/ht*
Oven 9
1
2
3
0903-1027
1106-1231
1357-1521
Average
Oven 10
1
2
3
0903-1027
1106-1231
1357-1521
Average
31.83
32.54
31.28
31.88
2349
2401
2308
2353
1821
1934
1958
1904

34.20
34.84
34.83
34.62
2524
2571
2571
2555
1859
1890
1882
1877
164
164
165
164
2.8
2.5
2.2
2.5

222
223
226
224
2.5
2.5
2.5
2.5
149.8
164.1
139.8
151.2
30.6
52.6
43.6
42.3
31.5
53.9
44.6
43.4
13.4
23.0
19.0
18.5

125.6
121.6
118.1
121.8
110.7
100.8
106.9
106.1
113.5
103.4
109.7
108.9
48.4
44.1
46.8
46.4
Ovens 9 and 10 Total Mass Rate, Ib/hi*
0.40
0.72
0.60
0.57

1.46
1.35
1.43
1.41
1.98
tv)
     * Feet per second.
     b Actual cubic feet per minute.
     c Dry standard cubic feet per minute.
     d Part per million, wet basis as propane equivalent.
e Part per million, wet basis adjusted for NDO contributions.
f Part per million, dry basis.
8 Part per million as styrene equivalent based on styrene response factor.
h Pound per hour.

-------
                                                             TABLE 2.23
                         SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                    AND MASS EMISSION RATES, CONDITION 6 - MAY 19,1997
                                                                                                                 LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps*
Volumetric Flow Rate
acrmb
dscfin"
Temperature,
op
Moisture,
%
THC Concentration
ppm, wetd
Adjusted
ppm, wef
ppm, dr/
ppm, as
styrene8
Mass Rate,
Ib/hr*
Oven 9
1
2
3
1605-1706
1734-1855
1936-2018
Average
32.68
32.64
32.22
32.51
2412
2409
2378
2400
1948
1942
1923
1938
164
164
162
163
2.2
2.2
2.2
2.2
156.3
161.4
167.2
161.6
80.4
62.2
69.6
70.7
82.2
63.6
71.2
72.3
35.0
27.1
30.4
30.8
1.11
0.85
0.95
0.97
Oven 10
1
2
3
1605-1706
1734-1855
1936-2018
Average
33.52
33.64
33.65
33.60
2474
2482
2484
2480
1814
1835
1837
1829
225
222
222
223
2.3
2.1
1.9
2.1
111.7
139.9
131.0
127.5
98.0
118.6
112.6
109.8
100.3
121.1
114.8
112.1
42.8
51.6
48.9
47.8
Ovens 9 and 10 Total Mass Rate, Ib/hr"
1.26
1.54
1.46
1.42
2.39
to
U)
      * Feet per second.
      b Actual cubic feet per minute.
      c Dry standard cubic feet per minute.
      d Part per million, wet basis as propane equivalent.
e Part per million, wet basis adjusted for NDO contributions.
f Part per million, dry basis.
8 Part per million as styrene equivalent based on styrene response factor.
h Pound per hour.

-------
                                                               TABLE 2.24

                          SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                     AND MASS EMISSION RATES, CONDITION 7 - MAY 20, 1997
                                                                                                                     LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps-
Volumetric Flow Rate
acfmb
dscfmc
Temperature,
op
Moisture,
%
THC Concentration
ppm, wef1
Adjusted
ppm, wef
ppm, dry'
ppm, as
styrene8
Mass Rate,
Ib/hr*
Oven 9
1
2
3
1449-1613
1705-1828
1913-2036
Average
32.00
32.27
32.56
32.28
2362
2376
2397
2378
1905
1898
1905
1903
164
168
169
167
1.2
1.6
1.9
1.6
146.3
121.8
109.9
126.0
39.4
51.2
45.3
45.3
39.8
52.1
46.1
46.0
17.0
22.2
19.7
19.6
0.53
0.68
0.61
0.61
Oven 10
1
2
3
1449-1613
1705-1828
1913-2036
Average
32.50
34.04
34.27
33.60
2393
2507
2523
2474
1746
1829
1833
1803
229
229
232
230
1.3
1.3
1.3
1.3
165.6
168.0
161.3
165.0
147.7
153.2
147.1
149.3
149.7
155.2
149.0
151.3
63.8
66.2
63.5
64.5
Ovens 9 and 10 Total Mass Rate, lb/hi*
1.81
1.96
1.89
1.89
2.50
to
U)
to
      ' Feet per second.
      b Actual cubic feet per minute.
      0 Dry standard cubic feet per minute.
      d Part per million, wet basis as propane equivalent.
e Part per million, wet basis adjusted for NDO contributions.
f Part per million, dry basis.
g Part per million as styrene equivalent based on styrene response factor.
b Pound per hour.

-------
                                                                TABLE 2.25
                           SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                     AND MASS EMISSION RATES, CONDITION 8 - MAY 22,1997
                                                                                                                       LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps'
Volumetric Flow Rate
acfmb
dscfmc
Temperature,
Moisture,
THC Concentration
ppm, wetd
Adjusted
ppm, wef
ppm, dry*
ppm, as
styrene8
Mass Rate,
Ib/hr*
Oven 9
1
2
3
0752-0844
0919-1049
1139-1309
Average
32.10
32.10
32.16
32.12
2363
2361
2367
2364
1926
1927
1929
1927
167
166
167
167
1.7
1.7
1.7
1.7
112.9
131.5
110.8
118.4
0.0
17.3
8.7
8.7
0.0
17.6
8.9
8.8
0.0
7.5
3.8
3.8
0.00
0.23
0.12
0.12
Oven 10
1
2
3
0752-0844
0919-1049
1139-1309
Average
34.24
34.19
34.41
34.28
2521
2517
2533
2524
1918
1883
1854
1885
214
213
215
214
1.3
3.1
4.9
3.1
62.4
64.4
101.1
76.0
40.8
41.6
81.6
54.7
41.3
43.0
85.8
56.4
17.6
18.3
36.6
24.1
Ovens 9 and 10 Total Mass Rate, Ib/ht*
0.55
0.56
1.10
0.74
0.86
to
U)
      * Feet per second.
      b Actual cubic feet per minute.
      0 Dry standard cubic feet per minute.
      d Part per million, wet basis as propane equivalent.
c Part per million, wet basis adjusted for NDO contributions.
f Part per million, dry basis.
8 Part per million as styrene equivalent based on styrene response factor.
h Pound per hour.

-------
                                                              TABLE 2.26
                          SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                     AND MASS EMISSION RATES, CONDITION 9 - MAY 22,1997
                                                                                                                   LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps*
Volumetric Flow Rate
acfmb
dscfmc
Temperature,
oF
Moisture,
%
THC Concentration
ppm, wet1
Adjusted
ppm, wef
ppm, dry*
ppm, as
styrene8
Mass Rate,
Ib/hr*
Oven 9
1
2
3
1802-1844
NA
NA
Average
31.20
NA
NA
31.20
2297
NA
NA
2297
1839
NA
NA
1839
160
NA
NA
160
4.5
NA
NA
4.5
Oven 10
1
2
3
1802-1844
NA
NA
Average
33.30
NA
NA
33.30
2452
NA
NA
2452
1763
NA
NA
1763
230
NA
NA
230
4.5
NA
NA
4.5
67.0
NA
NA
67.0
23.7
NA
NA
23.7
24.8
NA
NA
24.8
10.6
NA
NA
10.6
0.32
NA
NA
0.32

222.7
NA
NA
222.7
209.5
NA
NA
209.5
219.3
NA
NA
219.3
93.5
NA
NA
93.5
Ovens 9 and 10 Total Mass Rate, Ib/hi*
2.68
NA
NA
2.68
3.00
to
OJ
      1 Feet per second.
      b Actual cubic feet per minute.
      c Dry standard cubic feet per minute.
      d Part per million, wet basis as propane equivalent.
° Part per million, wet basis adjusted forNDO contributions.
f Part per million, dry basis.
8 Part per million as styrene equivalent based on styrene response factor.
h Pound per hour.

-------
                                                                TABLE 2.27
                           SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                     AND MASS EMISSION RATES, CONDITION 10 - MAY 22,1997
                                                                                                                       LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps*
Volumetric Flow Rate
acfrnb
dscfrnc
Temperature,
op
Moisture,
%
THC Concentration
ppm, wef1
Adjusted
ppm, wef
PPm,
dr/
ppm, as
styrene8
Mass Rate,
Ib/hr11
Oven 9
1
2
3
1959-2050
NA
NA
Average
31.12
NA
NA
31.12
2297
NA
NA
2297
1909
NA
.NA
1909
164
NA
NA
164
0.2
NA
NA
0.2
110.9
NA
NA
110.9
44.0
NA
' NA
44.0
44.1
NA
NA
44.1
18.8
NA
NA
18.8
0.58
NA
NA
0.58
Oven 10
1
2
3
1959-2050
NA
NA
Average
33.38
NA
NA
33.38
2464
NA
NA
2464
- 1851
NA
NA
1851
230
NA
NA
230
0.2
NA
NA
0.2
189.5
NA
NA
189.5
168.0
NA
NA
168.0
168.3
NA
NA
168.3
71.7
NA
NA
71.7
Ovens 9 and 10 Total Mass Rate, Ib/hi*
2.16
NA
NA
2.16
2.74
to
      ' Feet per second.
      b Actual cubic feet per minute.
      c Dry standard cubic feet per minute.
      d Part per million, wet basis as propane equivalent.
c Part per million, wet basis adjusted for NDO contributions.
f Part per million, dry basis.
g Part per million as styrene equivalent based on styrene response factor.
h Pound per hour..

-------
                                                              TABLE 2.28
                          SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                    AND MASS EMISSION RATES, CONDITION 11 - MAY 23,1997
                                                                                                                   LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps"
Volumetric Flow Rate
acfmb
dscfmc
Temperature,
op
Moisture,
%
THC Concentration
ppm, wef1
Adjusted
ppm, wef
ppm, dr/
ppm, as
styrene8
Mass Rate,
Ib/hr*
Oven 9
1
2
3
0912-1015
1040-1121
1200-1242
Average
32.04
32.40
32.19
32.21
2359
2385
2369
2371
1979
2001
1988
1989
156
156
156
156
0.5
0.5
0.5
0.5
59.2
67.8
71.5
66.2
2.1
14.6
12.4
9.7
2.1
14.7
12.4
9.8
0.9
6.3
5.3
4.2
0.03
0.20
0.17
0.13
Oven 10
1
2
3
0912-1015
1040-1121
1200-1242
Average
33.84
33.08
33.70
33.54
2492
2435
2481
2469
1872
1823
1843
1846
231
230
231
231
0.3
0.5
1.2
0.7
269.2
283.6
273.3
275.4
245.0
267.3
250.8
254.3
245.7
268.6
255.3
255.9
104.7
114.5
108.0
109.1
Ovens 9 and 10 Total Mass Rate, Ib/hi*
3.18
3.39
3.23
3.27
3.40
to
     1 Feet per second.
     b Actual cubic feet per minute.
     c Dry standard cubic feet per minute.
     d Part per million, wet basis as propane equivalent.
e Part per million, wet basis adjusted for NDO contributions.
f Part per million, dry basis.
g Part per million as styrene equivalent based on styrene response factor.
b Pound per hour.

-------
                                                               TABLE 2.29
                          SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                    AND MASS EMISSION RATES, CONDITION 12 - MAY 29,1997
                                                                                                                      LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps>
Volumetric Flow Rate
acfrnb
dscfmc
Temperature,
oF
Moisture,
%
THC Concentration
ppm, wet!1
Adjusted
ppm, wet?
ppm, dr/
ppm, as
styrene8

Mass Rate,
Ib/hr11
Oven 9
1
3
4
0835-0935
1104-1202
1230-1330
Average
60.17
60.03
59.67
59.96
4430
4419
4393
4414
3482
3511
3474
3489
Oven 10
1
3
4
0835-0935
1104-1202
1230-1330
Average
35.14
33.06
34.13
34.11
2587
2508
2512
2536
1920
1842
1818
1860
177
170
173
173

232
231
234
232
3.0
3.0
3.0
3.0
103.5
130.3
112.9
115.6
30.3
31.3
22.1
27.9
31.2
32.2
22.8
28.8
13.3
13.7
9.7
12.3
0.75
0.78
0.55
0.69

0.5
1.6
2.7
1.6
240.9
280.5
284.3
268.6
220.8
262.7
262.5
248.6
221.9
266.9
269.7
252.7
94.6
113.8
115.0
107.7
Ovens 9 and 10 Total Mass Rate, Ib/hi*
2.95
3.40
3.39
3.25
3.94
NJ
     * Feet per second.
     b Actual cubic feet per minute.
     c Dry standard cubic feet per minute.
     d Part per million, wet basis as propane equivalent.
* Part per million, wet basis adjusted for NDO contributions.
f Part per million, dry basis.
8 Part per million as styrene equivalent based on styrene response factor.
h Pound per hour.

-------
                                                               TABLE 2.30
                          SUMMARY OF OVEN STACK GAS CONDITIONS AND THC CONCENTRATIONS
                                    AND MASS EMISSION RATES, CONDITION 13 - MAY 29,1997
                                                                                                                    LASCO Panel Products
Run No.
Time
Stack Gas
Velocity,
fps°
Volumetric Flow Rate
acfrnb
dscfin"
Temperature,
op
Moisture,
%
THC Concentration
ppm, wef1
Adjusted
ppm, wef
ppm, dr/
ppm, as
styrene8
Mass Rate,
Ib/hr*
Oven 9
1
2
3
1518-1614
1637-1737
1801-1901
Average
59.97
59.81
59.92
59.90
4416
4404
4412
4411
3560
3530
3545
3545
172
171
173
172
1.0
1.6
1.0
1.2
124.6
130.8
121.8
125.7
29.9
27.8
38.6
32.1
30.2
28.3
39.0
32.5
12.9
12.1
16.6
13.8
0.74
0.69
0.96
0.80
Oven 10
1
2
3
1518-1614
1637-1737
1801-1901
Average
33.63
33.83
33.97
33.81
2476
2491
2500
2489
1804
1823
1814
1814
230
226
233
230
2.2
2.2
2.2
2.2
331.8
340.3
334.0
3354
308.9
318.7
318.9
315.5
315.8
325.9
326.0
322.6
134.6
138.9
139.0
137.5
Ovens 9 and 10 Total Mass Rate, Ib/hr*
3.94
4.11
4.09
4.05
4.85
to
U)
00
     * Feet per second.
     b Actual cubic feet per minute.
     c Dry standard cubic feet per minute.
     d Part per million, wet basis as propane equivalent.
e Part per million, wet basis adjusted for NDO contributions.
f Part per million, dry basis.
8 Part per million as styrene equivalent based on styrene response factor.
h Pound per hour.

-------
                        TABLE 2.31
         OVENS 9 AND 10 MASS EMISSION RATE SUMMARY
STYRENE, METHYL METHACRYLATE, AND CUMENE BY EPA METHOD 18

                                             LASCO Panel Products
Condition No.
1
1
1
Run
No.
1
2
3
Average
2
2
2
1
2
3
Average
3
3
3
1
2
3
Average
4
4
4
1
2
3
Average
5
5
5
1
2
3
Average
6
6
6
1
2
3
Average
Oven No. 9
Exhaust,
Ib/hi*
_b
-
-
-
0.040
-
-
0.040
-
0.026
-
0.026
-
0.457
-
0.457
0.044
-
-
0.044
-
0.050
-
0.050
Oven No. 10
Exhaust,
Ib/hi*
0.003
-
-
0.003
-
0.157
-
0.157
0.006
-
-
0.006
0.006
-
-
0.006
-
0.826
-
0.826
0.766
-
-
0.766
Total Oven Exhaust,
Ib/hr"
0.003
0.197
0.032
0.463
0.870
0.816
                           2-39

-------
                               TABLE 2.31 (Concluded)
Condition No.
7
7
7
Run
No.
1
2
3
Average
8
8
8
1
2
3
Average
9
1
Oven No. 9
Exhaust,
lb/hi*
0.006
-
-
0.006
-
0.006
-
0.006
0.032
Oven No. 10
Exhaust,
Ib/hr"
-
1.207
-
1.207
0.241
.
-
0.241
-
Total Oven Exhaust,
Ib/hr8
1.213
0.0247
0.032

10
1
-
1.555
1.555

11
11
11
1
2
3
Average
12
12
12
1
3
4
Average
13
13
13
1
2
3
Average
-
0.006
-
0.006
-
0.129
-
0.129
-
0.427
-
0.427
0.614
-
-
0.614
0.749
-
2.199
1.474
2.711
-
-
2.711
0.620
1.603
3.138
1 Pound per hour, total pounds of styrene and MMA measured.
b - = Sample not collected in this test condition.
                                           2-40

-------
2.10   RESPONSE FACTOR RESULTS

       The THC concentrations were monitored continuously according to EPA Method
25A guidelines, using flame-ionization analyzers (FIAs). The instruments were
calibrated onsite before and after each sample run using EPA Protocol propane-in-air
standards. Since the main HAP of interest was styrene, response factors (RFs) were
developed to determine instrument responses relative to styrene. A modified EPA
proposed Method 204F was used to prepare styrene bag standards.  From the bag
standards, instrument response factors were developed over three concentration ranges
used during sampling. The RF results are presented in Table 2.32. The factors were very
consistent over the three calibration ranges. An average RF value of 0.4263 was used to
convert all Method 25 A propane results to styrene. The RF laboratory results are
contained in Appendix C;
2.11   METHOD 204 TOTAL TEMPORARY ENCLOSURE VERIFICATION

       The room containing the process line was treated as a TTE, which enabled
sampling all HAP concentrations entering and leaving the enclosure.  Figure 2.1 is the
general layout (not to scale) of the TTE and dimensions of the NDOs and exhaust
locations.  EPA proposed Method 204, "Criteria for and Verification of a Permanent or
Temporary Total Enclosure" presents a five-point criteria for verification of a TTE. The
LASCO Wide Line process room was configured to meet these criteria of a TTE.  Natural
draft openings were minimized and an auxiliary room exhaust fan was added to ensure a
minimum negative static of 0.004 inches H2O.  The enclosure met the following criteria
required of a TTE:

       A)    Natural draft openings (NDOs) are at least four equivalent opening
             diameters from each VOC emitting point.

       B)    The total area of all NDOs shall not exceed 5% of the surface area
             of the enclosure's four walls, floor and ceiling.

       C)    The  average facial velocity (FV) of air through all NDOs  shall be
             at least 3,600 meters per hour (m/hr) or 200 fpm, or the negative
             static pressure in the enclosure must be £0.004 in. H2O. The
             direction of flow through all NDOs shall be into the enclosure.

       D)    All access doors and windows whose areas are not included in
             Criteria B and are not included in the calculation hi Criteria C shall
             be closed during routine process operation.
                                      2-41

-------
                            TABLE 2.32

             SUMMARY OF RESPONSE FACTOR RESULTS
                    STYRENE BAG STANDARDS
                                                LASCO Panel Products
Bag
Standar
d
Runl
Run 2
Run 3
Run 4
Run 5
Run 6
Run?
Run 8
Syrene
Injection, ppm
(Styrene)3
67.7
67.9
134.6
189.8
362.2
557.3
1106.2
1659.5
Average
Overall Average 0.4263
JUM1
Response, ppm
(Propane)b
161.1
160.3
319.0
441.3
855.9
1266
2636
3983
Respon
se
Factor
0.4202
0.4236
04219
0.4301
0.4232
0.4402
0.4197
0.4166
0.4244
Standard Deviation 0.75%
JUM5
Response, ppm
(Propane)6
156.9
157.8
316.3
431.4
843.9
1250
2642
4103
Response
Factor
0.4315
0.4303
04255
0.4400
0.4292
0.4458
0.4187
0.4045
0.4282
Standard Deviation 1.27%
"Part per million, styrene.
bPart per million, propane equivalent.
                                2-42

-------
                                   er
82'
         Outside
Natural Draft Opening (NDO) - A
        (32" X120")
         NDO-B
        (0.5" X 72")
       Fresh Air Supply
        (14"X26")
         NDO-C
       Doorway
       (Closed)
      (36" X 84")
       Doorway
       (Closed)
       (36" X 84")

        Doorway
        (Closed)
       (36" X 84")
      Overhead Door
        (Closed)
       (96" X 120")
                  Main Exhaust
                     (17.5")
Oven Area
                              Overhead Door
                               (120" X 168")
                                 (Closed)
                                 Fresh Air Supply
                                   (14" x 26")
                                     NDO-D
                                     Doorway
                                     (Closed)
                                    (36" X 84")
                                                                   Auxilary Fan
                                                                     Outside
                                                                     (19.75")
                                   Room Exhaust
                                    (24"X28")
                                        Air Sampling
                                        THC
                                        Styrene
                                        Cumene
                                        Methyl Methacrylate
               Figure 2.1  Diagram of Temporary Total Enclosure
                                     2-43

-------
      E)     Any exhaust point from the TTE shall be at least 4 equivalent duct
             or hood diameters from each NDO.

      PES measured the room, the doorways, the small gaps around the doors, the large
swinging doors and the volumetric air flow rate entering and exiting the room. This data
was used to demonstrate that the process room meets the criteria for a TTE.

      The TTE room measured 61 x 82 x 16.7 feet high. There are five doorways (one
was used for the auxiliary fan) which measure 36 x 84 inches and two large doors 120 x
168 inches and 96 x 120 inches-all are kept closed. Thus, the TTE met Criteria D.

      NDO-A is the largest opening and the closest to a VOC lay down area. The
opening is 2.7 x 10 feet, an area of 26.67 ft2, and the equivalent diameter of this opening
is 5.83 feet. The distance from the nearest opening to the VOC lay down area was more
than the required four equivalent diameters, thus Criteria A was met.

      The total surface area of the TTE room is 14,780 ft2. The total area of the NDOs
is 31.98 ft2 which is 0.2% of the total, which met Criteria B.

      The negative static pressure inside the enclosure must be ^0.004 in. H2O; the
enclosure negative static pressure ranged from 0.004 to 0.015 in. H2O, which met Criteria
C.

      All access doors were kept closed during the process operation except for ingress
and egress by workers and materials. When access doors were opened, the room
remained under negative static pressure. The four 36 x 84 inch doorways had gaps
around the bottom of each door about 0.5 inches wide. These gaps were considered
NDOs and were measured and labeled NDO-B. Thus, the TTE met Criteria D.

      All exhaust points from the TTE were at least four equivalent diameters from an
NDO, which met Criteria E.
                                      2-44

-------
3.0 PROCESS DESCRIPTION
LAS CO Panel Products is among the largest (perhaps the largest, since the recent
addition of the wide line) producer of reinforced plastic panels from the continuous
lamination process in the country. Various panel products are produced with applications
in both construction and automotive industries. The facility has two narrow "lines" (or
continuous lamination machines) and one wide line. The storage and mix preparation
processes involved with the application process were not a subject of this testing
program.

The lamination process begins with the unwinding of a large roll of transparent
film onto the dispensing table where a catalyzed resin mixture is applied across the width
of the film. This is the wet application area. Reinforcing materials are then added to the
resin. A top film is unwound from a second roll of film to cover over the wet mixture.
After the top film is added, the material moves into the oven curing area.

The emissions from the process come from the evaporation of the monomer,
which is either styrene or a combination of styrene, methyl methacrylate, and cumene.
The styrene content (98%) and cumene content (1.5%) make up greater than 99% of the
total HAP content. The methyl methacrylate was believed to be a small percentage
(<0.2%) of the total HAP content, according to LASCO personnel. While onsite, it was
discovered that MMA may account for higher percentages of the HAP content depending
on the type of product produced. At this point, it was decided to measure MMA along
with the other two primary HAP compounds. A fan ducted to a partial enclosure around
the table area helps draw air emissions from the wet areas and exhausts the air through a
stack on the roof (Main Exhaust site).

Process monitoring for this sampling program was provided to ESD by PES
through EPA Contract No. 68D10116, Work Assignment No. 6-01. Specific process data
is being handled as confidential business information (CBI) through that work
assignment. Therefore, a detailed process description and parameters are not included in
this test report

The following is a general description of the three room conditions that were
examined during this sample program. For each of the three conditions, the process room
was treated as a TTE with all access doors closed and NDOs minimized. The negative
static pressure in the room was maintained at -0.004 inches of water or greater.
3-1

-------
The current condition was the operation of the process line the normal way it
operates each production day. The main exhaust system is exhausting air emissions from
the table area to the main roof exhaust stack. The table area is covered partially. Most
top areas of the table are covered with panels and side areas mostly open. The initial
resin application area is partially closed, with some panels open. The sampling areas
consisted of the Main Exhaust which normally draws emission directly from the wet
application area, the Room Exhaust which draws fugitive emission from floor level in
one corner of the room, four natural draft openings (NDOs), and Ovens 9 and 10 exhaust
stacks.

The open condition involved the removal of panels and enclosures covering the
wet application area of the line. The top panels and hinged access panels were removed
or opened where possible. The Main Exhaust duct was disconnected so there was no air
being pulled directly from the table area. The Main Exhaust pickup lines were all closed
(knife dampers closed) and the pickup lines disconnected and taped off. The Main
Exhaust fan continued to draw fugitive emissions from above the table area. The open
condition was to simulate uncontrolled emissions from the table area. The Auxiliary
Exhaust was operated during the open condition so that pressure negativity could be
maintained in the room. The sampling areas consisted of the Main Exhaust, Room
Exhaust, Auxiliary Exhaust, three NDOs, and Ovens 9 and 10 exhaust stacks.

The closed condition was the operation of the line with everything covered and
panels in place on the process line. The Main Exhaust line was disconnected so there was
no air flow being pulled directly from the table area. The Main Exhaust pickup lines
were all closed (knife dampers closed), and the pickup lines disconnected and taped off.
Additional rigid panels were placed on any open areas on the top and sides of the table
area. The rigid panels were taped closed where possible. Areas where rigid panels could
not be used were covered with foil-faced foam insulation board and taped shut. The table
area was estimated to be 98% covered. The Auxiliary Exhaust was operated during the
closed condition so that pressure negativity could be maintained in the room. The
sampling areas consisted of the Main Exhaust, Room Exhaust, three NDOs, and Ovens 9
and 10 exhaust stacks.
3-2

-------
4.0 SAMPLING LOCATIONS
The Wide Line continuous lamination process was contained in a single room
with several emission points. The room was treated as a TTE to measure all emissions
exiting the room and emissions being drawn into the room through the natural draft
openings (NDOs). There were also two oven sampling locations (separate room from the
TTE) which were sampled simultaneously with the TTE sampling locations. The oven
locations were located inside the building, and sampling was conducted to determine if
the ovens emitted any hazardous air pollutants.

The air sampling locations were the Main Exhaust, Room Exhaust, Auxiliary
Exhaust, NDOs, and OvenNos. 9 and 10. Figure 1.2 in Section 1.0 is an overall
schematic of all of the sampling locations. The locations are described below.
4.1 MAIN EXHAUST STACK

The main exhaust stack pulls air from the table surface area (wet application area)
and exhausts the air emissions through a 17.5 inch inside diameter (ID) round vertical
stack through the ceiling. Sampling ports were located 42 inches downstream (2.4 duct
diameters) of the induced draft fan exhaust and 37 inches upstream of the exhaust (2.1
duct diameters) to the atmosphere. A total of 16 points, eight per port, were used to
traverse the duct for velocity measurements. Figure 4.1 is a schematic of the sampling
location.
4.2 ROOM EXHAUST STACK

The room exhaust duct pulls room air from the wide line application area and
exhausts air through a 24 x 28 inch rectangular vertical stack. The intake was at floor
level in the corner of the room nearest the Auxiliary Exhaust. The velocity measurement
location was in the wide line application room. The THC/M18 measurement location
was in the exhaust duct outside and above the roof. Four equivalent sampling ports were
located on the 14 inch side of the duct, approximately 143 inches (5.5 equivalent duct
diameters) downstream of the duct work intake and 72 inches (2.8 equivalent duct
diameters) upstream of the exhaust fan. A total of 24 points, six per port, were used to
traverse the duct. Figure 4.2 is a schematic of the room exhaust sampling location.
4-1

-------
     t
To Atmosphere
   17.5" I.D.
    Flow
                    37"
                     42"
Traverse Point
Number
1
2
3
4
5
6
7
8
Traverse Point
Location
0.50"
1.75"
3.38"
5.63"
11.88" .
14.13"
15.63"
17.00"
     Fan
                Figure 4.1 Main Exhaust Sample Location
                                4-2

-------
   Vent
               Duct Cross-section
  voc
  Sampling
  Port
Roof
                       72"
   Velocity
Sampling Ports
     Flow
                       143"
     Intake
X
X
X
X
X
X

X
X
X
X
X
X

X
X
X
X
X
X

X
X
X
X
X
X







I

                                                               28"
                      24"
Traverse Point
Number
1
2
3
4
5
6
Traverse Point
Location
2.38"
7.00"
11.63"
16.38"
21.00"
25.63"
                          Floor
                Figure 4.2 Room Exhaust Sample Location
                               4-3

-------
4.3 AUXILIARY EXHAUST STACK

The auxiliary exhaust stack was installed in an existing doorway of the wide line
application area about 24 inches above the floor to increase the volume of air exhausted
from the enclosure, for purposes of creating a TTE. A section of duct work connected the
sealed doorway to an auxiliary exhaust fan with straightening vanes inserted to prevent
cyclonic flow. Sampling ports were located approximately 114 inches (5.8 duct
diameters) downstream of the doorway and 40 inches (2.0 duct diameters) upstream of
the fan intake of the 19.75 inch round horizontal duct. Sixteen traverse points, eight per
port, were used to conduct velocity traverses. Figure 4.3 is a schematic of the auxiliary
exhaust sampling location.
4.4 NATURAL DRAFT OPENINGS

A total of four NDOs were present in the wide line application area TTE. Those
openings were the material feed opening to the oven area (designated as NDO-A), the
double door outside doorway (NDO-B), and two fresh air supply ducts as part of the
HVAC system (designated as NDO-C and NDO-D). NDO-A (material feed opening)
dimensions were 120 x 32 inches. NDO-B was 72 inches long by 0.5 inches high. NDO-
C and NDO-D dimensions were 14 x 26 inches. A Kurz hot-wire anemometer was used
at various points across the face of each opening to measure air velocity into the room
enclosure. NDO-A and NDO-B were negative drafts into the enclosure; NDO-C and
NDO-D were forced makeup air into the enclosure, as part of the building's HVAC
system. Figure 4.4 details the dimensions of each NDO.
4.5 OVEN EXHAUST NO. 9 AND NO. 10

The oven curing zone was a two section process that had a long, enclosed area for
curing the fiberglass panels. Each of the two oven sections had individual makeup air
supply ducts and a single exhaust duct. All sampling was conducted in the round,
horizontal 15-inch inside diameter (ID) duct work, prior to the outlet stack exhaust fan.
Sampling ports on No. 9 were located 50 inches (3.3 duct diameters) downstream of a
disturbance and 38 inches (2.5 duct diameters) upstream of the exhaust fan. Sampling
ports on No. 10 were located 55 inches (3.7 duct diameters) downstream of a disturbance
and 38 inches (2.5 duct diameters) upstream of the exhaust fan. A total of 12 points, six
per port, were used to traverse the ducts for velocity determinations. Figures 4.5 and 4.6
are schematics of the sampling locations for Oven Nos. 9 and 10.
4-4

-------






Building
Enclosure















— 114" to
r~
/
Traverse Point
Number
1
2
3
4
5
6
7
8
^ 40" ^
-i
t
/ f^ 10 71V1 i n
Flow / iT 19-f5 ' D
	 to / /
//
i

Auxiliary
Traverse Point
Location
0.63"
2.13"
3.75"
6.38"
13.40"
15.92"
17.68"
19.12"


Fan
Flow



         Sample Ports
Figure 4.3 Auxiliary Exhaust Sampling Location

-------
                 Product web
                                                      32"
                    120"

           Natural Draft Opening A
  -denotes sample location
                     72"
                                                     0.5"
           Natural Draft Opening B     (sample location outside
                                      of doorway-ambient air)
26"
   Fresh Air Supply
Ducts (HVAC System)
                    14"
        Natural Draft Openings C & D
     Figure 4.4 Natural Draft Opening Sampling Locations
                         4-6

-------
                                                               Roof
       50"
38"
Flow

1
15"I.D.O
I
Fan
                                     Traverse Point
                                       Number
                                          1
                                          2
                                          3
                                          4
                                          5
                                          6
                     Traverse Point
                       Location
                       0.7"
                       2.19"
                       4.44"
                       10.56"
                       12.81"
                       14.34"
Figure 4.5 Oven No. 9 Schematic of Sampling Location

-------
                                                                                    Roof
                                      55"
           38"
00
                    Flow
15"|.D.O
                                                                         Fan
Traverse Point
Number
1
2
3
4
5
6
Traverse Point
Location
0.7"
2.19"
4.44"
10.56"
1281"
1434"
                                    Figure 4.6 Oven No. 10 Schematic of Sampling Location

-------
              5.0 SAMPLING AND ANALYTICAL PROCEDURES
      The Wide Line continuous lamination process (application and oven curing areas)
was sampled for a variety of stack gas constituents following the procedures of EPA
Reference Methods 1-4,18, 24,25A, and proposed Methods 204 and 204F. Table 5.1
summarizes the testing parameters, test methods, number of tests, and duration of
sampling runs.  Brief descriptions of each method are presented below:
5.1    LOCATION OF MEASUREMENT SAMPLE/VELOCITY TRAVERSE POINTS

      EPA Method 1, "Sample and Velocity Traverses for Stationary Sources," was
used to select the measurement sites and to establish velocity and sample traverse point
locations. The measurement sites are discussed in Section 4.0.
5.2    DETERMINATION OF STACK GAS VOLUMETRIC FLOW RATE

       EPA Method 2, "Determination of Stack Gas Velocity and Volumetric Flow
Rate," was used in the measurement of stack gas velocity and volumetric flow rate from
the exhaust ducts of the wide line lamination process. Type "S" pitot tubes with an
assigned coefficient of 0.84 or Standard type pitot tubes with an assigned coefficient of
0.99 and inclined manometer were used to measure differential pressure of the stack gas.
Calibrated Type "K" thermocouples were attached to the pitot tubes to measure stack gas
temperatures. The average stack gas velocities were calculated from the average square
root of the velocity pressure, stack gas temperature, gas molecular weight, and absolute
stack gas pressure.  Volumetric flow rate is the product of velocity and stack cross-
sectional area.

       Velocities from the natural draft openings were checked with a Kurz hot wire
anemometer to verify a minimum face velocity of 200 feet per minute.
                                      5-1

-------
                 TABLE 5.1
SOURCES, TEST PARAMETERS, AND METHODS SUMMARY
  LASCO PANEL PRODUCTS - FLORENCE, KENTUCKY
Source


Main Exhaust Stack

Auxiliary Exhaust Stack
Room Exhaust Stack
Natural Draft Openings
A, B, C, & D
Oven Exhausts
Resin/Gel Coat Mixing
Tanks
Parameter
THC
HAPsc- Styrene
- Cumene
- MMA
THC
HAPs- Styrene
- Cumene
- MMA
THC
HAPs- Styrene
- Cumene
- MMA
THC
HAPs- Styrene
- Cumene
- MMA
THC
HAPs - Styrene
- Cumene
- MMA
Methane and Ethane
Volatiles, H20,
Density
EPA Test Methods
25A
18
18
18
25A
18
18
18
25A
18
18
18
25A
18
18
18
25A
18
18
18
18
24
No. of Tests
3"
ld
ld
ld
3"
ld
ld
ld
3"
ld
1"
ld
3"
ld
1"
ld
3b
ld
ld
ld
3b
1
Time per Test,"
Minutes
60
20
20
20
60
20
20
20
60
20
20
20
60
60
60
60
60
60
60
60
60
	
                     5-2

-------
                                   TABLE 5.1 (Concluded)
Source
Resin/Gel Coat Mixing
Tanks
Parameter
HAPs - Styrene
- Cumene
- MMA
EPA Test Methods
204F
204F
204F
No. of Tests
1"
\e
r
Time per Test,0
Minutes
	
	
	
" Time per test run varied between conditions based on process operation and production schedules.
b Three test runs were conducted for conditions 1, 2, 3, 5,6, 7, 8, 11, 12, and 13. Two test runs were conducted for
  Condition 4.   One test run was conducted for Conditions 9 and 10.
c Styrene and cumene were known HAPs for this site, and MMA was added while onsite based on discussions with
  Mr. Haberlein, a representative of the reinforced plastics industry. The styrene is believed to comprise 98% of the
  total HAPs and was the main pollutant of interest.
d One Method  18 sample was collected for every three Method 25 A sample runs.
e One Method 204F solvent distillation was conducted per condition.
                                                 5-3

-------
A pressure transducer was used in the enclosure to continuously monitor negative
static in the enclosure. The enclosure was kept at a negative static equal to or greater than
-0.004 inches of water column, which is the equivalent of 200 feet per minute through the
natural draft openings.
5.3 DETERMINATION OF DRY MOLECULAR WEIGHT

EPA Reference Method 3, "Gas Analysis for the Determination of Dry Molecular
Weight," was used to measure the percentages of carbon dioxide (CO2) and oxygen (O2)
present in each exhaust gas stream. Bacharach Fyrite combustion gas analyzers were
used to directly read concentrations of C02 and 02. All of the sources were essentially
ambient in nature (zero percent CO2, 21 percent 02).
5.4 EXHAUST GAS MOISTURE CONTENT

EPA Method 4, "Determination of Stack Gas Moisture Content," was used to
measure exhaust gas moisture content. This determination was made in two ways,
dependent upon the temperature of the gas stream. For locations that had a stack gas
temperature of 150°F or less, a wet bulb/dry bulb technique was used, utilizing calibrated
thermocouples and a psychrometric chart. On the oven exhaust ducts, an EPA Method 4
sampling train was used to collect condensate from the stack gas with a series of
Greenburg-Smith impingers contained in an ice water bath. The quantity of condensed
moisture was determined gravimetrically and then compared to the total volume of stack
gas metered to determine the volume percent moisture content. Figure 5.1 is a schematic
of an EPA Method 4 sampling train.
5.5 DETERMINATION OF HAZARDOUS AIR POLLUTANTS (HAPS)

EPA Method 18, "Measurement of Gaseous Organic Compound Emissions by
Gas Chromatography," was used to determine the concentration and mass emission rate
of styrene, cumene, and methyl methacrylate. This method was used in combination with
NIOSH Method 1501 for collecting aromatic hydrocarbons on sorbent tube media
(coconut shell charcoal) using low flow dry gas meters (100 to 250 cc/min) and vacuum
pumps. A pair of sorbent tubes were used in series to prevent sample breakthrough.
HAPs were desorbed from the sampling media with carbon disulfide. The first tube was
analyzed separately from the back tube to check for sample breakthrough. Analysis was
done in duplicate by gas chromatography with flame ionization detection. Methane and
ethane concentrations were collected in Tedlar® bags on the two oven exhausts in
evacuated canisters and also analyzed by GC/FID to determine the contribution of natural
5-4

-------
    FILTER
(ESTHER IN STACK
OR OUT OF STACK)
STACK
WALL
CONDENSER-ICE BATH SYSTEM INCLUDING
              SILICA GEL TUBE —3
                                                              AIR-TIGHT
                                                                PUMP
                  Figure 5.1 Schematic of EPA Method 4 Sampling Train

-------
gas to the air stream. At least one sorbent tube sample was collected on each exhaust
duct during each condition. Spiked samples were also run on at least one exhaust duct
per condition, with a control sample run concurrently to determine desorption/recovery
efficiency of the sampling and analytical procedures. Figure 5.2 is a schematic of the
EPA Method 18 sampling system for sorbent tubes, and Figure 5.3 is a schematic of the
collection system for methane and ethane concentrations.
5.6 DETERMINATION OF TOTAL HYDROCARBONS

EPA Method 25 A, "Determination of Total Gaseous Organic Concentrations
Using a Flame lonization Analyzer," was used to measure total hydrocarbon (THC)
concentrations at the sampling locations. THC concentrations were monitored
continuously in the main exhaust, room exhaust, auxiliary exhaust, and oven exhausts.
At these locations heated Teflon® sample lines were used to prevent polymerization of
styrene. One instrument was used to monitor the NDOs by alternating sampling lines
between the sampling locations. Unheated Teflon® sampling lines were used at all the
NDO locations. The FIAs were calibrated directly and through the sampling system
before each test condition began. The instruments were checked for drift by system
calibrations after each test run. Calibration gases were EPA Protocol propane-in-air
standards. Styrene-in-air calibration standards were used to determine instrument
responses. The sampling system consisted of a stainless steel probe and three-way valve
with Teflon® tubing connections to switch from calibration to sampling mode. A heated
Teflon® line routed stack gas to an internally heated FIA. Instrument responses were
recorded on strip chart recorders and Rustrak Ranger® data logging systems. Values
presented are based on data logging system averages. Figure 5.4 is a schematic of the
sampling system.
5.7 DETERMINATION OF VOLATILE MATTER CONTENT, DENSITY,
VOLUME OF SOLIDS, WEIGHT OF SOLIDS, WATER CONTENT, AND
HAPS BY DISTILLATION

EPA Method 24, "Determination of Volatile Matter Content, Water Content,
Density, Volume Solids, and Weight Solids of Surface Coatings," was used in the
collection of uncatalyzed resin samples used in the wide line lamination process. Volatile
matter contents was determined by ASTM D2369-81. Water content was determined by
ASTM D4017-81, using the Karl Fischer titration method. One uncatalyzed resin (UCR)
material sample per condition was treated to a solvent distillation by vacuum method.
5-6

-------
Stack
 Flow
  t
            Probe
                                         VOST Dry Gas Meter
Sorbent Tubes
   In Series
   Figure 5.2 Schematic of EPA Method 18 Sampling System - Sorbent Tube Method
                                5-7

-------
                                                                                                                 Vent
                     Stack
                   / Wall
      Filter
  (Glass Wool)
      o
                    Probe
               \
                \
00
   Teflon®
Sample Line
                                                        Vacuum Line
                                              Male Quick
                                              Connectors
        Ball
       Check
                                            Rigid Leak-Proof
                                               Container
                                                                                                        Flowmeter
                                                                                                 Charcoal
                                                                                                   Tube
                                     Figure 5.3 Schematic of Methane/Ethane Sampling System

-------
  Stack
                 3-way Valve
Flow
            Probe
Calibration Line
                            Heated Teflon® Line
                                                           Zero
                                                           Air
                                 Low
                                C3H8
Mid
C3H8
                                                                                 1
High
C3H8
                                                                                  Strip Chart
                                                                                  Recorder
                         Flame lonization
                            Analyzer
                                                                                       Data Logger
         Figure 5.4 EPA Method 25A Total Gaseous Organic Analyzer and Sample System

-------
 5.8   RESPONSE FACTORS FOR FLAME IONIZATION ANALYZERS

      The initial test plan method for determining styrene response factors was to use a
commercially prepared styrene calibration gas. The styrene calibration gas response
would then be compared to our calibration curve generated by the EPA Protocol propane
standards. The commercially prepared styrene calibration gases (styrene 102 ppm, 143.1
ppm, 250.7 ppm), showed responses which were non-linear.  EPA Method 18 tube
samples were run on the styrene cylinders, and it was found that the cylinder values were
higher than the Method 18 sample results. The cylinder values were believed to be
inaccurate and could not be used for comparison.  The cylinder styrene values were
unstable even at low concentrations and low pressures (<500 psi). It was decided the
styrene calibration gases were not stable and could not be used to determine response
factors.

      The alternative plan used EPA modified proposed Method 204F to determine
styrene response factors.  Bag standards of styrene were prepared in the lab and run on
three ranges to determine responses relative to propane.  The three ranges were: 0-500
ppm, 0-1000 ppm, and 0-5000 ppm as propane. The average response factor was 0.4263
based on 8 bag standards which were analyzed on two separate flame ionization analyzers
(FIAs).  The data was very consistent throughout the ranges. The following describes the
EPA Method 204F procedure used:

Preparing the Response Factor Mixture

       1.    The amount of VOC introduced to the process is the sum of the products
             of the weight of each VOC containing liquid used and its VOC content
             corrected for a response factor (RF). Typically, a sample of the resin is
             distilled to separate the VOC fraction from the inorganic contents. The
             distillate is used to prepare a known standard for analysis by  an FIA,
             calibrated against propane standards, to determine its RF. In this case,
              styrene was the primary VOC, and a 99% + styrene liquid sample was
             used to prepare bag standards.
       2.     The styrene concentration in the bag sample should be similar to the
              gaseous VOC concentration measured in the sample gas stream. To
              create a specific styrene concentration in the sample bag, the following
              expression was used:

                                 c       - ML
                                  styrene
                                      5-10

-------
where:  Cstyrme  =  Concentration of bag sample as styrene, mg/liter

        ML    =  Mass of styrene liquid injected into bag, mg

        BV    =  Volume of bag sample, liters
3.      The FIA used EPA Protocol propane-in-air calibration gas standards to
        develop a linear calibration line.  These calibration gases were
        commercially prepared in concentrations of parts per million (ppm).
        Therefore it was necessary to convert the styrene concentration from
        mg/liter to ppm. This conversion was performed by applying the
        following formula:

                            C h    x  C x 1000-^-
                             styrene
                    ppm
                                     MW
where:  Cppm   = Concentration of bag sample as ppm, styrene

        Cstyrene = Concentration of bag sample as mg/liter, styrene

        C     = Constant of 24.04 liters per mole.

        MW   = Molecular weight of styrene, 104.15 g/gmol
        The preparation of the styrene bag sample concentrations were
        performed in a consistent, repetitive manner.  A dry gas meter and pump
        were set at a constant flow rate of 3 liters per minute to provide the air
        for the bag sample. A Teflon® line carried the measured air volume into
        a glass injection impinger which was submersed in oil heated to a
        temperature of 400 °F. The styrene was introduced into the glass
        injection impinger by means of a Teflon® coated septum cap. The
        styrene tainted airstream was transported through a Teflon® line heated
        to 180 °F and into the Tedlar® bag.  The Tedlar® bag was kept in a
        heated box maintained at a temperature of 135 °F to eliminate
        condensation and adsorption in the bag.

        When the Tedlar® bag sample was filled with the required volume of air,
        the heated line from the glass injection impinger was switched to the
        FIA. The FIA pumped the styrene bag sample through the heated line to
        the detector.  The response from the styrene bag sample was  monitored

                                 5-11

-------
        until a stabilized measurement was reached and then for approximately
        five more minutes. Figure 5.5 is a diagram of the bag standard
        preparation system.
        The response on the FIA of the styrene bag standard was measured in the
        same units as the calibration gases. In this instance, the styrene bag
        standard was measured in ppm as propane. A response factor (RF) was
        developed from the ratio of the calculated ppm of styrene in the bag
        standard verses the measured styrene concentration reported in ppm as
        propane.  The following equation calculated the response factor for each
        bag sample.

                                    C
                                     ppm
                                    measured
where:  RF   =  Response Factor

        Cppm  =  Concentration of bag sample as ppm, styrene
          measured = FIA reading for bag gas sample, ppm as propane
6.      To ensure the quality assurance in preparing the styrene bag standards,
        the following procedures were performed:

        I.     The dry gas meter that measured the volume of air used to fill the
              Tedlar® bag was calibrated against a reference test meter to
              develop a dry gas meter calibration coeficient (gamma).

        II.    The ambient air used to fill the styrene bag standard was
              monitored by the FIA during the entire procedure of creating the
              standard.  The results of the styrene bag standard were corrected
              according to the measured ambient air VOC concentrations.

        III.   The styrene bag standard preparation system was always purged
              continuously between styrene bag standards. The Tedlar® bag was
              also purged after each styrene standard and the purged air was
              measured on the FIA to ensure that no residual styrene remained
              in the Tedlar® bag.
                                 5-12

-------
Dry Gas
 Meter
                                                        TTsyri
               Pressure
               Gauge
  Boiling
Water Bath
O                                Temperature
                                  Sensor
                                                          X
                Syringe


                   Septum
                       Midget

                       Impinger
                                                                                                 Heated
                                                                                                Container
              -tx-
                                 Air

                               Cylinder
                Figure 5.5 Schematic of Bag Standard Preparation System

-------
IV.   The styrene bag samples were analyzed on two separate J.U.M.
      FIAs to ensure consistent responses to the styrene standards.  The
      gas sample from the styrene bag standard was split to each
      analyzer. J.U.M. analyzer #1 was used at the main exhaust
      location at the LASCO Panel Products plant and J.U.M. analyzer
      #5 was used at the room exhaust location.

V.    Both J.U.M. analyzers were calibrated according to EPA
      Reference Method 25A. The maximum mid calibration gas drift
      was 0.77% of span value and no zero calibration drift was
      detected for any of the styrene bag standards.

VI.   The response factors for the J.U.M. analyzer #1 had a standard
      deviation of 0.75% for the 8 separate styrene bag standards tested.
      J.U.M. analyzer #5 had a standard deviation of only 1.27% for the
      response factors developed from the 8 separate styrene bag
      standards.
                         5-14

-------
              6.0 QUALITY ASSURANCE/QUALITY CONTROL
       The following section describes the specific quality assurance/quality control
(QA/QC) procedures employed by PES in performing this series of tests. The goals of
the QA/QC activities for this project were intended to ensure, to the highest degree
possible, the accuracy of the data collected. The procedures contained in the "Quality
Assurance Handbook for Air Pollution Measurement Systems, Volume III, Stationary
Source Specific Methods," EPA-600/R-94/038c, served as the basis for performance for
all testing and related work activities in this project.
6.1    CALIBRATION OF APPARATUS

       The preparation and calibration of source sampling equipment is essential in
maintaining data quality. Brief descriptions of the calibration procedures used by PES
follow.

Barometers

       PES uses aneroid barometers which are calibrated against a station pressure value
reported by a nearby National Weather Service Station corrected for elevation.

Temperature Sensors

       Bimetallic dial thermometers and Type K thermocouples are calibrated using the
procedure described in Section 3.4.2 of the Quality Assurance Handbook. Each
temperature sensor is calibrated over the expected range of use against an ASTM 3C or
3F thermometer. Table 6.1 summarizes the types of calibrations performed and the
acceptable levels of variance. The calibration data is contained in Appendix E.  The
temperature sensor calibration results were within the acceptable levels of variance.
Thermocouple read-out devices are calibrated using a thermocouple simulator having a
range of 0-2400°F.
                                       6-1

-------
           TABLE 6.1
SUMMARY OF TEMPERATURE SENSORS
   CALIBRATION REQUIREMENTS
Temperature
Sensor Usage
Impinger Outlet
Thermcouple
Dry Gas Meter
Thermometer
Stack Temperature
Thermocouple
Number of
Calibration
Points
2
3
4
Calibration Media
Ice Bath
(0°C)
*
*
*
Ambient Air
(20-25°C)
*
*
*
Hot Water
(40-50°C)

*

Boiling Water
(100°C)


*
Heated Oil
(150-200°C)


*
Tolerances
±1°C
±3°C
±1.5% of
reference
temperature

-------
Pilot Tubes

PES uses Type S and Standard type tubes which are constructed to EPA Method 2
specifications. Type S pitot tubes meeting these criteria are assigned a baseline
coefficient to 0.84 and need not be calibrated. Standard pitot tubes are assigned a
coefficient of 0.99 and also need not be calibrated. The pitot tube calibration data is
contained in Appendix E. The calibration results are within the acceptable levels of
variance.

Differential Pressure Gauges

PES uses Dwyer inclined and inclined/vertical manometers to measure differential
pressures. These include velocity pressure, static pressure, and meter orifice pressure.
Manometers are selected with sufficient sensitivity to accurately measure pressures over
the entire range of expected values. Manometers are primary standards and require no
calibration.

Dry Gas Meters and Orifices

Dry gas meters and orifices are calibrated in accordance with Section 3.3.2 of the
Quality Assurance Handbook. This procedure involves direct comparison of the dry gas
meter to a reference dry test meter. The reference dry test meter is routinely calibrated
using a wet test meter or a liquid displacement technique. Before its initial use in the
field, the metering system is calibrated over the entire range of operation. After each field
use, the metering system is calibrated at a single intermediate setting based on the
previous field test. Acceptable tolerances of the initial and final dry gas meter factors and
orifice calibration factors are ±0.02 and ±0.20 from average, respectively. The dry gas
meter and orifice calibration data are in Appendix E. The calibration results are within
the acceptable levels of variance.
6.2 ONSITEQA/QC

The onsite QA/QC activities included:

Measurement Sites

Prior to sampling, all stack dimensions were checked to verify measurement site
locations, location of test ports, and stack inside dimensions. Inside dimensions were
checked through all available test ports to determine uniformity of the stack cross-
sectional area and the sample test ports were checked to verify that they do not extend
beyond the inside wall. The stack inside dimensions, wall thicknesses, and sample port
depths were measured to the nearest 1/16 inch. When stack dimensions are found to be
6-3

-------
out of round or uneven, then multiple traverse point locations are required on the pitot
tube.

Velocity Measurements

       All velocity measurement apparatus were assembled, leveled, zeroed, and leak-
checked prior to use and at the end of each determination. The static pressure was
determined at a single point near the center of the stack cross-section.

Moisture

       Stack gas moisture content was determined during each test run using calibrated
wet bulb/dry bulb thermocouples and a psychrometric chart on all ambient type sources.
EPA Method 4 sampling trains were used at the oven exhaust because of higher (>150°F)
stack gas temperatures. All impingers were measured gravimetrically prior to and at the
end of each sampling run.

Total Hydrocarbon Concentration

       Total hydrocarbon concentrations (THC) were measured following the guidelines
of EPA Method 25 A.  The flame ionization analyzers were calibrated with three EPA
Protocol propane-in-air gas standards and zero gas. A bias check and response time test
were conducted initially.  Bias check acceptability is a difference of not more  than five
percent between direct injection measured values and system injection. The bias check
must be within ± 5% to proceed with the sample efforts.  Prior to sampling, PES
performed the bias check, response time tests and calibration error tests. Calibration drift
checks were performed after each test run; acceptable drifts for zero or span gases is ± 3%
of span. Table 6.2 summarizes the maximum system calibration bias, calibration error
and drift percentages for each FIA per each condition.  Calibration data is contained in
Appendix A with the field strip charts.

Hazardous Air Pollutants

       Analysis for target hazardous air pollutants (HAPs) was performed onsite by
DEECO.  Spiked tubes were prepared onsite based on THC measurements conducted
during each sampling condition. Sample tube blanks were also collected and  analyzed
onsite.  Samples were desorbed and analyzed within specified holding times for the
individual compounds. Following are the laboratory quality assurance procedures.

              There were duplicate injections of each sample aliquot, with agreement
              between both injections to within 5% of the mean of the injections.
                                        6-4

-------
                                                    TABLE 6.2

                           SUMMARY OF CALIBRATION RESULTS FOR THC ANALYZERS
                                              CONDITION NOS. 1-13
                                            LASCO PANEL PRODUCTS
Cond.
No.
1
2
3
4
5
6
7
8
9
10
11
12
13
Main Exhaust
System
Bias,
%
1.53
1.92
2.70
2.70
2.29
2.29
1.53
1.53
1.53
1.53
1.91
1.91
1.91
Calib.
Error,
%
0.98
0.39
0.56
0.83
0.17
1.06
0.08
0.24
0.20
0.20
0.25
0.43
0.43
Drift,
%
0.4
0.8
0.4
1.5
0.4
1.1
0.8
0.8
1.2
0.4
1.2
0.8
0.8
Room Exhaust
System
Bias,
%
0.40
1.52
1.13
1.1
1.53
1.53
0.76
2.27
2.27
2.27
2.68
2.68
2.68
Calib.
Error,
%
0.60
0.41
0.60
0.21
0.06
0.15
0.45
0.34
0.24
0.24
0.36
0.44
1.09
Drift,
%
0.8
1.5
3.0
1.2
0.4
1.5
0.4
0.8
0.8
0.0
1.1
1.9
1.9
Auxiliary Exhaust .
System Calib.
Bias, Error,
% %
Drift,
%
NA
NA
NA
NA
1.9 0.24
0.8
NA
NA
NA
NA
NA
NA
3.44 0.87
3.44 0.87
1.5
1.9
Oven No. 9
System
Bias,
%
3.6
3.7
2.1
2.8
1.6
1.6
3.1
3.2
3.2
2.5
1.8
2.9
2.2
Calib.
Error,
%
2.8
2.8
4.1
4.1
2.2
2.2
2.2
2.8
2.8
2.8
2.4
2.2
2.2
Drift,
%
0.9
0.8
0.4
0.7
1.3
0.9
0.7
1.3
0.0
1.2
1.0
1.0
0.5
Oven No. 10
System
Bias,
%
2.0
3.8
3.6
0.7
0.9
1.1
2.5
1.8
1.1
1.4
2.4
2.1
1.3
Calib.
Error,
%
3.5
1.0
4.8
4.8
2.6
2.6
2.2
2.8
2.8
2.8
3.2
2.0
2.0
Drift,
%
1.0
1.0
1.3
0.2
0.5
0.3
1.1
0.1
0.1
0.1
0.3
0.5
0.3
NDOs
System
Bias,
%
3.0
3.4
3.6
3.2
2.8
2.8
4.5
3.2
2.4
2.8
3.2
2.2
4.5
Calib.
Error,
%
3.2
3.2
3.6
3.6
4.1
4.1
2.6
2.8
2.4
2.4
2.9
2.2
2.8
Drift,
%
2.1
0.8
1.6
2.4
1.5
1.2
0.8
2.1
0.2
1.2
1.4
1.4
1.1
Note: Values listed for each condition are maximum for each set of test runs.
NA - Not applicable for these conditions.

-------
• There were three point calibration curves for all components (based on
least squared regression analysis) with the curve range bracketing sample
concentrations.

• Calibration curves were developed every 24 hours.

• All calibration points agreed within 10% of the theoretical value.

• For at least every nine samples, a field blank, duplicate and spiked sample
were conducted. The blank sample was an unopened sample tube. The
duplicate sample results were used to determine method precision.

Analysis for the target HAPs were measured following the procedures of EPA
Method 18. Sampling media consisted of activated coconut shell charcoal in sorbent
tubes, a pair in series. Pre-test and post-test leak checks were conducted on each set of
sampling trains. Spiked sorbent tubes were run in duplicate with another set of sample
tubes to determine recovery efficiency of the analytical method. Run No. RES-4-1
recovery efficiency was 195%, which was the result of over spiking the tube compared to
measured stack values. The spike amount was non- representative of sample conditions,
and the data was not used to correct stack concentrations. Run No. AFS-12-4 recovery
was borderline at 68%. All other styrene recoveries were within the acceptable range.
Styrene and methyl methacrylate results were adjusted for recovery efficiencies. At least
one spiked duplicate was run per each of nine samples run. Target compounds were
styrene (primary), cumene and methyl methacrylate.

Table 6.3 summarizes the Method 18 quality assurance results for the sample
tubes spiked with styrene standards and run in duplicate with a separate unspiked sample.
Recovery efficiencies are listed for the test runs conducted at the sample locations under
different test conditions. EPA Method 18 guidelines specify recovery efficiencies
ranging from 70% to 130%, with the majority of the spiked runs within this range. Table
6.4 summarizes the desorption efficiencies for the three compounds of interest: styrene,
cumene and methyl methacrylate. Desorption efficiencies for styrene averaged 89.1%;
cumene averaged 131.3% and methyl methacrylate efficiencies averaged 80.0%.

Methane and Ethane
Methane and ethane concentrations were collected in Tedlar gas bags during each
THC measurement run on the oven exhausts to determine the natural gas contribution to
the total gaseous organic concentration. Volumes recorded were based on air
displacement in the evacuated containers with pre-test and post-test pressure
measurements.
6-6

-------
                    TABLE 6.3
SUMMARY OF EPA METHOD 18 QUALITY ASSURANCE RESULTS
          STYRENE RECOVERY EFFICIENCIES
Run No.
MES-3-3
RES-4-1
AFS-5-2
MES-6-2
MES-11-2
RES-11-3
MES-12-3
AFS-12-4
Recovery Efficiency, %
94
195
70
103
85
79.0
111
68
Acceptable Range, %
70%- 130%
70%-130%
70%-130%
70%-130%
70%-130%
70%-130%
70%-130%
70%-130%
Pass
Yes
No
Yes
Yes
Yes
Yes
Yes
No '
                    TABLE 6.4
        SUMMARY OF DESORPTION EFFICIENCIES
Compound
Styrene
Styrene
Styrene
Cumene
Cumene
Cumene
Methyl Methacrylate
Methyl Methacrylate
Methyl Methacrylate
Spike Level, mg
0.9009
4.5045
9.009
0.86
4.30
8.60
0.9306
4.653
9.306
Desorption Efficiency,
%
85.0
92.1
90.1
138.0
134.8
121.0
60.7
93.9
85.2
Acceptable Range,
%
70%- 130%
70%- 130%
70%-130%
70%-130%
70%-130%
70%-130%
70%- 130%
70%-130%
70%-130%
Pass
Yes
Yes
Yes
Yes
Yes
Yes
No
Yes
Yes
                        6-7

-------
  APPENDIX A




RAW FIELD DATA

-------
 Appendix A.I

Manual Methods
 Raw Field Data

-------
          APPENDIX A. 1.1

      Method 1 Field Data Sheets
(includes flows, moistures, and Method 18)

-------
        TRAVERSE POINT LOCATION FOR CIRCULAR DUCTS
Plant:.
Date:
Sampling Location:    f)(*~  A/->-  ^   C
Inside of Far Wall to Outside of Nipple:	
Inside of Near Wall to Outside of Nipple (Nipple Length):
Stack I.D.:	// "	
Distance Downstream from Flow Disturbance (Distance 3):
                 £O    inches / Stack I.D. =  3. ** dd
Distance Upstream from Flow Disturbance (Distance A):
                  30    inchee / Stack 1.0. =  2. ^ dd
Calcuiatad Bv:    "^-	
                                                               Schematic of
                                                             Sampling Location
Traverse
Point
Number
/
L
1
Y
r
(f






Fraction
of
Length
O.o W
o.(
-------
        TRAVERSE POINT LOCATION FOR CIRCULAR DUCTS
Plant:
Data:
                 A?
Sampling Location:
                                 0 u
                                    //" '"
Inside of Far Wall to Outside of Nipple:	
Inside of Near Wall to Outside of Nipple (Nipple Length):  _y






Nipple
Length
(inches)
0"




•
L










Traverse Point
Location
(Sum of Col. 4 & 5)
0.7
ZJ1
r.fY
/O.ffe
/2.. 8/
//. 3y






-------
        TRAVERSE POINT LOCATION FOR CIRCULAR DUCTS
Plant: l-ASCO  V^pp\j(_T%
Date: -
Sampling Location:  )T\Al Y\l

Insida of Far Wall to Outaida of Nippi.:    K//A _
ln.id. of Near Wall to Oub,oa of Nippl. 
-------
      TRAVERSE POINT LOCATION FOR RECTANGULAR DUCTS

Plant: _tA
Sampling Location:.
Duct Width, inches:.
Inside of Far Wall to Outside of Nipple:.
Inside of Near Wall to Outside of Nipple (Nipple Length):.
Duct Length, inches:     3**1  3~ *£>
Equivalent Diameter = 2xLxW/(L + W) = £>*.£.
Distance Downstream from Flow Disturbance (Distance B):
           ~                               \S
                 inches / Equivalent Diameter
Distance Upstream from Flow Disturbance (Distance A):
                 inches / Equivalent Diameter =
                                                                 i  •  • «
                                                                                          .vJP
Calculated Byt   A.
                                                  dd
  Schematic of
Sampling Location
Traverse
Point
Number
i
21
J
M
5"
OD





Fraction
of
Length
o,o§3
O,ZT
OMH
G,5B3
orwTo
0,-iH





Length
(inches)
-2/B




>
y


/






Product of
Columns 2 & 3*
(To nearest 1/8")
o2,32_
"7. OC3
It. 8
!^,32_
J2 /. OO
^25".(^€,





Nipple
Length
(inches)
A/VA




\




/





Traverse Point
Location
(Sum of Col. 4 & 5)
3.3/3
"7
)l£/B
I t^/S
ai
25 Vq





             If No Ports, Calculate Distances From Stack Walls For Port Locations
Number
of
Ports








Fraction
of
Width








Width
(inches)








Port Location .
Product of Col. 2 & 3*
(To Nearest 1/8*)








         *-AII points or ports should be an equal distance from each other (0) and 1/2 of
        -that distance from the stack walls (0/2), where 0 - Width / # of points or ports
-------
j at
               TRAVERSE POINT LOCATION FOR CIRCULAR DUCTS
      Plant: LASCQ
      Date:
      Sampling Location: Hux: \LvAfg-V f2.ce>Kr\ PvVMAO^I
      I raid* of Far Wall to Outside of Nipple:      f^ / A _
      Inside of Near Wall to Outside of Nipple (Nipple Length): N I f\
      Stack I.O.:
Oiatanca Oownstrcam tram Flow Disturbance (Distance 3):

                         inches / Stack 1.0. =  -^
                                                      dd
      Distance Ucntream from Flow Oisturtsance (Distance A):

                             O inches / Stack I.D. = <3. 0  dd
      Calculated 8y:
                                                               Schematic of
                                                             Sampling Location
       Traverse
         Point
        Number
roauct of
jmns 2 & 3
learest 1 /8")
.(i3
o7
53
?8
*o
1-2.
^8
IZ.



Nipple
Length
(inches)
A///1






\!






/


•

Traverse Point
Location
(Sum of Cot. 4 & 5)
£/e
^Hs
33A/
6 ^S
|33/3
15%
17%
nfa




-------
          APPENDIX A. 1.2

             Condition 1
(includes flows, moistures, and Method 18)
-------
                 GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:
Sampling Location:
Run »:
                                                     Date:  5
                                                     Clock Time:
                                           Operators:
                                    2&.S6 Static Pressure, in. HoO:
Barometric Pressure, in. Hg:
Moisture, %:    ^^      Molecular wt., Dry:_2£!jL Pitot Tube?Cp~I
Stack Dimension, in.  Diameter or Side 1:      (7.5" "    Side 2:      —
Wet Bulb, ° F:     (A	Dry Bulb, ° F:
Tr«v«™«
Point
Number
/
7
3
f
/
c.
7
f
/
i
3
^
5
(*
7
*






•



Velocity
Head
. in. H2O
/7
.2^
.30
?/
.33
.36
.2*
37
• 26
.2*
.2f
.^0
."2?
,^0
.3Z
.2-7









^P -0.^^18
Stack
T*mp.
°F
^/
f/
^7
f2
?2
42
11
11
-------
          WET-BULB/DRY-BULB MOISTURE CALCULATION
                                       Location:
                              -  13.6
Plant:	
Site: HFMKJ E*w*uL^-r  Operators:f/V/P^eRun #'• MfH'1     Date:
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack =   Pbar
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of HpO at Tw (from Table) =
                                   (Ps - Fvw) x
Vapor Pressure of H2O = Pva = (Pvw) •
Phar= 28.aa
Pa = T.«^
PS= 2£.So
TW = t>e>
Td= ftq
AT= 2.1
Pvw = 0 . b902>
in. Hq
in. HO
• 2
- in. Hg
°P
°F
°F
in. Hg
                )-
                                   2SOO-(1.3xTw)

                                   )X(  2.1  .   )
                       2800 -(1. 3 x lo
Proportion of Water Vapor by Volume = Bws
Una - (Ps)
T«mp.
OF
0
10
20
30
40
50
60
70
80
90
100
110
120
130
140
150
180
170
180
190
200
210
220
230
240

0
0.0370
0.0031
0.1025
0.1047
0.2478
0.3020
0.5210
0.7392
1.032
1.422
1.932
2.590
3.446
4.525
5.881
7.569
9.652
1220
1520
1941
2347
28.78
3540
4241
5044-

1
3.0398
0.0000
0.1000
0.1710
0.2370
0.3704
3.5407
0.7848
1.080
1.487
1.992
2.672
3.543
4.647
6.034
7.759
9.888
12.48
18.63
1942
2346
2043
3848
43.11
51.76
( Zt.io )
VAPOR PRESSURES OF V\
In Inches of Mercury
2
0.0417
0.0090
0.1127
0.1003
0.2077
0.3900
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
18.98
1944
24.46
2042
3647
4S42
52.70
3
0.0441
0.0728
0.1100
0.1878
0.2702
0.4052
0.5802
0.6183
1.138
1.561
2.114
2.629
3.744
4.900
6.350
8.180
10.36
13.07
16.34
2027
24.97
30.82
3747
44.74
5348
4
0.0403
3.0708
0.1248
0.1955
0.2891
0.4203
0.6009
0.8482
1.175
1.610
2.178
2.911
3.848
5.031
6.513
8451
10.61
13.37
16.70
20.70
2548
31.13
37.78
4847
5442
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2243
2.998
3.954
5.165
6.680
6.557
10.66
13.67
17.07
21.14
2640
31.78
3640
4641
5840
                                                        0.«7l(,     in. Hg
PER

<
r?o.z
27 It. <<
e
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9040
1.253
1.712
2.310
3.081
4.063
5.302
6.850
8.767
11.12
13.98
17.44
2149
2643
3246
3024
4727
5640
7
0.0541
0.0092
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.961
11.38
14.30
17.82
2245
27.07
3342
3040
48.14
5741
8
3.0571
0.0932
0.1502
0.2292
0.3304
0.4858
0.6903
0.9668
1.335
•1.619
2.449
3259
4.289
5.585
7202
9.200
11.65
14.62
1821
2242
2742
3347
40.78
4048
5843
9
0.0598
0.0982
0.1567
0.2383
0.3493
0.5038
0.7144
0.9989
1.378
1.878
2.821
3.331
4.408
5.732
7.384
9424
11.02
1446
1841
2240
28.18
3448
4142
4048
8047
-------
3 aa cza
                   GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: Lfl&tO Date: f '-#-97
Sampling Location: fl\A\/\ £vH«.o«/ Clock Time: /.?26
Run #: MS
Barometric P
Moisture, %:
Stack Dimen
Wet Bulb, °F
TrovcrM
Point
Numter
/
Z
3
1
S
c.
7
1

1
^
3
y
s
(,
7
f





•



-1-7- , Onerators: "7*^
ressure, in. h
3.*
q: 7A^2. Static Pressure,
Molecular wt.. Drv: 2& 0f Pilot
sion. in. Diameter or Side 1 : /7,5' " Side
V/k^ 5.
in. HoO: "^ 0 /
TubeT Cp: <4£ •??
2: 	
: 0f.t. nryflulhOF- #7

V.tooty
HMJ
in. H20
^,z./
^."2-"2-
^.'i'A
^.7.2-
0.W
0.23
03)
0.10

0,04
Q^
o ,VO
o ^\
b.VU
o .04
o ,»q
o ,T.D








^F-0,Y«g^
Stack
Temp.
°F
 * (0.32 X %02) + (0.28 X%N2>
Md - (0.44 x ) ••• (0.32 X ) f (0.28 x )
Md- Zfc.fc/
% HO % HO
100
M.-( )X(1--^5-
Mi- ^%Mk
T:. f/ °F- 5V/
P« - Pb + S'P' = ( )
13.0
P»- •7.<2/'?t^ln-H8
^P-^ Y0^
— r
v« • as.4» x Cp x ^AP x A|-
V« - 65.40 x ( ) x (
v«. ^3 ^^-7 IM

*•• /,fc> n2
1^« • W« v AA y MA «/m

Q«- x
Qs • 2, 2 00 £• aedm
JJV1.5
pg
Q« ..- Q« x 17.847X — x
ltd T,

Qi.,- X17447X-
*r •»"
100 '
^'•'-TB-'
°R (°F^460)
13.8
Ts^R)
Ps x Ma
,-J
JT-y
XOO
%H,0
i-^S-)
	 x(1--^
                                                  dMfcn
-------
         WET-BULB/DRY-BULB MOISTURE CALCULATION
Site: ^fei'" fc^-*-" Operarnrs-
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack = Pbar + -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of HpO at Tw
Vapor Pressure of H9O = Pva = (Pvw) -
7^/fo Run #: Mg- /- i
Pbar =
Pg =
-&-
Tw =
Td =
AT =
(from Table) = Pvw =
(Ps - Pvw) x (AT)
Xr<5*~0t-, t^y
- Date: 5^//%^7
2& ?2- , in Hn
t.-Ql in HO
2*3, ?2- in Hn
9f °n
£7 ; °P
6 OF
/ ^^ in Hn

                              2800-(1.3xTw)
Pva=(
                    2800-(1.3 x

Proponion of Water Vapor by Volume = Bws

                     (   /.oof*   )
1.00*1
(Ps)
Tamp.
°F
0
10
20
20
40
SO
60
70
80
90
100
110
120
130
140
150
100
170
100
190
200
210
220
230
240

0
0.0370
0.0631
0.1025
0.1847
0.2476
0.3820
0.5218
0.7392
1.032
1.422
1.932
2.590
3.440
4.525
5.001
7.569
9.052
1240
1549
1941
2347
20.75
3540
4241
5044-

1
0.0398
0.0060
0.1060
0.1718
0.2576
0.3764
0.5407
0.7648
1.060
1.407
1.002
2.072
3.543
4.047
6.034
7.759
9.005
12.40
15.03
1042
2340
2943
3540
43.11
51.70
in. Hg
( rw^)
VAPOR PRESSURES OF WATER &1, \
In Inches of Mercury 2_6»?'^-7
2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3006
0.5601
0.7912
1.102
1.513
2.052
2.749
3.042
4.772
0.100
7.952
10.12
12.77
1540
1944
24.40
2942
3047
4342
52.70
3 .
0.0441
0.0728
0.1186
0.1678
0.2782
0.4052
0.5802
0.8183
1.130
1.501
2.114
2.029
3.744
4.900
6.350
0.150
10.30
13.07
10.34
2047
2447
3042
3747
44.74
5345
4
0.0463
0.0768
0.1248
0.1955
0.2091
0.4203
0.0009
0.0462
1.175
1.610
2.170
2.911
3.848
5.031
6.513
0.351
10.01
1347
10.70
20.70
2540
31.13
37.78
4547
5442
5
0.0409
0.0010
0.1302
0.2035
0.3004
0.4359
0.6222
0.6750
1.213
1.660
2443
2.995
3.954
5.165
6.000
6.557
10.00
13.07
17.07
21.14
2040
31.75
3040
4641
5540
a
0.0517
0.0846
0.1370
0.2116
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.001
4.003
5.302
6.050
0.707
11.12
13.90
17.44
2149
2043
3240
3944
4747

7
0.0541
0.0092
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.705
2.379
2.169
4.174
5.442
7.024
8.901
11.30
14.30
17.02
2245
27.07
3342
3949
40.14
5741
• 8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4850
0.6903
0.9660
1.335
1.019
2.440
3.259
4.209
5.505
7.202
9400
11.05
14.62
1641
res?
27.02
3347
40.75
4948
5043
9
0.0590
0.0002
0.1567
0.2383
0.3403
0.5035
0.7144
0.0009
1.370
1.075
2421
3451
4.400
5.732
7.364
9.424
11.92
1446
1641
2240
20.10
3443
4142
4049
5947
-------
            PlantL
            Date-
                               METHOD 18 FIELD DATA SHEET
                               	     Tested Ana!yte:_^y.
        Location:
        Run#:
        Stack l.D.:.
        Pbar:	2i
                      ^  / - .•».
           Sample Tube *-
           Operators :
Orifice Tank #:.
Pump/Rotometer #:	
Pt:  Pretest (mm HaV. ^ooc <&. ic
    Post-Test (mm Hg)-_
Tt:  Pretest
                                                    Post-Test fF):.
        Leak Check: Pre:
                                   Post:
Time: Start! / Ac Finish: /dteSTotal:  *p. fr<
\nii-i. *,!   r>/n. &1   r*\  t      /^r^ .   '
)»
•1.3C
*
 V*-^V
Time
}$to
\U'o
IbOO
/<^C5'



Gauge
Vacuum
(Hg)
G
C
O
o



Row
Setting
Mc&fa'*
••>,...

*i
'

^
•

/
r
/
?

               Trev*rM
                D^I^A
                HOIIlt
               Numbar

                  2
Velocity
 HMd
In. HgO
                         ^92
                                                73
Md -


Md • (0.44 X


Md-
                                                              -t- (0.32 x


                                                             ) + (0.32 X
                                                                            ) •*• (0.28 x     )
                                                                         %

                                                    M.-


                                                    T.-
                                                 ---H
                                    Stack
                                    T.mp.
                                      73
-
 13.B
                        13.6
                                                    Vl - 85.48 X Cp x
                                                    Vs - 85.48 x (
                                                                      PaxM*


                                                                 )x(        )x
                                                                  ft/s
                                                      - V«xA«x8O«/m
                                                                            xM
                                                                  •dm
                                                                    Pt      %KLO
                                                    °«— "Q»* 17.647 x	x(1	2_)
                                                      •"            Tt       100
                                                             X 17.047 X-
                                                                                        100
-------
WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: / A$£O /hy&xJ-s- Location: /^£>-t*~^, f<^
Site: /fa. £xt*~ir Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of Stack = Pbar j; -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H^O at Tw
Vapor Pressure of H-.O = Pva = (Pvw> -
-7^- Run*: tff-l-3 Date: #
phflr= 2>%.T*~
Pg= -t-,01-
_P2_ Ps= 28,^
i y.b a,
TW = *fe
Trf. 73
AT= 7
(from Table) = Pvw = r ^^
(Ps - Pvw) x (A-T)
/"/T-7
in. Hq
in. HJO
in. Hq
°F
°F
°F
in. Hq

                                               2800-(1.3xTw)

                                                        7
                                                                      1.
                                2800 -(1. 3 x

 Proportion of Water Vapor by Volume = Bws
                                                                                in. Hg
 Bw-_
(Pva)
 (Ps)
                           (   /,/£/    )
O.o
                                                                                     
6s\0 o <&•
8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.819
2.449
3259
4.289
5.585
7.202
9200
11.65
14.62
1841
2242
2742
3347
40.79
4843
5843
9
0.0598
0.0982
0.1567
. 0.2389
0.3493
0.9039
0.7144
0.9988
1.376
1.679
2.921
3491
4.406
5.732
7.384
9424
1142
1446
1841
2249
28.18
3443
4142
4943
9947
-------
                 GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:.
Sampling Location:
Run#:
                                                       Date:
                                                       Clock Time:  ( 2.
                                             Operators :
Barometric Pressure, in. Hg: £%??£ 2ft.BQ  Static Pressure, in. H2O:_
Moisture, %:    A 9       Molecular wt., Drv:   W,^   Pilot Tube, Cp:.
Stack Dimension, in. Diameter or Side 1:     -2-V "       Side 2:_
Wet Bulb, ° F:      6*7         Dry Bulb, ° F:     1<	
   Tr
    Point
   Number

 n  i
       3
               Velocity
                in. H20
               • D-?
               .no
                . 1 1
Stock
 mp
 °F
                           T«mp.
                            °
                           ~77
                           77
                            -? r
                             -n
Md - (0.44 x %CO2) + (0.32 X %O^) + (0.28 X %f^)

Md - (0.44 x    ) + (0.32 X    ) + (0.28 X     )

Md -  2,$.tf
          % HO      % HO
M«-Mdx(i-—i_)*ia(—-i-)
            100         too

M« - (Zt-W ) x (1 -  ''^  ) * 18 ( A^  )

      _ / *v
M«-
                                        P«-Pb
                                               S.P.
                                               13.8

                                        P«- 28.15   In-Hg
                                                          ) *
                                                               13.8
                                                    —  , /   Ta (°R)
                                        Ve- 65.40 xCpx ^P x W	p9J(Ma
                                        V« • 65.40 x ( .

                                        V..

                                        A..
                                                     tt/«
                                                               xeo
                                        Qt-
                                                      idm
                                                       p,     %H-0
                                        Q> ..- Qt X 17.847 X	jc(1- 	a—
                                          M           !•      100
                                                    X 17.847 X-
                                                              536
                                                                           100
-------
          WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: Lf&0
Site: £00^ £,4^^ Ooerators:
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack = Pbar ± -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw
Vapor Pressure of HA;6 = Pva = *Pvw\ -
Location: fa* 30v«,«.f-
*tf\- Run*: tffi. |_i Date: .«;
Pbar = Z&tf
Pq = ~ . 6S
-£2- Ps= Z&-IS
Tw = 01
Td = 7f
AT= ll
ffrom Table) = Pvw = C,66» ^
(Ps - Pvw) x (AT)
i
^XM?-7
in. Hq
! in. HO
in. Hg
°F
'-°F
°F
in. Hg

                                2800-(1.3xTw)
                     2800 -(1. 3 x
 Proportion of Water Vapor by Volume = Bws
 Bws =
(Pva)
(Ps)
(
Tamp.
                       (  z*,-75  )

                     VAPOR PRESSURES OF WATER
                          In Inches of Mercury
                                                              in. Hg
OF
0
to
20
30
40
50
00
70
80
90
100
110
120
130
140
150
160
170
180
190
200
210
220
230
240
0
0.0370
0.0031
0.1025
0.1047
0.2478
0.3020
0.5218
0.7392
1.032
1.422
1.032
2.596
3.446
4.525
5.881
7.589
9.652
1250
1559
19.01
23.47
28.75
3540
4241
5044-
1
0.0398
0.0680
0.1080
0.1718
0.2970
0.3784
3.5407
0.7848
1.066
1.467
1.992
2.672
3.543
4.647
6.034
7.750
9.685
12.48
15.83
19.42
2348
2843
35.86
43.11
51.78
2
0.0417
0.0898
0.1127
0.1803
0.2077
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.740
3.642
4.772
6.100
7.052
10.12
12.77
15.88
1844
24.46
2842
3647
4342
52.70
3
0.0441
0.0728
0.1188
0.1878
0.2782
0.4052
0.5602
0.8183
1.138
1.561
2.114
2.829
3.744
4.900
6.350
6.150
10.38
13.07
18.34
2047
24.87
30.82
3747
44.74
5345
4
0.0403
0.0708
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
0.513
8.351
1041
13.37
16.70
20.70
25.48
31.13
37.78
4847
5442
5
0.0489
0.0810
0.1302
0.203S
0.3004
0.4359
0.6222
0.8750
1.213
1.860
2.243
2.995
3.954
5.185
8.880
6.557
10.66
13.67
17.07
21.14
2640
31.75

46.41
5540
6
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.850
8.767
11.12
13.98
17.44
2148
2843
3248
3844
4747
5840
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.981
11.36
14.30
1742
2245
27.07
33.02
3048
48.14
5741
8
0.0571
0.0932
0.1502
0.2292
0.3304
0.4858
0.6903
0.9668
1.335
1.819
2.449
3559
4589
5.565
7502
9500
11.65
14.62
1841
2242
2742
3347
40.78
4048
5848
9
0.0598
0.0982
0.1587
0.2383
0.3493
0.5035
0.7144
0.9080
1.378
1.878
2.521
3451
4.408
5.732
7.384
9.424
11.82
14.88
1841
2248
28.18
3448
4142
4848
5047
-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant- LftbLD Date: •5"-/^'-?"7
Sampling Location: /£»,* R^«^~ Clock Time: l$1o
Run*: RS-/-2- operat«r<:- rjQ- /£>+<*-£
Raromptrir Prt»s*i,ira ip Hg: 2tT f2 Static Pressure, in. HUO: -,&£

Molecular wt.. Drv ^^. ^ V Pitot Tube. CD: _ •?? 	
Stack Dimension, in. Diameter or Side 1 : W " Side 2: ?•%"
Wet Bulb. °F: &/ Drv Bulb. °F: ~r(s

TrovcrM
QA|K*
roint
Number
/
Z
3
y
$
*
i
t
>
V
f
0
/
Z
V
¥
5
Q
«
^
3
^
y
0
^••^^••^•^^^^•^^••M


Velocity
Head
in. H20
, O^
»6
j rt«
,n
Md-(0.44x 0 )>(0.32X 2-C )*(0.2Bx7f )'
Md- W.tf
% HO % H20
M..Mdx(i--j— )*ia< )00 )
M« - ( )x(1- 	 --— > * 1B( inf> >
M«- 2g^7
T;. ^/ °F- ^V/ °R(°F*4«»
0 p
P-"Pb*l3* ' * 13.6
P«- 2&«7 '"-"a
^- 0 ^^^
f Ta ^R)
17^ 1 _. , "U-
V« • 65.49 X Cp X VAP X \| -p, „ M,

v«- /7,Z77 «"
— V,67 n2
Qt- VtxAaxMa/m
Q.. X X00
Q.. y^3^5«*n
Pt %H7°
Of _n-Qi XI 7.647 X 	 x (1 • • * )
•to TJ 100
^•Id" X17.847X 	 — x(1- 1fl0 )
-------
        WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: LA*ff>
s'te: ILgr S^t^st Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of Stack = Pbar ± -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw
Vapor Pressure of H2O - Pva - (Pvw) -
Pva=( fl/W? ].(2%$7 -tfcH
Location: /^P/^**O., /^—
f4/P> Run*: ^-/-^ Date: $/
Pbar = -2W2-
Pq = ~.(e>5
-^- PS = ?l 67
13.6 / i
Tw= £Y
Td = ~7Ce
AT= f1~
(from Tahlp) = Pvw = 0. (oOO^
(Ps-Pvw) x (AT)
2800-(1.3xTw)
?? )*< /•&- ) O.Vlb

'"A?
in. Hg
in. H_0
2
in. Hg
°F
°F
°F
in. Hg
in. Hg
                   2800 -(1. 3 x



Proportion of Water Vapor by Volume = Bws



   -      -      (   OMlif }
WVVd
Tamp.
OF
0
10
20
30
40
SO
00
70
BO
90
100
110
120
130
140
150
160
170
160
190
200'
210
220
230
240
(f
0
0.0376
0.0031
0.1025
0.1047
0.2478
0.3020
0.5216
0.7392
1.032
1.422
1.932
2.596
3.446
4.525
5.661
7.569
9.692
1240
1549
19.01
23.47
28.75
3540
4241
5044-
3s)
1
0.0398
0.0660
0.1080
0.1716
•0.2570
0.3764
0.5407
0.7648
1.066
1.467
1.992
2.872
3.343
4.947
6.034
7.799
9.999
12.48
1943
19.42
2348
2943
3948
43.11
91.78
O.oit*   ttY.
( 2«.&7 ) ^
VAPOR PRESSURES OF WATER _^j?- \
In Inches of Mercury 17/7
2
0.0417
0.0696
0.1127
0.1803
0.2077
0.3906
0.5601
0.7912
1.102
1.313
2.052
2.749
3.642
4.772
6.190
7.992
10.12
12.77
19.98
19.94
24.46
2942
3947
4942
52.70
3
0.0441
0.0728
0.1186
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.829
3.744
4.900
6.390
8.190
10.36
13.07
16.34
2047
2447
30.82
3747
44.74
9348
4
0.0403
0.0768
0.1248
0.1955
0.2091
0.4203
0.6009
0.8462
1.175
1.610
2.176
2.911
3.846
5.031
6.913
9.391
10.61
13.37
16.70
20.70
25.48
31.13
37.78
4847
5442
5
0.0489
0.0610
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2443
2.995
3.994
5.165
6.660
8.557
1046
13.67
17.07
21.14
2640
31.75
3840
4941
5940
6
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.083
5.302
6.850
8.767
11.12
13.98
17.44
21.99
2043
3248
3944
4747
5940
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4666
0.6669
0.9352
1.293
. 1.765
2.379
3.169
4.174
5.442
7.024
6.981
11.38
14.30
17.82
2249
2747
3342
3949
48.14
9741
a
0.0571
0.0932
0.1502
0.2292
0.3304
0.4858
0.6903
0.9666
1.335
1.819
2.449
3.259
4.289
5.585
7.202
9400
11.69.
14.62
1841
CT.H
2742
3347
40.79
4949
5943
9
0.0598
0.0982
0.1567
0.2383
0.3493
0.9039
0.7144
0.9969
1.378
1.678
2.921
3491
4.409
5.732
7.384
9.424
1142
1449
1941
2249
29.19
3449
4142
4949
5947
^
-------
3UC3 CZ3
                              METHOD 18 FIELD DATA SHEET
       Plant:
       Date:  OS <3
Location:.
Run #:_
Stack I.D.:_
Pbar: M.1
                              - /-3
Sample Tube #t Ae"-JL-fliyAig-l.a4g
Operators: T4/awis'.	
                   	Post:   -
       Leak Check: Pre:
            Time
          Travcra*
            Point
          Number


                3
                 Gauge
                Vacuum
                  (Hq)
                          0
                           0
                          0
                          O
                          0
                Velocity
                 HMd
                         O-7
                         no
                          O9
                        / OS
                           10
                         ,/o/u
 Row
Setting
 Stack
 T.mp.
                           -79
                             7
                                     "'
                                   71
                                       Tested Anaiyte:
                                       Orifice Tank #•
             Pump/Rotometer #:_
             Pt:  Pretast (mm Hg): /ecofr.
                                                  Post-Test (mm Hg)-__f_2£o(*/
                                              Tt:  Pretest f F):        	
                                                  Post-Test
                                              Time: Start: <5HI  Finish: liHi  Total: ljb»»«v>
Md - (0.44x%CXl2) •!• (0.32 X%O2) + (0.28 X1*,^)


Md - (0.44 X    ) + (0.32 X    ) + (0.28 X     )
                                                            %H,0

                                                           l-T3->

                                                           .)*ie(--.)




                                                             °n (°F*4«o)
               i- Mdx(1
          %H20

          ~Tob~J
                                                               100
             M«-
             ')
             Te-
        13.8


P«-  'Z<8.«7  In. Hg
                       13.0
                                               V« - 85.40 x Cp:
                                               V« - 85.48 X (
                                                   xJSPx^
                                                                   PsxMt
                                                                 )x
                                               Qs-
                                        Qi^,- Qs x 17.647 x ~^-
                                          ttd           T,
                                                               xflO
                                                                      100
                                         Qi^,-
                                                           X 17.847 X-
                                                                                  100
-------
WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: 1.4&C0 r/^JLc.^ Location: /^V^****. e fa.
Site: ]}„*  	
: ftfr/-3 Date: £
Phar= ^9. f2
Pg = -.£6
Ps= Zt.tl
Tw= (03
Td= 81
AT= /<£
Pvw= £^222-
(AT)
*r/7>
in. Hg
in. H_C
2
'in. Hg
'°F
°F
°F
in. Hg

   2800-(1.3xTw)



•*fc )x(
                                                   p.
                    2800-(1.3 x



Proportion of Water Vapor by Volume = Bws
           )
(Ps)
T«mp.
OF
0
10
20
30
to
50
00
70
00
90
100
110
120
130
140
150
180
170
160
190
200
210
220
230
240

0
0.0370
0.0031
0.1023
0.1047 .
0.2478
0.3020
0.5218
0.7392
1.032
1.422
1.932
2.598
3.448
4.525
S.381
7.589
9.852
1220
1529
19.01
23.47
28.75
35.00
4241
5044-

1
3.0398
0.0600
0.1080
0.1710
0.2570
0.3764
3.5407
0.7848
1.068
1.467
1.992
2.872
3.543
4.847
6.034
7.759
9.885
12.48
15.83
19.42
23.98
29.33
35.68
43.11
51.78
                                  in. Hg
( 2*.«7 )
VAPOR PRESSURES OF WATER •'' ?f. ? _
In Inches of Mercury 2. ~7( &. f
2
0.0417
0.0090
0.1127
0.1803
0.2077
0.3900
0.5601
0.7912
1.102
1.513
2.052
2.749
3.842
4.772
6.190
7.952
10.12
12.77
15.98
19.84
24.46
2942
3847
4342
52.70
3
0.0441
3.0728
0.1100
0.1078
0.2782
0.4052
0.5802
0.0183
1.130
1.561
2.114
2.829
3.744
4.900
0.350
8.150
10.38
13.07
18.34
2027
24.97
30.82
37.07
44.74
5345
4
0.0403
0.0708
0.1248
0.1955
0.2891
0.4203
0.6009
0.8402
1.175
1.610
2.178
2.911
3.848
5.031
0.513
8.351
10.61
13.37
18.70
20.70
25.48
31.13
37.78
4847
5442
5
3.0489
3.0810
3.1302
0.2035
0.3004
0.4359
0.8222
0.8750
1.213
1.660
2243
2.998
3.954
5.185
6.680
6.557
10.88
13.67
17.07
21.14
28.00
31.75
3840
48.41
5540
6
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.083
5.302
0.850
8.787
11.12
13.98
17.44
2149
2843
3248
3924
4727
5840
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4688
0.6689
0.9352
1.293
1.765
2.379
3.189
4.174
5.442
7.024
8.981
11.38
14.30
17.82
2245
27.07
yyp;
3949
48.14
5741
8
0.0571
0.0932
0.1502
0.2292
0.3304
0.4858
0.6903
0.9668
1.335
•1.819
2.449
3259
4.289
5.585
7.202
9.200
11.65
14.62
1821
2242
27.82
3347
40.78
4ffffj
5843
9
0.0598
0.0982
0.1587
0.2383
0.3493
0.5035
0.7144
0.9989
1.378
147S
2.521
3481
4.406
5.732
7.384
9.424
1142
1448
1841
2249
28.18
3443
4142
4043
5947
                                                                  #J
-------
a at
»
•
Plant:  t-ASCte
Data:   2-M-4
Location
Run#:
                             METHOD 18 FIELD DATASHEET

                            	     Tested Analyte:_
                            	     Orifice Tank
Stack I.D.:
Pbar:   Z*. 9±
                 - 7-2
       Sample Tube
       Operators:
       Leak Check: Pre:   iX  Post:.
           Time
           3 i
 Gauge
Vacuum
  (Hg)
                        0
                        0
                        
           Point
          Number
           D
               Velocity
               HMd

                           Flow
                          Setting
Stack
T.jnp.
                                170'
                                             Pump/Rotometer #: A/^v
            Pt:  Pretest (mm Hg);_
                Post-Test (mm Ha): .010
            Tt:  Pretest CF):.
                Post-Test
                                                                          /<
                                      Time: Start: rag Finishing Total:
                                                     -  02:  -
            Md - (0.44 K %CX>2) + (0.32 X


            Md-(0.44K 0  ) -M0.32X
+ (0.28 X %r4j)


)+(0.28X  7f
                                                %H2O

                                                ~^b~;
                                                   f
                                               "
                                                         ln.HQ

                                             V«.«5.48xCpX VAP X
                                                                 pxM«
                                      V« - 65.48 x (


                                      v«- 32.7^  «/•
                               .#
-------
3 aca i_^
                       GAS VELOCITY AND VOLUMETRIC FLOW RATE
      Plant:	
      Sampling Location:
      Run#:  9- / - /
                                                     Date:   S'-)V-97
                                                     Clock Time:
                                                  Operators:
                                                  Static Pressure, in.
Barometric Pressure, in. Hg:,9?. 
,ao
,31
,^6
/ClG
/ 10
, /q
f /o
<^o
rQ^
,op














Stock
T«mp.
°F
I&G
IL'1
\(,. ^
JbA
/*,?
/*e
If, 7
//,^
m
(1 r>
,-o i
/••) j













TJ- /(,*»
                                             Md - (Q.44x%CC2)


                                             Md - (0.44 x &  } > (0.32 X t/  ) f (0.28 x 7*?  )
                                             M« • Mdx(l
                                                %H2O

                                                  100  "     100

                                                ) x(1 - -
                                                      100
                                                            13  ) + 18(-^_)
                                                                       100
                                                                   13.0
                                             P«-
                                                         in. Hg
                                             V.. 85.49 XCPX^PX
                                                         -=   I   TsfR)
                                      V«- 65.49 X(
                                             A..
                                                      .77
)x(
                                      as-  32.^   x J.i3
                                                                   xeo
                                                          «*n
                                          - QlX1 7.847 X — x(1
                                                     Tl
                                                                   100
                                             CJi^,-
                                                  X 17.647 X-
                                                                              100
-------
Plant	
Sampling Location  $-t
Run Number 9 - / • ^  Date:  JJTW-^^
Pretest Leak Rate:  tOQc   cftn @ i£  in. Hg.
               • • - •  i i   i  ^^ —-
Post-Test Leak Rate: . g&c cfm @ /<£_ in. Hg.
Post-Test Leak Check: Pitot: wx)   Orsat: -
FmwM
Point
Number



























Sampling
Time
(mln)

/0
Po
r?o























Clock Time
(244iour
dock)
J24o
iteo
/3oo
I*>IO























GM Meter
Reacting
(Vm)n3
4/
11 $,-)!>
<)H?>W>




. -


















Velocity
Head (Ap)
lnH2O
Oriic* Pressure Differential
(AH) in H20
Desired
| Actual
Stack
Temp.
a^
• Temperature
°F
Probe
'/////////////////////////////////'


























APr^
/• W
y- fxd





































































































| Filter
Impinger
Temp.
°F
Dry Gas Meter Temp.
Inlet
(Tm in°F)
Outlet
(Tm out°F)
Pump
Vacuum
(in. Hg)
y//////////////////////////


























9H
^
y<^>























73
7^
9^

















































V
*
*








^














                       T«=  ~
              Tm=
-------
                       SAMPLE RECOVERY DATA
PLANT

DATE
                                              Run No.
                       Sample Box No.  A/-/     fab No.
                                                             . Qg>3
SAMPLE LOCATION

TRAIN PREPARER
                                              Filter No.
                                                          A/fr
SAMPLE RECOVERY PERSON
                                             , ELL.
COMMENTS

FRONT HALF
Acetone
Container No.

Filter
Container No.

Description of Filter
                   EPA.
                                   4
                    IJ
                          vx^U.

                            Liquid
                            Level Marked

                                              Sealed
                                              Sealed
Samples Stored and Locked

BACK HALF/MDTSTpKF,
Container No.
Liquid Level Marked
                                              Sealed
IMP. NO.
1
2
3
4
. 5
6
CONTENTS
ZVT «,o
nr »,c
£vWv
&/,-.« (^1


TOTAL
INITIAL VOL
(ml)
/CO
/OO
—
200



WEIGHT fgranui
INITIAL
(iC*..S
606, V
^72
^26.fi


25 2> t.^
FINAL
b^?,l
tO^.8
44TA
fi2>!.3


254S-0
NET
' Z.\o
o.4
o.bck^ad
4.S


&>l^r$'
                                                                          n/
-------
^ OC3 f ~3
fcs
              EPA METHOD 4 MOISTURE CALCULATIONS
      PLANT:  LEA(LO	SOURCE/RUN *' 3.-1-2-  DATE: 5-14-    scf
                                wstd
       4. Percent Moisture, by Volume

           R  -       VWSW
           DUL/C -~ ~
                    V    -»• V
                     wstd   mstd
           Bws =
              ^= O.Oife
                  I.S %  Ptoi4TURE
-------
              GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:  • / 7 - ~; j
ung Location: f>/ry  Static Pressure, in K,n- -,~>V
jre, %: \ .-frS^
_ Molecular wt., Drv: Z«.6^ Pilot TubB^Co: . ^
Dimension, in. Diameter or Sid
ulb,°F: - nrv

nra*
lint
nter
(
Is
3
V
5
V

/
•i.
*
V
b
^














V.loeny
H««d
in. H20
,/^,
'90
rSf
-3\
-90
,93

,/v
,/<3
_.^/
.^a
,53
.SI












fip-o,v*ni
Stock
T«mp.
°F
/?/
/'75
/7 3
/7V
/7V
y7V

/7V
/7*/
^75
/7 V
/7 Y
/9V












ft- 1-73

81: -l^t* Side 2: 	 	
Bulb.°F:
Md - (0.44 x %CO2> + (0.32 X %O2> -t- (0.28 X %l^)
Md - (0.44 x ) * (0.32 X ) + (0.28 X )
M«- Z£.S>, °F- V.B3 °R(0F*460)
P« M Ok j. ^-"* _ / -iQ Li.rv \ j. *"T?-"^O
13.8 -(2&&D)+ ,38
P«- ^."H In-Hg
^-c.M-1>1
r= J Ts ^R)
V.- 05.49 »CpxVAP x ^ P9XMB
V. .aSdflV( T<^ )»( MH>\ )»J ,., ^»£2>
V »>M • ^«..
v«-32>.»fc ft/«
A.- \.Z3 ft2
Q» - VixA«xeot/m
g^
Qi-jfciW^ x x80
°»- tM^^ ««*n
Pt ^K.0
Q« •4»Q«xi7.e47x 	 x(t. — *— )
•" T« 100
a, -n X1TMTJ1 ^M i.&
«» toib '«
QMd- 1^2^- d«tai~
-------
                                              RELDDAiA^FiEET
Plant
Sampling Location
Run Number: 9-/~ 3
Pretest Leak Rate:
                     Date:
                      cfm
             Sample Type: in-
             Pbar
             CO2:
                                                             Operator:
                                                         Ps:
O2:    —
15  in. Hg.    Probe Length/Type:
           Pilot*:  -
Nozzle ID:   —     Thermocouple #:
Assumed Bws: 1.8%. Filter #:      —•
Meter Box #:  /*/  Y: ..^ C_AH@:
Post-Test Leak Rate: .^c,g_cfm @   in
Pretest Leak Check: Pilot: Mrt Orsat:  -
                                         Stack Diameter:  15*    As: 1.2. 3 fl-*     Post-Test Leak Check: Pilot: N/3 Orsat:  —
Point
Numto
V
















;









Sampling
Tlnw
(rrtn)
D
/O
2*
3e>



















•



CkxfcTbM
(244iour
dock)
/5<^
/^5V?'
/ew
It/0























GaaMeUr
Reading
(Vm)«3
949. 7f^
75?, 3
#**
•fo. ?^»




.


















Velocity
Head (Ap)
inHZO
Oriica Pr«Mur« Differenlial
(AH) in H20
Desired
Actual
Stack
Temp.
as)
Temperature
°F
Probe
'/////////////////////////////////S




















































^7
/.1
t. °)











































































Filter
knpinger
Temp.
°F
Dry Gas Meter Temp.
Inlet
am in°F)
Outlet
(Tm out°F)
Pump
Vacuum
(in. Hg)
'///////////////////Y///////


























t*>
**
^^


i




















?#
*z
?g























*?
*1
?
-------
                        SAMPLE RECOVERY DATA
PLANT ^-^CO
DATE 5-l4--<=n
SAMPLE LOCATION

Sample Box No. /1/--5
OVEM * q ~^c


Sealed


Sealed
Samples Stored and Locked

BACK HALF/MPTSTTTRq
Container No.
Liquid Level Marked
                                                Sealed
IMP. NO.
I
2
3
4
5
6
CONTENTS
AT tfcC
PT rt-,o
£=-v"/?J-y
£ki*f**\


TOTAL
INITIAL VOL
(ml)
/o o
/oo
• 	
2.00



WEIGHT (gnnii
INITIAL
•5&8.0
-5T7.Y
yfe?
7^/o


Z4o^ rL
FINAL
57^,5
S&8.Z.
4^3,4
71>5.&


24113
NET
• z.e
o.a
O.(o
4, a


a. T

ft
-------
r=~
              EPA METHOD 4 MOISTURE CALCULATIONS
      PLANT: Lfr.^0 _ _ SOURCE/RUN #:_iik2i_ DATE:  5-/4-*f7


      1 . Leakage Correction for Volume Metered
          Vmc=vm-(Lp-0.02)x0


          Vmc=(       )-(       -0.02) x(


                     *   ft3
      2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)


                                Pbar+(AH/13.6)N
          Vm   = 17.64 xV_rxYx
            mstd         mc
                                        m



                        U4-.II8 )x(o.^t
       3. Volume Water Vapor Collected, Standard Conditions


           Impingers & Silica Gel = V...  = 0.04707 x (W. - W.)
                                 std            T    '

                              Vw  = 0.04707 x(  a .7   )
                                 std

                              V.«  =   Q.41O   set
                               wstd

       4. Percent Moisture, by Volume
           V

*WS=    w
                        wstd
                     wstd   mstd


                     (  o.4lo  )
                   0.410
   — l.fe  %  Moit>TuR.C
                                                                       .a
-------
Date:__^
Location:
Run #: *Q- /-
Stack I.D.:
Pbar:
                      METHOD 18 FIELD DATA SHEET

                      	    Tested Analyte:_
                      	    Orifice Tank #:.
                                     Pump/Rotometer #:	
                                     Pt:  Pretest (mm Hal: .  ceo
Sample Tube
Operators:
                                         Post-Test (mm Hq)>
• A \
, IQ
i /#
r£O













\
SUck
Temp.
°F
&£ ">
0 )<
OSltl
•5QC
.3/>O~
'99C
cyj
p^
•J30
9/<7^-
3/'7 r
a?d;













                                                      -°2:
                                                              -C02L
     Md - (0.44 x %C02> + (0.32 X %a,) + (0.28 X %N2)


     Md.-(0.44x 0  ) + (0.32 X a. I  )+(0.28x7^
  o I / 0
    Md-
                                     M. -
                                              %H2O
                                                        %H,0
                                                          2
                                          .7%
                                      '-  1&.&
                                                IH.HB
                                                                        .? '
                                                         i(°R)
                                               ^.^7
                                    V« - 65.40 X < frr**??*) X (
                                                             •V
                                                                28.15,
                                    A.-  //ZZ;7   n


                                    Qt-VsxAaxflOi/m
                                                          x0o
-------
FIELDDAlAWiEET
Plant	
Sampling Location <&.'«.*»
Run Number  /&vL-/ Date
pretest Leak Rate:  .ooV  cfm @ /^  in. Hg.
Pretest Leak Check Ptot: A>^ Orsat:  -
Sample Type: A\ " V   Operator:
Pbar-^frfofr     Ps:	
CO2:  *fe-a°    Q2:	
Probe Length/Type:	
Stack Diameter:  /t>x/>
                 Nozzle ID:
                                                    Thermocouple #:
                 Assumed Bws: .2. > Filter*:
                 Meter Box i
   Pilot #:
As:_L23-fVL
                                                            AH@:
                                    ost-Test Leak Rate:  gol  cfm @ /T in. Hg.
                                   Post-Test Leak Check: Pitot: l-4A Orsat: ' —
TravwM
notnt
Numb*

.,,
*
























Swiping
Tkm
(mlrj
CO

fin
™0























OockThm
(244tour
dock)
;<9y^
/o^o
/( *^
;/ /o























Gas Meter
Raacfing
(Vm)ft3
99^,^6 S
^63,90
?// 10
0o























Velocity
Head(Ap)
lnH2O
Oil ca Pr«e«ur« Differential
(AH) in H2O
Desired
Actual
Stack
Temp.
fTs)
Temperature
°F
Probe | Filter
s/// //////////////////////////////,


























A?&
I ,U
t'Zi*





































































































Impinger
Temp.
°F
Dry Gas Meter Temp.
Inlet
(Tm in°F)
Outlet
(Tm out°F)
Pump
Vacuum
(in. Hg)
///////////////////////////




























-























*1
^
-------
                       SAMPLE RECOVERY DATA
PLANT .

DATE  	

SAMPLE LOCATION  	

TRAIN PREPARER    T/?~
                                              Run No.
                       sample Box No.  A/O   Job No.
                                              Filter No.
                                                          "A
SAMPLE RECOVERY PERSON

COMMENTS
FRONT HALF
Acetone
Container No.

Filter
Container No.

Description of Filter
                                 4
                            Liquid
                            Levei Marked
                                              Sealed
                                              Sealed
Samples Stored and Locked

BACK HALF/MOISTimF
Container No.
Liquid Levei Marked
                                               Sealed
IMP. NO.
1
2
3
4
5
6
CONTENTS
®T #*o
-or *iO
^W/
$ke« G-e.1


TOTAL
INITIAL VOL
(ml)
)Q O
/OO
. 	
£00




WEIGHT (gnnsi
INITIAL
55?. £
66V. 7
5/A ^
^3y,6


25fc3.4
». » i
FINAL
55*7,2.
btS.7
ftt.o
e>&^


zztb.s
NET
• 6.7
l.o
o.4
4.e>


/£&



. .£,- »- . >•. /•**/
-------
        EPA METHOD 4 MOISTURE CALCULATIONS
PLANT:  L^<^p _ SOURCE/RUN *' /o-M   HAT& 5-14-97


1 . Leakage Correction for Volume Metered
    Vmc=vm-(l-p-0.02)x0.


    Vmc=(       )-(        -0.02) x(


                   ft3
2.  Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)


                          'Pbar+(AH/13.6)N
         = 17.64 xVmcxYxx
                                 'm
                                                      /13-6)'
          = 17.64 x(23.-73S )x(o.itu   )x
      ISM                          ,..^       (s^s  }


                   _dscf
 3. Volume Water Vapor Collected, Standard Conditions


    Impingers & Silica Gel = V ...   = 0.04707 x (W, - W. )
                         w             v
                           std
                         wstd

                        Vw   a  0. b07    SCf
                         wstd
 4. Percent Moisture, by Volume


                Vwstd
                      mstd
     Bws =
           (o.bo7
           2.1  %  P\OI6TUR£
-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: LA^tO Date: 6'l^'9~)
Sampling Lo
cation: <9 Us A' ^/O 2xfiWs'T Clock Time: I32£
~ / ~^ Ooerators: 73 /Mi*. S .
Barometric Pressure, in. Hg: ^ ? ^- Static Pressure, in. HoO: _!_^gBL -' ^
Moisture. %: 2, 3 tf ^
ii Molecular wt.. Drv: Zti.g'S Pilot Tube. CD: -93
Stack Dimension, in. Diameter or Sid
Wet Bulb. °F: - Drv

Travaraa
Point
Numbar
A- 1
9
3
V
3
6
a- /
5
3
V
b
6












^••••M^BMUBMB^^MMi


Valochy
Haad
in. H2O
rQl
^.9->
,9;
' /?
<^?
^/
,M
,/6
, / 1
,-96
.-^9
.9 S













XP.OV&'
Stack
T«mp.
°F
s>(/
91)
a ; •>
J7/5
.9/ r
•9ir
.9/<
-?t
%3 /
.9^0
910
3 n













Tl. 9 /U
B1: TV*/<" Side^: —
Rulh^F- —
Md - (0.44 x %C02) + (0.32 X %O2) + (0.28 X %**£
Md - (0.44 x ) ••• (0.32 X ) + (0.28 X )
•"-Wf A-;/~
% H.O % H20 '
Ma • Mdx(1 - 	 ) * 18 ( — — — )
100 100
Ma-( )x(l- tnn )>ia( >
M.- Z^^
^-2/r °F'^7f °*(°r + *«»
SP • - fS'"
13.6 J(^8'/1) ' 13.8
*- 2^85 in- HS
^p-^y^3
	 / T. («Q1

Va - tO>.4li x (J0 x VA^ « V "Tax Ma
V.-85.48X, ,^ )*<.**# ,xJ_iZ±-r
1 2#.tffi 1*-)
V.- ^VJ3 ft/a
A.. /. 1^7 n2
Qa - VaxAaxeOa/m
Qa- x xOO
v,0«- l^."/ adm
P« %H2°
O»^- Q« X1 7.847 x — x(1- * • >
•to Ts 100
Oi^- Xl7.e47X^ 	 Xd* 	 )
                                            100
-------
              GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:
Samplinq Location: djesJ A9 Z*k4j<± Clock Time: M2t>
Run #: /O - / - 3 Ooer^"^' PA^ /TO
Barometric Pressure, in. Ha: $%< Zd Static Pressure, in. K,O: ^
3
*f
^
^









•




Velocity
Head
in. H^

,41
'35

.33
,33
.$3
,3ti
- 26
..96












OP-O.tW
Stack
T«mp.
°F
35*0-.
9-9 a
9^-3
,^S>3
3&\
BSO

W§
222
Zl*
333
9£>\
33i\












Tf- 222.'^
91: 7^'^ /5 Side 2: ^ 	 '
pi,|hOp- — .
Md - (0.44 x %C02> •*• (0.32 X %
Sa
13.0 13-8
P»- 2^/73 "«-H8
^SP- «/^7
— f Ts ^H)
P~ J ' ' \ "'
Ve - «5.48 x Cp x 4b? x y " "p, ,; ^8

V
v«. 3^ 700 «/•
Ae- |.Xl? n2
Q»- V«xA»xeOi/m
Q«- x xOO
Q«- Z£7£3 «*"
Pfl %H?°
0* ...QiXl7.e47x 	 x(1- * }
*td T, 100

-------
                                            FIELD DA IA SHEET
Plant:
L.Jt->Lt?
ling Location
lumber: /£>~j
t Leak Rate:
1 Leak Check

*v*+^l£>
i-2 Date: 5-#-f7
.•»£. cfm@ iff in. Hg.
: Pitot: MA Orsat: -
Sample Type: ft- 7
Pbar Zf.tf Ps:
CO2: O O2:
Probe Length/Type:
Stack Diameter: K"
Operator: 7^
2.8.9-
2-J
	 Pitot #:
As: |.23



; 	
-ft2
                                                              Nozzle ID:   ~    Thermocouple #:  —
                                                             Assumed Bws: > -1"^ Filter #:   ^-
                                                             Meter Box #:  /^   Y:  #££, AH@
                                                              Post-Test Leak Rate:  ga^ cfm @ /fa in. Hg.
                                                             Post-Test Leak Check: Pitot: Nf 
-------
                       SAMPLE RECOVERY DATA
PLANT  /. h^L
DATE   5- H-T7     Sample Box No.  A/- 6

SAMPLE LOCATION  0\/£Ki  ** 10  ».A\A

TRAIN PREPARER
Run No.

Job No. .
                                                            CO
                                              Filter No.
SAMPLE RECOVERY PERSON
COMMENTS

FRONT HALF
Acetone
Container No.

Filter
Container No.

Description of Filter
                   EPK   NUruors   4
                            Liquid
                            Level Marked
  ^


 Sealed


 Sealed
 Samples Stored and Locked

 BACK HArF/MOTSTTTRF
 Container No.        	
 Liquid Level Marked
                                               Sealed
IMP NO

i
2
-3
4
~ 5
6
TO]
POKmrxTrr

TXT it,o
or y?o
E*«x?A/
V/,-c^
66 6c/


RAL
INITIAL VOL
(ml)
/CC)
/OQ
	
zoo




INITIAL
. $-9 A 9
662.3
VSSf
764/.^'


247 4, /
WEIGHT (gnnui
FINAL
5^5. a
bb1),0
45UO
7t>J.t>


2.483,8

NET
• 3.3
a7
D,b
•5.1


w
-------
        EPA METHOD 4 MOISTURE CALCULATIONS


PLANT:  LkSQD _ SOURCE/RUN *' /A-t-% DATE:


1 . Leakage Correction for Volume Metered
    Vmc=(       )-(       -0.02)x(
2.  Volume Metered,,Standard Conditions (68 F, 29.92 in. Hg)


                          Pbaf+(AH/13.6)N
    Vm   = 17.64 xVmcxYx
     mstd    .     mc        ... . .T
                                  m.

    Vm   = 23.5   rterf
      mstd
 3. Volume Water Vapor Collected, Standard Conditions


    Impingers & Silica Gel = V    = 0.04707 x (W, - W. )
                           std            f   '

                        Vw  = 0.04707 x( ^,
                           std

                        Vw   = 0.45-7   scf
                         wstd
 4. Percent Moisture, by Volume


                Vwstd
              V    + V
               "'      mstd
               (  0,457  )
           (0.4-57
-------
METHOD 18 FIELD DATASHEET
i-'ianrz/'i^ Tested An^iy*0' fyr***^
Date: 5Vy-*T Orific0 T^ *' *#T*"?
Location: ^v£0- \/b& Pump/Rotometer #: - , _.,,
Run*: toBD- / r- 7, M Nfr- I - 3 Pt: Pretest (mm Hg)- 	 Z 	
Stack I.D.: ^2^HaSr & t.s'x^" Post-Tflst (mm Hg); -
Pbar: 2f.fr Tt: Pretest PR:
Sample Tube #
• fi/DB-/-St-. /UDB-I-3& Post-Te«?t fP)1
Time: StartMS'ft? Finish: H»*
/i>y. ^>4«>
/SS7. 09/4&>
Gauge
Vacuum
(Hg)
* /
/
/
r
/
1
/

Flow
Setting
i/
^\
£»
?j
-*i
zl
i\

Trov*raa
Point
Number

























Velocity
Head
In.H^

























Stick
Temp.
°F

























• 	 • 	 £. 	 £
Md - (0.44X%C02) •*• (0.32X%02> + (0.28x%N2)
^t- Md - (0.44 x ) + (0.32 X ) •»• (0.28 x )
1?
w Md"
% HO % H20
^ M..Mdx(l--^r> + l8(-j3-)
Me - ( 'x'1 100 100
^/
93 "*"
^ Te- °F- °R(°F*4«0)
SP. V
P"Pb*^TJ<< )+ 13.8
Pt . In. Hg
J5P-

V« - 6SM X Cp X VAP x ^ p,XMe

Ve - «/•
A.- n2
Q«- VexAexOO«/m
OB- x xW
Oe • aeftn
Pi %H2°
Q> ..» 01X17.647 x — X(1« )
•id Ti 100
<*.«- ^'•fl4;x 	 x(l' loo'*
Otgtd* dMfen
-------
3OQ S
o
/6
20
3<>
^
^
^
Plant: ^/^^^
Date: <-///-f7
Location: /l/D<3 «-^*j/c/»/ ^
Run#: n/n/J- /- /
Stack I.D.: 32." x ^"
Pbar: ^fr.^2.
Sample Tubi
Operators: ,
9*- NDA-l-\Q M^fi'l-IH
T*
L_eak Check: Pre: ^ Post: "^
Gauge
Time Vacuum
(Hg)
/&<:. 7V,$ i-
Flow
Setting
1.1
"if
Zl
~?.i
11
z/
21

Trov«r««
Point
Numbar

























Velocity
HMd
In. H^O

























Stack
T«mp.
"F

























/*k-
f"
^^5
50
^^
[?1
*7
^f
61
                              METHOD 18 FIELD DATA SHEET

                                              Tested Analyte:	t&
                                              Pump/Rotometer #:_
                                              Pt:  Pretest (mm Hg):   —
                                                   Post-Test (mm
                                              Tt:  Pretest fF):.
                                              Time: Start: iVXe Finish://?/ Total:

                                              W/B:	D/B:	O2: ^c CQ2:

                                                                    2v         W
                                              Md • (0,44*%CQ2) + (0.32 X%02> -t- (0.28 X%^)


                                              Md - (0.44 x    ) + (0.32 X    ) + (0.28 X    )


                                              Md- -2.5.64-

                                                         % K,0      % K,0
                                              Mi-(


                                              Ma-

                                                                 ) +
                                              Pt •
             In. Hg
Va - 65.40 x Cp X VAP X




V« - 85.40 X (        ) X (



V«-           fl/«
                                                                    p,xM§
                                                                         )X
                        i
                                              A.-
                                                 . V«xA»x«0«/m
Q»»

Qs»


^rtd
- Q«XI7.847x	x(1
                                                            oeftn

                                                              p.     %H.O
                                                             - X1- — •*-
                                              ^Md-

                             •x(1
-------
"""Plant:
  Site:  Wfrfr
    WET-BULB/DRY-BULB MOISTURE CALCULATION
LASCC	       Location: _A/DO  -
                                Run #:
                       Operators: f/
-l '3   Date:
                         Pbar±-f3f
  Barometric Pressure, in. Hg =
  Static Pressure, in. H20 =
  Absolute Pressure of Stack =
  Wet-Bulb Temperature, °F =
  Dry-Bulb Temperature, °F =
  Temperature Difference, Td - Tw =
  Saturation Vapor Pressure of H2O at Tw (from Table) =   Pvw =
                                    (Ps - Pvw) x (AT)
Pbar =
Pg =
Ps =
Tw =
Td =
AT =
Pvw =
7_tf.tfO
0.0\
L3.V>*
6V
ID
L
.(,60^
in. Hg
in. HLO
2
in. Hg
°F
°F
°F
in. Hg
  Vapor Pressure of H20 = Pva = (Pvw) -

  Pva=(
                                   2800 - (1.3 x Tw)
                                   ) x (    6     )
                       2800-(1.3 x  i
Proportion of Water Vapor by Volume = Bws
«.„._   (Pva)    _       (
(Ps)
T«mp.
OF
0
10
20
30
40
50
60
70
60
90
100
110
120
130
140
150
160
170
180
190
200
210
220
230
240

0
0.0370
0.0631
0.1025
0.1047
0.2478
0.3020
0.5218
0.7392
1.032
1.422
1.932
2.590
3.440
4.525
5.681
7.569
9.652
12.20
1529
19.01
23.47
28.75
35.00
42.31
5044-

1
0.0398
0.0600
0.1080
0.1710
0.2570
0.3764
0.5407
0.7648
1.068
1.467
1.992
2.672
3.549
4.647
6.034
7.759
9.885
12.48
15.63
19.42
23.96
29.33
35.68
43.11
51.76
                                                                     in. Hg
( i«.efl )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0096
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
15.96
19.84
24.46
29.92
36.37
43.92
52.70
3
0.0441
0.0728
0.1100
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.629
3.744
4.900
6.350
8.150
10.36
13.07
16.34
2027
24.97
30.52
37.07
44.74
5345
4
0.0403
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
6.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.87
5442
5
0.0469
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
0.880
8.557
10.86
13.67
17.07
21.14
26.00
31.75
38.50
46.41
5540
6
0.0517
0.0840
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
0.850
8.787
11.12
13.98
17.44
2149
26.53
3248
3924
4727
5640
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.961
11.38
14.30
17.82
2245
27.07
3342
3949
48.14
5741
8
0.0571
0.0932
0.1502
0.2292
0.3384
0.4858
0.6903
0.9666
1.335
•1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1821
22,sg
27.62
3347
40.75
4943
5843
9
0.0598
0.0982
0.1567
0.2383
0.3493
0.5035
0.7144
0.9989
1.378
1.875
2.521
3.351
4.408
5.732
7.384
9.424
11.92
14.96
1841
2249
28.18
3443
4142
4943
5947
-------
          APPENDIX A. 1.3

             Condition 2
(includes flows, moistures, and Method 18)
-------

                         METHOD 18 FIELD DATA SHEET
I
Plant: £-*}€,<> Tester* Analyta- -Vw r*~*-
Date: ^/'i/if Orificn Tank *• ^17/3 - 2— -
ocation: AM frl*~-r Pump/Rotnmeter #:
Run*: /*
V
J
(^

A

$ V
7.
t,
. I*-®
0, 2.7
^."27
. ?.. £oV3





Stack
Tamp.
If
f =1
f 2-
^ 2-
f 2—
f »-
9 'Z—
f /

10
(^)
/^^
(/ 6 Md . (0.44 x ) + (0.32 X ) * (0.28 X
% HO % HO
70 M.-Mdx(1.-^-) + 18(-— )
"7 ' Ma-( )x(1- 	 ) + 18( )
100 100
M*" *2&rf( ^^.(1)6 ^
Ta« ^2- °F- 5^2^-°R (°F-|-4«0)
13.8 13.8
^P- .5W3
1 T. XJB»
?= < 1 ' '
va - <».«* x up x «y- x ^ P, x Ma
Va - 85.40 x ( ) x ( ) x \l 	

/st*0 C-'
, 2
** " 1 ,v> /

Qe • VaxAax80e/m

Qa • x x80
/> j^/J ^^
°*" 3j^T2^ "^ Jiil'P
P«J /• VteU
Qa.. -Oexi 7.647 x 	 x(1- • )



s








6?t>~*~-
o
>/ r /
/-V^A^ -
If^t^f^
i*t>£

100
-------
         WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: /_,^0 ^^>r I orar,nn- ^ 	 r ^,,
Site: /^U, £>£,,,, Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of Stack = Pbar + -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H20 at Tw
Vapor Pressure of HoO = Pva - (Pvw) -
D-°''03.^C kit
PW«=/ rcm } (.2f.e/ - T^>;
M- Run*: Wf-t
Pbar =
Pg =
-EL- Ps =
13.6 KS
Tw =
Td =
AT =
(from Tc^ei = Pvw =
(Ps - Fvw) x (A"0
2SOO-(1.3xTw)
^£.
fflx( ZY )
p
-1 Date: $//#$ 7
^0.«.Q^ in Hg
£g OP
f-L- Op
2-y -OF
. (*#*£ _B£ in. Hq
su u> i 0_3
?.<-/
-------
cia
                   GAS VELOCITY AND VOLUMETRIC FLOW RATE
  Plant:
  Sampling Location:   /£.«„ £yU~.tr
                                         Date:	
                                         Clock Time:  2.*-1*-/
  Barometric Pressure, in. Hg:   "Z-ft sy	  Static Pressure, in. l-^O:
  Moisture, %:     0. 3     Molecular wt., Drv:  ^gftV    Pitot Tube, Cp:_»
  Stack Dimension, in. Diameter or Side 1:    ' 7 £         Side 2:   	
  Wet Bulb, °F:__£/_
                 Drv Bulb. °F:   10
     TrovcrM
      Point
     Number
           S
  V.tecity
&-0.t/ffl
   Stack
   T«mp.
                            11
                            1*
                            91
S- ^V-
Md - (0.44 x %CO2) * (0.32 x %02> + (0.28 x -Klty

Md - (0.44 x    ) ••• (0.32 x    ) + (0.28 X     )

"<-  28,
                                                   % HO
                                                               HO
                                                         100
                                                                    ,00
                                         P«-Pb +
                                  S.P.
                                  13.0
                                  ) +
                                                                '3.8
                                           J  T9<°R)
                                            ^  Pa x MB
                                         V« • 65.40 x (
                                           )»(
                                         )x
                            ^
                                           > • V« x A* x 60 i/m
                                          Qs«

                                          Q«-
                                        x

                                      «7aefcn
                           Os -^=Q«x 17.847 x
                                                           x(1 -- *— )
                                                                100
                                                      X 17.847 X-
                                          QHtd-
                                                                            100
-------
  Plant:
  Site:
            WET-BULB/DRY-BULB MOISTURE CALCULATION
                              xfr  	Location:     j-^c&^&^c* / ^
                           Operators:
                                   -  13.6
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of StacK =   Pbar
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw (from Table) =   Pvw =

                                     :  (Ps - Fvw) x (A"H
                                            Run ff: //(T-2^2-   Date:   S/wfa?
Pbar= 2-%W
Pg = +. 0 I
PS= 2-0,0 /
Tw= (0(
Td= 10
AT= 1?
Pvw= .*VO'.
in. Hq
in. H C
in. Hg
°F
°F
°F
7 in. Ha
Vapor Pressure of H2O = Pva =

Pva=(  .5V07  ).(_9*0"
                                .! A:
                                        2800-(1.3xTw)
                                         )x(
                          2800-(1.3 x

Proportion of Water Vapor by Volume = Bws
    =   (Pva>     =        (  0.7-W7 }
          (Ps)
                                                                   2387    in. Hg
                                                             0.-00&
                                                                         7.8*
T«mp.
 °F
 o
 10
 20
 30
 40
 50
 60
 70
 80
 90
100
110
120
130
140
150
160
170
180
190
200
210
220
230
240
      0
     0.0376
     0.0631
     3.1025
     0.1047
     0.2476
     0.3626
     0.5218
     0.7392
     1.032
     1.422
     1.932
     2.596
     3.446
     4.525
     5.881
     7.588
     9.652
     1240
     1549
     19.01
     2347
     20.75
     3540
     4241
     5044-
             3.0398
             0.0660
             0.1060
             0.1718
             0.2576
             0.3764
             3.5407
             0.7648
             1.086
             1.487
             1.992
             2.672
             3.543
             4.647
             6.034
             7.759
             9.605
             12.48
             15.03
             19.42
             2340
             2943
             3540
             43.11
             51.70
( 2e.&r )
VAPOP PPPSQI mcc r^e rA/A-rrrn #2^>,/

2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
15.90
19.04
24.40
2942
3047
49.92
52.70
In Inches of Mercury
3
0.0441
0.0728
0.1186
3.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.629
3.744
4.900
6.350
6.150
10.30
13.07
10.34
2047
2447
30.52
3747
44.74
534S
4
0.0463
3.0768
3.1248
3.1955
3.2891
3.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
9.513
8.351
1041
1347
16.70
20.70
25.40
31.13
37.70
4547
5442
5
0.0489
0.0810
3.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.860
2.243
2.995
3.954
5.165
6.680
6.557
10.80
13.07
17.07
21.14
20.00
31.75
3040
4041
5540
e
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.001
4.083
5.302
6.650
8.707
11.12
13.90
17.44
2149
2043
3240
3944
4747
5040
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
6.901
11.30
1440
17.02
2245
2747
3342
3949
40.14
5741
-2,
a
3.0571
3.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.819
2.440
3.259
4.289
5.585
7.202
9400
11.65
14.02
1041
2242
2742
3347
40,75
4843
5043
72.1
9
0.0598
0.0982
0.1587
0.2383
0.3493
0.5035
0.7144
0.9969
1.370
1.075
2.521
3451
4.400
5.732
7.304
9.424
1142
1440
1041
2249
28.10
3443
4142
4843
5947
                                                                                     -,  &
-------
3 ag i-za
                    GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: L&CO /^J^-t - H»*-~ ^ 	 Hate: evY*/* 7
S
R
B
k
S
V









ampling Loc
un#: A
atiorv A4*/« gx&+~*r Clock Time: 2.3*0
if-i-i orwatnrs' t
^,^2-






Stack
T«mp.
°F
*tz-

?t>
. to
*]0
9o

<2>%
<3?
g?
^f
fO
90
*?
.





1
•\- 17-f* Side 2: -~
nlh.Op- ^7
Md - (0.44x%CO2> •»• (0.32x%O2> + (0.28 X%f^)
Md - (0.44 x 0 ) + (0.32 x 2 / ) * <°-20 x ^T )
Md - 2.&?*f
% HO % H20
100 1^O
Mt- Z^."?^
CD 9 ^U
Pl"Pb*'l"3.C (M™ 13.0
P,. 2-f.f^ ln.Hg
/is* 52*^
 x 00 t/m

Qt- x x«0
0.. -1^2,7^ adm
?• %^°,
Q* -,-QiX 17.847 x 	 x(1- * )
nd fs '"••
                           I                                           a
                 Lff-.fflafcRS-l?	1    Q>--3"»-'- X17.647X ^  ML^
-------
           WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: Lh$to
Site: ty/lfM ^xwdUA-f- Ooerators-
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of Stack = Pbar ^ -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw
..<••?• V
Vapor Pressure :o1 Ho O = Pva = (Pvw) -
Pva=/ «/«n . ( *f.tf - •*
2800 -(1.3
Location: ffltl A £•*
•rtV/fJt Run #: Aie-z-3
Pbar =
Pa =
-^L. PS =
Tw =
Td =
AT =
(from Table) = Pvw =
(Ps - Pvw) x (AT)
2800-(1.3xTw)
7*l)x( 2? )
x Cel )
W^f- •
Date: 5-;V-^7
Z«.^V in Mr,
» ^^ in W 0
2 f. W in Hg
L,\ OP
rl QC
^f °F
•Wl in Hg
2^ #" in. Hq

 Proportion of Water Vafaor by Volume = Bws
Tamp.
 OF
 o
 10
 20
 30
 40
 50
 60
 70
 60
 90
 100
 110
 120
 130
 140
 150
 160
 170
 180
 190
200
210
220
230
240
(Ps)
0
0.0378
0.0831
0.1025
0.1647
0.2478
0.3626
0.5216
0.7392
1.032
1.422
1.932
2.596
3.446
4.525
S.661
7.569
9.652
1240
1549
19.01
2347
28.75
3540
4241
5044-
1
0.0398
0.0880
0.1060
0.1716
0.2576
0.3764
0.5407
0.7648
1.066
1.467
1.992
2.672
3.543
4.647
6.034
7.759
9.885
12.48
15.63
1942
2346
2943
3948
49.11
51.78
( zffV ) y-
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0896
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
15.98
1944
24.46
2942
3647
4342
5&70
3
0.0441
0.0728
0.1180
0.1876
0.2782
0.4052
0.5802
0.8163
1.138
1.581
2.114
2.629
3.744
4.900
8.350
8.150
10.36
13.07
18.34
2047
2447
30.52
3747
44.74
534S
4
0.0483
2.0766
3.1248
3.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
8.513
8.351
10.61
13.37
16.70
20.70
2548
31.13
37.78
4547
5442
5
0.0469
0.0610
0.1302
0.2035
0.3004
0.4359
0.8222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.680
6.557
10.86
13.67
17.07
21.14
2640
31.75
3840
4841
5540
&
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.850
8.767
11.12
13.98
17.44
2149
2843
3248
3944
4747 -
5840
7
0.0541 .
0.0892
0.1429
0.2203
0.3240
0.4686
0.6689
0.9352
1.293
1.765
2.379
3.189
4.174
5.442
7.024
8.981
11.38
14.30
17.82
2245
2747
3342
3949
48.14
5741
a
0.0571
3.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.819
2.449
3.2S9
4.289
5.585
7.202
9.200
11.85
14.62
1841
22.52
2742
3347
40.75
4943
5843
9
0.0596
0.0982
0.1587
0.2383
0.3493
0.5035
0.7144
0.9989
1.378
1.878
2.521
3.351
4.408
5.732
7.384
9.424
11.92
14.98
1841
2249
28.18

4142
4949
5947
-------
r
                        METHOD 18 FIELD DATA SHEET
Plant: ^^co fa^ &,<>.< Tested Ana'vte: SAyu. —
C
L
F
g
F
c
C
L

o
ft-* "
1 Z4
r ;
*o
ifc *°*
,!K <"*
r
»
>>&<, ~—
§>5"
late: 5/A//V 7 Orific« T*»"i< *' '"^ '/
ocation: ^^>^ £>4u/><. Pump/Rntnmeter #:
lun#: #£-T.-l Pt: Pretflst (mm Hq):
tack I.D.: 2-«/ * *•« v Post-Tact (mm Hg):
'bar: i*.fl# Tt- Prntflst I°FV ... -
>ample Tube
Operators*
^- Ac--L-f Rost-T««t fF)'
szX/'tff Time: Start' *** Finish: ^ zi- Total: 6 o —
eak Check: Pre: i-^ Post: ,/ W/B:^I D/B:^^O0: - COr,:^ —
/9, i?i?3 »y /&
/?. tf#o ^r 2-"
Gauge
Time Vacuum
(Hg)
10 X-O
»*»- 767f.5ifl '
lo 1 0
^&^» 7^2.^ /
20Vt. .
£$*> 76>eY, 35 /
2x>* i-* • /
&££> 7e~7L1 4,2-1 /
Flow
Setting
& $ - ZSocc.
**>
o.l
0.3
0.2
A3
*s

Traverse
Point
Number
/
I.
$
Y
}
L
g t
i.
>
V
£
c>
0 (
1
3
V
>
(>
P 1
2,
J
V
$
(o
#I*^#£
O,ol
o. 07
P.Ot
0.*.o%
0. D7
O.OCe
o. ?7
0.0%
o.t>l
b.oV,
o.O 7
Q>. 0(s
6> o(e
&.&(*
o.oie
0. 05
0, 0$
O.Ole
0. 0(e
V, 740-7
Stack
Temp.
°F
8(*
<§ D/.t/ dedm
-------
         WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: LA^o fi^JL.*
Site: /$L«~ ^.C^r Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack = Pbar 3 -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw
Vapor Pressure of H^O - Pva - (Pvw) -
P™ =<<„., 7 ) '.?** ••*•«
Location: /^st/Vv~_, /t^
A£/^ Run #: J>£-T,-\ Date: **/
Pbar = 2.«. ff/
Pq = -'.66'
-mT Ps = ^ 7?
13.6
Tw = 7 )X( 2-/ ) £> 32,^

'/V/* 7
in. Hg
in. KLO
2
in. Hg
°F
°F
°F
in. Hg
in. Hg
    •••"-'  '      2800-(1.3 x




Proportion of Water Vapor by Volume = Bws
(Ps)
Tamp.
OF
0
10
20
30
40
SO
60
70
60
90
100
110
120
130
14O
150
160
170
180
190
200
210
220
230
240

0
0.0370
0.0031
0.1025
0.1647
0.2478
0.3020
0.5218
0.7392
1.032
t.422
1.932
2.596
3.444
4.525
5.081
7.589
9.652
12.20
15.29
19.01
23.47
28.75
35.00
42.31
5044-

1
0.0398
0.0600
0.1080
0.1710
0.2570
0.3764
0.5407
0.7648
1.006
1.467
1.992
2.672
3.543
4.647
6.034
7.759
9.885
12.48
15.63
19.42
23.96
29.33
39.68
43.11
51.76
                                           0.011
( 2*3.7? ) i
VAPOR PRESSURES OF WATER 5"? >, }
In Inches of Mercury
2
0.0417
0.0096
0.1127
0.1603
0.2077
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
15.98
1944
24.46
2942
3647
4342
52.70
3
0.0441
0.0728
0.1180
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.829
3.744
4.900
8.350
8.150
10.36
13.07
16.34
2027
24.97
30.52
37.07
44.74
5345
4
0.0463
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
6.513
8.391
10.61
13.37
16.70
20.70
25.48
31.13
37.78
4847
54.62
5
0.0469
0.0810
0.1302
0.2035
0.3004
0.4359
0.0222
0.8750
1.213
1.860
2243
2.998
3.954
5.165
8.680
8.597
10.66
13.67
17.07
21.14
26.00
31.75
3840
46.41
5540
a
0.0517
0.0840
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
0.850
8.767
11.12
13.98
17.44
21.59
2643
3248
3924
4727
5640
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.981
11.38
14.30
. 17.82
2245
27.07
3342
3940
48.14
5741
— —
z
8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9668
1.335
1.819
2.449
3259
£289
5.585
7.202
9200
11.65
14.62
1821
2242
27.62
3347
40.75
4043
5843
7*-°.7
9
0.0598
0.0982
0.1587
0.2383
0.3493
0.5035
0.7144
0.9969
1.378
1.875
2.521
3.381
4.406
5.732
7.384
9.424
1142
1446
1641
2240
28.18
3443
4142
4043
5047
                                                               .-. ve/
-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: LASCO fi^JL,.**- /?£*.-&, ^ Date: *//v/*7
Sampling Location: fo~* exU^i*- ' Clock Time: 2.205
Run #\ ft
£"- 2.-Z— Onfirarors! ^X/-7>
Barometric Pressure, in. Hq: 'iG.lf Static Pressure, in. HoO: -'I U»
Moisture. %: / O
Molecular wt. Drv- ^fteV Pilot Tube. Co: .77
Stack Dimension, in. Diameter or Side 1 : *2*V '' Side 2: 'Z^ *
Wet Bulb. °F: £ c
T.
.3
V
5
fr
6 '
i.
3
V*
5
0
C 1
2.
3
V
$
(,
D <
i.
3
V
5
b



Vateety
Haad
!n,H2O
7
^>.t?f
^. ^ft
A ^«
^?^7
^.0T
^.^
^,l
0.0-J
0.0
O.o-l
0.0-7
0.0
M.- ^«-73
T:. ^>"2.«F. ^vz, °R(°P.4«»
C D
Pa • Pb -t- i ( ) t .
13.8 ' 13.8
P«- T&.II In. Hg
^P-/17?7
— / Ts (^R)
Va-6b.4WxCpxV5P x ^ P9JCM9

V«- (f.l^ (t/t
A.. ^01 **


Qs> x x60
0»- £j 'hi/ft «*n
- ^y ^/ x/ ^ -•..•.
Pi *K,O
Qt .^-Qi XI 7.847 x 	 x(1- —2—)
•W !• 100
'
Q»rtd" X17.847X x(1"1oB^
-------
30C3 -
_
               WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: ^Mrj> /L^s* - £
Site: /?^w ^r£*
Pbar = 2-fc e«/
Pa = — . b(f
Ps= ^8.7?
Tw= <^
Td= e»-
AT= l-l-
= Pvw = A 5"2^8
ix (AT)
V*7
in. Hg
in. HO
2
in. Hg
°F
°F
°F
in. Hg

                    )
                                   2800-(1.3xTw)

                                   )x(  2.2-   )
                         2800 -(1. 3 x


      Proportion of Water Vapor by Volume = Bws
             (Pva)
(
a
                                     in. Hg
(Ps)
Tamp.
OF
0
10
20
30
40
so
60
70
60
90
100
110
120
130
140
ISO
160
170
180
190
200
210
220
230
240
( 2-S.7? )
VAPOR PRESSURES OF WATER
In Inches of Mercury
0
0.0370
0.0031
0.1025
0.1047
0.2470
0.3020
0.5210
0.7392
1.032
1.422
1.932
2.596
3.446
4.525
5.801
7.569
9.652
1220
1529
19.01
2347
28.75
3540
4241
5044-
1
0.0398
0.0660
0.1 080
0.1710
0.2576
0.3764
0.5407
0.7648
1.066
1.467
1.992
2.672
3.543
4.647
6.034
7.759
8.885
12.48
15.63
19.42
2346
2943
3S48
43.11
51.76
2
0.0417
0.0090
0.1127
0.1003
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
0.190
7.952
10.12
12.77
15.98
1944
24.46
2942
3647
43.92
52.70
3
0.0441
0.0728
0.1188
0.1670
0.2782
0.4052
0.5802
0.8183
1.136
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.36
13.07
16.34
2027
24.97
30.82
37.07
44.74
5348
4
0.0403
3.0760
0.1248
0.1955
0.2091
0.4203
0.0009
0.8402
1.175
1.010
2.178
2.911
3.848
5.031
0.513
0.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
4847
5442
5
0.0409
0.0810
0.1302
0.2035
0.3004
0.4359
0.0222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.680
8.557
10.86
13.67
17.07
21.14
2640
31.75
38.80
4641
33 JO
6
0.0517
0.0040
0.1370
0.2110
0.3120
0.4520
0.0442
0.9046
1.253
1.712
2.310
3.061
4.063
5.302
0.850
8.767
11.12
13.98
17.44
2149
2643
3248
3924
4727
5340
7
0.0541
0.0092
0.1429
0.2203
0.3240
0.4666
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.981
11.36
14.30
17.82
2248
27.07
33.02
3949
48.14
5741
a
0.0571
0.0932
0.1502
0.2292
0.3304
0.4858
0.6903
0.9060
1.335
1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1821
2242
27.62
3347
40.75
4949
5843
!/
£V-7
2-Tzlr-
9
0.0598
0.0982
0.1507
0.2383
0.3493
0.5035
0.7144
0.9989
1.378
1.878
2.521
3451
4.406
5.732
7.384
9.424
1142
14.98
1841
2249
28.18
3443
4142
4943
5947
                                                                      ,~l
-------
UfflQ CJ
                   GAS VELOCITY AND VOLUMETRIC FLOW RATE
     Plant:
Date:
Sampling
Location: <£«,*, £">< £«^>««- " Clock Time: 2 3$^

He-?.-** Onprators- X* /?#
Barometric Pressure, in. h
Moisture. %: /. /
q: ^S.tY Static Pressure, in. hUO: %—^ ^''
MolprularAArt, nrv 2A firV PitOt Tube, Cp: „ T7_ ._
Stack Dimension, in. Diameter or Side
Wet Bulb. °F: (no Orv F


TrovtrM
Point
Number
fl t
-^
3
V
$
If
6
\
2.
3
V
5
k
£ /
z,
3
V
5
(f
£ \
2.
3
V
.5
(^



Vatoeny
HMd
in. H20
ac^ .
o. o<-f
C-oti
o.o^
0,0^
0.0&
D.07
r2 03
o,o<£
O,oio
fr 07
tO.cl
0. If
OJO
0..&1
0,01
(0.01
O.Ot
o, (o
0,li>
Q.O%
0,d1
0,0(0
0,0 7


Stack
T«mp.
°F
»o
&c "
<&o
%o
Bv
QO
#0
®0
®<0
@£>
<60
#0
82-
9>\
9>l
9)1
&(
*&(
%1
i)\
$/
8/
8/
Ql

X- VI
1: -2-V Side 2: 2-e
5ulbTOp- «8/
Md - (0.44 x %CXlj) ••• (0.32 X %02) + (0.28 X %N2>
Md - (0.44 x ) + (0.32 X ) + (0.28 X )
Md- ^'^/
% H20 % H20
M..( )X(1.___)*,B(___) I**
— ^B O __— O O
v ' t-< ** p *~*fi I Ml P ^ 4QQ1
13.8 13.8
P« - 2^^. 7*7 1"- Ha
— I Ts i^R)
V"°"*"^"^X V p«M-



'
A»-y^7 ft2
Ott • \Jm « A* w AA »/m

o«- x xeo
°«" ^o? «*"
Pt %H,°
Qi .,-QtX 17.647 X 	 x(1 	 ^-)
•" T* IV

°*«td" x 17<647 * 	 "" X ( 1 ' 100 }
-------
Plant:
Site:

           WET-BULB/DRY-BULB MOISTURE CALCULATION
                                        Location:   ^C^-LJ^^. , /£ -v A^c^y
                       Operators: j
                                        Run
                              ~  13.6
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of Stack =   Pbar
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td • Tw = .                   „
Saturation Vapor Pressure of H2O at Tw (from Table) =   Pvw =
                                   (Ps - Pvw) x (AT)
            Date: 5//y/
Pbar =
 Pg =
 Ps =
 Tw =
 Td =
                                                                      in. Hg
                                                          01
in. Hg
°F
°F
°F
in. Hg
Vapor Pressure of H2O = Pva"=: (Pvw) -

Pva=(   ,S"l/fc  )--
                                   2800-(1.3xTw)
                            ,$W  )x(    2~I    )
                       2800-(1.3 x     fro   )
                                                                     in. Hg
Proponion of Water Vapor by Volume = Bws
        (Pva)
w**
-------
   f
          Plant:
          Date:  S-M-I-I
                           METHOD 18 FIELD DATA SHEET
                          —.	    Tested Analyte:_5^/
                          —.	    Orifice Tank
          Stack I.D.:__nf_
     Sample Tube #:.
     Operators: *-yvt
     Leak Check:
       10
tm.  
-------
                                               FIELD DA I A SHEET
Plant:
Sampling Location  ft
Run Number: ?-.Q- I    Date: g/l

5fc> •TO Clock Time (24-hour dock) ^^i.K' ocyy^> y\/> ij^~ £0$^ ,._ Gas Meter Reading (Vm)«|3 ^^ V;3g ;©-3 , -70 A! o .- 5^ // S"» *?V7 • Velocity Head(Ap) inH20 Oriica Preoour* Differential (AH) in H20 Desired Actual Stack Temp. (Ts) •:* Tempeiature Probe Fitter Impinger Temp. °F Dry Gas Meter Temp. Inlet (Tm in°F) Outlet (Tm out°F) Pump Vacuum (in. Hg) Y///////////////////M frsfiC^ )•• ?6 I &/ \ • ?£> 1-7 \ ?9 f? "SV ^T7 5s-?

-------
                        SAMPLE RECOVERY DATA
PLANT
LK-SC.Q
                    Run No.
DATE   5-11- 9~1    Sample Box No.  M-5    Job No.   S4-QS.6QS

SAMPLE LOCATION   U^N °\	  Filter No.     M K	
TRAIN PREPARER
SAMPLE RECOVERY PERSON

COMMENTS
 FRONT HALF
 Acetone
 Container No.

 Filter
 Container No.

 Description of Filter
                  Liquid
                  Level Marked
                    Sealed
                                     Sealed
 Samples Stored and Locked

 RACK HALF/MOTSTTJRE
 Container No.        	
 Liquid Level Marked
                                      Sealed
    IMP. NO.
     CONTENTS
              bX Hi.0
           TOTAL
INHTAL VOL
   (ml)
                             /£>£>
                     t
                  /0O
                                                   WEIGHT (grams)
                                         INITIAL
                                            FINAL
                                                                   NET

-------
         EPA METHOD 4 MOISTURE CALCULATIONS



PUNT:   lA<>a> _ SOURCE/RUN #: ^-2-1 DATE:


1 .  Leakage Correction for Volume Metered


    Vmc=Vm.(Lp-La)xe


    Vmc=vm-(Lp-0.02)xQ



    vmc=<       )-(       -0.02) x(       )


                   ft3
2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)


                          P-MAH/13.6)N
    Vmstd
                                             (548   )
                                      •\


                    , dscf
3. Volume Water Vapor Collected, Standard Conditions


    Impingers & Silica Gel = V ...   = 0.04707 x (W. - W. )
                         wstd             T    '

                        Vw   = 0.04707 X(  U-0  )
                         wstd
                        vw
                         wstd
4. Percent Moisture, by Volume



    _           Vwstd
    BW8~    w    TTT
                     mstd
    B
     W8
          (0.-LB2. )+(2/,52Z )

-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: ^45 Co Date: f'/^H
Sampling Loc
Run#: 9~C
ation: DL'JSL/l1 T* 9 Clock Time: JRSft #?^O
J-3L nporntnrs- /)/V\ /££>
Barometric Pressure, in. H
Moisture, %:/A
//<7
, 99
. aa
/•3 1
xfjy













^p-0,H^l
Stack
T«mo.
°F
.v^fr-
165
I&S
1 tot>
\<*t,
Iblo
16$
/63
I(a6
J66
ibn
IbO













S./^'F
1: /fX/ Side 2: 	
nlhOp -
Md - (0.44 x %CO2) + (0.32 X -fcOj) * (0.28 x %Nj) ;
Md - (0.44 x ) + (0.32 X ) f (0.28 X )
M-- Z?.^
% HO % HO
M.-MdX(1 io(j )-lB< 1QO ) ^^
M.-< ,xO--— -)*18(_— -) ^
Mi- J6.?/
^- ((/5> °F- t^ °R ("p*460'
Pa - Pb * S'P' = ( ) + 	
13.8 '3.8
*- 2^.~7°l ln-H9
^'n^ZM
— ,/ Ts^R)
Vi - 85.49 X Op x VAP X U - p9 x M,

Vta-3l.(^2/1 «*

A«- |.W> I2
O* • Va v Aa x 00 i/m

Qa» x x80
Qi- 252B «*n
P« *H»°
0-.M- Q-*17.647X — x(1 • -^j- )

Oi^- X1/.84/X 	 *(l" 100 J

-------
3 BC3 C^3
                      GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:  LASC.O
                                                          Date:
Sampling Location:
Run*:  Tfl-A -'
                          -* J&
                                                          Clock Time:
                                                Operators: -
       Barometric Pressure, in. Hg: Gp.ft,	 Static Pressure, in. HoO:  ">
       Moisture, %:   	 /./'/•  Molecularwt., Drv:   23.*V   Pitot Tube, CD:  .'99
       Stack Dimension, in. Diameter or Side 1:   K"	Side 2:  •-	
      Wet Bulb, °F:
Trav«rM
Point
Number
A - ?
^
3
V
.<
£>
A- /
5
3
y
f
&














Velocity
H«M
in. H20
,//
f\*t
r90
'92
•W
'99
, 9^3
,93
,29
,21
,99
,99













$P -, \
Ibh
/fod
Ibto
Jb&
/*£>!>
'/t*
K>¥













ft. /6^
                             Dry Bulb, °F:

                                     Md -
                                                          100
                                            Md
                                                      % H,O     % HO
                                            M«- Mdxd •  - — 1 -r 18 ( - £-)
                                                       100 '
                                            MI-
                                      Pa - Pb
                                                   s-p-
                                                   I3.fl
                                                            13.0
                                            Vt m 65.40 x Cp 1
                                            Vi«85.40x(,
                                                                PsxMs
                                            v.
                                                   ft/*

                                                   .2
                                             Q« • V« x A* x CO «/m
                                             Qs-
                                                                   xflO
                                                          «*n
                                      Qs M- Q» x 1 7.847 x - x (1
                                                           p.     %H-0
                                                          - x 1 - — •-

-------
FIELDDAiAS&EET
Plant:
C/1,i>CO Sample Type: /ty- V Operalor: DSA/d'G
Sampling Loo
Run Number:
ition lU'rT ^ 9 Pbar 9SM?/> Ps: ^'B°> '
33-"? Date: ^"•/V'9'7 CO2: 	 ~
Pretest Leak Rate: . CO c cfrn @ >\
££ , V o
6 (<> , Q Vo























Velocity
Head (Ap)
inH2O
Oriioe Presaure Oiftarential
(AH) in H20
Desired
Actual
Stack
Temp.
Us)
Nozzle ID: /v>4 Thermocouple #: T"(i> J?
Assumed Bws: AJA- Filter #: — * "
Meter Box #: /f
Y: /^6bAH@: htfb '^
Post-Test Leak Rate: / COO cfm @ ^
in. Hg.
Post-Test Leak Check: Pilot: yX" Orsat:.-- 	

Temperature
°F
Probe ) Fitter
Impinger
Temp.
°F
y////////////////////////////////////////////






/gcoct
f 1 '^
1 <$
f ]/
/ 1 1
. \^>
, £•-}

,££.
40

'/*
,99
'3$






l.'ft)
/:<£<&
It %d?



rs
9k' "^
5 r7
#)jf
0? 1^
52 )
9 O o.

Q/ C,
5??"?
g»&iO
^/^ )
*^\ ^^ ,^ \
^^^ t^ j<_
9&0













••«? 	
























,
-J






































































£"}
£C
t-1ft























Dry Gas Meter Temp.
Inlet
(Tm in°F)
Outlet
(Tm out°F)

Pump
Vacuum
(in. Hg)
'////////////y///.
#-y
^t?
^3-









-













^.3
S^
^"^>























3
^
3























s
           r.
is
ft-

-------
                      SAMPLE RECOVERY DATA
PLANT   L.teCjL>
                                             Run NO.
DATE   0^XT

SAMPLE LOCATION 	

TRAIN PREPARER   	Q
                      sample Box No.   M-l     Job No.
                                             Filter No.
SAMPLE RECOVERY PERSON

COMMENTS
FRONT HALF
Acetone
Container No.

Filter
Container No.

Description of Filter
                                  4
                                   v^c
                           Liquid
                           Level Marked
Sealed
                                             Sealed
Samples Stored and Locked

RACK HALF/MOTSTTIRF
Container No.        	
Liquid Level Marked
                                             Sealed
                                                        -^- 3

IMP. NO.
1
2
3
4
5
6

CONTENTS
b? ^0
bT ^0
*"/•**
3/t. ic. A £f£L*


TOTAL
INITIAL VOL
(ml)
sao
/(SO
	
SL-5TO



WEIGHT (grams)
INITIAL
btfU
c,o(o,a>
4^1.5
631 .3.


WHf
FINAL
(0/0,0
(obl.o
in*
B ?*.f


tffV-l
NET
• 0.7
0,T-
&,1*>
Z,6


5.1
                                                                      1,1

-------
        EPA METHOD 4 MOISTURE CALCULATIONS

PLANT: - Lfl^c. _ SOURCE/RUN #:^i2^_ DATE: &

1 . Leakage Correction for Volume Metered

    Vmc=vm-(Lp-La)xe

    Vmc=vm-(Lp-0.02)x0

    Vmc=(       )•(       -0.02) x(       )

                   ft3
2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)

                          P-MAH/13.6)N
                                  m
                                       (   <«*>) + < /  6U /13.8)
                                   )x
                     dscf
3.  Volume Water Vapor Collected, Standard Conditions

    Impingers & Silica Gel = Vw  = 0.04707 x (W, - W.)
                         wstd          v f   •'
                        Vwst(j = 0.04707x( 5\ i

                        v,.  AD,

4.  Percent Moisture, by Volume
                V,..
    BWS= •
           wstd
             V
              w  ••   m
              wstd    mstd
    Bws =
(  . 2101   )
          0.

-------
j aa L-
                        GAS VELOCITY AND VOLUMETRIC FLOW RATE
       Plant:
       Sampling Location:
       Run #\ /O ~3 - /
                                                      Date:  f'H-
                                                      Clock Time:  =9
                                            Operators:
       Barometric Pressure, in. Hg: ffg-JC _  Static Pressure, in. HUP: -
       Moisture, %:     — —     Molecular wt., Dry: _ Pitot Tube, Cp:
Stack Dimension, in. Diameter or Side 1:  /£*'
Wet Bulb. °F:       —	Dry Bulb,0F:.
                                                             Side 2:
          TravcrM
           ^_l_.A
           KOfnt

          NumMr
         .4 •  /
              V
              V
              .r
               Velocity
                Head
               in. H2O
                       ,?£>
                       ,31
              r  IX
Stack
T«mp.
 °F
                                     7
                                9)
Md - (0.44 x %CO2) + (0.32 X %Q^ + (0.28 X %Nj)


Md - (0.44 x    ) * (0.32 X    ; *• (0.28 X

Md -


Ms • Mdxd


MS- (
                                                          100
                                                            % H.,0
                                                       * .    ico
                                                              100
                                                                         100
                                              Ms
                                              Pa.Pb
                                               p.-
                                                                      13.0
                                               Vi « 65.4Q x Co X
                                        Vt • 65.48 x (
                                                                    T3
                                    (°R)
                                                                   Pax Ms
                                                               ) x (
                                               Q» • V« x A* x 00 «/m
                                               Of-

                                               Q,.
                                                                      xeo
                                                      adm

                                                       Ps
                                                       •M^lV
                                                       Ts
                                                           X 17.647 X-
                                                                                  100

-------
METHOD 18 FIELD DATA SHEET

3lant: L/ttCO Tested Analvte: Sfy/^-t
Date: 5" H -S *) Orifica Tank #• 	
1
(
I
?1/ '^
«3 -7S-
5Sb-^^
JVI?
\ , 7^
ttH '53
>h ^'
\J)6".35
,s-^
ocation: ®tf CW£
.ct&&£')\
Gauge
Time Vacuum
(Hg)
i^co O
3900 O
»5130 ^
aa-so o
&>^0 O
3£ £"° 0
3300 o
STrtTKL -.'{$"3
Trtveree
Point
Number
4-f
a
^
^
<
&>

n i
3-
j
y













Velocity
Heed
In.H^O
//O
tiL
,n
. i f
,1 ?
^^>^/

' ]<^
.S&
,9^
. Q.K
. 1*
/ l<4












Flow
Setting
$& Cti/^
\
/



>//

Stack
Temp.
917
3 /->
J)-7
? /*»
391
'4W

3>~>
§^O
&&0
&ac
3d/
<$dl












6 W/B:/l'.4 D/B:A;/» O«: CO0:
Md - (O.WxttCCy -l- (0.32 X%02) + (0.2BX%N2)
Md.(0.44x )-|.(0.32x )-f(0.28X )
¥&- I***
*?/**' %H,0 %HO
?7/j£--Md*(1--!»f) + ia( — ' J
•8'3'Um -1 IvH 	 l-t-181 	 )
Me • ( )xn- — r=— ' f'oi »
fS/S^-7 1°°
^7 2e^
Ta- OTTj °F- (c,&0 °R(°F*4«0)
^VP?
fc- ""*•&-< ^•tD)* -rlr-
P«- ^.H ln.Hg
^p . 0 .42-5D
«. ^f \I T8(°R)
Ve - 85.48 x Cp x VAP x W paxMe

V.-3^.UfS ft*
Ae- ft2
O»- VaxA«xeo«/m
Q,. |.72V x x80
08 • ^^/P^ "*"
p. %H,0
Q»^,-QiXl7.B47x 	 x(1- — •*-)
•W te 1°O
^ud' Xir(fl dedm
                                             ./if

-------
FIELD DA IA SHEET
Plant:
Ln5(LO Sample Type: Al- */ Operator: &&&/&!>
Sampling Loci
Run Number:
ition £>l)gUV &-JO Pbar.9$ffC Ps: Zfi.^H /
/0-2-3L Date: 5"-/i''97 CO2: — — O2: -^
Pretest Leak Rate: -Oco cfm@/s in.
Pretest Leak Check: Pitol
I
Traverse
Number



























Sampling
Time
(mln)
O
Jc>
9Q
30























dock Time
(244iour
dock)
'3301
a&n
333(
&&3f























y *t"4
: A'Ar Orsat: /t

Gas Meter
Reading
(Vmjft3
;^x9^3
.9£ ' ^7 O
3»V >*To
Vd / S'/ 





































































































f»= 2.3.75?' v£p= "~ AH= l,ft(j ^^Ts= 	
• -''•»- •.»••:«./' ,^


























^?
^9
5'^



















• 'V



^L
9^>"
^^



















'"- '-'•



^9
56
&*3























Pump
Vacuum
(in. Hg)
^t
{.£
(,5 s> ^^

1
x«

-------
=355
                           SAMPLE RECOVERY DATA
PLANT
                                                 Run No.
                                                              - 2.-
    DATE      5//c/7V   Sample Box No.  NJ-la    Job No.   S4QS . QO3>

    SAMPLE LOCATION    ^"^  1°   ^V^tfA      Filter No.      M/A*
    TRAIN PREPARER
SAMPLE RECOVERY PERSON

COMMENTS
                                      4-
     FRONT HALF
     Acetone
     Container No.

     Filter
     Container No.

     Description of Filter
                           Liquid
                           Level Marked
Sealed
                                             Sealed
     Samples Stored and Locked

     BACK HALF/MOISTURE
     Container No.        	

IMP. NO.
1
2
3
4
5
6
CONTENTS
DX VA-2.O
t>i uto
eriwpry
SlMCA ^EL


TOTAL
INITIAL VOL
(ml)
/*>
/ffO
—
-250



WEIGHT (grams)
INfTIAL
5^6.2-
Ubl).0
45b.O
7^,b


^63.8
FINAL
517.7
£6^3
^/5*6//
7 75 *•/


2v\Q(b.'f
NET
' 2.^
o.J
o.(
3.8


•t.7"

-------
3 aa cj
              EPA METHOD 4 MOISTURE CALCULATIONS



      PUNT:  ZA«*Q _ SOURCE/RUN #:_/£llil_ DATE:



      1 .  Leakage Correction for Volume Metered



         vmc = V 
-------
Plant:	
Sampling Location: UN«T
Run#:	19-2-3
                 GAS VELOCITY AND VOLUMETRIC FLOW RATE

                                                      Date:
                                                      Clock Time:
Barometric Pressure, in. Hg:   ?%.
Moisture, %:   \H ?6.	Molecular wt., Dry:.
Stack Dimension, in. Diameter or Side 1:     i.V
Wet Bulb, °F:
 Operators:	£
 Static Pressure, in. H2O:_
      I	PitotTube, Cp:.
      	Side 2:   —
                               Dry Bulb, °F:	^
Travaraa
Point
Numbar
A -*i
2,
S
<-/
^
(S

e>- <
2
?
*/
<>
L,













Valocity
Haad
In. H2O
<-V
<£
/U
l>
. IT-
•fr

2o
)^2.
ZO
^e
^2
?.<












^P-O.M^MI
Stack
Temp.
°F
^17-
^)>
2»ft
J'<*
Z^l
72-2,

2-»e
21 V
2-ZjC?
2-1-t
2- "2-2.
i.Zo












k- an
                                       Md - (0.44 X %COZ) + (0.32 X %O2> + (0.28 X %r^)


                                       Md-(0.44x    J-M0.32X    )-t-(0.28X     )
                                       Ma - Md x (1 -
                                        Ms-
                                         i-Pb +
                                        P..
                                                 % H-0
                                                            % HO
                                               S.P.
                                               13.8
                                                               13.8
                                                    ,n.Hg
                                        Va - 85.49 x Cp X


                                        Va • 85.48 X (
                                                  &
                                        Va- $2r*ftt ft/a

                                        Aa-  I-Z2LV  ft2


                                        Qa-VaxAax60a/m

                                        Qa •          x
                                        0*
                                                            PsxM8
                                                        |x(
                      )x
i
         x          X80

          adm

            Pa     '
.-Qaxl7.847x	x(1- 	^—)
*            Ta       100
                                        0»^-
                                                    X 17.847 X-
                         •x(1
                                                                          100
-------
g_ao_c
                        METHOD 18 FIELD DATA SHEET
Plant: uflS«« C^^t/> Tsstart Analvtfi- ^A**—
C
L
F
c
F
c
C
L

0
<$
1*
5»
V*
5«
fo
Date: s //«//« 7

Orifirp Twnk #• 7^>»e^ l/£>' \> \L»_J?.
.ocation: fiJtoo-k Pump/Rntnmfiter #:
lun#: x/*4-2-»- pt- pretoct (mm Hg)-
Stack I. D.: 3lM;t> Post-T«ct (mm Hg)-
=bar: -2-».«Y Tt- Prfltnst <°FV
Sample Tube
Operators:
#: fJOA.z-i- pc«:t.Tflet CF}-
>e-A Time: Start: 22** Finish: «*•* Totaled -.•-
.eak Check: Pre: */ Post: ^ W/B: — D/B: - O0: ^ CO,,:_2 	


Gauge
Time Vacuum
(Hg)
2-^ /3J7/i /
tt/^ / 3 

Qtctd* dtetm
-------
a aa cu
r=~
p
D
L
R
S
P
S
C
L

O
10
I*
3o
«/o
k
METHOD 1 8 FIELD DATA SHEET
lant: LlA<>t.o fa A.** TesteH Anslyts- 5s-yu~^
ate: *//v/r7 Orific° Tanu- *• "xrfW» i/g ..-"3
acatiorv /J D B> Pump/Rotnnnetar #:
un#: A/PB-2-3 Pt: Pretest (mm Hq):
tack I. D.: 0-5" *}2." Post-Test (mm Hq);
bar: ^«-*/ Tf Protect r°R-
ample Tube
Jperators: >
eak Check: F
O.oa
#• /Vj)£-2.-Z pCct.T«ct f F) •
fl4 /Ta Tim«- start:/'** Finish:/23o_Total:_i^*i^
're: ^ Post: .X W/B: - D/B: - GV,: ** CO0:_2 —
> ~t 11" .*a ~*  rtf7.it /
7A** llsMo I
Mlb l-*& ko 1
Wo /3^,3« /
11 to rlU.eZ f
Row
Setting
10
Zo
^0
2Z>
^o
I O
L*>

Trov*rM
Point
Number

























Vttectty
HMd
In.HjO

























Stack
T.mp.

























Md - <0.44x%CO2) -t- (0.32 X%02) + (0.28x%N2)
£_ Llrf _ in AA w ^ ^ let 32 « ) -f (0 28 X )
3t
Md - •:
'fu
^ %H.O %HO •••
<\( M.-Mdx(1--^-) + 18(-T5r) '
^Z M«-< )x<1 	 __)-.- 18 (_—-)
93
^3 M>-
?v T.- °F- °R(°F*4«0,
SB
^""'^iir ( ' 13.6
Pt - In. Hg
£P-
S= . 1 T» <^R)
vt • 99.40 x up x »ur * M Pa x Ma
Vi - 65.48 x ( ) x ( ) x -U. 	
V» • ft/a

A »2
A* • R

Qt - Va x As x 80 a/m

Qs- x x«

Q«« adm
p, %K,0
Qi ..-Qi XI 7.847 x 	 x(1- - ' )

lf 	 !


QHtd- dMta
I.
-------
          APPENDIX A. 1.4

             Conditions
(includes flows, moistures, and Method 18)
-------
METHOD 18 FIELD DATA SHEET
p
D
L
R
S
P
S
C
L

^25 »
^H ^7 5,j i (}

j<-/5<; >£,

H^t 3S)
™<* &
*"
lant: Art5/0 TesteH Anaiyte- Vi//^^^
ate: ^-;<>'- O«: '!' CO«: O _.


Gauge
Time Vacuum
(Hg)
226! 
. 3 /
.3to
. 31?
• 33
. i^"
.2.1

. ^$3^






Stack
T«mp.
1L,
<%&
%O

?l
-r/

VO

90
iij \J
4? J
& t
31
5>/
7l
VO

^o






¥* C Md - (0.44 K %COZ) -t- (0.32 X %02) + (0.28 X %h^)
m Mrl • (D Al v 1 -(- (0 32 X ) + (O.2B x )
% H2O % H2O f .O'f
M»-( )X<1" 100 , ) + l8< 100
Ta - ^ O °p " 5^0 R ( F + *«0)
P. Ph t S'P- - < ) t
P' Pbf 13.8 ' ' 13.8
^SF " t) *B£30
\ T. /°m
r^ , | Ta r n)



'
i / -f .2
"

Q> • Vt x A» x 80 «/m

Qt. x X80
_ •) -> T> .
»• 37/2- «
-------
            WET-5ULE/DHY-EULE MOISTURE CALCULATION
                                J^chc+r _scaticn:
            &<*£,
                                                            ^  ^
                           oerators:
                                                  Date:
                                                  Pbar =
                                                   Pg =
Barometric Pressure, in. Hg =
Static Pressure, in. M20 =
Absolute Pressure of StacK =   =bar •<•   3/wl x
                                      2Boo
     = (
                         2800- (1.3 x  57

 Proportion ot Water Vaoor oy Volume = 6ws
          (Pvaj
r-------
 m^^m ^^w ^•^
 ass. £3
IB-
                                       18 FIELD DATA SHEET
        PlantL
        Date:_
          Location:^
          Run #:_jh
          Stack I.D.:.
          Pbar:	
                  £ - 3 - z,
                       n.
        Sample Tube
        Operators :_u
          Leak Check: Pre:	^
                   CQ( <.f ZQ"
                              Post:
l^8
            Tr«v«ra«
             Point
            Number
                         V«iodiy
                          H««d
                         In. H^O
                      &, to
                       0. Z(
                       0.11
                        , JZ-
                                  . *>* ^
/?
/(?
20
Time
/fa> - 2t/0- ^
/(/to 2 T-91, '~
/<* <= t ,v
/**•«.




Stack
T*mp.
 °F
                                  77
                                  PO
                                  too
                                     (60
                                   00
                                   to
                                   VO'F*
                                                Tested Anaiyte:.
                                                Orifice Tank #:_
           Pt:  Pretest (mm Hg):	
               Post-Test (mm Hg)L
           Tt:  Pretest fF):_
           Time: Start: /Us  Finish: JkMTotal:_£D£$L
           W/B:J52_D/B:^_O«:^/_
                                              Md - <0.44x%C02) f
                                             .
                                          • -- Md - (0.44 x    ) -t- (0.32 X    ) + (0.28 X    )
                                           '
                                              :Md
                                                        %'
                                                                     %H,0
                                                              100
                                                                         100
                                               T.-
13.8
                                                                     13.8
            Vi - 85.40 X Cp



            V«« 65.48 X( /


            *-3fc.W
                                                            X^P x y-

                   •V-
                                                  > V«xAaxOOt/m
                                                  Qi-

                                                  Qs«
                                                                      xOO
                                                              p.     %H_0
                                               Qi .^-QiX 17.847x	x(1	•*-]
                                                 •ta           T*      100
                                                                                     -
-------
Plant:
Site:
             WE7-3ULE/DRY-SULS MOISTURE CALCULATION
           //feo  &«J?  /^oJlj-j     _scaucn:
                             nerators-
                                    -  : 3.6
aarometrtc Pressure, in. hg =
Static Pressure, in. H20 =
Absolute Pressure of Stacx =    =bar
Wet-Bulb Temperature. °F  =
Ory.8ulb Temperature. °r =
Temperature Difference. Td - Tw =
Saturation Vapor Pressure of H,Q at Tw itrcm fabtei =    =vw =

Vapor Pressure of K,G = Pva = .Pvw,.
                                         28CXD -(1.3X Tw)
                           2800 - (1.3x

Proporaon of Water Vaoor oy Volume m 6ws

8ws=   -LPva»
                           VAPOR PRESSURES OF WATEH
                                  In IncfiM of Mercury
3F
• 3
'0
20
30
«O
SO
00
70
90
00
100
110
.120
'(30
140
190
180
170
180
180
200
210
3
3.0378
3.0031
".1023
3.1847
0.2478
0.3828
0.9218
0.7382
1.032
1.422
(.832
2488
3448
4.828
S481
7.988
9482
1240
1349
1841
2947
2841
                \
              ^.03841
              3.0880
              0.1080
              0.1718
              0.2378
              0.3784
              0.3407
              0.784*
              t.C
              1.4

              2J02
                        2
                      : O4I7
                      -1127
                      0.1803
                      0.2877

                      0.3801
                      0.7912
                      1.102
                      1.319
                      2.740
              4.047
              7.79

              19
                      4.772
                      8.180
                      7.088
                      10.12
                      12.77
30728
0.1188
0.1878
0.2782
0.4082
0.3802
04183
 1.138
 1.981
 2.114
 2J28
 3.744
 4.1
  4
: 94O3
:0788
M248
3.1893
3.2881
3.1
0.1
0.1
 1.179
 1.810
2.178
2J11
8.180
1008
1347
1844
2OBT
2447
     4841
             4841
                               9747
9481
0419
8481
1041
1347
18JO
20JO
2948
31.19
37JI
  S
3.0488
C.0810
0.1302
04033
04004
0.4
0.1
04790
 1.213
 1.880
 2449
 2488
 3484
 9.183
  a
3.0317
0.0841)
0.1370
C.312O
0.4820
0.0442
04OM
 1.299
 1.712
 2410
 3481
 4J
8487
1048
1947
1747
21.14
«J
8J8T
11.12
1948
1744
2140
                                                3149
                                                                      Date:
Pbar =
Pg =
Pa =
Tw **•
Td =
-2-8.90
f. c2-
74. fO
&
eo
m. Ha
in. H-.Q
2
in. Hq
°F
°F
                                                                     .Z&2-
                                                                                   m. Mg
  r
3.0341
3.0882
0.1428
04203
0.324O
0.4
O.J
 1.289
 1.789
 2478
 3.188
 4.174
 9442
 7.024
 8481
 1148
 14
 17J
   9
 :0371
. :.OB32
 :.15O2
 3.2282
 3.3384
 0.4
 0.1
 OJ
 1.339
 1.818
 2.4441
 3498
 4488
 9488
 7402
                                                                                   a.
0.1887
                 04144
1471
                                                                                    U
                                                                                    2.
                                                                                    3481
 1148
 1442
 1841
tl
1
1
                                                                  2747
-------
                              METHOD 18 FIELD DATASHEET
       Plant:  Lfeco
       Date:   v-/5--
5L
           Trav«ra«
            Point
           Numbar
                           Velocity
                            Hud
                           In.H^O
                             Stack
                             T«mp.
                              °F
                                                   Tested Analyte:.
                                                   Orifice Tank *•   -
                                                   Pump/Rotometer #:	^
                                                   Ft   Pretest (mm Hg):	
                                                        Post-Test (mm Hg)L
                                                   Tt:   Pretest
    Post-Test (°F):	:
Time: start: ^%  Finish:
                                                                            Total:
                                                    Md « (0.44 x %C02)


                                                    Md - (0.44 x    ) + (0.32 X


                                                    Md-

                                                              %H_O
                                                                 10O
                                                                        ) + (0.28 X    )
                                                                       HO
                                                                            100
                                                Mc-
 P«.Pb •»•-§£--(      )-t-	
        13.0              13.0
                                                    Pt»


                                                    ff"


                                                    Vi • 65.48 X Cp X
                                                             In. Hg
                                                             JS?x^-

                                                V« - 65.48 x (        ) X (


                                                Vs-           ft/I
                                                                               )x
                                                                       ^
                                                A>«
                                                     Qs»V«xAtxflOi/m


                                                     Qs«          x

                                                     Qa>           acfcn


                                                     Qt -j-QiX 17.647x —x|
                                                      ltd            Tt


                                                     Qi^,-       x 17.647 X-
                                                                         xW
-------
                       METHOD 18 FIELD DATA SHEET
,- 5 >
Plant: I-HS&
Date: 35
. 33

,2.3
.2^
-» tV
,Z0
.?>o
/3I
•32
.3/

^,^57












H/r-3- 3/?

3ost: .,
Flow
Setting
/ jo < -
, /*'*•'
/7* '•'-
/^ f t-




Stick
T«mp.
°F
9O
-79
tfe>
to
2&
€°
•to
It

7?
^»o
••» J .. . , „ H \ , 

QHW-^i/Zy dtcta ,^r
-------
           •  WET-5ULE/DRY-BULS  MOISTURE CALCULATION
 ?lanr      />fe£Q   &^J?  /wt^   .scanon:    /=Z^« . &.A,*L^
 3ite:  /fa*  £*C—^    Coerators: -ftfa  =un IF-  tff-3-1     Date:  5//$/? 7
 Barometric Pressure, in. Hg =                         Pbar =      2?,/0        ,n. Hg
 Static Pressure, in. H20 =                               pg -      —, z/        ,n ^Q
 Absojute Pressure of Stacx =   =bar 3 -^-            Ps =      2^f, og        in. Hg
 Wet-Bulb Temperature. °F  =                            Tw =       5^	 o p
 Ory-8ulb Temperature. °F =                            Td _      €&	 o F
 Temperature Difference. Td • Tw =                       &T =      2-/	 a F
 Saturation Vaoor Pressure of (-LQ at Tw (from Table) =   3vw =     0* £~3o£      in. Hg

 Vapor Pressure ot K,G = Pva = ,Pwv, -   '** ' ^™ * '^
                                       2BCXD - (1.3 X Tw)
 Pv..<   ^05    )  (/Zf^ ' .5^>5)x(    2,/      )  =  __^J/£5__ ,„.Hg
                          2800- (1.3 x
 Proportion ot Water Vaoor oy Volume = 8ws
 Bwa=   (Pva>     =       (   0.3/05  )        _        0.0 If *   /JY.
                          VAPOR PRESSURES OF WATER
T4mo                              In Inches of Mercury
 °C    °        '       ^       3       4        5        9       7       9       9
 •0   3^1    ^SS    :04"    3'0441    :34M    0-°*88    3-M17   :-0341     30S71    OJ
 20   -ToM    ^'?«~    :OM*    107M    :07M    3-M1°    3-084a   ^O892     =-08»    0-OBB
 20   ..1023    -.1MO    :.,,2r    anaa    rJ24-    ^lMa    o_jaro   ^UM     ,_is(a    W9§r
tao   AIM    ^-*,    3-84a     3744    it**     '-M*     *««     «•»»     «^««
130   4128    4447    4.772     4800    S4B1     9.189     1392     1448
198    7988    7718    J'25    ""    MM     9J8°     aj98     TOM
'"    -_    I'!8*    7-88«    «.»»0    9^81     8A7     a«fT     8jm
;:    :sr    :^    i—     «*«•    s     ;s     ;jz     !J2     ;^
                                              J1.14     21.88
                                                              27J07
                              3.1878   3.1899    OJ033    04118   34203   3.2282    0.
                              9.2782   3.2881    0.3004    OJ120   0.3240   3.3384
                              0.4062   3.4203    0.4388    0.4820   0.48M   3,
 70    n'^    «'^T1    g-a°°1    °-MOa   °-a°OB    °-taa    O'8*43   O-"8*   O-"08    ""**
 M    ,'S    i^J    °'79ta    0'81M   °-84«    °-8780    °*>*«   OJ»»   OJ»"    OJi"
 oo    .'!»     ^!    '•1oa    '•1M    '-17S     '-213     ••»»    '•»     1-33S    1JJ>
100     an     'p»    '4ia    1'sei    '-910     '-680     '-71?    '•r«     '•«•    '*•
,10    ,.«.    ,!-    2
-------
                     METHOD 18 FIELD DATA SHEET
Plant:
3ate: y
. o~i
.$£
. tJtr
,lO
.11-
.tl
,6~J
.o<*
06
«/?
.ov
.<^"7
,05
.Ob
DO
/£?
P, Q-7fcU»
Stack
T«mp.
°F
"? t
76
75-
7^'
75
Iv5"
76j
~ICf
~)$
If
7 ^
7^
76*
?<>
75
75
75
7^
T6-
-j<^
-75
7-^"
7$
75
T-S"
Tested Analyte:	'
Orifice Tank #:	z_
                                    Pump/Rotometer #:  v^
                                    Pt:  Pretest (mm Hg)-
                                        Post-Test (mm
                                    Tt:  Pretest f F):
                                        Post-Test fF):      	
                                    Time: Start;j±zl_Finish:.^£_Total:
                                    W/B:Jf_D/B:Jg®_O2:_i_C02:.
                                     Md - <0.
 Md-(0.44x 0  ) *(0.32X -Z/
                                                             (0.28x
                                                        % HO
                                     M. -  Zfc.
                                            13.6
                                     Pa . ZV. Jr ">  In. Hg


                                     &-o.

                                     Vt - 65.48 X Cp X


                                     V* - 05.40 X I
                 t
Pax Mi
                                      Qs - V« x A* x 80 i/m
                                      0.-
                                                            xOO
                                                  X 17.647 X-


                                                   d-8fcn
                                  100
-------
             WE7-3ULE/DHY-6ULS MOISTURE  CALCULATION
                                        ch     -scaocn:
                             oeraiors:
                                                                       Date:
                                    -  : 3.6
3arometnc Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stacx =   ~bar
Wet-Bulb Temperature. °F =
Dry-Bulb Temperature. °F =
Temperature Oifference. Td -  Tw =
Saturation Vapor Pressure of  H.Q at fw (from Fabte> =    3vw
Pbar = _.
Pg = -
Ps = _
Tw = _
Td = _
£J=_
^VW —
2$.      =        (O
           (Pa)               T  '
                                                                    O.W&7     in. Hg
                                                               0.00%
                            VAPOR PRESSURES OF WATER
                                   In Ineftss of Mercury
                                                                                 - «. ice. J
^
•9
20
  80
  70
  ao
  90
 100
 110
.120
't30
 140
-190
 180
 170
 180
 100
 200
 210
  3
3.0378
3.0831
3.1023
3.1847
0.2478
0.3820
0.9218
0.7382
 1.032
 1.422
 1.832
 2488
                \
              C. 038*1

              3.1080
              0.1718
              0.2378
              OJ784
              0.9407
              0.784*
               1.000
               1.44J7
                         2
                       :04<7
4.828
S481
7,<
flj
1240
1948
1841
2347
23JI
              3441
              4447
              0404
              7.7W
                       3.1127
                       0.1803
                       0.2077

                       0.9001
                       0.7012
                        1.102
                        1.913
                        2493
                        2.740
                        3442
                        4.778
                        8.100
                        7.082
                        10.12
                        12J7
  3
3.0441
30728
3.1188
0.1878
0.2782
0.4082
0.9802
04183
 1.138
 1.981
 2.114
 2428
 3.744
 4.1
                                          0788
                                        3.1998
                                        0.2881
                                        0.4203
                                        0.8008
                                        04402
                                         1.178
                                         1.810
                                         2.178
                                         2411
  5
3.C
3.0810
3.1302
04039
04004
0.4
0.1
04750
 1.213
 1.800
 2443
 2J
  a
3.0917
3.08441
0.1370
04118
04120
0.4820
04442
04048
 1.293
 1.712
 2410
 3481
                       II
                       2448)
8.180
1048
1347
1844
2047
2447
                                3747
                                        5431
                                        8413
                                        8481
                                        1041
                                        1347
                                        18JO
                                        28JO
                                        2948
                                        31.13
                                        37481
 9.183
 848O
 8437
 1043
 1347
 17.07
 21.14
8480
8J87
11.12
1348
1744
2143
  7
:.0341
3.0882
3.1428
0.2203
Q424O


04332
 1.283
 1.788
 2478
 3.188
 4.174
 9442
 7.024
 8481
 1148
 14
 17J
.3.
 3.1302
 3.2282
 3.3384
 0.4
 0.1
 OJ
 1.333
 1.818
 2440
 3493
 4438
 9488
                                                                            1143
                                                                            1443
                                                                            1841
                                                                   2747
                                                                            274
                                                                                 a
                                                                               o.e

                                                                               0.1887
                                                                               OJ
                                                                               OJ144
                                                                                1473
                                                                                     U
                                                                                     2.
                                                                                     3431
          11
          1
          1
                                                 3149
-------
jag cza
                       GAS VELOCITY AND VOLUMETRIC FLOW RATE
       Plant:
       Sampling Location:  /3
       Run#:_&£^ 3 ~ 2
               Date:  s--/.r-?7
               Clock Time:
       Barometric Pressure, in. Hg:  Z*?,/	
       Moisture, %:    <2. ?       Molecular wt., Dry:.
       Stack Dimension, in. Diameter or Side 1:	
       Wet Bulb.°F:     £G>	Dry Bulb,°F:
     Operators:   • *V*"5	
     Static Pressure, in. HUP: —,
               PitotTube^Cp: , ??
               Side 2: _
TravarM
Point
Number
/
2
")
^
5
0
/
i
"b



ol
,cft
,Q(J
.oG
.01
JO

^P-.t7^3
Stack
T«mp.
°F
7^
7^
7^
7-5
75
•75
7^
7^
75
75
75
75
7^
75
75"
•75
7JS
75
7>S
75
75"
75
75
75

S. 75
Md -


Md • (0.44 x
                                                           •*• (0.32 X    ) + (0.28 X    )
Md -  ^7, 0

Me - Mdxd

Ma»(
                                                       % H,O
                                                         100

                                                       )x(1-
%H2O
 100
                                                             100
                                                                        100
                                             TS.
                                             Pa.Pb
                                                     13.8

                                                     '.05" ln-H9
                                                                    13.8
                                                          —      TsT^fl)
                                             V..85.48xCpx^Px ^  paxM,


                                             v«-as.48x(  |cl^   )x( i^a, )XA/.
                                                           ft/a
                                              A.-
                                              Q« - V« x Aa x 60 «/m
                                                                    x80
                                              Q« -,-Qax 17.847 x - x(1- ——)
                                               •*           T»      100
                                                          X 17.847 X-
                                                                                100
-------
             WET-BULE/DHY-BULS MOISTURE CALCULATION
.-,««. /./rou? r**v>C Au^A -scancn: /Tfc/^a /fTT ^
3ile: ^..*i /fjjr/^,* Coeraiors: T^/^T =un «?• fie-S-t- Qafe: 5//f/r7
3arometnc Pressure, in. Hg =
Static Pressure, in. H2Q =
Absolute Pressure of StacK = ?bar 3 ?q
Wet-Bulb Temperature. °F =
Dry-Bulb Temperature. °F =
Temperature Difference. Td - Tw =
Pbar = 23. /Q
Pq = -, £?
ps = 2-?- **
Tw • £(f
Td= 75-
AT = ft
m. Hg
m. HJD
2
°F
°F
°F
 Saturation Vapor Pressure of H.Q at Tw (from Table) =   =wv =    /2 t-f'?2Q      ,n> Hg


 Vanor Pressure of K,O = Pva = -Pvw, .   'Ps ' P>/W> X'^
                                       2300 -O 3x Tw)


                                                 	\  _     0. I?i*     in.Hg
                          2800- (1.3 x


 Proportion of Water Vapor oy Volume = 6ws

 8w3=   (Pva>     =       (  0. l$W  }       _          G.oot-^   0.
                          VAPOR PRESSURES OF WATER

                                 In Inches of Mercury

 9P    . a

                                      	    ......    ..„_    ,.__..    0.0888
 '0   0.0831    3.0800    :.oeaa    3.0728    :.o788   c.oaio    S.OBM    o.oaaa   .0.0933    o^ooi

 M   ! 2     :'1M°    :1127    a-l1M    -"*•   5.1302    0.1370    3.1428    0.1302    0.1987
      3.1847    3.17IB    -,,«.    3-1878    XJ9M   Q^^    OJ|la    Q_ao3    3Ja>1    OJa§a
                      OJ808    0.4082     	     	

 n   n'S!    'I!!7    °-aa°1    °-aa«   °-BI"   °:«»   ^w*5    0-"»"    °-«»    ««••
 «    ,'^     ^?    °-7918    °'8IM   O"8*"   "»    0-«««    °-««    0«"    0-«»
 8O    t.032    1.QOB    • ••>•    . ...     	     .	                      __      _
                                                                              1.378
                      1.919    1.981    1.010     1.800     1.712     1.789    1.810    1.870
                      2.748
•S   !£            *••    3-744
 'S    i»^    ;T^    :rn    ig-*    '*•«     iaw     "•«    "•»    «*•
                                                                              i
 iaa    !!U    !nr    IMB    IM*    1M°     "•°T     «w*    ^«    '*«     »
 2    IS    Il±    1M*    M»    20JO     2t.1«
 ^S    SS    25    2Mt    24*7    2M«     2MO
 »    ™    2?    »•    ««    3».M     SW
-------
                 GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:	
Sampling Location:  #„ »  gj^
Run #:  ft£-3U^
               Date:   ?-ti
               Clock Time:
                                           Operators:.
Barometric Pressure, in. Hg:  ~_
,o7
.0^
.o-7
JO
.0%

.oS
.°3
. to
.11
.10
.D~r
.oS
,oG
.(/
,/*
.10
c?1
•on
.ol/
.»
7<>
76,
76,
76
76
76
76^
-?<-?
-107
-7C,
TO
1^
10
76,
-«/
lu*
n^

S-7fc*F.
                                      Md - (0.44x%CO2) f (0.32 X%O2)


                                      Md - (0.44 x    ) + (0.32 X   ) + (0.28 X   . )
  - Mdxd
                                                % H.O      % HO
                                                - —) + 18 ( - i_)
                                                 100         100

                                                )X(1.___).,8(_
           P.
 ,-Pb+-!£_.,
       13.8
                                                           °R(°F*460)
                                                             13.6
                                      Vs - 65.40 x Cp :
                                      V* - 65.49 X (
                                      A.-
                                                   =      Ts f R)
                    Pax Ma


                )x(       )x
                                                    ft/a

                                                    .2
                                      O« - v« x A» x eo t/m
Qg

Q.
                                                             XflO
                                                    «*"
                                                     p,     %HLO
                                          .»QtX 17.847 X	x(1- 	2_)
                                          '           ft      108
                                                  X 17.847 X-
                                                                        100
-------
             WET-3ULE/DHY-5ULE  MOISTURE CALCULATION
?lant: l/hS(jg> £>^ A^..t
Site: J60*»« ^/f/C^./- Coerators: "/^/r/
Barometric Pressure, in. Hg =
Static Pressure, in. H2Q =
Absolute Pressure of Stacx = =bar ••• "q
— 'TS
^ -ccaticn: /i
=un ff1 /?£ ~ -
Pbar =
Pg= ,
P3 as
a */17
in. Hq
	 in. HO
in. Hg
Wet-Bulb Temperature. °F =
Dry-Bulb Temperature. °r  =
Temperature Oifference. Td • Tw =
Saturation Vaoor Pressure of H-.G at Tw (from Table) =
                                                          Td =
 Vaoor Pressure of K,O = Pva = iPvwi -
Pva=(  0.
                                           'Ps-
                                                     x (&T")
                                           2800 - (1.3 x Tw)
                            2800- (1.3 x

 Proportion of Water Vapor oy Volume = 6ws
           (Pva)
           (Ps)
                            VAPOR PRESSURES OF WATEH
                                   In InehM of Mercury
 o
 '0
 20
 30
 40
 SO
 00
 70
 00
 00
100
110
 140
 190
 180
-170
 180
 180
 200
 210
         3
       3.0378
       3.0031
       M023
       3.1047
       0.2478
       0.3828
       0.3218
       0.7382
        1.032
        1.422
        1.032
        2.588
      4.128
      5481
      7.588

      1249
      1!
  i
3.03B8
3.0880
3.1080
0.1718
04378
04784
0.3407
0.7848
 1.080
 1.487
 1.888
 2472
 3443
 4447
                         2
                        0417
               r.78»
 .1127
3.18O3
0.2877
0.3808
0.9001
0.7812
 1.102
 1.313
 2432
 2.748
 3442
 4.772
 0.180
 7.882
 10.12
               1848
      2347
      28JB
                       1!
                       1(
                       2448
  3
30441
30728
3.1108
0.1878
0.2782
0.4082
04802
04183
 1.138
 1.981
 2.114

 3.744

 0480
 0.180
 1048
 1347
 1844
 2047
  4
: 0403
:07BS
:i248
3.1999
3.2881
3.4203
0.8008
0.8482
 1.179
 1.810
 2.178
 2411
 3448
 5431
 0413
 848t
 1041
 1347
 18JO
 20LJO
  0
3.0317
3.0846
0.1370
04118
0412O
0.4820
04442
04048
 1.233
 1.712
 2410
 3481

 9402
 0480
 8.787
 11.12
 1348
 1744
 2148
 2843
                                                                     -7
                                                                     To
                        3847
                                3747
                                        31.18
                                        aunt
  7
3.0341
3.0892
3.1429
0,2203
04240


04332
 1.283
 1.789
 2478
 3.188
 4.174
 1442
 7.024
 0481
 1148
 1440
 1742
 2248
 2747
 3342
1?Z?


    3
  :0371
 .3.0932
  :.1S02
  3.2282
  0.3384
  0.4488


  1.333
  1.818
  2448
  3498
  44
                                                              7J
                                                              9400
                                                              1148
                                                              1442
                                                              1841
                                                              2749
                                                              3347
                                                                                     m. Hg
                                                                                      in. Hg
  a
o.e

0.1987


04888
OJ144
04888
 1471
 1471
                                                                                     3481
           7J
           8484
           1141
           14
           If
                                                                                     ait
-------
3 aa i_3
                  GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: £A$e& Date: 5V<- ?7
Sampling Location: £>L>£_/I; d-ty Clock Time: /^S~~
Run*:  Static Pressure, in. HUO: -, &<*
o MolPrnl3r\A^ Rry ^«. 6^ PitOt Tube^Co: ,<79
Stack Dimension, in. Diameter or Side 1 : / 3 Side 2: 	 	 '
WetBulb.°F: -^~~~ nrvfiulb.OF: .. 	

Travarm
Point
Number
/H
3
3
*/
5
6

A-/
a
3
V
<
C:









•




Velocity
Haad
in. H20
.OS
x/9
,/6
,sa
»a^
rCV?>

,/-9
,31
,<5T
' 9^
-52
-•/^












^KF - o,«ran
Slack
T«mp.
°F
/fct
IbU
l£,->
Ibl
i W
ibi

l<0^>
lb f (0.32 X %O2> + (0.28 X %N2>
Md - (0.44 x ) * (0.32 x ) 1- (0.28 x )
Md- tt^&{^7•^
% H2O % H.,0
M..Mdx(1-^j-)*i8(__ )
M.-( ,x(1.-_ -)>ie<— ->
Ma- 2f ««
Tj- /^ °F- °R(°F.460,
13.8 13.8
P«- ^S,8^ m.Hg
^P - ^ y??2-
^= | "is (°R)
Va-«5.4«xu>x JSP x y P9XM8

Va- V,!1/1/ ft/.

A.- /. 13 ft2


Oa- x xeo
Qa - 1 30 ^ aeftn
Pa %H.O
Q« ..-Qtx 17.847 x 	 x(1- — 2—)
«w Ta 100


                                        IKS
-------
  ik
I
   ,)•
                          METHOD 1 8 FIELD DATA SHEET
Plant: tASCr- Tested Analyte: JYx/ft^/*'*.
Date: C '/<•<> 7 Orifice Tank #: ^ —
Location: Q\lKAJ tt 
// *9
't/*t4
l(oL.
If- *Z
~ *•
/^•^
1 f.t<%-
l~)fj
/"?/
y -»/o
y 6^*

l(o7










Md - (0.44 x %Cag) + (0.32 X %Cy + (0.28 X %f^)
Md - (0.44 x ) 4- (0.32 X ) +• (0.28 X )
Md - 2-7 - V
* S^ ' «. » 0 « H 0 /6,'>^
7* HjVJ 7b ~2W
'Ss^v " x<1 " 100 * 100
<££/$*
* * 100 ' 100
/3A ,/ &^\j t *y ^^
S P
13.8 13.0
P»- 2V,8f In.Hg
®-o.mf
==: . F Ts rR)
VI • A9.4U x  3 "
Q«- VexAexflO«/m

Q«- x xM
^
Q§" /. 3 ' D M*"
Pi *H,O
Q§ .j-Q«x 17.047 x 	 x(1- 	 =— )
"™ !• 100

eta 100

OKU- //?/7^ -------
                        FIELD DA I A SHEET
Plant:	
Sampling Location
Run Number: ft-3-
Pretest Leak Rate: '&)
Pretest Leak Check: Pilot:
,/ tf <]
ate: 5' t$'
Date
 cfm
Sample Type:
Pbar  9 ft
CO2:
                                       Operator:
.P»:_
 02:.
      l£ in. Hg.
  / '5
Probe Lengthflype:
Slack Diameter: / if'
                                          As:
Nozzle ID:  —    Thermocouple X
Assumed Bws: ""'   Filter #: •
Meier Box #:  /»   Y: ;*?%6 AH@: /j	
Post-Test Leak Rate: > aco cfm (g)^'  in. Hg.
Post-Tesl Leak Check: Phot: ~~~  Orsat:	
TrcvwM
Point
Numbtr



























Sanipling
Tbiw
(mln)
0
y^>
r9*6
// ^
/.- ^






























































































































5?
60
61-
'&t






















^^
^7
-------
 iSSS
If—
                       SAMPLE RECOVERY DATA
PLANT

DATE
                                                   Run No.
SAMPLE LOCATION	

TRAIN PREPARER    ft
                            Sample Box No.  M-l    Job No.

                                                   Filter No.
SAMPLE RECOVERY PERSON

COMMENTS        M
     FRONT HALF
     Acetone
     Container No.

     Filter
     Container No.

     Description of Filter
                                   A
                                          erf 1/nainae.f
                            Liquid
                            Level Marked
Sealed
                                               Sealed
      Samples Stored and Locked

      RACK HALF/MOISTTrRF
      Container No.        	
      Liquid Level Marked
                                               Sealed
IMP. NO.
1
2
3
4
5
6
CONTENTS
Z>£ 4O
Dr f^o
£#yalt/
^HJC.A(=tfL-


TOTAL
INITIAL VOL
(ml)
/^t?
/fft>
-
Zero



WEIGHT (grams)
INITIAL
5-5*2
US.7
S/2.0
BS14


2§7t>,3
FINAL
5&.l>
t>t>5,7
511. b
845-1


j?£T83.0
NET
• 0.4
o.o
O.b
*.1


b.T
-------
         EPA METHOD 4 MOISTURE CALCULATIONS


PLANT:   LAS^P _ SOURCE/RUN *' 4-3-2   DATE:


1 . Leakage Correction for Volume Metered



    Vmc = V (L  - La) x 6
    Vmc=Vm-(Lp-0.02)xe


    Vmc=(       )-(        -0.02) x(       )


    Vmc=  JMO'  ft3


2. Volume Metered, Standard Conditions (68  F, 29.92 in. Hg)


                           Pbar-MAH/13.6)N
    V_   = 17.64xVmrxYx
      mstd          mc
                                  m


                                    )x
3. Volume Water Vapor Collected, Standard Conditions


     Impingers & Silica Gel = V...   = 0.04707 x (W. - W.)
                          wstd             f    '

                        Vw   = 0.04707 x(  fc.y
                          wstd
                         Vw
                          wstd
 4. Percent Moisture, by Volume

                 V,
                  wstd
               wstd   mstd
                  o.-ivs
-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: LAZee? p^o- 
Sampling Lo
Run#:  nnprarnr*:- flftX //?/V
Barometric Pressure, in. Hg: d*.1o Static Pressure, in. Ho O: '4^
Moisture. %: < — - /,/•/, MniPrM^rWT Prv -2*-*^ Pit«t Ti ihft>rv , |«»
rOOTI
Number
4-1
^
j
^
S
£

OH
51
3
Y
i

/w
/7<0
m
/•-7I
/(, $
Jt><\












*- M
91: /<'' Side 2: 	 '
3ulb.°F: -— 	
Md - (0.44 x %CO2) ••• (0.32 X %Q^ + (0.28 x %^42)
Md - (0.44 x ) + (0.32 X ) > (0.28 X )
M«- zz&f-v?^ ,
%H20 %H20 fiifrSt"
M« m Md x ( 1 • — — — ) •*• 1 8 ( ^^— )
100 100 1 1
M. -< )xd- — — — ) * ie<_— -_>
100 1OO
Mt- 2&3&- ^M^
T*~ ((>7 °p- 62-7 0R(°P*«o)
4 D
Pti — Pb +• ( ) +•
13.8 13.6
P"- "2-t.gr ln.Hg
^P - C?. ¥J<^
— / Tn /°R1
r— ,| ' J ' "I
V.-«b.4UxCpx^P X ^ p98M9
V« m 85.40 X ( ) X ( ) X J
V
v«- 3i',?6' m
.*•-/.«.> ^
Q«- V«xAsxOOa/m
Q«- x xflO
Qs-^^^^ adm
p, %H,0
Q.itd-Q.xi7.847x — x(1--j^-)
**• X17-W7X X(1-"ST>
                             dM*n
-------
                          METHOD 18 FIELD DATA SHEET
    -9V
    31
Av -
Plant: ff»*co 	 y Anaivte: 
LOcation-zLZLLj") L/C/V Pump/Bolometer*: -~
Hun»: ;cu 3 -( R. p^st fmm Hal: ^
siack i.y.,_U 	 Poct.jest (mm Ha) :x—
Hbar:_^4d) Tf Prntn-rt (°R- ^
sample Tub
Operators:^
\fJQ-5-M 10-3-iH Post-Test fR:-
/JA /(









yitt'l HL, - . <$($
Velocity
HMd
in.H^D
, K
.(/.
.11
'3*
,3*
.J ^

tf? -7<
. pA
. Off
)tf
,»*>
' &1*

f . ¥^^









Stack
T.omp.
GZ&
'JJL&,
#a~)
Q ir<
&&$ —
9&

33ft
3? 1
^32
'J 3V
:^-3'i?
y^-3 •

22.*









Md - (0.44 x %CO2) + (0.32 X %<%) + (0.28 X %^)
Md - (0.44x ) + (0.32X ) * (0.28X )
'^. 2?.o
WJ %Hn *H20 ^'^
Sti, L Mt i- Md x M - . 1 -t- 1H f . ^ ii
WAO 100 100 /, / /
•>0/f5Z.
^y UA . ^ >**/4 \i.«a/ \
?y» I0° ""
jy//?" M
V/S's'm ^ °F" ^f °R<°F«.4ao)
0 D
Pa . Ph * °'r> » ^ ) +
13.6 13.8
*- ^e.9/ |n-Ha
^p-^yi^l
r= J T8<°R>
V.-05.48.CPXVSPX ^ p8xM§
V« • as AQ vf )y/ )v4f
vt- 35:V33 fi/B
*•• /,23 «2
Qi • V« x Aa x CO a/m
Q»» x xM
Qi- it/5" -^
Pi *K,0
Ql^j -Ql XI 7.047 X 	 x<1- 	 2_)
•* !• 100
Md '100
0%M- /?/0 d«fc" . y
-------
                                              FIELDDAlASREET
Plant       	
Sampling Location €>£/£/,'-# 10
Run Number /0-3-1    Date:  5 • i-1
Sample Type:
Pbar
CO2:
                                                             Operator:
                                                        O2:
Pretest Leak Rate: n3cr)   cfrn @ /fl  in. Hg.
Pretest Leak Check: Pilot:
Probe LengthAType:  J  ^ "*
Stack Diameter:   /«T v   As: 1-2.3
                                                                   PHot #: yy 3
Nozzle ID: ••	*  Thermocouple #: l£> '
Assumed Bws:	Filter #:  -^—-
Meter Box #:  /f   Y^fedyAH®:  A > cfm @ KXJn. Hg.
Post-Test Leak Check: Pitot:  •— Orsat:	
Point
Number























\



z~~r~~
Sampeng
Time
(mln)
0
ID

3O
So


















j
i


OocfcTbm
(244iour
dock)
\*4Q(o
/H3C
W *l^>

/5'^4j






















Gas Meter
Rearing
^ i 47^1
'7*1* / y <
^p/c
^fl, ^
q-7, 



- -


















Velocity
Head(Ap)
inH2O
Orif oa Pressure Differential
(AH) in H2O
Desired
Actual
Stack
Temp.
(Ts)
Temperature
°F
Probe
Y/////Y///////////////////////////


























// 56
)' ?&
It $k
h ?6































"




































































Filter
Impinger
Temp.
°F
Dry Gas Meter Temp.
Inlet
(Tm in°F)




















•






5 ^?
fj fc*
^&
~$~?






















%*/
&9
&}.
£*-1






















Outlet
(Tm out°F)
Pump
Vacuum
(in. Hg)
s//////////
%Q
SI

f^2






















3
3
"3>
-3






















                                                                                               Tm=
-------
                       SAMPLE RECOVERY DATA
PLANT
                               Run No.
                            lo
DATE   5"-/sT-9 "?    Sample Box No.  /V-5     Job No.

SAMPLE LOCATION  -# /O  Ougw  o^ie'T    Filter No.

TRAIN PREPARER
SAMPLE RECOVERY PERSON
COMMENTS

FRONT HALF
Acetone
Container No.

Filter
Container No.

Description of Filter
             Liquid
             Level Marked
                    Sealed
                               Sealed
Samples Stored and Locked

RACK HALF/MQTSTTIRF
Container No.        	
 Liquid Level Marked
                               Sealed
    IMP. NO.
CONTENTS
              Dl  IV
           TOTAL
INITIAL VOL
   (ml)
            (bO
                            0
                                                 WEIGHT (grams)
                                        INITIAL
                                     FINAL
                                                  77*4
                                       NET
                                                7,5
-------
                                              FIELDDAlASREET
Plant	
           i
Sampling Location
Run Number /0-3-J
Pretest Leak Rate: rdcD
                            10
Date:
 cfrn
Sample Type:
Pbar
C02:
                                                             Operator:
                Ps:
                02:
                                                                            Thermocouple #:
                                                                           -Filter #:
                            /Q  in. Hg.
Pretest Leak Check Pitot: — — Orsat:
Probe Length/Type:
Stack Diameter:
                          Ptot #: ££_3
                                          As:_U3_
Nozzle ID:	
Assumed Bws: _^
Meter Box #:  I1
Post-Test Uak Rate: „. Qg>-> cfm @	
Post-Test Uak Check: Pilot:  -— Orsat:
TravwM
Point
Nurabw























\



SmpKng
Tbm
(mln)
0
/£>
i?t
30
*/o


















i
i


Oodclbiw
(244iour
dock)
;v^6
/H3C
W *t^
/H S&
i$ dt>






















Ga*Met«r
Heating
(Vm)ft3
£4 . 401
•7 ^OG



- -


















Velocity
Head(Ap)
inH2O
Oil ca Pr«Mur« DHtercntiat
(AH) in H2O
Desired
Actual
Stack
Temp.
(Ts)
Temperature
°F
Probe
'//////////////////////////////////


























/^4
},9&
1,5k
\,?L































«r




































































Filter
Impinger
Temp.
°F
Dry Gas Meter Temp.
Inlet
am in°F)
Outlet
(Tm out°F)
Pump
Vacuum
(in. Hg)
'///////////////////////// '//



















•






5<£
V-,f
5^
5"7






















Ft
£f
^
gi






















KQ
81
?3
?->


















....



3
3
•*>
•~3






















                                                 AH=
-------
                       SAMPLE RECOVERY DATA


PLANT   Lfl$£&	Run No.   / ®

DATE    S'-JS'-y 1    Sample Box No.  A^-5    Job No. .
SAMPLE LOCATION  -# IP   Oue-w  o^ieT-    Filter No.
TRAIN PREPARER
SAMPLE RECOVERY PERSON
COMMENTS

FRONT HALF
Acetone
Container No.

Filter
Container No.

Description of Filter
                            Liquid
                            Level Marked
Sealed
                                              Sealed
Samples Stored and Locked

RACK HALF/MOTSTTTRF.
Container No.        	
 Liquid Level Marked
Sealed
IMP. NO.
1
2
3
4
5
6
CONTENTS
Dl IV
SZ HT?
^PV"
Stf'c. (*&


TOTAL
INFTIAL VOL
(ml)
/t>0
foo
0
z&



WEIGHT fgrams)
INrHAL
<7/^g>
£68.7
^3,"&
-7tf.(c


Mtt:°(
FINAL '
&r*.f
s$?.y
wf,J
77^4


2H3t^
NET
•





7,5
-------
3 ap g
                       GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:	
Sampling Location:
Run *:  /<3 ' 3 - 3
                                                            Clock Time:
                                                  Operators :
       Barometric Pressure, in. Hg: 3%.3Q	  Static Pressure, in. HoO:  "-
       Moisture, %:		Molecular wt., Drv:  -2&#"  *	Side 2:
       Wet Bulb, °F:.
          Number
        A- /
        A- i
            2
             5*
               Vttecrty
                H«ad
               in. H2O
              .19
                              Dry Bulb, °F:.
Stock
T«mp.
 °F
                               931
                               239-
                               130
                               ,9^3
                                             Md • (0.44 x %CO2) + (0.32 X %O2> + (0.2B X %Fty


                                             Md - (0.44 x    ) ••• (0.32 X   ) + (0.28 X    )
                                                 % HO      % HO
                                           Mdx(1 - - — ) +• 18 ( - — )
                                                  100        100
                                                             	) + 18 ( 	)
                                                             100        100
                                             71-
                                                - Pb
                                               S.P.
                                               13.8
                                                                    13.8
             P.-
                                                    ln.Hg
                                              V« • 65.40 x Cp X
             V> « 65.49 x (
                                                                  PsxMs
                                                       ) x (
                                                                       )x
                                                   /,2-3   «2
                                        Q»»

                                        Qg"
                                                                    xOO



                                                                   %H_0
                                                                     2-
                                                                    100
                                                          X 17.847 X-
-------
                  FIELD DA IA SHEET
Plant-
LAf^CLC^ Sample Type: /*?- y Operator: y)AXy£xi;
Sampling Location O0£/^**- 1O Pbar. 9 Ps: — / § / '
Run Number:
;<9'3-3 Date: (f-fZ- 97 CO2: 	 O2: 	
Pretest Leak Rate: ,fyo elm @ r < in. Hg. Probe Lengthflype: / ' *S Pilot*
Pretest Leak Check: Phot
Point
Number









d-(
3

*V
4-
6

ift-/
5?
3
^
^
^





Sampling
Time
(mln)
O
/o
:9O
$ D
4-O






















Clock Time
(244iour
dock)
]")'3^
({$
$5
iff &<.
jY( *$






















: ^X^Orsat: —
ST-3
• 	 Stack Diameter: /5" As: |. Z,? 4*

Gas Meter
Reading
(Vm)«3
/^o. o*/^?
/^o,^o
IV$"^0
/5'3r^5'
;^/ /^^o

















/4»«.>ir?




Velocity
Head (Ap)
inH2O
Orifice Pre»oure Diflerential
(AH) in H2O
Desired
Actual
Stack
Temp.
as)
Nozzle ID: •*•"" Thermo
Assumed
Meter Bo
Post-Tesl
Post-Test
Temperature
°F
Probe
Filter
Bws:-^- Filter #
<#:^i
LeakRa
LeakCh
Impinger
Temp.
°F
couple #'. ^ &
Y: ,/te'6AH@: /- /4ii?
'e: «€fe'J
eck: Pilot:
cfm @/£
«^ Orsa
in. Hg.
t: 	

Dry Gas Meter Temp.
Inlet
(Tm in°F)
y/y////////////y//////////////////////////////////s







\ftiotiil

' 1 "$>
,0 1

/2"?
..3S1

* ir
3 Q
>£ /
,/SF
^^ /
, ^C5
c» V5b8




// %b
1 s£&
] p£
i • 1 £>



X



















































Sr/? <*-£..
QP^,
93 Y

<3.*9-3
QPO
&J>/

93 1
Q.3 <^
i>36
^>3.f
S>3 ?
P3C







































^JL-
M> -
\/5 ^
A-

d^t*^
JL$^~.











<^a
5'cS1-
^? /
s* ^




17-3
28.S7
2V.7/
l9.$
<3r






















Outlet
(Tm out°F)
*y*7
9~?
/Cuf^i
/QC>






















Pump
Vacuum
(in. Hg)
2
^
3
3






















AVm-
-------
                       SAMPLE RECOVERY DATA
PLANT

DATE
                                              Run No.
          -/ 
91 H^O
t^*^
S-ftu GJ


TOTAL
INITIAL VOL
(ml)
/&£>
/H>
0
IslO



WEIGHT (grams)
INITIAL
blo.Q
bo 73

...
issi.o
NET
• -0./
1.0
0.2.
5.5


Afc ^f
•^y • *
-------
   3 OP CZ3
                           METHOD 18 FIELD DATA SHEET
Af: H 
/o
10
w
0
-o
^
Plant: A/?S£# Tested A«»'yt«' ^v/~"-
Date: 5 - /? -•» T Orifice Tan1' *' -
Location- ,VD# Pump/pntnmRter *: \,-"frr 3
Run*: /VD/J-3>-7 Pt: PretflSt (mm Hg):
Stack I.D.: 52." * \x&" Post-T«st (mm Hg): —
Pbar: 2.^.\ Tt: Pretest <°R: ^
Sample Tube
Operators:
a#:/VDA-32* uM--)-2* Post-Test fR: ^~
•r4/^
_eak Check: Pre: /^ Post: ^"
Gauge
Time Vacuum
(Hg)
UcTL i~7 )
I Jfc £..«**' \
i3n^,SS i
\?n^,^3 i
131^.31 i
v^n^.^i *
I 3 *>3 .0* ^

Tr«v«rs«
Point
Numb«r

























Flow
Setting
3 \
B\
z\
si
a\
91
TL 1

Velocity
Heed
In. H^O

























Stack
T«mp.
°F

























Time: start:l5sV Finish:ii>^.Total:JjjjaiM
w/R-_^0/B: - 02: 2-' C02:_ g —
Md - (0.44 X fcCCty -•• (0.32 X %02) + (0.28 X %N2>
^2, Md - (0.44 x ) + (0.32 x ) •*• (0.28 X )
n
Md-
"^ %H,0 %HO
-
^^ TS- °F- °n (°F**ao)
SP. i
Pi-pb*-sr"( } i"
Pt . In. Hfl
^s?-

vt - as.48 x CP x VAP x ^ psxM«

Vt« ft/*
A.- n2
Qa»VtxAaxflOa/m
Qa^ x xW
Qt • acfm
Pt %H2°
Q§_^- Q» XI 7.647 X 	 x(1- *•)
. «td T« I*
Q-.W- ^'-«*'x *(l< ,00 '
Qa^d- dacfcn /|
-------
                       METHOD 18 FIELD DATA SHEET
Planr_L
Date:	:
                                                 Tested Analyte:.
                                                 Orifice Tank #:_
          Location;  ^D
          Run #:_
          Stack I.D.;
          Pbar:	22
                                       Pump/Rotometer #:  V
                                       Pt:  Pretest (mm Hg):
                                            Post-Test (mm Hg):'
                                       Tt:  Pretest fF):^
Sample Tube #: NOB -3-3)1, i^i
Operators:
                                                      Post-Test fF)L
          Leak Check: Pre:
                       Post:
            Time: Start: 113 5" Finish: tfl3& Total: faS m.^
            W/B:   -  D/B: -  O: ^'
I
I
Time
v»*a.l(o
l^^^.^^f
v^ S"».4f
L"Mo.toS
t?t 3.^3
t^5. to-?
v^^.oV
Gauge
Vacuum
(Hg)
1
\
I
1
i
1
i
Flow
Setting
31
al
•^\
3t
3)
X
3-1
tas
40
-------
          APPENDIX A. 1.5

             Condition 4
(includes flows, moistures, and Method 18)
-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: [h^LO Date: .s*-/5""1'*7
Sampling Loc
Run #: we
ation: A\«;/> £>tav»* Clock Time: "?o<.s-
- *-i-i Oneratonv Trt/s-5
Barometric Pressure, in. H
Moisture, %: - 1 1
Stack Dimens
Wet Bulb, °F
TrimrM
Number
,
2.
3
^y
5
0
7
tf

I
2
3
4
6
\j>
1
3





•

.

q- z ef. Z. Static Pressure, in. F-UO: „ /i
Molecular wt.. Drv: ZK:W PitOt Tube, Cp: ^_i?
jion, in. Diameter or Side
5"f DrvB

V«bcity
in. H2O
,ii
. W
, 3O
•^G
, 51
. 31T
.3S
•S-/^

i3C7
, 30
, 33
. 3S
.^1
V6>
.11
.11








£P-,5l*H
Slack
T«mp.
°F
' '1^ .*
~>d
i^
~7^
7?
1?
~7t
7^

~7f
^^
"IS
1°l
If
T?
T?
If








S--7J?
1- &i /TS Side 2: •*$»
nlh'Op. 78
Md . <0.44x%CO2) -f (0.32 X%O?) -i- (0.28x%N2)
Md - (0.44 x & ) * <0.32 x 5 1 ) + <0:28 x 1  ^
%H.O %H-0
M kJd M 1 ' 1 B ( )
•7V . '/| — . 	
*-tfl <-/^-<
Vt. "°'^" ft/«
\ Col •,
Aa« nz
Qt • Vi x Aa x 80 */m

0.. t|o.^ x 1.6 1 xoo
Qt • "°5 ? acfm
p. ItHjO
^itd"0**17'847* T. *°" I'M '
Urto 31-»l -^
0*^- UI7.M7U s^ Jed 1QO )
-------
              WE7-5ULE/DHY-SULS MOISTURE CALCULATION
                                                                 .„    .CU.  .;
  3lte: MfllM
                           Ccerators:

 Barometric Pressure, m. r-tg =
 Static Pressure, in. H-O =
 Absolute Pressure ot Stacx =   -bar 3 —
 Wet-Bulb Temoerature. °r  =
 Ory-Sulb Temoerature. °~ =
 Temoerature Difference. Fd • Tw =
 Saturation Vaoor Pressure ot H.G at Fw .from fabie» =
  Vanor Pressure ot K,G = ^va = ,PVW, .
                       (
                                                 x
                                          2BOO-M.3xfw)
                           2800-n

Proportion ot Water Vaoor ny Volume
         (Pvai
          (Pa)
                                       6ws
                                        I   )
                            VAPOR PRESSURES OF WATEH
                                   In Inerm ot Morettry
  '0
  :o
 50
 00
 70
 oo
 M
 100
 110
.130
'l30
 14O
 190
 iao
 17B
 180
 108
 200
 210
       3
      .0378
      .out
      .1023
     3.1847
     3.2478
     0.36M
     o.uta
     0.7382
      1.031
      1.42S
      1.831
      2JM
3.C
:.ioao
3.1718
3.2970
OJ7B4
O.S407
0.7
 1.C
 1.4
 1.1
 2J
                         2
                        0417
 1127
3.18O3
3.2877

0.5001
0.7012
 1.102
 1.913
                      2J40
     4.1
     SJM
     7.!
  3
30441
70728
3.11M
3.1870
3.2782
0.4082
3.3802
04183
 1.138
 1.981
 2.114

 3.744
 4.1
*0788
: 1248
3.1858
3.2881
3.4209
3.1
3.1
 1.179
 1.810
 2.178
 2J11
:.oaio
3.1302
0 2O35
o;
0.4
0.1
04790
 1.213

 2.243
 2J
  a
30317
3.0844)
3.1370
Oil IB
04120
0.4820
04442

 1.293
 1.712
 2410
 3411
 4J
     t:
     I!
     1841
             7.751
         0.100
         10.12
         12J7
         II
         II
         8.180
         1041
         1347
         II
        S431
        9413
        8481
        1041
        1347
        18JD
                                   5.189
                               2447
                               301
                               374
         II
         1347
         174T
         21.14
          8JV7
          11.12
          1341
          1744
          214*
                                                                                   in. Hg
                                        3141
-------
oga rj
                       METHOD 18 FIELD DATA SHEET

Date: £->s-^i Orific« Tank *•
Location: m«;rt «=,^4- Pump/Rotnrnfiter #- ^"^ z-
Run#: n&-4-z Pt: Pretest (mm Hq):
Stack I.D.: n . *; Post-Tost (mm Hq); *
Pbar: w.i It- Prntflst (°R: - —
Sample Tube #
Operators' -pr
:jmir--v-zrt i*ie"4-5-(? Po«t-Tflst fF):
^ 	 , ' Time: Start- Finish: 	 Total: 	
Leak Check: Pre: A/ Post: / W/B: *? D/B:^7J1_O,,: ^ CO0:_£ —


ex/** c
f1-
-'3? i?
2V VO /O
Iime,6

fe
^3&to
j|'7l
Time
23.76 5"*y
-/-V7. 36'
iz-^n, ^i
22^B. 5V



/
Gauge
Vacuum
(Hg)
/
/
t
t



34-ftVi.- r /-. o •>
Traversa
Point
Number
/
?
3
^
•5
C-
7
fr

(
z.
•J
H
5
Is
7
?







-TZrWfi 4vA*
V«tecrry
HMd
In. H^O
-•27
,3/
,35-
.37
, T7
,38
,59
.-//

.20
.3/
.33
.36
.^7
. 3V
.^0
,vo







• ^*
75

7?
77
75
78"
iy
73
7*
TT







"7X
Md - <0.44x%CO2) -i- <0.32X%02) + (0.28 X*^)
^ ^^
Md - '-' >
Si
% H.O % HO
5, M..MdKJi--^.) + ie(-— )
-^ M«-< -?<•» ) X (1 - ' ' ° ) + 18 ( ' '® >
v" l"( '*•'' 10O 1CXJ
M.- ?^ \°\
T8. ~?5 °F- SlS °H (°F*4«0)
13.0 13-«
p, . 0 "\ • 3O In. Hg
£F- .S^SJ)
^= J T» "R)
vt • «».4» x v*p x r7 |T-1Ti, -L^-7«> l-° ,
"••Id" Al7-e47x- 	 ^ x(1 -jjj-t

Q*,^- ^"i> dwfcn
-------
              WET-5ULS/DHY-BULH MOISTURE CALCULATION
 •=iant:
 Site:
                      0
                                               -scaticn:
                             Coerators:
                                                                      Gate:
Baromatnc Pressure, in. rig =
Static Pressure, in. i-UQ =
Absolute Pressure ot Stacx =    =bar 3  ^
Wet-Bulb Temperature. °r  =
Ory-8ulb Temperature. °~ =
Temperature Difference. ~d .- £w =
Saturation Vappr Pressure of H-C at Tw itrom Tabtej =
  Vanor Pressure ot
Pva t=(
                               = ,PVW, .
                                           'p« •"
                                           2300 • i i .3 x
                            2800-,;  2 x

Proportion ot Water Vaoor oy Volume  = 8ws

     =    (Pva)
           (Pa)
                             VAPOR PRESSURES OF WATER
                                    In IneriN ot Mercury
  0
  •0
  :o
  30
  «o
  so
  oo
  70
  00
  90
 100
 MO
,120
'l»
 140
 190
 iao
 170
 iao
 iao
       3
     T0378
     c.oaat
     3.1847
:.ioao
3.1718
          2
          0417
     o.sata
     0.7392
      1.032
      1.422
      1.832
      zjaa
 1127
3.1803
3.3877
0.9407
0.7B4*
 t 008
 1 .4*7
 1.081
0.7812
 1.102
 t.913
  3
3044*
10728
3.tiea
3.1878
0.2782
O.I
0.!
0.8183
 1.138
 1.961
 2.114
              3JU
                       1748
 0788
 12441
3.1898
3.2881
3.4203
o.e
0.1
 1.17S
 1.810
 2.178
 2J11
                          3.C
                          :.oaio
                          3.1302
                          0 2039
                          0.3004
                          0.4
                          0.1
                          0^790
                           1.213
                           1.080
                           2.243
  a
30317
3.0«4«
0.1370
                                   3J120
                                   0.4820
                                   04443
              7.7W
210
      tut
      2SJT
      2UI
4.773
9.180

10.12
12JT
H
II
2440
                                3.744
                                4.800
                                    : 233
                                    i.na
                                    2J10
                                    3
                                    4J
                                        lost
                                   S.1B9
                                a.180
                                ioao
                                13JOT
                                U
                          1041
                                    8J07
                                    11.12
                                    1
                  2447

                  87JDT
                          18JO
                          2O9D
                           17JOT
                           21.14
                                                           21JH
                                         3148
                                         37JI
                                                          Pg =  - *  •
                                                           Pa =  _
                                                          Tw =  _.
                                                           Td =  _
                                                          ^T=  _
                                                                   \
-------
  SOS. £3
JK -- 5
         Plant:
         Date:  ?-/j.--h • f1
T) I 2. II




Trav«rM
Point
Number




























































Vacuum
(Hg)
/
/
l
/




Velocity
Head
In. H^O

























nvw
Setting
: SOc-L-
! 50 < <-
r-,0 tc.
i-^,0 1 1'




Stack
Ttmp.
°F

























ISM - (0.44 X %C02) -t- (0.32 X %O2) + (0.28 X %Nj)
-^— Md - (0.44X ) + (0.32 X ) •»• (0.28X )
?d
Md -
<•<*>
% HO % H2O
^ M.-Mdx(1--j35-)*18(-j3r)

M«-( )x(1 10Q ' *101 ,QO '
M«-
T.- °F- °R(°F*4«J)
S P i
h- ""*•&•< '* 1"

^SP •

j== J T"<°R'
V«« 65.49 X Cp X VAP X \l p,xM«




V»- ft/«

At- ft2

Qt • V« x As x 00 «/m

Qg» x xOO

QB • adm

_ %K,0
Qi_1J-Q«xl7.e47x — x(1- )
•id Ti 100

0. - X17.647X Ml- )

Qi«tU'" dtofcn
-------
a OQ czj
                        METHOD 18 FIELD DATA SHEET
 1-2,2
Plant: L&fO TesteH AnaiytP- ^,^
Date: ^-K-n Orific« T*ni< *•
Location: fW.n £«»,flu-;v- Pump/Rntnmeter #: VJ-H 2-
Run#: fie - 4- 1 Pt: Pret««* (mm Hg):
Stack I.D.: •A'/x^B' Post-Tact (mm Hg): -
Pbar: 29.2-0 Tt: Pretest f°R:
Sample Tube
Operators:
S*:ftf-H-^ i^r-^-ift Poet-Tflfit fF): -
rA Time: Start: -><•"* Finish: -020 Total- «*
Leak Check: Pre: ^ Post: ^
Gauge F)ow
Time v«*|{m Setting
2.2^,*
• j 1^0 u.
•2*7* 5. 2& / i#7«.
•>ai£ °r \ \ 1*0 n
129C, ^/3 ' ,3*14,



<*»/.-/ = — , 6^
Trov«rM
Point
Number
1
I
1
^
.•S
i,
1
1
•>
4
5
(/
/
I
T
N
}
u

i
-J
M
5
/.;

V«tedty
HMd
In. H^3
,J&
,05
-cr
.aLf
,c~r
.0~l
.0?
07
,oC
05"
oi1
. 'O
. »z
. /o
T,//
.0%
.0?
.06
£»<•
.<»-7
JO
O.ZWL
Stack
T«mp.
°F
If
I*/
T
Md - (0.44 x ttCC^) -t- (0.32 X KO^) + (0.28 X %^)
-In— Md - (0.44 x v) )-t-(0.32x r», ) + (0.28 x""5 ^ )
^
^ M- z&e?
% H.O % H,0
SG M..Mdx(i--^-)*ie(~^r)
-S"C u. _ / 1 '-i \ v M "^ 1 + 18 ( •' )
M«.< a-] )xd- — — ) + i«( 100 >
M.. -? f.^ f
T.- 7ff °F- ^"^ °fl(°F + *«»
s p ^- —. - ^^Y
"•-^-S"'0^* 13.8
P« - ZT. & in- Hg
^P- 0.2.^^
r ^? \/ T9<°R)
Vt-65.49xCpX VAP x W paxM,
.j n-rin 1 "^^ lirf ^/-<1"')-/'
V« - ^ r ( *> «/•
A* - a . o?~) n2
Q«. V«xA»xflO«/m
OB- i 73'l S x ^'^"7 xeo
a*" Stf*? £ «dm
p. %H_0
Q«^.- Q« XI 7.847 X 	 x(1- • — ^-)
•W T« 100
P1./S , <4C.
^rtd' ^^ J X17.047X ^ x<1'-^
QNW- L\<^Lj(j>tM>m
-------
             WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: <_^-* r^cA,^,
3ile: ^or^ £^^4. Ccerators:
3arometnc Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stacx = Pbar -^ -
Wet-Bulb Temperature. °r =
Dry-Bulb Temperature. °" =
Temperature Difference. Td - Tw =
Saturation Vapor Pressure of H~Q at Tw
Vapor Pressure of K,O - Pva - iPwvi -
i 2°WK . U<;
Pv»«< US-v, } ( IS 'b
_2caticr.: ( ** <= »v\ £"< u « ^ ^-f
*Vr/i =un ff- $£-<•/- / Date: V,
Phar= ^3
Pq= - • <^
=cf Ps= ^1.|Q
• J.b .
T^= ^?^
Td. ^
AT= ^
itrnm TnhlP* = =VW = • ^S^O
'Ps - P«/w» x (&T)
2800 - (i.3x Tw)
'^b)x< n ) .^^

(<3/?-)
in. Hq
in.H.0
2
.. in- Hg
°F
°F
°F
in-H9
in. Ha
                            2800 '(1. 3 x

Proportion of Water Vaoor oy Volume = 6ws
T.me.
 9P
  0
  '0
  20
  30
  4O
  so
  00
  70
  80
  00
 100
 110
.120
'(30
 140
-f90
 180
 170
 180
 190
 200
 210
                            VAPOR PRESSURES OF WATER
                                   In Inehas of Mercury
       3
     0.0370
     0.0031
     3.1047
     04478
     0.3829
     0.3218
     0.7392
      1.032
      1.422
      t.032
      2499
5411
7.!
OJ
1240
1549
1041
2347
28L78
:.0380
o.ooeo
0.1000
0.1718
04978
04704
0.3407
0.7848
 1.009
 1.487
 1.999
 2479
 3443
 4447
 8434
 7.781

 1248
 1!
 II
                   2
                 :04«7
0.1127
0.1803
3.2877

0.3801
0.7812
 1.102
 1.313
 2489
 2.749
 3448
 4.772
 0.190
 7.889
 10.12
 12J7
 1!
 II
  3
0.0441
0.0728
0.1100
3.1078
04782
0.4082
0.3802
04183
 1.138
 1.581
 2.114
 2429
 3.744
 4.900
 0490
 8.180
 1049
 1347
 184*
 2047
 2447
  4
 0409
 0788
 .1240
0.1959
3.2891
3.4203


 1.173
 1.010
 2.179
 2411
 3449
 3411
 8.313
 8481
 1041
 1347
 1&70
 20JB

                       2949
                                3747
                                          31.10
                                          37.71
   9
 00371
.0.0832
 0.1302
 3.2292
 3.3384
 3.4889


 1.338
 1.819
 2449
 3499
 4499
 3498
 7409

 1148

 1841
 2949
 2749
 3947
  a


0.1987
                                                                                0.7144
                                                                                1471
                                                                                1478
                                                                                2481
                                                                                      im
                                                                                      2849
-------
Plant:  I-fa to
               GAS VELOCITY AND VOLUMETRIC FLOW RATE
Date:
-/*•-k.,,<,+ Clock Time: ^20^
~ n-t Onerritors1 r^/5S ,
Barometric Pressure^ in. H
Moisture, %: * °!S
Stack Dimeni
Wet Bulb, °F
TramrM
P^_I_.A
r*Otnt
Number
f
i
3
**
-*
fr
1
z
3
^
5
(X
I
7
T
V
5
ion, in. Diameter or Side
^7 DryE

Vtlocny
H««d
in. H2O
• o<*
, of
,uu>
'01
(si
.01
,0*
.&%
.ol
.03
,oLff
10
/3
.0?
,&<<>
.0^
.05
Jl
'II
.<4
6(*
.0*
Stock
T«mp.
°F
•7V
7V
7V
7V
-7V
-7V
7-S
75-
7^
IS
7V
7V
75
75"
7^
7V
7V
vi
75
75
75
75
1- Z*y " . Side?' 2^f^
iiilh.op- -7.^
Md - (0.44 x %CX^) -f (0.32 X nCty + (0.28 X %N2>
Md - (0.44X 0 ) * (0.32X .21 ) +• (0.2BX~/ T )
Md - 2'7
%HO %HO
100 tOO
^ 1 100 1 00
P,. •S0!. /^ in.Hg
^SP- ,.>Tf6
— f fs(°R)
V..«b.4«xLpx^H x ^ P9JCM8

/ S'?'3

v«» t^5."% "2. ft/«

A.. %* n* t^ t^
Q> • V« x Aa x 60 «/m
4-tr"
QC m I "=? • 1 2. X 3' • ( * / 1>V x *
a, » 7^; cv •efc^r5^r>\
-------
 ^lant:
 Site:
      WE7-5ULH;DRY-EULE MOISTURE CALCULATION
                     -va =
                                      zaoo - r, .3 x
                         2800- (i.3x

 Proporaon of Water Vaoor oy Volume = Qws
                         VAPOR PRESSURES OF WATEH
                                In IncftM ot Mercury
 9ai


210


                     s





                                    3MS
                                                          Oate:   Vr«T
                                              pg= _
                                              P9=    *•*•'.*
                                              Tw = _
                                              rd = _
               in. Mq
               m. H^O
               m. Mq
                                                                      m. Mq
                                                                           m. Hg
                                                       2.0S41
                                                       3.0882
                                                                      8
                                                                    : 0371
0 2201
0
                                                       2J78
                                                       3.101
                                                       4.174
                                                       1443
                                                       7.084
                                                                    :.isoa
                                                                    ^3.2282
                                                                    0.3304
                                                                    3.4


                                                                    1.339
                                                                    i.ait
               o.i
                                                                            1471
        4.2M
        9JB8
        7202
                                                             17
                                                             2U
                                                             arjor
                                                               11
                                                               1
                                                               1*41
                11

                1
-------
3JC3 CJ
                   GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: LflSclc Date: <- 15 -
Sampling Loc
Run*: ?-*
:ation: CVeyt' ^9 Clock Time: 3"
/-/ Dnorators: iDftA /<£• &
Barometric Pressure, in. H
Moisture, %:
Stack Dimen;
Wet Bulb, °F
TravarM
Q— 1— A
rOinl
Numbar
/?- "\
:>
3
V
,r
^.

A- )
P
3
^














q: JftfO Static Pressure, in. HUO: ~- &"?
Mnlpnilarwt Prv 	 Pitot Tube, Cp: ??
sion, in. Diameter or Side
• 	 ' Drv E

Vatociiy
in. H20
.oy
1 />7)
I")
5X
Ite^
/6V
113
Wb

/fo 1
I fob
)&6?
f<6 /
Ibfr
1 &^>












fj. ito^
1: /5V Side 2: -
nlh.Op 	 • 	
Md - (0.44 x %COZ) + (0.32 X %0Z) * (0.28 x K^)
Md - (0.44 x 0 ) -i- (0.32 X 3 , ) -t- (0.28 X ~) =) )
Md - ^ S
% H2O % H2O
M..< .5^ )x(1.±_5_) + i6(-L5r)
Ma- 3^-^^
T;. loV °F- 4=3^ °R(°F*460)/
c p
Pa - Pb + ' = ( ) •*• 	
13.8 13.8
f& - , ^ ^m
— / Ts^R)
Ve-«S.4BxU>x Jf& x y p9xM(|



Aa- \-'P3 ft2
Qa . Va x Aa x 00 t/m

Oa • #i*^i x I- "5? x^O
/
0»m 3^$ adm /
P. ^HjO^

"3*-sS x -L

-------
I
i
•ii
          PlantL
          Date-
          Location :-Qil£AL-?L
          Run #:  
Pa /c
pa^o
£3 3o
fv^^
Gauge
Vacuum
(Hg)
O
O
C
&
O
O

Flow
Setting
9SD ty/W-c
/




^
             Trovers*
              Point
             Numbar
                -£
                 6
                         Vatoctty
                          H
                         In.

                          •JO.
     Stuk
     T«mp.
      °P
                                   M
                                     ><*
                                                  Pt:  Pretest (mm Hg):  —
                     Post-Test (mm Hg):  —	
                 Tt:  Pretest fF): —-~"	
                     Post-Test fF): -^	
                 Time: Start^225iFinish:^^OTotal:_^Q_
                 W/B:  —D/B:  —O2:  	CO


                 Md - (0.44 x %CO2> -I- (0.32 X %Q$ -t- (0.28 X %h^)

                 Md«(0.44xc?  )+(0.32X'J(  ) + (0.28x~~? J )
                                                            %H,O      %H,O
                                                  M*-Mdx(1 - - —) + 18 ( - L_
                                                             100        100
                                                                  100
                                                                             100
                                                  Mi.
                 Pt -
.-»
 13.8

. 3 *)  in.
13.8
                                                                Hg
                                                 Vs - 85.49 x Cp X
                                                 V« - 65.49 x (
                                                                      Pax Mi
                                                 A.-   t-97
                                                  Qt-V«xA«xflO«/m
                                                               x  i, -yi    xeo

                                                               •dm  Qaxl7.647x	x(1-
                                                                 T.       100
                                                                                    \.-2)
                                                                                    100  ,
                                                               dM*n
-------
Plant	
Sampling Location
Run Number:  ^"V/ *£.  Date:
Pretest Leak Rate: .pot  cfm i
Pretest Leak Check: Pitot:
                             FIELD DA I A SHEET
                                     }'*1    Operator:
Sample Type:
Pbar
CO2:
                                       Ps:
                                       O2:
                                                          Thermocouple
                                                          Filter #:  -^
               in. Hg.
        Orsat:
Probe Length/Type: /
Stack Diameter:  /3 v
                           Pitot #:
                       As:  1.
Nozzle ID:  ---
Assumed Bws:
Meter Box   ___
Post-Test Leak Rate: .poo  cfm @ J^ in. Hg.
Post-Test Leak Check: Pitot:	Orsat:
Traverse
Point
Number



























Sampling
(mln)
£
20
30
•30
I/O






















OockTime
(24-hour
dock)
fttec
£1 V0
0(50
22,00
0.9//D






















Gas Meter
Reading
(Vm)lt3
/<93,<93/
PO / '£o
96)^ / /O
%S? I 9 . £>
g 0*r/ u?S^






















Velocity
Head (Ap)
inH2O
Orif ce Pressure Ditterential
(AH) in H2O
Desired
Actual
Stack
Temp.
(Ts)
;• Temperature
y. op
Probe
Filter
Impinger
Temp.
°F
Dry Gas Meter Temp.
Inlet
(Tm in°F)
y///////////////////////////y/////////////////////,


























/'?£>
i f*&>
\ , %fa
1 < ?&






























































































































^f
^"V
j^
<^»O






















9^-'
£6
Q^
Q**-*
^






















1 Outlet
(Tm out°F)
'//////
9v
^S
9r;























AVm
         AH=
                                                       Tm=
                                                                                      :  •
-------
                  SAMPLE RECOVERY DATA
Plant:.

Date:_
                                            Run No.:
                     Sample Box No.: N-(
                                            Job No.:   6405 .
Sample Location:.

Sample Typp- EPA> Kg-ruoo   4

Sample Recovery Person:

Comments:	~~
                                            Filter No.:
FRONT HALF
Acetone
Container No •
                          Liquid
                          Level Marked:.
Filter
Container No.:
                                             Sealed:
                                             Sealed:
Description of Rlter:
Samples Stored and Locked:

BACK HALF/MOISTURE
Container No.:.
Liquid Level Marked:.
                                             Sealed:
IMP. NO.
1
2
3
4
5
6
CONTENTS
DX HT.O
DX HLO
Grv^^
^ICI^A. £*&—


TOTAL
INITIAL
VOL (ml)
/oo
/ot>
—
^50



WEIGHT (arams)
INITIAL
Ufl.1
bO&.O
496,2.
84o,?


•2&Tr
FINAL
bU.1>
^oe.l,
Wt.7
%
-------
        EPA METHOD 4 MOISTURE CALCULATIONS
PLANT:   L^^	SOURCE/RUN #:±±JL PATE:
1. Leakage Correction for Volume Metered
    Vmc=(       )-{       -0.02) x(       )
    Vmc=	ft3
2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)
                          'p^+tAH/iaef
    V_   = 17.64xV__xYxl —	
      mstd          mc    V      Tm
                                   )x
       51U

    Vmstd =	^-2—dscf
 3. Volume Water Vapor Collected, Standard Conditions
    Impingers & Silica Gel = V    = 0.04707 x (W. - W.)
                           std            *    '
                        Vw  = 0.04707 X(  -?.'J

                         wstd
 4. Percent Moisture, by Volume
     P	wstd	
     DWS-    y    ~^~T/
               wstd   mstd
     Bws =
-------
/I --
i
si
           PlantL
           Date:
              5(10
                    METHOD 18 FIELD DATA SHEET
                   	    Tested Analyte:.
           Location:_
           Run #: /O
           Stack I.D.:	
           Pbar: A?'9d
                   /
    Sample Tuba *• /£ -H/t   to -f -
    Operators:
    Leak Check: Pre: rg0o  Post:
         Time
             i<
         36
         2c
                      ±
             Gauge
            Vacuum
              (Hg)
                             0
                       O
                             O
                      O
                             Q

                                      Row
                                     Q0ttinr,
                                     Setting
Tr«v«re«
 Point
Numtar
V«tocity
 H
In.
                   ^J.

                 T
Stack
Tamp.
 °F
                            .••^•"i*
                            .•vl-^rr
                                   Orifice Tank #:   —	
                                   Pump/Rotometer #:	
                                   Pt:  Pretest (mm Hg)f_I
                                        Post-Test (mm Hg)-,.
                                   Tt:  Pretest CF):.
                                                      Post-Test fF):_
                                                  Time: Stan^ge* Finish::?/^Total:  ^.A
                                                  W/B:"—  D/B:  —Q:
                        Md - (0.44 x %CO2> -I- (0.32 X %O2> + (0.28 X %^)


                        .Md-(0.44xO  )-t-(0.32x  ii ) +(0.28X •)•)

                        f6>
                        Md-   0^   •:•;
                                                  M»-Mdx(l
                                              tH2O

                                              lob~!
                                                                 100
                                                 • )
                                                           100
                                                                      100
                                                                °R (°F t-480)
13.8
                13.8
                                           P. .
                                           Vt - 05.48 x Cp X
                                           V.-85.48x(
                                                                PaxMt
                                                                              • ar.
                                             « V«xA«xeOi/m
                                               - Q« xl 7.647 x
                                                              X17.647X
                                                                        x(1
                                                                             100
-------
                                              FIELD DA I A SHEET
Plant	
Sampling Location
Run Number:
Pretest Leak Rate: .002.
Date:
 cfm
                                         Sample Type:
                                         Pbar:
                                         CO2:
                                                         V   Operator:
                                                             Nozzle ID:
                               Thermocouple
                                                         Pa:
                                                         O2:
                                in. Hg.
Pretest Leak Check: Pilot: "V  Orsat:
                                         Probe Lengthflype:
                                         Stack Diameter:  /<
Pilot #:
                                       AH@:
                                           As:
Assumed Bws: —  Filter #:
Meter Box #:  )fy   Y: ,?&£
Post-Test Leak Rate:  Exso cfm @ /£ in. Hg.
Post-Test Leak Check: Pilot:  v^Orsat: —"~
TrawwM
Pbht
NunuM



























Samp**
Time
(mln)
©
/o
£t)
3®
lO






















Clock Time
(24-hour
dock)
P£>C^
50 /£>
5?o 9^»
•j>63^
9&'i&






















Gas Meter
Reatfing
(Vm) t|3
/^* $ ' c^C>O
/^ ^ / **£
1 77 / yo
; ^$ / J iT
/ 3 3 . /^c-






















V«locrty
Head(Ap)
lnH2O
Orif ce Presfture Drtterential
(AH) in H2O
Desired
Actual
Stack
Temp.
(7s)
Temperature
°F
Probe | Filter
Impinger
Temp.
°F
Dry Gas Meter Temp.
Inlet
(Tm in°F)
CXjDet
(Tm out°F)
Pump
Vacuum
(in. Hg)
Y/////y///////////w


























jf $£
l> %&
1 < c^ t
/ , ?^»


























































	 —


































































&CJ
5v~
£Q
6*7






















0^
£r V
2'D
&*?






















«^s-
f6
-------
Plant:.

Date:
•L
SAMPLE RECOVERY DATA

                   	  Run No.:

                   -£    Job No.:
                     Sample Box No.:
Sample Location- /O

Sample Type:
                                            Filter No.:
Sample Recovery Person:

Comments:
FRONT HALF
Acetone
Container No. •_
                          Liquid
                          Level Marked:.
Filter
Container No.:.
                                     Sealed:
                                             Sealed:
Description of Filter:
Samples Stored and Locked:

BACK HALF/MOISTURE
Container No.:	
Liquid Level Marked:
                                             Sealed:

IMP. NO.
1
2
3
4
5
6
CONTENTS
b* fcv
§) "£ ti-^0
£~<~pfy^~
5ft<~W


TOTAL
INITIAL
VOL (ml)
foo
L/^
0
1*0



WEIGHT fqrams)
INITIAL
^7.7
bbn
-------
        EPA METHOD 4 MOISTURE CALCULATIONS
         /
PLANT: — — fr<^o  V-'WjJr   gni IPPF;PI IM #• to-i/-/  DATE:  VrS/9"?


1 . Leakage Correction for Volume Metered



    vmc = V (Lp - La) x e
    vmc=(       )-(        -0.02) x(
    V   =
    vmc
2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)
                                       /('
       'std



    Vmstd
 3. Volume Water Vapor Collected, Standard Conditions


     Impingers & Silica Gel = V ...   = 0.04707 x (W. - W. )
                          w                T   '
                            std
                         Vw   = 0.04707 x(
                           std
                         Vw   =^_!±L_scf
                          wstd
 4. Percent Moisture, by Volume

                 V,
     R             wstd

      ws      V,..  4.  V
                       mstd
     Bws
     BWS—
-------
                 GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:	
Sampling Location:  OV&/V &• /O
Run #:
                                      Date:   5
                                      Clock Time:  3 (

Barometric Pressure, in. Hq:  9$<30	 Static Pressure, in. h^O:	'_
Moisture, %:    	      Molecular wt., Dry;	•      Pitot Tube, Cp:   •??
Stack Dimension, in. Diameter or Side 1:    )5*	Side 2:	
Wet Bulb, °R.
     Point
    Nurnbar
      9*
      3
  ft-  /
       G
Velocity
 LJ^.-i
 nMH
in. H2O
Stack
T«mp.
               Dry Bulb, °F:

                       Md-
               r/0
                  93
                          P3I
           32 °>
            931
            Md-(0.44x

            Md-
)-t.(0.32xOl
                                  % H,0     % HO
                        M« . Md x (1 -  	—) * 18 ( —-i- )
                                   100       100
                                       Mi-
                                                           °R(°F*4ao)
                                              13.B
                                       p,.
                                                  ^
                                                              13-8
                                    m. Hg
             Vi • 65.40 X Cp X 1EJP x
                                       v«-as.48x(
                                 P9XM9
                                        A.- ,.-2.1    ft2

                                        Q»m V«xA«x60i/m
                                        Qt» Z^"? "1   ac*m

                                        O* .,-QiX 17.647X	
                                                              100
-------
  3 OC3 CZ3
                          METHOD 18 FIELD DATA SHEET
     O
 aic S £<
/n
Plant: Ls s< -^ TesteH Analyte: xA,r^^
Date: 5 /"i •:/?-? Orific« Tank *• u*rr **.?
Location: A/Oj - A
Run afc- A/D4 ~ H ~t

PI imp/HrtfomsTer #: -"

Pt- Prfltflst (mm Hq):
Stack I.D.: 32' x (2 &" Post-Test (mm Hq): —
Pbar: Zt> — •
Leak Check: Pre: S Post: ^ W/B: — D/R 	 (X,:2 i CO0: k


Gauge
Time Vacuum
(Hg)
i^fi'.^^. ' i
/¥o/.^ /
/#/£ •*.»-, / "
/¥^.^ :'V
1^0=1^3 /
1MU.O-? \
mi 2. <»* i

Trav«rB«
Point
Number

























V.tecrty
HMd
In.H^O

























Flow
Setting
^\
, M'
-z-/
7-1
*\
^\
-i^

Stack
T«mp.
°F

























Md - (0.44 x -SCXy + (0.32 X %02) + (0.28 X %(^)
^^ Md-(0.44x )+<0.32x )*(0.28X )
:^
Md«
£7
% H_0 % HO
^ M.-Mdx(1--^-)* "(-Eg-)
'^ M« • < )x(1- 	 ) + <8( 	 )
fl" l ' * 100 100
4l
fa- Ma-
 ft

Qa«V«xAsx60«/m

Qa» x xM

Qt» acftn
P. %K,0
Qi.a-QiKtr^Tx— -xd- -^-)


Qi^- X17.847X 'X(1- 10JJ J

OHM- <
-------

p
D
U
R
S
P
S
C
L

d\1» o
Z/W '«•
Ltfo *
Aaoa 58
2,2. (o-K
•l^ "36.30
* (to
,
METHOD 18 FIELD DATA SHEET
lant: i-A-^o TesteH AnaiytR- ^^y^.
ate: -r-x^-ri Orific« Tank *• ~
acation: /w ft & Pump/Pntnmpter #: yo-W-
un #: M n&- -4-2. Pt: Pretest (mm Hq): " _,.
tack I. D.: £>.$"•< ?2." Post-Test (mm Hq);
bar: -2^2- rt- Protect <°R-
ample Tube
(perators:
eak Check: F
#• AW-V-24 NDB-4-'2R Po«ft-T«fit CF):
55 ' Time: Start:? ijp Finish:^"o Total: 5t>
re: ^^ Post: -" W/B: — D/B: - 00: ^' C00:_o —

Gauge
Time Vacuum
(Hg)
iH'S.Tf ;
l¥*'k.^ (
/^fl-1,/8 I
'1-3-P-3"? I
^31,31 l
• l C* O- • • i ^
| Ll <^5l C ~7 i
Flow
Setting
27

2-(
dl
-ai
•31
*\

Travaraa
Point
Numbar

























Velocity
Head
In. H^O

























Stack
Tamp.

























Md - (0.44 x %COZ) 4- (0.32 X %02> +• (0.28 x X^)
f
lr*_ Md « (0 44 X ) +• (0,32 X ) +• (0.28 X )
_ Md-
^ % H20 % H20
*"' 'X( " 100 100
lie iia
Pt « In. Hg
fi? -
I y X)R>
_—^ , j is r n)
va - as.48 x up x iw x ^ p8 x Ma
Va - 85.49 x ( ) x ( ) x A/ 	 	
Va- ft/t
A.. ft2


Qe » VaxAaxOOa/m

Qt» x X00

Q»m adm
Pa *H_O
aid" T« K 100


•to iw

Otgm~ dacftn
-------
          APPENDIX A. 1.6

             Condition 5
(includes flows, moistures, and Method 18)
-------
   OS
                                 METHOD 18 FIELD DATA SHEET
k>
          Plant:
          Date:  
          Pbar:
Sample Tube
Operators:  -
                                         /A
          Leak Check: Pre:  ./   Post:
Travaraa
Q— !_•
"Olni
Number
i
Z.
T,
-/
5
6,
*7
<<-

/
i
?>
V
<5
0
7
?








Valecity
Head
In. H^O
23
26
2.7
26,
• z*
-32
»36
.iff

.26
.30
-29
27.
Zto
.ZO
.2*7
•2. -?7



Gauge
Vacuum
(Hg)
/
/
/
/



Flow
Setting
/ 50 /,-
y £O £•!-
,40 t'-'
,4£>u



T»
-a-
•rt
16
iS
Time: Start:o?c-5 Finish: a ^>^> Total:
W/B: 70  D/B: f 7  O2: ^y CO2:


Md - (0.44 x %CO2> •!• (0.32 X %O2) -I- (0.28 X %Nj)


Md - (0.44 x  O  ) + (0.32 x z/ )  + (0.28 x 7<

Md.  ZC.W

           %HO      %H O
M« - Mdxd  - - — ) + 18 ( - — )
            100        100
                                        Ma « (
                                                            ) x (1 - - ) + 18 ( - )
                                                                  100        100
 T.- -87  °F- 5Y7
                                                                   480,
                                                         13.6
                                                                         13.8
                                        Vs - 65.48 x Cp x



                                        Vs - 65.48 x (


                                        Vs.  3£. *f


                                        A.-  >,G~»    ft
                                                                   W
                                                                  ) X (
                                                                       Ps x Ms
                          )x
I-
                                                               ft/a

                                                                2
                                                  Qs-VixA*xeoa/m
                                                  Qi-
                                                                ~
                                                                 !•
                                                              X17.647X'
                                                               xeo


                                                              %H2o
                                                               100
                                                                                     100
                                                                                             A, I)
-------
;aa c
       Plant:
       Site:
WET-BULB/DRY-BULB MOISTURE CALCULATION
   	Location:  /*}&;« Ft^n-
            Operators: .r»/,^   RUn #:
       Barometric Pressure, in. Hg =
       Static Pressure, in. H2O =
       Absolute Pressure of Stack =  Pbar
       Wet-Bulb Temperature, °F =
       Dry-Bulb Temperature, °F =
       Temperature Difference, Td - Tw =
       Saturation Vapor Pressure of H2O at Tw (from Table) =  Pvw =
                                          (Ps - Pvw) x
       Vapor0"""-1	•"-* ^ - "--   '"---•-
       Pva =
ne-s-i Date: 5-/?-.%?4 }
.3 x Tw)
7 ) &5fr2«
)

£?. o "7-. f> <*

' in. Ha


. ^*o%
                              VAPOR PRESSURES OF WATER
Tamp.
OF
0
10
20
30
40
50
60
70
80
90
100
110
120
130
140
150
160
170
160
190
200
210
220
230
240

0
0.0376
0.0631
0.1025
0.1647
0.2478
0.3626
0.5218
0.7392
1.032
1.422
1.932
2.596
3.446
4.525
5.881
7.569
9.652
1250
1559
19.01
23.47
28.79
35.00
4241
5044-

1
0.0398
0.0660
0.1080
0.1716
0.2576
0.3764
0.5407
0.7648
1.066
1.467
1.992
2.672
3.543
4.647
6.034
7.759
9.885
12.48
15.83
19.42
23.96
2943
35.68
43.11
51.78

2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.842
4.772
6.190
7.952
10.12
12.77
15.98
19.84
24.48
29.92
36.37
43.92
52.70

3
0.0441
0.0728
0.1186
0.1878
0.2782
0.4052
0.5802
0.6183
1.138
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.36
13.07
16.34
2057
24.97
30.52
37.07
44.74
5345

4
0.0463
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
6.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.87
54.82

5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.680
8.557
10.86
13.67
17.07
21.14
26.00
31.75
38.50
4041
5540

6
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.650
8.767
11.12
13.98
17.44
21.59
26.53
3248
3954
4757
5640
/
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.370
3.169
4.174
5.442
7.024
8.981
11.38
14.30
17.82
22.05
27.07
33.02
3949
48.14
5741
•*V " I
8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4058
0.6903
0.9666
1.335
1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.82
1841
22.52
27.82
3347
40.75
4943


9
0.0598
0.0982
0.1567
0.2383
0.3403
0.5035
0.7144
0.9989
1.378
1.679
2.521
3.351
4.408
5.732
7.384
9.424
11.92
14.98
1841
2249
28.18
3443
4142
4943
5947
-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant- Lflsto Date: s-/9-9~?
Sampling Loc
Run #: />te -
ation: /fy «,;•/, £f\\**t!- Clock Time: ///
V
5
0
•7
£





•

-

a:z# ^ Static Pressure, in. HUO: -'°3
MnlPr.ilar\wt nrv-2^/ PitOt Tube. CD: -^
iion, in. Diameter or Side
-72. DrvB

Vstocity
Head
in. H2O . ,
,22
,25
,2.5
l£
,3O
,33
i35
.3^

.26*
, 3i5
' 2-^
.Zff
.^6?
'2"?
.21
/2^








SUck
T«mp.
°F
fo
:7^
^
90
10
70
Jo
90

to
90
9o
?o
^?
^^
9*
yo








$F - >^i tr«- ^^c?
1- /7^S Side 2:
Mih.op- TO
Md - (0.4A x ) * (0.32 X ) + (0.28 X )
Md- ?"/
% HO % HO
MS- MO XII 100 100
13.0 13.0
p* . 0^. "ti^ In. Hg
£p -.??«..
-= / Ts(°R)
V.-«5.48XCPX^P X ^ P9XM9
1
Vs - 85.48 x ( ) x ( ) x A<
v.. 3C-55 m

A 1 »2
A-" '-6~7
Qt — Vs x A* X 00 i/m

Qs» X xOO
Os • 3G(p S Acfcn
p. %H,0
Qi .,-Q* XI 7.847 x 	 x(1 	 ^-)
•» Ti 100

•to 1w-
-------
WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: i-^co Location: w*;* FWi,^y-
Site: /1/lfM EAtoud- Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of Stack = Pbar + -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of HpO at Tw
Vaoor Pressure of H-.O = Pva =''(Pwi\ •
rn/jt Runs*: ne-s-z. Date: .•/-/•
Pbar = ^"? . Vf
Pg = -^03
Pg p<5= s V- So
IJ.b
Tw = -T3
Td= 10
AT= 11
(frnpn T^hl») = P^W = ^ ' ^ ___
(Ps - Pvw) x (A"0
f'rfl
in. Hg
'. in. KLO
2
in. Hg
°F
°F
°F
in. Hg

                                    2800 - (1.3 x Tw)
Pva=(
                                                          ~ G
                        2800 - (1.3 x



Proportion of Water Vapor by Volume = Bws
(Ps)
T«mp.
OF
0
10
20
30
40
50
60
70
80
90
100
110
120
130
140
150
160
170
180
190
200
210
220
230
240

0
0.0378
0.0831
0.1025
0.1847
0.2478
0.3828
0.5218
0.7392
1.032
1.422
1.932
2.598
3.446
4.525
5.881
7.589
9.652
1250
1559
19.01
23.47
28.75
35.00
42.31
50.84-

1
0.0398
0.0680
0.1080
0.1718
0.2578
0.3764
0.5407
0.7648
1.066
1.467
1.992
2.672
3.543
4.647
6.034
7.759
9.665
12.48
15.63
19.42
23.96
29.33
35.68
43.11
51.78
in. Hg
( )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0698
0.1127
0.1803
0.2877
0.3906
.OJSgpi
lOJSMT)
1.102
1.513
2.052
2.749
3.642
4.772
8.190
7.952
10.12
12.77
15.96
19.84
24.46
29.92
36.37
43.92
52.70
3
0.0441
0.0728
0.1188
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.829
3.744
4.900
8.350
8.150
10.38
13.07
16.34
20.27
24.97
30.52
37.07
44.74
53.65
4
0.0463
C.0768
0.1248
0.1955
3.2891
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
9.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.67
54.62
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.8222
0.6750
1.213
1.660
2.243
2.995
3.954
5.165
6.660
8.557
10.66
13.67
17.07
21.14
26.00
31.75
38.90
4641
55.60
a
0.0517
0.0846
0.1370
0.2118
0.3120
_ 0.4520
' 0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.650
8.767
11.12
13.98
17.44
21.59
26.53
32.38
3924
4757
56.60
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4688
0.8669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
6.981
11.38
14.30
17.82
22.05
27.07
33.02
3949
48.14
57.01
a
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.619
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1851
22.52
27.62
33.67
40.75
49.03
5843
9
0.0598
0.0982
0.1567
0.2383
0.3493
0.5035
0.7144
0.9969
1.378
1.878
2.521
3.351
4.406
5.732
7.364
9.424
11.92
1446
1841
2249
28.18
3443
4142
4848
5947
-------
3 at
                  GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: UftStO Date: >-/?-?-;
Sampling Location: M»7rt (^IV,^A Clock Time: /35"~7
Run #: 








|ft- ^2--
1: i 7. -5" Side 2: —
it Jib OF- ?2
Md - (0.44x%CO2) + (0.32X%02) f (0.28 X%Nj)
Md - (0.44 x ) •)• (0.32 X ) •)• (0.28 X )
Md- 2-f.<9
% H.O % HO
J,.Md*(1 -j^-) ' 1fl< )OQ )
M.., )x(,.__->*18(_j^.)
M.. w.ii
T:. <^2. °F- 5^2^ °n (°p*4«o)
e p
r' ° 13.8 ' ' 13.8
?•- 2-^^^ In-Ha
^SP - ^ ^^>
— / Ts fto)
V.-U5.4WXLPX JAH X \l P9XM8



A.. /.^^ n2


Q»- x xOO
Q« » "?">/> / «c*n
^7^/
Pt *H>°
Q.ttd.Q.X17.647x — «<1.-j^->


-------

           WET-BULB/DRY-BULB MOISTURE CALCUU\TION
Plant:
Site:   /|fU,fl
Operators:  7
                                        Location:  AO^..^ £->hc,^ /-
                                        Run #:
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack =   Pbar i  ,. _
                                  I J.U
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw (from Table) =   Pvw =—Q.
                                   (Ps - Pvw) x (AT)
A»e - 5- 3 Date:
Pbar = "2^,^*
Pq = -t- . o 1^
Ps = 'Zt. &$
Tw = 7o-V )
)
&oZ.<°$}
VAPOR PRESSURES OF WATER ^/Z.Z- ^ n
In Inches of Mercury 2. 7o^
2
0.0417
0.0090
0.1127
0.1803
0.2077
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
8.190
7.952
10.12
12.77
15.98
19.84
24.46
29.92
36.37
43.02
52.70
3
0.0441
0.0728
0.1186
0.1878
0.2702
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.38
13.07
18.34
2027
2447
30.82
37.07
44.74
8348
4
0.0463
0.0708
0.1248
0.1955
0.2891
0.4203
0.0009
0.8462
1.175
1.010
2.178
2.911
3.848
5.031
0.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.87
54.62
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.0222
0.8750
1.213
1.000
2.243
2.995
3.954
5.165
8.680
8.557
10.86
13.67
17.07
21.14
26.00
31.75
38.50
4841
5540
e
0.0517
0.0848
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
0.850
8.787
11.12
13.98
17.44
21.59
26.83
3248
3924
4727
56.60
7
0.0541
0.0092
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.981
11.38
14.30
17.82
22.05
27.07
3342
3949
48.14
5741
a
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1821
2242
27.82
3347
40.73
4043
5843
I7Y?

9
0.0598
0.0982
0.1567
0.2383
0.3493
0.5035
0.7144
0.0080
1.378
1.878
2.521
3.381
4.408
5.732
7.384
9.424
11.02
14.08
1841
2240
28.18
3443
4142
4043
8947
-------
                        METHOD 18 FIELD DATA SHEET
e'C
*'

3lant: L-fe<-O Tactqd Analvte: S^/^a
jate: ^-/v-«n nrifjra Tank #:
.ocation: — S^^^h^t Pumr/Rotometer #: i^sT *" /
Sun #: Re - ~ - I p». Pr-ntest (mm Ha^:
stack I.D.: 2.8v 2zv - PmMest (mm Hcrt: -
JDar: ..z*.fS Tt. Pretest<°R:
sample Tube
Operators:
#:A£^-i+(Rt-<-/K Post-Test t°F):
r/* Time- Start:<*°-/ Rnish: <*>*i Total: 4^
Leak Uheck: Pre: ,/ Post- ^


Gauge
Time Vacuum
(H9)
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QN«- &££>««* V4L!o> A ,
-------
           WET-BULB/DRY-BULB MOISTURE CALCUU\T!ON
Plant: Lfc0 Op
^^ OP
19 °F
'73^? in. Hg

                                   2800-(1.3xTw)
 Pva=(
                       2800-(1.3 x

 Proportion of Water Vapor by Volume = Bws

 Bws=
T«nnp.
 "F
 o
 10
 20
 30
 40
 50
 60
 70
 80
 90
 100
 110
 120
 130
 140
 150
 160
 170
 180
 190
 200
 210
 220
 230
 240
(Ps)
0
0.0376
0.0631
0.1025
0.1647
0.2478
0.3626
0.5218
QgH?
1.032
1.422
1.932
2.596
3.446
4.525
5.881
7.569
9.652
1240
1549
19.01
23.47
28.78
35.00
4241
5044-
1
0.0398
0.0660
0.1060
0.1716
0.2576
0.3764
0.5407
0.7648
1.066
1.467
1.992
2.672
3.543
4.647
6.034
7.759
9.888
12.48
15.63
19.42
2348
2943
38.88
43.11
51.78
in. Hg
( )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
15.98
19.84
24.40
29.92
36.37
43.92
52.70
3
0.0441
0.0728
0.1186
0.1878
0.2782
0.4052
0.5602
0.6183
1.138
1.561
2.114
2.629
3.744
4.300
6.350
8.150
10.36
13.07
16.34
20.27
24.97
30.82
37.07
44.74
53.88
4
0.0463
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
6.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.76
45.87
54.62
5
0.0469
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.660
8.557
10.86
13.67
17.07
21.14
28.00
31.78
38.80
4841
5840
6
0.0517
0.0646
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.850
8.767
11.12
13.96
17.44
21.59
26.53
3248
3944
4747
56.60
7
0.0541
0.0692
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.961
11.38
14.30
17.82
22.05
27.07
33.02
3949
48.14
5741
8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.619
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1841
2242
27.82
33.87
40.78
4943
5843
9
' 0.0598
0.0962
0.1567
0.2383
0.3493
0.5035
0.7144
0.9989
1.378
1478
2.821
3.351
4.408
5.732
7.384
9.424
1142
14.98
1841
2249
28.18
3449
4142
4943
8847
-------
3 aq_ cza
                   GAS VELOCITY AND VOLUMETRIC FLOW RATE
=lant: } fao Date: ^' /v?~^7
Sampling Loc
Run #: /^
ation: a,™ £•*/,.. ^*- Clock Time: ;/vz
-5-2. Qoerators: -fr/jj
Barometric Pressure, in. H
Moisture, %: 1- • 3
Stack Dimens
Wet Bulb, °F
Point
Numb«r
1
I
i
M
.5
6
,
x
•»
4
5
c.
f
z.
3
*f
5
6
i
2.
•,
f
5 '
0


q- 2^ , O Static Pressure, in. hUO: ". 6 2,
Molecular wt..Drv: ?e.fV Pitot Tube. Cp: ion, in. Diameter or Side
"I/ DrvB

V«loctty
in. H2O
• £>5
i ^-S
,oS
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,06
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.66
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 •*• (0.28 X%Nj)
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M«-( )x • V« x A> x 00 t/m

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Q. . IfW^ adm
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                                                                          IA
-------
WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: l_te%
( rub >
VAPOR PRESSURES OF WATER ^_£jL_^ ^
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
8.190
7.952
10.12
12.77
15.98
19.84
24.46
29.92
36.37
43.92
52.70
3
0.0441
0.0728
0.1186
0.1878
0.2782
0.4052
0.5602
0.8183
1.138
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.36
13.07
16.34
2057
24.97
30.52
37.07
44.74
53.65
4
0.0463
3.0768
3.1248
0.1955
3.2891
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3,348
,5,031
?.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.87
54.62
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.6750
1.213
1.660
2543
2.995
3.954
5.165
6.660
8.557
10.86
13.67
17.07
21.14
26.00
31.75
38.50
46.41
55.60
6
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.850
8.767
11.12
13.98
17.44
21.59
26.53
32.36
3954
47.27
56.60
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
6.981
11.38
14.30
1742
22.05
27.07
3342
3949
48.14
5741
27^7""
a
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.619
2.448
3.259
4.289
5.565
7.202
9.200
11.65
14.62
1841
2242
27.62
33.07
40.75
4943
5843
9
0.0598
0.0982
0.1567
0.2383
0.3493
0.5035
0.7144
0.9989
1.378
1.675
2.521
3.351
4.406
5.732
7.384
9.424
11.92
14.98
1841
2249
28.18
3443
4142
4943
5947
-------
             GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:
Date:  5-/y-»7
Sampling Loc
Run #: fi£ -
atiorv &»-„, £*/v ^ Clock Time: 14 to
* - ~\ Oner?nors: r*/xx
Barometric Pressure, in. H
Moisture, %: 2 - 0-
Stack Dimens
Wet Bulb, °F:
TravarM
Point
Number
/
I
2>
^
5
L.
i
1
^
<,
5
(j
,
^
3

q
?•
L
—

9- 7 /<-.,- Stati^ Pressure, in. HUO: '.61
Molecular wt.. Drv: zT.^v 	 Pitot Tube, Cp: _<_2f 	
ion, in. Diameter or Side
1\ DrvB

Valocny
in. H2O
,0?
,^•1
.00
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Md- CH
%H.O %H O
'"" """" "* " 100 '00
Ma — ~)-o''~"i(j:
Q O O ^
TM • cx £^ P * S if C H ' r ^ **oO|
Pa - Pb * S'P' = < ) * 	 — —
13.8 13.8
Pa- Ti'j'-Oy In. Hg
^P» ^OC.^J
-;; / Ts"PR)
Va - 65.48 x Cp x VAP x W "pg"x Ma
, J

Va - \3> - 7 I «/•

A* • i i(f 1 "
Qs • Va x Aa x 00 a/m

a.. x xeo
Q,. ^01°] adm
p. "^o,
Qs ..* Qa x 17.847 x — x (1 • — — - )
Qt^- X17.647X 	 X(1'~^J"*
                                                                      i.u
-------
WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: '<.&<>£.&
Site: j^o-x E*Ua4 Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of Stack = Pbar 3 -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw
Vapor Pressure of H^O = Pva = (Pvw) •
Pvn=( ).
Location: fe^ £,h<...^L :-.-
£5 Run if. fy?- *- "S
Pbar =
Pg =
-£2_ Ps =
1 J.O
Tw =
Td =
AT =
(from Table) = Pvw =
(Ps r.vpwv) x (AT)
2BOO-(l.3xTw)
)x( )
Date: s -/    =      (
       (Ps)
                     )
( )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
o.oeoa
0.1127
0.1803
0.2877
0.3008
0.5601
0.7812
1.102
1.513
2452
2.748
3442
4.772
8.160
7.852
10.12
12.77
1848
1844
2446
2842
3847
4842
52JO
3
0.0441
0.0778
0.1188
0.1878
0.2782
0.4082
0.3802
0.6163
1.136
1.561
2.114
2.828
3.744
4.800
8450
8.160
1048
1347
1644
2047
2447
3042
3747
44.74
9348
4
3.0483
0.0788
0.1248
3.18S5
0.2881
0.4203
0.8008
0.8482
1.175
1.810
2.178
2411
3446
5.031
8.513
8451
1041
1347
16.70
2070
2548
31.18
3778
4847
5442
5
0.0460
0.081 0
3.1302
0.2035
04004
0.4358
0.6222
04750
1.213
1.860
2-243
2.988
3454
9.165
6.660
8457
1046
1347
1747
21.14
2840
31.78
3840
4841
5840
a
0.0517
3.0846
0.1370
0.2118
0.3120
0.4820
0.6442
0.8046
1.253
1.712
2410
3461
4463
5402
6490
8.767
11.12
1348
1744
2148
2849
3248'. •
3844
4747
5840
7
0.0541
0.0882
0.1428
0.2203
0.3240
0.4688
0.6688
0.8352
1.283
1.785
2478
3.168
4.174
9.442
7.024
6481
11.38
1440
1742
2248
2747
3342
3848
48.14
5741
a
0.0371
3.0832
0.1302
0.2282
0.3364
0.4888
0.8803
0.8686
1.335
1.818
2.440
3258
4.288
5.585
7202
0400
11.65
1442
1641
2242
2742
3347-
4078
^ffftf
9848--
0
0.0586
0.0882
0.1567
02383
04483
04938
0.7144
04888
1478
1478
2421
3481
4408
9.732
7484
8484
1142
1448
1841
2248
2848
3448
4148
4848
8847
-------
^ag cza
                    GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: M5^> Date: 5 -/•/-?-!
Sampling Loc
Run #: f\ F
ation: ,W\Wv/ ^/> Clock Time: /wztf
- *T- 1 ' Operators- 7"#/£5
Barometric Pressure, in. H
Moisture, %: ^ /
Stack Dimenj
Wet Bulb, °F
TrivarM
p— i— *
rOlfn
Number
/
2-
.3
y
£
6
7
r

/
7.
3
y
5
£
*7
ar





•



a: ^.^S Static Pressure, in. HUO: - -~l "7
Molecular wt.. Drv: SLfe.<^ PltOt Tube, Cp:^/:i 	
sion, in. Diameter or Side
/O DrvE

V.tewty
H«U
in. H20
.^>O
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pn . Pb t ?-P>. - ( ) •"• — : 	
13.8 '3.8
P.. T.B.7-7 IO.HQ
^' ^.^
-------
Plant: L$uo
Site: K
flfni'kcj fu^v
Operators: />/•
            WET-BULB/DRY-BULB MOISTURE CALCULATION
                                         Location:
                                  	Run #:
 Barometric Pressure, in. Hg =
 Static Pressure, in. H20 =
 Absolute Pressure of StacK =  Pbar
 Wet-Bulb Temperature, °F =
 Dry-Bulb Temperature, °F =
 Temperature Difference, Td - Tw =
 Saturation Vapor Pressure of H2O at Tw (from Table) =   Pvw =

 Vapor Pressure of^O = Pva = (Pvw)     (PS ' FVW) X ^
-r_P2_
-  13.6
"1- #i^x . 'I <"•••«/ rh «
AF-S-I
Pbar =
Pg =
Ps =
Tw =
Td =
/
Date: •:-/•
2-£t>$T
-.77
28,77
-70
$1
->
in. Hg
in. H00
2
in. Hg
_°F
°F
AT= tl °F
Pvw =
0.7 &1-
_ in. Hg
 Pva=(
)-
     2800-(1-3xTw)

        (   '3     )
                         2800-(1.3 x
                                         in. Hg
 Proportion of Water Vapor by Volume = Bws
                          (
Ttmp.
 op
 0
 10
 zo
 30
 40
 50
 00
 70
 80
 80
 100
 110
 120
 130
 140
 150
 160
 170
 180
 180
 200
 210
 220
 290
 240
(Ps)
0
0.0376
0.0831
0.1025
0.1847
04478
0.3826
0.5218
0.7382
1.032
1.422
1.832
2.586
3.446
4.825
5481
7.569
8.682
1240
1549
1941
2347
28.78
3540
4241
5044
1
0.0388
0.0660
0.1080
0.1716
04576
0.3764
0.5407
0.7648
1.066
1.467
1.802
2.672
3449
4.647
6.034
7.759
8.888
1248
1843
1942
2349
2949
3848
49.11
51.78
                      &.Q2-I
( Z8. 7? )
VAPOR PRESSURES OF WATER ^£££ ^ £>.
In Inches of Mercury Z- 7° ?
2
3.0417
0.0888
0.1127
0.1803
0.2677
0.3808
0.5601
0.7812
1.102
1.513
2452
2.748
3.642
4.772
6.190
7.952
10.12
12.77
1548
1944
2446
2942
3947
4942
5&70
3
0.0441
0.0728
0.11B6
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.829
3.744
4.800
6.350
6.160
1046
13.07
1644
2047
2447
3042
3747
44.74
5348
4
. 3.0463
3.0768
3. 1248
3.1955
0.2681
0.4203
0.6008
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
0.513
8.351
10.61
1347
16.70
20.70
2948
31.13
37.78
4847
5442
5
0.0488
0.0810
3.1302
0.2035
0.3004
0.4358
0.6222
0.8750
1.213
1.660
2443
2.998
3.954
5.165
6.660
6457
1046
13.67
17.07
21.14
2840
31.78
3840
4641
5540
8
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.8046
1.253
1.712
2410
3.081
4.069
5.302
6.850
6.767
11.12
13.98
17.44
2149
2843
3249
3944
4747
5840
7
0.0541
0.0882
3.1428
0.2203
0.3240
0.4666
0.6668
0.8352
1.293
1.765
2479
3.169
4.174
5.442
7.024
6.981
11.36
14.90
1742
2245
2747
33.M
3940
46.14
5741
a
0.0371
0.0832
3.1S02
0.2282
0.3364
0.4658
0.6803
0.8666
1.335
1.618
2.448
3458
4.288
5.585
7.202
8.200
11.65
14.62
1641
2242
2742
3947
40.78
4949
5949
0 .
0.0596
0.0962
0.1567
04363
04499
0.5095
0.7144
0.9989
1.378
1.878
2421
3481
4408
5.732
7.384
9424
1142
1449
1941
2249
28.18
3449
4142
4848
5847
-------
                               METHOD 18 FIELD DATASHEET
        Plant;
        Date:	s
        Location:.
        Stack I.D.:_i'
        Pbar:  og. ti
        Sample Tube
        Operators:.
Leak Check: Pre:
                               Post:  i/
//
             Time
 Gauge
Vacuum
  (Hg)
                            Flow
                          Setting
                                      e. c
            Tr«v«re«
             Point
            Number
               V.toetty
                HMd
               In.
            stack
            T«mp.
             °F
                                       Tested Analyte:_l^
                                       Orifice Tank #:	
                                       Pt:  Pretest (mm Hg)-_
                                           Post-Test (mm Hg);
                                       Tt:  Pretest
                        Time: Start;//££_Finish
                        W/B:  -  D/B:  -	O9
    Md - (0.44x%CO2) + (0.32X%O2> + (0.28 X"*^)


•^flt- Md - (0.44 X     ) -f (0.32 X    ) -t- (0.28 X    )

-------
jog a
                      METHOD 18 FIELD DATA SHEET











//£? o
H 19
. '2# if
"3S- v,
Hi* no
'/£« *°
/4cf to
/i 11 ~i 1^1
4V- f.13
^ ^
M J
























PlantUJ^
Date: -s-/
Location: /J,
Run#: /IP*
Stack I.D.:
Pbar: Z*.*
Sample Tube
Operators :_:
Leak Check:

Time
1111. o~i
7122, LC
™\ vf
nz"•
:*Of.L.

\6Oti.
t^Ot-i.
)S£>LL

Stack
T.mp.
?i
^3
^2.
^^?
?V
^-5
94
^S

#4
M
$
w
?1
94
?4
9*1







rt
Tested AnaJyte: 5^^^
Orifica Tank *:
Pump/Rotometer #: y^sr^ |
Pt: Pretest (mm Hg):
Post-Test (mm Hg): -
Tt: Pretest f F):
Post-Test <°F):
Time: Start: nan Finish: Total: ^
W/B: "7O D/B: ?Y Q^: *zi CCL: c5
^ ^ •~-^~-
Md - (0.44x%CO2) 4- (0.32 xXOj) -I- (0.28 x%Nj)
— £*- Md - (0.44 n ) -t- (0.32 X ) -t- (0.28 X )
** ^<*
— P?
% H_O % H.O
<\? M«-Mdx(1- 	 l_)-i-l8( 	 — )
c 100 100
^V ^- 1 9 - I
' Ma ml \ v M 1 i IB ( , \
Mt ( )X(1 10Q ) 1H( )
15
,„ "" ^^
,. T.. XV ">F. S^ °fl(°F,4Ji In Ha
" CT5- /*y HI. ny
fi? - ' S^4 ~)
'*»• -J O I '
1= ,1 T"**")
V.-M.4«MOpxVAP X ^ P8XM.

W« « A^ Afiy/ \ •* 1 \ Y + I

Mm L)/0 /^-/ »/.
¥• • TV/--' / ft/I
^-i 1 ? o
A* - o/ » v S n*

Q«- V«xA«xOO«/m

Qi- x xflO
s~ t _ i 1
Q«- ? l^*y adm
PB S H_0
Q« .,-Q« XI 7.847 x 	 x(1 	 2_)
•*• T« 100



QHtd- ^ ^"? "^ dMfcn
-------
          WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: /_* < < ,,
Site: Aut.tcttj Pi A Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of Stack = Pbar 3 -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw
Vapor Pressure of h^O = Pva = iPwv) -
Pva - ( ) -
/i < • '-
Location: '/f-j*'' «w -x-» «*<•»•
•»^ri Run ff: Af-^ • "5 Date: -.
Pbar= ^-<*
Pg = - - i S
_PO_ ps= V?. -7V
U.b
Tw = -75
Td= ^^
AT= ^
(
 o
 10
 20
 30
 40
 50
 00
 70
 80
 90
100
110
120
130
140
150
160
170
180
190
200
210
220
290
240
(Ps)
0
0.0376
0.0631
0.1025
0.1647
04478
0.3626
^2,jg18
^OTMifr)
1.032
1.422
1.933
2.598
3.446
4.828
5.881
7.589
9.683
1240
1549
1941
2347
28.78
3840
4341
5044
1
0.0398
0.0660
0.1080
0.1716
0.2578
0.3764
0.5407
0.7648
1.068
1.467
1.883
2.872
3.543
4.647
6.034
7.789
8.888
13.48
1949
1843
2346
2943
3848
4S.11
81.76
                       (
( )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1603
0.2677
0.3906
0.5601
0.7812
1.102
1.513
2.052
2.749
3.842
4.772
6.180
7.8S2
10.12
12.77
15.88
1844
24.48
2842
3847
4842
52.70
3
0.0441
0.0728
0.1188
0.1676
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.628
3.744
4.800
0.350
8.180
10.36
13.07
16.34
2047
2447
3042
3747
44.74
5348
4
0.0463
0.0768
0.1248
0.1955
0.2891
0.4203
0.6008
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
0.513
8.381
10.81
13.37
16.70
20.70
2548
31.19
37.78
4847
5442
5
0.0469
0.0610
0.1302
0.2035
0.3004
0.4358
0.6222
0.8750
1.213
1.660
2449
2.888
3.854
5.185
6.880
6.887
1046
19.87
17.07
21.14
2840
31.78
M.BO
48X41
5540
0
0.0517
0.0846
0.1370
0.2116
0.3120
0.4520
0.6442
0.8046
1.253
1.712
2410
3.081
4.069
5.302
8.880
8.767
11.12
1948
17.44
2148
2849
3248
3944
4747

7
0.0541
0.0692
0.1429
0.2203
0.3240
0.4666
0.6669
0.9352
1.293
1.769
2.379
3.169
4.174
5.442
7.024
8.881
11.38
14.30
17.82
22.03
2747
3342
3949
48.14
S741
a
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.819
2.448
3458
4.288
5.585
7.202
9400
11.68
14.82
1641
77,57
2742
3347
40.78
4948
5848
0
0.0588
0.0882
0.1567
04383
04483
0.8098
0.7144
0.9989
1.378
1.878
2421
3481
4408
5.732
7.984
9434
1142
1448
1841
2249
28.18
9448
41J2
4948
5847
-------
J aa eg
                  GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: Lteto Date: 5-^.^7
Sampling Location: /ju,;i,f,n, £.rt Clock Timp- ;
«-7
y-7
77
^/

?-/
ffe
?s
ft*
^4
?^
Jt
g^7








S- 8C
a1: it. is Side 2:
3ulb.°F: 97
Md - (0.44 x ^COj) i- (0.32 X %O2) t- (0.28 X -JfeNj)
Md » (0.44 x ) -t- (0.32 X ) + (0.28 X )
Md- ^
% HO % HO
M« - Md x ( 1 • 	 ) -t- 1 8 ( 	 )
100 100
Mt-< )x(i- -— — ) + ia<— __)
100 100
Mi. ^^77
T*- fy °F- ^(f °R(°F*4«),
o p
Da _ OU j. :3'r- i \ ^.
13.6 13.8
*• 2 8, ^ in-Ha
^Sp - ^ 5^^
— I Ta (°R1
r^ .1 i j i iij
v.-«b.4wxu>x VAP x ^ P9XM8

V
v.. 37,277 n/t
A.. 2. ^3 ft2
Qt- V«xA«xeo«/m
Qs- x x60
*• $oio "*"
Pa *H,0
Q«^- Qi XI 7.847 X 	 x(1- —2-)
•" !• 100
•" 100
-------
           WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: / ft^o
Site: Au7i(u. Date:
Pbar = 2- §, k $
Pg = -. 8 >
_±2_ Pfi = 1%, ^
IJ.b
Tw = 7 f
Td= V7
AT= «*
(
-------
ooa a
^ »> i—.— i
      Plant: JASda
      Date:  S-tf-T
      Location:
      Run#:
 METHOD 18 FIELD DATA SHEET

	.	    Tested Anaiyte:_
—.	    Orifice Tank #:.
      Stack I.P.:
      Pbar: ,
      Sample Tube*;
      Operators:
               Pump/Rotometer #:
               Pt:  Pretest (mm Hg)-_rzi_
                   Post-Test (mm HQ): —
               Tt:  Pretest
                   Post-Test fF)
                                          Time: Start:oycw Finish: lew Total:  60
                                          W/B: —  D/B:  "~ O~: —
Time
M0
(fa
Its
rYn
l(<\
1$











l&i
j-n
ting
"//>i/n
- i




f

k
P.

)
1,
D-
D-
j

r^
<;
fe>
,7
-7
f?











AOi
Md - (0.44 x %C02) ••• (0.32 X %O2) + (0.28 X %r^»
Md - (0.44 x ) + (0.32 X ) + (0.28 X ) .
^I/^C
'•/. Md -
?ys^
* I % H.O % H.O
M«-Mdx(1--l&T-)*18(^o-)
7f :-^
M»-(e3r.r< ' x (1 ' — ^5~ 100^
M.- 1^,5^
T». '04 °F- 0"2-"/ °R (°F*4«0)
S P ~> GO
P»-»**-S-W.2i >* 13(J

jXp - zj 'XcJ o

j== J T«<°R'
V.- 65.48 xcpx^x ^ paxMt


V ^.20 / Zii e
v/ O
v« - *' ' *•/ n/»

Aa- 1,2-5 nz

Qa- VexAaxOOa/m

Qa- "il .^3) x 1,13 x«>

Q.-L.'bH^ «'

Qa^- , * l) dwftn
-------
                                              FIELD DA I A SHEET
Plant   6/).3dQ
Sampling Location
Run Number: *•£- 1
Sample Type:
                                                             Operator:
                                        Nozzle ID:
Thermocouple #:   >
                     Date:  $*•/TQ   Post-Test Leak Rate: .peg ctm
                                                                                                                 in. Hg.
                                                                As:
                                        Post-Test Leak Check: PHot:  — Orsal:
Point
Number
























j


Sampling
Tim*
(rnin)
o

90

LffQ
Vv





















OockTbm
(24-hour
dock) .
GGIO<
(09/<
O93s
/*>9 '3i'
&&£'
O^Vfi





















Gaa Meter
Reading
Qf) 3 ' s rffl O
CJ^'T,. ;ri
3V L /
g^C-' ,^^
<^^T - 7fc>
P60 ,V/6





















Velocity
Head(Ap)
inH2O
Oil ca Pressure Differential
(AH)inH2O
Desired
Actual
Stack
Temp.
(Is)
Temperature
°F
Probe
Biter
Impinger
Temp.
°F
Dry Gas Meter Temp.
Inlet
(Tm in°F)
Outlet
(Tm out°F)
y///////////////////////////^^


























//£"£>
/• J7^

/,/^
p y
' *




























































































































(Of)
3
$~ £
<£>O
£ f





















^

$6
*&
5*^





















?3^
jp —y
£?/
^ ^
^f





















Pump
Vacuum
(in. Hg)
Y/Z
3
^
^
-7
j:i-




















                 AVm-
                                                                                               Trn
-------
                        SAMPLE RECOVERY DATA
PLANT 	

DATE    £ ~ I  °\ •  °i 1    Sample Box No.
                                               Run No.

                                               Job No.
SAMPLE LOCATION
TRAIN PREPARER
                      °V  QQ^O
                                               Filter No.
SAMPLE RECOVERY PERSON
COMMENTS

FRONT HALF
Acetone
Container No.

Filter
Container No.

Description of Filter
                            Liquid
                            Level Marked
                                               Sealed
                                               Sealed
Samples Stored and Locked

BACK HALF/MOTSTTTflF,
Container No.        	
Liquid Level Marked
                                                Sealed
                                                                 o*
    IMP. NO.
               CONTENTS
                           INITIAL VOL
                              (ml)
                                                  WEIGHT (grams)
                                         INITIAL
                                                     FINAL
                                                                  NET
                                        Lit.*
                                        9ft 7
          TOTAL
-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: Mt*>C 0
                         Date:
Sampling Location: £)(,'Jf /I/ #" 

,;^
r,3/^
,.93
9P
..01
.90












£p-,VV*
Stack 1
T«mp.
°F
160
Ibl
( (*<*
/62
160
1 6/

tbH-
jfyf*
/v~>
IA1
I&1
ll>«












ft- /AV
Md - (0.44 x %C02> f (0.32 X -KOj) + (0.28 X ^~*^~
%H2°, ,Bf%H2°, /^/*3* /.^"/
M.-Mdxd--^-) -ie( io(J )
M,-<.iv.w )X(i. —^5 -) *18<-^5~>
MS- 2g;73
Tl. ;CV °F-6ZV °R(°F*4«J)
OL bw a. S-P- _. 124 15 1 r - "" '^-n.
13.8 13-a
Pt- i.'j-'Z- In. Hg
^- .^S*
/ fa (^R)
Vt « 65.48 x Cp x  n2
Q«. V«xA»xeO«/m
Qt. X xM

^ /40( ""^
Pt *H_0
Q.ttd-Q.Xl7.647xirx(1.-^r)
1*2- , . i
Q.^. xir.fl47x-z:I^ 	 «n-ToT»'
                                          /A.
-------
FIELD DA IA SHEET
Plank
LM^C.Q Sample Type: r\'li Operator: JN^/&G
Sampling Loci
Run Number:
itk>n Qj«.irJ ^ V Pbar ly*/1. Pd> Ps: *~, ££>
our
dock)
j3£l
l^fl^
1 *l /'3
"..IT £}*J
/ **l 3 3






















— Stack Diameter:
/6T" As: 1.23^
3T-3
r*

Gas Meter
Reading
(Vm)fl3
292 -9,0"^
2>G I /5^>
^^q, |^
l!)!") ^ / <>
J?S>^ • 7 ?3



t/ftl-G£iry
'
/i-l
Q
••^
^
l^
&

/v /
3
n,
Y
^"
X




Velocity
Head (Ap)
inH2O
Orifice Pressure Differential
(AH) in H20
Desired
Actual
Stack
Temp.
(Ts)
Nozzle ID: *' Thermc
Assumed Bws: • — Filter #
Meter Box #: /^ Y: '%
Post-Test Leak Rate: ,^00
Post-Test Leak Check: Pitot:
Tempeiatura
Op
Probe
Filter
Impingar
Temp.
°F
couple #: y ^
^ AH@: A £^2.
cfm @ /^ in. Hg.
— Orsat: —

Dry Gas Meter Temp.
Inlet
(Tm in°F)
Outlet
(Tm out°F)
Pump
Vacuum
(in. Hg)
y/////y/////////y/////////////////////////^







|j_ **9 rf^*"ii
^f 	
. 11
, 1 '3
V.o
I?O
' 2 ^
rj ^5



t d&~
9 I
. 9 1
/ 1 S




/' £&>
1 ' d(?

I t%k



>i 	 **-<

























t


























lifP
/£•<>'
/^?6
/^»"7
/i>~^
/6^

/fj 3
/6 £>
l& "?
Its *
/ fa C^
/ fo 5












"V


























K&-- tf.L
/U.4 - 26-
Ps - 2-t
Ms-- 3|,
^c^--
X'ic/r* =











<£>O
Sj
s<£>
&#
9
3»






















                               -.
-------
                        SAMPLE RECOVERY DATA
PLANT
DATE
SAMPLE LOCATION
TRAIN PREPARER
                        sample Box No.

                          Ov>
-------
JOI
              EPA METHOD 4 MOISTURE CALCULATIONS


     PLANT:__J^2LQ	SOURCE/RUN *•  ^'5-i   DATE:


     1.  Leakage Correction for Volume Metered


         Vmc = V 0-p - La) x 9


         vmc = V 0-p - 0.02) x 0


         Vmc=(       )-(       -0.02)x(       )


         Vmc= 35-^0  ft3


     2.  Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)


                              ,'Ptar-M AH /13.6)N
               = 17.64
                                       m
                                                   ( 541

                         dscf
     3. Volume Water Vapor Collected, Standard Conditions


         Impingers & Silica Gel = V ...   = 0.04707 x (Wr - W. )
                              wstd           v  f   i'
                                           — SCf
                              "sta
     4. Percent Moisture, by Volume


                     V^

         Bws=    —
                   w      m
                   wstd   mstd
          W8
                                                           [A ft
                                                           Ml jJI
-------
                 GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:  LA $(2 &	 Date:_5
Sampling Location:
                                In
                                                      Clock Time:
Barometric Pressure, in.jHg: 99
Moisture, %:
                                            Oporatnrs-
                                      	  Static Pressure, in. I-^O:
            	Molecular wt., Drv:        —   Pilot Tube,
Stack Dimension, in. Diameter or Side 1:    I5~fl	Side 2:	
Wet Bulb.°F:
   TravtrM
     Potat
   Number
       V
        + (0.28 X S)^)

Md - (0.44 x    ) + (0.32 X    ) + (0.26 X    )

Md-  1.W
          % H,0      % HO
Mt-Mdxd- 	i_)-18(	—)
            100        100
                                        M« - (
          )x(1
                                                        100        100
                                               13.0
                                                               13.8
                                        Vt - 65.49 x Cp x
                                        Vi • 85.40 x (
                                                             Pax Ma
                                                        ) x (
                                                                  )x
                                        Qs • v« x A« x 00 a/m
                                                               xeo
                                                      adm
                                                       Pt
                                                       Ta
                                                               100
                                                    X 17.047 X-
                                                                           100-
-------
FIELD DA IA SHEET
Plant MS
Sampling Lbcj
Run Number:
Pretest Leak R
Pretest Leak C
Traverse
Point
Numb*



























Time
(mln)
/}
/o
26.
•Tf)
*i&






















V;>T
itk>n_£
/0-5T-
ate:
Sample Type: /*7'^ Ope
XJC/l) #" /O Pbar^f3>
— "" Stack Diameter: /C" As: /,Q.3 s^f-t

Gas Meter
Reading
(Vm)«3
9&Q .faQ?
910*6, 60
O"?6'$^
Q ^ !*>O
ol^ 0- i^^)i^
cfm @) £
in. Hg.
"- Orsat: 	

Dry Gas Meter Temp.
Inlet
(Tm in°F)
1 Outlet
(Tm out°F)
y/////y//////////////////////////////////////////////////


























l.ftfa
h 
-------
a at
                       METHOD 18 FIELD DATA SHEET
•
<
l
?72- 6S'
M<3<>
•)1. 1 ^
>*,*>?
«a,«*
<|^,-7*'*?
Date: r-/9-9'P Orificft Tank *• 	
ocation: D\}t£A) & /O pump/pntnmRter #:
Run*- SO~f-3 Pt: Pretftst (r>m WG)' —
Stack I.D.: /*" Post-Tast (mm Hg); ^—
3bar: 3)30

y/s
o.i 
T/ Mi-( )x(1- 10^-' + 1(" ,00 '
^y?i
— 2*. ^
y^T.- ^^ °F- ^3 WF + 'W
S P V
p"Pb*^-( >*-^5-
P.. 27. /^ In-Hg
«P- Ot*4&
. ^? \l T9<°R)
V« - 85.48 X Cp X VAP X ^ P8XM.

v.. 3V. 0/ ft/.
A.- / 23 «2
Q«- V*xA»xCOi/m
Q§. x xM
Cfc « 'Jfd 1 *cfcn
p, *H,0
QiJJ-OiXl7.e47x 	 x(1 	 •*-)
•Id T« 100
^•W" X17.647X 	 "(^ 1fl0 '
" QNM--/ft40 
-------
                       SAMPLE RECOVERY DATA
PLANT

DATE
                                              Run No.
         ^\ °l • cl "?     Sample Box No.   A/-5"  Job No.

SAMPLE LOCATION   -44 10  Ov^\>  QvV-«fc      Filter No.

TRAIN PREPARER          "
SAMPLE RECOVERY PERSON
COMMENTS

FRONT HALF
Acetone
Container No.

Filter
Container No.

Description of Filter
                            Liquid
                            Level Marked _
                                              Sealed
                                              Sealed
Samples Stored and Locked

BACK HALF/MQTSTTIHF
Container No.
Liquid Level Marked
                                              Sealed

IMP. NO.
1
2
3
4
5
6
CONTENTS
J#X*
D2 f/,o
£~f+r
5;ltu, W


TOTAL
INITIAL VOL
(ml)
/av
fro
0
26*



WEIGHT (grams)
INITIAL
5727
5*4 ¥
Wi
77*(f


- . •• - '•
M • ^' >»• • ~m . . *m"
FrKAL
Sw'.^
s:,:,-?
-4^.1
-7-7^3



NET
' ?./
(•£
o
1.1


l*.(e

JR
-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: ZJKCr- Date: $V?t-9'7
Sampling Loc
Run#: /ft.
ration: fr\)r*) i* If) Clock Time: /V«V^
>T--3 nnoratnrs: ftftt >te
•V
r
6

/}- /
9
•3>
<5V
•9P^,
t> a~>
?5t ^
^5^

^a^
Q3C
o i a
5-?S
^y^
35* -2,












T*-XK^

wt Dry • 	 Pilot 1 uoe, up. 

Q.^. xir.e47x— 	 x<1'-^
-------
         Plant:.
         Date:
         Location: /NJnA
                      METHOD 18 FIELD DATA SHEET

                     	     Tested Analyte:_
                     	     Orifice Tank #:_
         Run #:  A/Dl - s-\
         Stack I.P.: 3i"*
         Pbar:   2.6 35
                                     Pump/Rotometer #:  iV)<;r
                                     Pt:  Pretest (mm Hg):	i_
         Sample Tube #:.
         Operators:.
Leak Check: Pre:.
                              Post:
    Post-Test (mm Hg);
Tt:  Pretest f F):
    Post-Test
Time: Start: ofo*
W/B:
 	          Total: oo
D/B:-	O2: 2.1 CO^.  o
  ^32.
/AY-15.6

c,
/'£>
^>
3o
/i^
50
6*



























Time
IH^^.l
1 H 1 Q.1
y-/3^/
/^/^7. 5
A/ 40 . ' i
/-9VZ.C?
I^S.^!

Travars*
Point
Number


























1
3
z
2-






























Gauge
Vacuum
(Hg)
1
»
/
/
/
/
I

v«tocrty
H«d
In. H2O




























































Flow
Setting
3-1
a(
£/
z./
TL/
^/
Z|

Stack
T«mp.
°F

























Md - (0.44 x %C02) + (0.32 X StCty + (0.28 X Tt^)
-^- Md - (0 44 x ) ••• (0.32 X ) + (0.28 X )
«l
V Md-
%H,O %H20
-~ll M>.Md;x(i--T^-) + i«(-jSr)

M. -, )x(1- -^5-' + '•< 100 '
^
^ M"
^ Ts- °F- °R(°F^4flO)

p,.Pb«.-i:l-=( ) + — -— ; —
13.8 13-8

JTp.

^? \l Ta(°R)
Vt-a5.48xCpx VAP x ^ P8XM,

. /


Vc «l/«

A.- nz

Q»-VixAax00a/m

Q«« x xOO

Qfm «Cfm
_ ^ u o
Q« ^,-Qax 17.847 X 	 X (1 • 	 )
^•td u"1'' T- 100

Q,^. X17.M7X 	 X(1'"^T>

Q0«M^ cfvopn
-------
                          METHOD 18 FIELD DATA SHEET
#
Plant: L^Lo Tested Analyte: ^y^^
Date: 5"-M-n Orific« Tank jfc- ~~
Location: wn£> Pump/Rntnmeter #: y^-f -^s
Run #: A/Dft - 5- Z Pt: Pretest (mm Hg)-
Stack I.D.: P.S* * ?2" Post-Tact (mm Hg): -
Pbar: Zf.r Tf Pretest f°FV
Sample Tube
Operators: 4.
#• AX>£-Z-zA NDP>-S-Z& Poet.Test r°F)-
S , Time: Start- ifdft Finish:rioft Total: 06
Leak Check: Pre: vX Post: v/ W/B: - D/B: - O^: ^ CO0:_a 	


Gauge
Time Vacuum
(Hg)
nm. M*. i
/^»V 7, ^5 /
/•V5o. iS /
IMW.ST (
W5M.1-7 |
^5T. S3 I
I*5V
-------
          APPENDIX A. 1.7

             Condition 6
(includes flows, moistures, and Method 18)
-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: u&CO Date: --'•*-?!
Sampling Loc
Run #: iv\e
ation1 M
*/
5
(*
1
%





•



9: ^?.7% Static Pressure, in. HoO: f *^
Molecular wt,. Drv: ^?.^/ Pitot Tube, Cp: , f f
•ion, in. Diameter or Side
"73 Drve

V.looty
in. H2O
,^ ,25"
Z-7
,3d
3o
i 3V
, 37
. ^1
-V/

ZC
, 3tf
. 3/
,32)
.3Z
/3>2.
.3/
.2^









Stack
Ttmp.
°F
^&
$g
(0.28x~l$ in. Hg
£P- .560.
— / Ts^R)
Vl - 85.48 X Co X JhP X U p, Ms
1
I 5^^
V if TS" * 27
v. . 1^. ^^ n/i

A«» /.G~7 n2
Qt • Vi x A» x CO i/m

Q»- -if- Of x /.6T xeo
Qt • *%0*7v/ adm
Pi ^H.0
O.^Q.xi^x — .cd.— >
Z.».7« •i-8'
(to f t5*» *f 100
                  QHtd- ^ S O ctofcn
                                                   .//I.
-------
           WET-BULB/DRY-BULB MOISTURE CALCULATION
Plam:  LKco	:	  Location:  ^^  e. ^
Site:    M,N
                       Operators:
                                    Run
Date:
                                                                 <•_/?-* -7
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack =   Pbar
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw (from Table) =   Pvw =
                                   (Ps - Fvw) x (AT)
Pbar= ^-79
Pa = - o z-
Ps = 1$. IV
Tw= ^3
Td= *«
in. Ha
in. HnO
2
in. Hq
°F
°F
AT= ^ °F
PVW= ;*'*?>
in. Hq
Vapor Pressure of HjO = Pva = (Pvw) -
                                   •2800-(1.3xTw)
Pva=( ,
                       2800-(1.3 x   1*
Proportion of Water Vapor by Volume = Bws
=   JPva)
(Ps)
T«mp.
OF
0
10
20
30
40
50
00
70
80
00
100
110
120
130
140
190
160
170
180
190
200
210
220
230
240

0
0.0376
0.0031
0.1029
0.1047
0.2478
0.3020
0.9218
0.7392
1.032
1.422
1.932
2.998
3.446
4.829
5481
7.989
0.882
1220
1929
10*1
2347
28.78
3940
4241
9OM

1
0.0398
0.0800
0.1080
0.1710
0.2978
0.3784
0.9407
0.7840
1.008
1.407
1.992
2.072
3443
4.647
8.034
7.7S9
9.088
12.40
1943
19.42
2348
2043
3948
43.11
91.78
                         (
                                                                  in. Hg
( 1*/1« )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0098
0.1127
0.1803
0.2877
0.3908
0.9801
0.7912
1.102
1.913
2.092
2.749
3.842
4.772
0.190
7.992
10.12
12.77
19.98
1944
24.40
2942
3047
4342
52.70
3
0.0441
0.0728
0.1100
0.1870
0.2782
0.4092
0.9802
0.8183
1.130
1.901
2.114
2.829
3.744
4.900
0.390
8.180
10.30
13.07
1044
2O27
2447
3042
3747
44.74
8348
4
3.0403
3.0700
0.1240
o.i ass
3.2891
0.4203
0.0009
0.8402
1.179
1.810
2.178
2.911
3.848
5.031
6.913
0.391
10.81
1347
16.70
20.70
2148
31.13
37.78
4847
9442
5
0.0409
0.0810
0.1302
0.2033
0.3004
0.4359
0.6222
0.8790
1.213
1.000
2243
2.998
3.994
9.189
6.600
8.997
10.80
13.07
17.07
21.14
?flOQ
31.78
3040
4041
9840
6
0.0517
0.0040
0.1370
0.2118
0.3120
0.4520
0.0442
0.9040
1.293
1.712
2.310
3.001
4.003
5.302
0.090
0.707
11.12
13.90
17.44
2149
2043
3248
3944
4747
9840
7
0.0541
0.0092
0.1429
0.2203
0.3240
0.4000
0.8609
0.9352
1.293
1.769
2.379
3.169
4.174
5.442
7.024
8.981
11.38
. 14.30
17.82
2248
2747
3303
3940
40.14
9741
a
0.0571
0.0932
3.1502
0.2292
0.3364
0.4090
0.0903
0.9000
1.339
1.019
2.449
3.299
4.289
5.989
7.202
9.200
11.89
14.62
1841
2242
2742
3347
40.78
4943
9843
0
0.0998
0.0982
0.1507
02303
0.3493
0.9038
0.7144
0.9980
1.378
1.078
2421
3481
4.400
9.732
7.384
9.424
1142
1440
1841
2240
28.18
3448
4142
4048
8047
-------
Plant:.
Date: 5- 23'-«n
                        METHOD 18 FIELD DATASHEET
                       	     Tested Analyte:_
                       	     Orifice Tank #:_
Location: A>*.\-
Run #:  Mfig-//-?.
Stack I.P.:  n 5
Pbar:  1,1.
                                         Pump/Rotometer #:.
                                         Pt:   Pretest (mm Hg):_
                                             Post-Test (mm Hg):
                                         Tt:   Pretest f°F):
Sample Tube #
Operators:  r«*
                                             Post-Test fF):_
Leak Check: Pre:
                        Post-
O
/o
*t
Time
77^£.L<.
J**CC.
AUty£-



-T
• i^*
V V
Tf
'//
    Travarsa
     Point
    Numbar
                 Velocity
                  H«ad
                 in. H2O
Stack
Temp.
 °F
            Time: Start:/o39  Finish:/*s9 Total:
            W/B:  —D/B:  —- O2:  a*jCO2:


            Md = (0.44 x %CO2) -t- (0.32 X %O2) -r (0.28 X Kt^)

            Md = (0.44 x O  ) -t- (0.32 x «-/ ) + (0.28 x 7*
                                          Md
                                         Ms o Md x (1 • •
                                                     !0(

                                         Ms = ( £*f*t ) xd


                                         Ms -


                                         Ts -       °F =
                                                      HO      % HO
                                                      -t_; - 18 (    *  '
                                                                100
                                                          	) -i- 18 (	I
                                                          100        100
                                                               °R<°F~460)
        c p
Ps-Pb *^Jl-= (
        13.6
                                                                  13.6
                                          Ps
                                                       in. Hg
Vs.
Vs
Vs
As
Qs
Qs
Qa
- 85.49 x Cp x JS^ x "W —
- 85.49 X( .W )X(
ft/8
ft2
• Vs x As x 60 s/rn
• x
• acftn
Ts(°R)
PsxMs
ml
' \l

x60
                                                          P,     %H-0
                                           Qs . .= Q8X17.647X	x(t • 	*—
                                            •W            Ts      100
                                           Qs

                                                       x 17.647 x-


                                                        dscfm
                                           •x(1

-------
   a
V
                                  METHOD 18 FIELD DATA SHEET
Plant:.
Date:
          Location:
          Run #:  me.-)/-
          Stack I.D.:_Z2i£
          Sample Tube #: */?-/>• •»* .
          Operators:
          Leak Check: Pre:
                       Post:
                                                  Tested Analyte:.
                                                  Orifice Tank #:_
                                        Pump/Rotometer #:_i
                                        Pt:  Pretest (mm Hg):	
                                            Pest-Test (mm Hg):_
                                        Tt:  Pretest
                                            Post-Test fF):	n^
                                        Time: Start:.£*LRnish:j»ff£jotal:_££.
Time
2325.54
2326. f\
7-1,26. 01




Gauge
Vacuum
(Hg)
/
/
/




Row
Setting
ISetc.
]*<><.<-
tSocc




T»
ts
                                                   Md = (0.44 x %C02) - (0.32 X %O2) -r (0.28 X "/oNj)


                                               ^~ Md = (0.44x O  )+(0.32X1'  } * (0.28 x7*


                                                   Md =
Traverse
Point
Number
1
I
3
if
9
t,
7
r

f
t
i
V
/
V
7
J








Velocity
Head
in. H,O
.Z5
36
.3*
.3z
.35
.^e
.vo
.^•2.

.ZT
.36
. 2>l
.3-2
.30
,3/
.32
.^•z

f9.^%3






Stack
Temp.
°F
7?
•)1
7?
7f
7f
•»f
7f
7*

T
7?
7f
7t
7T
7?
7?
?4

7?






                                         Ms = Md xl) -
                                                   MS-
                                                   Pa - Pb
                                                             %H O
                                                             - =— '
                                                              100
   - 18(


  I  >   ,
   100  '
                                                              100
                                                                              100
                                                S.P.
                                                13.6
                                                                           13.8
                                         Ps= Z-^'


                                         J&m 0.

                                         Vs » 65.49 x Cp x
    i
                                                                         Ts(°R)
                                                                        Pax Ms
                                         Vs - 85.49 x(  • 9f  )x(

                                         Vs - 3% MX.   ft/,

                                         A.-  7,6,7    «2

                                         Qs - Vs x As x 60 s/m
                                                                             )x
                                                                                V Z*.
                                                                           x60
                                                    Qs-
                                                       acfm
                                          Qs . .= Qs x 17.647 x
                                           std
                                                                   Ps
                                                                      x (1
                                                                           100
                                                    Q«
                                                      std"
x 17.647 x-


 dsclin
                                                                             100
-------
                              METHOD 18 FIELD DATA SHEET
        Plant;
        Date:	2.
        Location:.
        Run #:  ;;
                                      Tested Analyte:   5/y,~e.^
                                      Orifice Tank #:	~
       Stack I.P.:   n.S"
       Pbar:    zr. 7?
                                      Pump/Rotometer #:_
                                      Pt:  Pretest (mm Hg)L
       Sample Tube
       Operators:.
                                          Post-Test (mm Hg);	r_
                                      Tt:  Pretest fF):_
                                          Post-Test fF)L
Leak Check: Pre:
                              Post:
Time: Start:fl33  Finish:'7**Total: /<
W/B:  73 D/B:^  O*: -'  CO2:  &
/ 7 .V?
Time
no6.6-7
-71 31, 3S




Gauge
Vacuum
(Hg)
/
/
/




Row
Setting .
,£*<*
/j#r^
/SO^
•




0 N"
O i
                                              Md a (0.44 x


                                              Md a (0.44 x


                                              Md-
                                              Ms = (
                                                   + (0.32 X %O2) + (0.28 X %Nfe)


                                                  ) •»• (0.32 X   ) + (0.28 X    )
                                                       % H.O
                                                          % H.O
                                                IX(1 - 	) -(- 18 (	
                                                      100        100



Travtra*
Point
Number




























V.tocrty
H»ad
In. H^O




























Stack
Tamp.
















•








Ma -
Ts- °F- °R (°F 1-460)
S P
D« _ OK j. ^-r" _ / \ ,
13.8 13.6
Ps = In. Hg

fir*

== . 1 Ta (°R)
VB - (J!j.4U x Cp x VU^ x U ps x Ma



Va • ft/a

A.. »2
Aa • ft

Qs • Va x As x 60 s/m

Qa - x x 60

Q«- acfm
Pa %H2°
Qs.. .= Qs x 17.647 x 	 x (1 • 	 =— )




Q^fltd™ dscfm
-------
                                 METHOD 18 FIELD DATA SHEET
         Plant;
         Date:	£_
         Location:.
         Run #:*
         Stack I.D.;   .1.5
         Pbar:    z?. 7 a
         Sample Tube
         Operators:   -r
         Leak Check: Pre:_
Post:
TV- >?»
Trav«ro»       Velocity
 Point         H«ad
Number       In. I
                         .26,
                         .li
                          36
                          3,7
                                     Stack
                                     T.mp.
                                     10
                                     9?
                                     8*1
                 Tested Analyte:_j3£u
                 Orifice Tank #:__
                 Pump/Rotometer #:.
                 Pt:  Pretest (mm Hg)L
                     Post-Test (mm Hg);	n
                 Tt:  Pretest fF):	r_
                     Post-Test
Time: Start: n 33Rnish:^v 3> Total:
W/B:75
Time
z^c^, yc
2.30*?, *JH
13/0. 2?




Gauge
Vacuum
(Hg)
/
/
/




Row
Setting
iso*-*-
'** "'
^o-




T~
-77
'IT
l^r
                 Md - (0.44x%CX)2) -t-


                 Md = (0.44 x  
-------
"Pa :—r
                WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: /^AsC& /^W^
Site: ,A.v, /jr/C^ Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack = Pbar + -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H0O at Tw
Location: flonVnCC, |£V
-70 Run??: fif-t-i- Date: 5,
Pbar = 24. 7B
Pq = "~. -a ?
-rnr Ps = 2*- 7*
Tw= ?J
Td= $1
AT= /£
(from Table) = Pvw = 0. 8/S3

'//I /i 7
in. Hg
in. H.O
2
in. Hg
°F
°F
°F
in. Hq
       Vapor Pressure of H^O = Pva = (Pvw) -
       Pva=
              (Ps-Pvw) x (AT)
              2800-(1.3xTw)

(2B,it   -,e/*3  )x(   /£    )
    2800 -(1.3 x   73    )
                                                              in. Hg
Proportion of Water Vapor by Volume = Bws

    -   (Pva)
(Ps)
T«mo.
op
0
10
zo
30
40
50
00
70
00
00
100
110
120
130
140
150
180
170
180
100
200
210
220
230
240

0
0.0378
0.0831
0.1029
0.1847
0.2478
0.3828
O.S218
0.7302
1.032
1.422
1.832
2.308
3.446
4.S2S
5481
7.580
9.852
1240
1350
10.01
2147
28.78
3UO
4241
5044

i
0.0308
0.0880
0.1080
0.1718
0.2978
0.3784
0.9407
0.7848
1.088
1.487
1.003
2.872
3.949
4.847
8.034
7.780
0.889
12.48
1843
1042
2348
29.33
3848
43.11
81.78
                                                              2.3%
( 24, 7e )
Lfu 7 IS
VAPOR PRESSURES OF WATER
In Inches of Mercury 2'70$V
2
0.0417
0.0808
0.1127
0.1803
0.2877
0.3808
0.9601
0.7912
1.102
1.513
2.093
2.749
3.643
4.772
6.190
7.993
10.13
12.77
1948
1944
2446
2943
3647
4943
53JO
3
0.0441
0.0728
0.1188
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.581
2.114
2.829
3.744
4.900
0.390
8.180
10.36
13.07
18.34
2047
2447
3042
3747
44.74
5948
4
3.0483
0.0788
0.1248
0.1055
0.2801
0.4203
0.6009
0.8482
1.179
1.610
2.178
2411
3446
5.031
0.913
0491
1041
1347
16.70
20.70
2546
31.13
37.78
4847
5443
5
0.0480
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8790
1.213
1.660
2443
2.995
3.954
5.169
6.660
8.987
10.66
13.67
17.07
21.14
2640
31.78
3840
4641
5840
0
0.0517
0.0840
0.1370
0.2118
0.3120
0.4520
0.8442
0.9046
1.253
1.712
2410
3.061
4.069
5.302
6.850
8.767
11.12
1348
17.44
2149
2649
3348
3944
4747
5640
7
0.0541
0.0802
0.1420
0.2203
0.3240
0.4888
0.8889
0.9392
1.293
1.789
2479
3.189
4.174
5.442
7.024
8.981
11.36
14.30
1742
2348
2747
3342
3949
48.14
5741
a
0.0371
0.0032
3.1502
0.2292
0.3384
0.4858
0.6903
0.0668
1.339
1.819
2.449
3.299
4.289
5.585
7.202
0400
11.69
14.82
1841
2242
2743
3347
40.78
4943
9849
0
0.0508
0.0082
0.1987
0.2363
0.3493
0.9038
0.7144
0.9969
1.378
1.678
2431
3481
4408
5.733
7.384
0434
1143
1446
1641
2349
28.18
3448
4143
4948
8047
-------
jag cia
                  GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: / f&CO Date: jr-/*-*?
Sampling Loc
Run #: (v\&-
ation: ^-^ f^. ^ Clock Time: /f^o
'• -"*> Ooentors! ^/r/
Barometric Pressure, in. H
Moisture, %: / 9 ?
Stack Dimens
Wet Bulb, °F-
Traverse
Point
Number
1
7
••>
f
5*
6
7
7

i
i
5
T*
y
<*
1
y





•



9: z?,^ Static Pressure, in. H«O: c>^
Molecular wt Drv Zs-Sl PitOt Tube, Cp: (ff
iion, in. Diameter or Side
6^ DrvE

Velocity
in. H20
,21
2-1-
• 2?
,29
33
•15
• *>~~)
• 3>
?&.
yc>
fll CO
O- /
{/ *L_^
CJ ttf
«-&
^6

95
?^>
^•6»
#6
76
^6.
^G
»^








• ft- ^
1- ^7 , J Side 2: —
ulh^F- ff(^
Md - (0.44 x %C02) f (0.32 X %O2> * (0.28 X KNj)
Md - (0.44 x O ) ••• (0.32 X 2. / ) * (0.2B X ~* ** )
Md- Z-3--*17
% H20 % H2O
100 100
" 100 100
M«- 2-6.C?3
Pn - Pb + ™P' - ( ?$• vy ) *• — O.O^>
13.B ' 13.B
P, . 2^ f, g / In. Hg
fif - 0 5£}2~-
	 / Ts (^R)
u i S X MS


v.- 3^ ^73 «/•

*•• /.^ n2
Q* — V« x A» x CO a/m

Qc« x xeo
0»- T.g/5" tdm
ji/i j
Pt ""2°
^ttd" * X ' 7
-------
Plant:
Site:
          WET-BULB/DRY-BULB MOISTURE CALCULATION
                                       Location:
                 ~,r   Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of StacK =   Pbar +
                                 1 J.D
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
    Run if: /^f£~- 6>- 2
           Pbar =	
            pg = _:
          .  Ps =	
            Tw =	
            Td =	
                                                           Date:
                                                         . 0 3
                                                         17
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw (from Table) =   Pvw = —^ 7/yy
                                   (Ps- Fvw) x (AT)
Vapor Pressure of H2O = Pva = (Pvw)

Pva=(  o.l (^   )--
2800-(1.3xTw)
)x(    17     )
                                                          /.
                       2800 - (1.3x
Proportion of Water Vapor by Volume = Bws
                         (   0.&SO )
                                            )
(Ps)
Tamp.
OF
0
10
20
30
40
50
60
70
80
90
100
110
120
130
140
150
160
170
180
190
200
210
220
230
240

0
0.0376
0.0831
0.1025
0.1847
0.2478
0.3826
0.5218
0.7392
1.032
1.422
1.932
2.598
3.446
4.525
5.881
7.569
9.652
1220
1529
19.01
23.47
28.75
3540
4241
5044-

1
0.0398
0.0680
0.1080
0.1718
0.2578
0.3764
0.5407
0.7648
1.066
1.467
1.992
2.672
3.543
4.647
6.034
7.739
9.883
12.48
16.83
19.42
2348
2943
33.88
43.11
51.76
                                                   O.
                                                              /? '•
                                                                     in. Hg
                                                                     in. 1^0
                                                                     in. Hg
                                                                     °F
                                                                     in. Hg
                                                                     in. Hg
( ZMf )
VAPOR PRESSURES OF WATER -^TT
-; o. (7W
In Inches of Mercury T,?!0-
2
0.0417
0.0896
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.842
4.772
6.190
7.052
10.12
12.77
15.98
1944
24.46
2942
3847
4348
52.70
3
0.0441
0.0728
0.1188
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.629
3.744
4.900
6.330
8.150
10.38
13.07
16.34
2027
24.97
30.32
37.07
44.74
53.63
4
0.0463
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8482
1.175
1.610
2.178
2.911
3.848
5.031
6.513
8.331
10.61
13.37
16.70
20.70
25.48
31.13
37.78
4547
54.62
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.680
8.537
10.66
13.87
17.07
21.14
26.00
31.75
3840
46.41
5340
a
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.850
8.767
11.12
13.98
17.44
2149
2643
3248
3924
4727
5640
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4688
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.981
11.38
14.30
17.82
2243
27.07
3342
3949
48.14
3741
8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9668
1.335
1.819
2.449
3.259
4.289
5.583
7.202
9200
11.63
14.62
1821
2242
2742
3347
40.75
4943
3843
9
0.0598
0.0962
0.1567
0.2383
0.3493
0.5035
0.7144
0.9989
1.378
1.873
2.321
3.331
4.406
5.732
7.384
9.424
11.92
1448
1841
2249
28.18
3443
4142
4943
8047
-------
a
a
       Date:  5-
       Location
       Run#:
                        METHOD 18 FIELD DATASHEET

                       	     Tested Analyte:_
                       	     Orifice Tank #:.
             iY\ c.-*.»•>,• ..i-.-f-
       Stack I.D.:
       Pbar:
       Sample Tube #;
       Operators:
Leak Check: Pre:
                               Post:
                  S^t/c^-  -.
          Trovtrea
           Point
          Number
               Velocity
                H««d
                       .05"
                       ,O(a
                       OS
                       .OS
                *
                               LJ L,
Stack
T«mp.
 °F
                           5-2.
                                  ZL
                                   # I.
                                 3$	
             Pump/Rotometer #:_L
             Pt:   Pretest (mm Hg) i
                                             Post-Test (mm Hg):_
                                         Tt:  Pretest
Time
-1-729.^^
71-Vi.TL
"T7 > 9^
-?-? T,3, ^7
-11 3^.03
77^5, 75

Gauge
Vacuum
(Hg)

^
i
t
,
1

Row
Setting
/<0^
/£(j (£,
/$(><•£.
,j$f <:<-
/4& r<-
,40"


37
                 Post-Test fF):	
             Time: Start: /&*, Hnish:'^  Total: 4-T
             W/B:"1/  D/B:03    O^: ^/  CQ~: &
                                  & ^^~^    <:

             Md-(0.44x%C02) +


             Md - (0.44 x O ) + (0.32 X 2./  ) + (0.28 X

             Md-
                                                          % HO       % HO
                                                Ms = Mdx(1 - 	£_) + 18 (	=— )
                                                           100         100
                                         Ma-( ^


                                         Ms-   -
                                                                100
                                                                           100
13.0
                 13.8
                                                            |n.Hg
                                        Vs - 85.49 x Cp x



                                        Vs-85.49x(  -^


                                        »     
-------
         WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: Li^LO
Site: Kbav* &t)(\Qut
-------
        WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: Lfeoo fL^L^
Site: ^,,>«, £><•£—<./' Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of Stack = Pbar ± -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw
Vapor Pressure of HpO - Pva - (Pvw) •
Pva=(/07/$V0 )-( ^'73 ''7**
Location: rkr^Wf( £V
~7& Run #: fa- 6- 2- Date: *
Pbar = 2^5. 7$
Pq = -; £ -2—
-3L- PS= 2*7.3
Tw = 7/
Td= B3
AT= /2-
(from Table) = Pvw = 0, 7b /£
(Ps - Fvw) X (AT)
2800-(1.3xTw)
# )x( /Z- ) AW/1/

X/1/*7
in. Hg
in. HP
2
in. Hg
°F
°F
°F
in. Hg
in. Hg
                   2800 - (1.3 x



Proportion of Water Vapor by Volume = Bws
(Ps)
Tamp.
OF
0
10
20
30
40
SO
60
70
60
90
100
110
120
130
140
ISO
160
170
160
100
200
210
220
230
240

0
0.0376
0.0631
0.1025
0.1847
0.2478
0.3626
0.5216
0.7392
1.032
1.422
1.932
2.596
3.446
4.52S
5.681
7.569
9.652
1220
1520
19.01
2*47
28.75
3540
42.31
50.84-

1
0.0398
0.0660
0.1060
0.1718
0.2576
0.3764
3.5407
0.7848
1.068
1.487
1.003
2.872
3.543
4.847
6.034
7.758
9.88S
12.48
15.63
19.42
2346
20.33
3548
43.11
51.78
                                                     2,
( 2-9.73 )
VAPOR PRESSURES OF WATER ^*f_ „ 0 /
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.740
3.842
4.772
6.100
7.052
10.12
12.77
15.08
1044
24.46
2842
3647
4343
52.70
3
0.0441
0.0726
0.1166
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.629
3.744
4.900
6.350
6.180
10.36
13.07
16.34
2027
2447
3042
3747
44.74
5345
4
0.0463
0.0766
0.1248
3.1955
0.2691
0.4203
0.6009
0.6462
1.175
1.610
2.178
2.911
3.848
5.031
6.513
6.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
4847
54.63
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.860
2243
2.995
3.954
5.165
6.680
6.557
10.86
1347
17.07
21.14
26.00
31.78
3840
4641
5540
6
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.8442
0.0046
1.253
1.712
2.310
3,081
*063
5.302
6.650
8.767
11.12
13.08
17.44
2140
2643
3248
3024
4727
5640
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4666
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
6.081
11.38
1440
17.82
2345
27.07
3342
3040
48.14
5741
1 70 7. 7
8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.619
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1821
fj*a
27.62
3347
40.73
4043
5843
— "t <
9
0.0508
0.0082
0.1567
0.2383
0.3403
0.5035
0.7144
0.0080
1.378
1.875
2421
3.351
4.408
5.732
7.384
9.424
1143
1446
1841
2349
28.18
3443
4143
4943
5947
-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: i-$&£> Hate: J-^-fl :
Sampling Loc
Run#: Rg-
ation: £,^ £V/v,,^f Clock Time: I7sf
/--I, nporptnrs- T#/55
Barometric Pressure, in. H
Moisture, %: "2- 2-
Stack Dimens
Wet Bulb, °F
TrcvarM
Point
Number
/
->
c
"*>
V
5
C
/
1
">
^
5
t,
i
T.
5
*/
5*
C
i
7.
3
4
5"
L


q: 28. 7^ Static Pressure, in. hUO: — ,CZ
Molecular wt.. Drv: .^f- ^V Pitot Tube, Cp: . ion, in. Diameter or Side
I/ DrvE

Vvleeity
H««d
in. H2O
lOG?
.^7
,^c^
^>"7
,^7
.oy
.0^
.<&
ol
,ou>
,oa?
>>0
,lb
.
^
•y^

^P-ft2-773
Stack
T«mp.
°F
^3 1

Sy3
5^>
43
 f (0.28 x %^42)
Md - (0.44 x ) * (0.32 X ) f (0.28 X )
Md - 2^7. o
% HO % H20
Mi-Mdx(1 ioQ '°l 10Q
M..( )x(,.___) + ia(-^5-)
M«- ^.7^
?;. g> °F- c5YJ °R(°F*460)
P» - Pb » S'P' = ( ) +• ——
13.B 13.8
Pi - 2^. 7 3 in. Hg
£?- ^7^773
— J Ts (^R)
V«-«b.48xU>x VA^ x )| ~p9x"M8"


v» - /f, o 3 ft/i

A..- ^6-7 «2
Qt • Vi x A« x 00 i/m

Qs • x XOO
Q,- <3S/ «<*"
Pt *H2°
0.-td=O.K17.B47x-?-x(1.-jS-)

Qt^- X17.647X 	 "C(1'"^T>
                     ywto
-------
jag c^a
                       GAS VELOCITY AND VOLUMETRIC FLOW RATE
      Plant:.
      Sampling Location:
      Run#:  Rt-(,'^
               Date:  <-/t-^
               Clock Time:   /9so
      Barometric Pressure, in. Hq:   ?j£,    	
      Moisture, %:    X?	Molecular wt., Dry:.
      Stack Dimension, in. Diameter or Side 1:	
      Wet Bulb.°F:      Ct	Dry Bulb,°F:
     Static Pressure, in. HoO:  -« 6V
     i*.ti     Pilot Tube, Cp:  .99
       	Side2:_
Trover**
• Point
Number
1 ' V-
z
^
V
5
C
i
1
^
1
5
(j
i
L
^
H
5
u
/
2
•}
V
5"
d/


Velocity
H««d
in. H20
.OG,
^••.^7
.0?
.0?
.0?
.09
.a?
,/0
.0?
.01-
,o«
,yo
>//
./o
,c*£
,0^
-OG
JO
,o->
.0*
.05
.05
.0(s
,to


Stack
T«mp.
°P
£''
£>
?/
11
*l
91
VI
V/
8'
*/
W
9/
?/
8/
t'
y
71
VI
*l
$/
11
tl
-si
W

T5-9/
                                             Md - <0.44 x KCOg) + (0.32 X %O2) * (0.28 X %l^)


                                             Md - (0.44 *    ) + (0.32 X    ) > (0.28 X
                                                       % HO      % HO
                                             M« - Mdx(1 - 	_) * 18 (	1- )
                                                         100        100
                                                             100
                                                                       100
                                               i-Pb+-i^-=(     )* 	
                                                     13.8             13.6
                                             P«- 2-Q. ~7*f  In. Hg
V» • 65.40 x Cp ]


V» - 85.40 x (


Vl»


A«-  ^|<6T   1

Q>« V«xAax80i/m


Os-          x

Q«.


                                                                        ^
                                                                    xOO
                                                 - Qi x 1 7.847 x— — x(1
                                                            T«
                       100
                                             *rtd-
                                             QNtd-
            X 17.847 X-
•x(1
                                                                               100
-------
•^a a.-
                     WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: ^feco ?*„£ Z.o.
Site'- Jtoov /^T'/^r^ Ooerators:
Barometric Pressure, in. Hg =
Static Pressure, in. HpO =
Absolute Pressure of Stack = Pbar -*- -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H^O at Tw
Vapor Pressure of H~O = Pva = (Pvw> -
>cfo Location: /% Date: ^
Pbar= 2-£0y
Pa= -.*/
-$-- Ps= -£& 79
TW= (*e
Td = VI
AT= /3
(from Tabled = Pvw = #, & ?<>2>
(Ps - Pvw) x (&T) :

/ti/r?
, in. Hg
in. HLO
2
in. Hq
°F
°F
°F
in. Hg

                                                 2800-(1.3xTw)
         Pva =
                                   2800 -(1.3 x
         Proportion of Water Vapor by Volume = Bws
        Bws=    (Pva>
                   (Ps)
       Tamp.
        °F
         0
         to
        20
        30
        40
        50
        60
        70
        80
        90
        100
        110
        120
        130
        140
        150
        160
        170
        160
        190
       200
       210
       220
       230
       240
  0
0.0376
0.0631
0.1025
0.1047
0.2478
0.3626
0.5218
0.7392
 1.032
 1.422
 1.932
 2.596
 3.446
 4.525
 5.681
 7.568
 9.652
 12.20
 15.29
 19.01
 23.47
 28.75
 35.00
 42.31
 50.84-
  1
0.0398
0.0660
0.1080
0.1716
0.2576
0.3764
0.5407
0.7648
 1.066
 1.467
 1.902
 2.672
 3.543
 4.647
 6.034
 7.759
 9.885
 12.48
 15.83
 19.42
2348
2943
39.88
43.11
31.76
                                                                                         in. Hg
( ^W0| )
VAPOR PRESSURES OF WATER ^^ *
In Inches of Mercury 2- 7 < 1—
2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.842
4.772
6.190
7.952
10.12
12.77
15.98
1944
24.48
2942
3847
4942
52.70
3
0.0441
0.0728
0.1186
0.1678
0.2782
0.4052
0.5802
0.8163
1.138
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.38
13.07
18.34
2047
24.97
30.52
3747
44.74
5345
4
0.0463
0.0768 .
0.1248
0.1955
0.2891
0.4203
0.6009
0.6462
1.175
1.610
2.178
2.911
3.848
5.031
6.513
8.351
10.61
13.37
16.70
20.70
2548
31.13
37.78
4647
5442
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.860
8.557
10.86
13.67
17.07
21.14
28.00
31.75
3840
4841
5540
6
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.083
5.302
6.650
6.787
11.12
13.98
17.44
2149
2843
3248
3944
4747
5840
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
6.981
11.38
14.30
17.82
2245
27.07
3342
3940
48.14
5741
8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.619
2.440
3.259
4.289
5.555
7402
9400
11.65
14.62
1841
n «g
27.62
3347
40.75
4943
5543
9
0.0598
' 0.0982
0.1567
0.2363
0.3493
0.5035
0.7144
0.9989
1.378
1.675
2.521
3.351
4.408
5.732
7.384
9.424
11.02
14.98
1841
2249
28.18
3443
4142
4041
9047
                                                                                   41
-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: / /} ^ C Date: 5 -//f *f
i -» / nneratnrs! ^JA /G ^
Barometric Pressure, in. H
Moisture, %: 	 2. 2-
Stack Dimenj
Wet Bulb, °F
Travsrsa
Numbsr
A- f
Q
3
9
^
£

& - /
<£
3
^
^~
&









•



;ion, in. Dian

q: i) ?.s2£"S
,3\













Stack
T«mo.
°F
/<"*/
1 tol












fJ- /4>^
1: /«T Side 2: 	
it. fl r~ ~~
ulb.uF:
Md - (0.44 x %CO2> + (0.32 X -fcO^ + (0.28 X %l^)
Md - (0.44 x ) + (0.32 X ) 1- (0.28 X )
;jMd- HO
% H20 % H2O
MS- 2.8.7k
P, Pb ^ S'P- M ) -
13.0 13.8
P.. Z7, 2O in. Hg
^f / ^f ' ^s
/ Ts(^R)
Vs-«b.4Uxu»xVSP x \l P9J(MS
i
V«- 32, 6^> ft/8

As- /, Z3, ft2
Qs - V* x Aa x 60 s/m

Qs- x x«
0.. Ol/(2^ «*n
Ps *^0
Qs ..-Qs XI 7.847 x 	 x(1 	 *-)
std TS 100

•to iw
                                           All
-------
METHOD 18 FIELD DATASHEET
Date: <- fa . 9 7 Orific« T^ *'
L
F
c
F
£
C
L

f,%
I,?
I0t>b,&>
\o*<&
tell ^
\,&

ocation:  Tt: Pretest (°R; —
lample Tube
)perators: /I
#•9/^-3/9 «to-J>A Post-Test f'R ; -^
fU
.eak Check: Pre: ,oco Post: *X

~)
/6K
/^f-
>^ ^
/^£)











IW Am
	 	 — ' C
Time: StartuZ23Finish:_L£22Totai:jc£zC_
W/B:* — D/B: — CL: ^ CO^: —
Md - (0.44x%CX32) -t- (0.32 x%02) + (0.28 x*!^)
Md - (0.44 x ) + (0.32 X ) + (0.28 X )
^
™/W %H20 %H20
^M.-Mdx(1--^-)*.e(_;— ) l.Zt
^V^Me-( )x(1- ) + l8( 	 -)
-------
Plant
    FIELD DA IA SHEET
Sample Type:  M' ^  Operator:
Nozzle ID:
Thermocouple
Sampling Loci
Run Number:
Pretest Leak R
Pretest Leak C
Print
Number

















i










Sampling
Time
^>
to
Qn
1t>
H&























ition &j£/l) & i Pbaro'S,'!?^) Ps: *-0-Gl«
9 -£O Date: 5'/$-9'? CO2: 	 	 O2: 	 -
ate: t &M> cfm @ /O in
heck: Phot: 	 Orsat: '

dock Time
(244iour
dock)
m*
/*/£*>
. #£&
/ fr JO
| 83O























. Hg. Probe Length/Type
•~~ Slack Diameter:
5: / ' SS Pilol#: SF3
/
3^3 ijO

t^j^.'«9^>l





Velocity
Head (Ap)
inH2O
Oriice Pressure Differential
(AH) in H2O
Desired
Actual
Stack
Temp.
fTs)
Assumed Bws: -~ Filler #
Meier Box #: /^ Y:..ty6
Posl-Tesl Leak Rate: it)O
Post-Test Leak Check: Pilot:
Tempeiature
°F
Probe
Filter
Impinger
Temp.
°F
: • —
L AH@: / fi1'^
cfm @^2-in. Hg.
	 	 Orsal: — -^

Dry Gas Meter Temp.
Inlet
(Tm in°F)
Outlet
(Tm oul°F)
Pump
Vacuum
(in. Hg)
y///////////////////////////////////////////^^









/' S6>
/, $b
l( ^
/ tS'Cf





I1 i^yyte?/'?-xi

/QM
/n
jnl
'lit
Ilir
>w

/3-u
/wf
ill
IV
•Jr
















































*
9^
/<5b



















••



^S
y&
^s^
/£>
-------
                        SAMPLE RECOVERY DATA
PLANT
                                Run No.
DATE    £- / I- 9 9   Sample Box No.  A'-fc   Job No.  -SV'l.
SAMPLE LOCATION

TRAIN PREPARER
                 Qu7<-«
                                                Filter No.

SAMPLE RECOVERY PERSON
COMMENTS

FRONT HALF
Acetone
Container No.

Filter
Container No.

Description of Filter
                             Liquid
                             Level Marked
                                Sealed
                                                Sealed
 Samples Stored and Locked

 RACK HALF/MQISTTJRK
 Container No.        	
 Liquid Level Marked
                                 Sealed
    IMP. NO.
CONTENTS
           TOTAL
                           INITIAL VOL
                              (ml)
                                                                 -7
                                                    WEIGHT (grams >
                                          INITIAL
                                       FINAL
                                                                    NET
                                                                     a. 6
-------
             GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:
Sampling Location: QIJ& A' ^- S

Clock Time: £ti&®9cc
£ - ^> Ooerators: QI&Jd(\
Barometric Pressure, in. Ha: 3 ^ ^O Static Pressure, in. HoO: -,&&
Moisture. %: — 	
Molecular wt.. Drv: -T^ Pitot Tube. CD: •• .9^
Stack Dimension, in. Diameter or Sid
Wet Bulb. °F: 	 	 Drv

Trov«rM
^ ^.i 	 ^
rotnt
Number
fl-\
9
3
V
f

, 3^
e Q^
, ^ ;












JSP - ,^a
Stock
T«mp.
°F
tSX
l<4
11*0
/ 1»-'??
/6(
/V^

/<^^
!<*<<
lte£>
1 (*£.
J^
16V












TS./#L
nv / + (0.32 X %O2> «• (0.28 x %N2>
Md-(0.44x J-M0.32X )+ (0.28.x )
Md- 1?l;0 AWSA^2
%H2°, ...%H2°, ? -L'/,
M..Mdx(1--^5-)^8( 10Q » 4.* 'i
Ms-< )x(1 )-H8( )
Mt- 2.^7^
T« - /£ £- °P •' ^ £2^ °R (°F * «o)
^•^13.0 * ' 13.8
P,. 2?.(5' ln-H8
^>^-7^
Ts (°R)
/I- 1
V» « 85.48 x Cp X W X W p, „ M,
V» - 65.49 x ( ) x ( ) * V 	
1
v«- 32,22- ft*
A- /^ ft2
Q» - V« x A» x «0 «/m
Qt. X X00
Q.. ^37^ adm
Pt %H2°
Qi^-Oi.!^.— «0--— )
Qi^- X17.047X 	 •*(!• 10Q )
11 13
                                         d«*n
                                                              .///ff
-------
   30 £
                          METHOD 18 FIELD DATA SHEET
d
  \<.*

Plant: Lfttf.O TesteH Anaiyte- Slrtf^z
Date: S't1'<47 Orific« Tanic *• 	 •
_ocation- f9.;tv* /O Pump/Potnmeter #: 	
Run #: //O- ^ - / Pt: Pret««r* (mm Hg)- 	 	
Stack I.D.: /< Post-Test fmm Hg): 	
Pbar: 3?,20 Tf- Prfrtflst l°R: —
Sample Tube
Operators: 0^
#• /n<6-M J - l£ Poct-Tnet fF)' 	
W^oc.i/n




\ /
^^
WT/C1-VK2 CJ'
, Trav«re«
Point
Number
/-I -7
i
"•5
^
^
6

n- /
a
.3
Y
*
6)












Velocity
Head
In. HjO
, ^
• <
'//>
. .Q/5
o^;
.p-7

'IS
ro/
.^
-tc
,5-s
rP?











/ao - vr?*
Stack
Temp.
°F
<3D^
r^QI
<93^
ci?5/fv
55^
^J2^

3-3Z*
13 S>
St&S
3Q 1
,42 4
92 *>
•










93 7^ /^^
,7^ %HO %HO .
^*M..Mdx(1--^.) + l8(-^r) 2.,i
I Me-( )x(1- 	 )-t-18( 	 )
3^- ^
aj T.- 2.2-5 Ofr- L& 0R(°P*-«JO)
p"rb*T5F ( ' i3.e
p.- 27,/Y m. HO
^" ft^J^
;== , I Ts <^R)
V« « 03.48 X ^p X 
-------
                                             FIELD DA I A SHEET
Plant	
Sampling Location CA*£A/ *  1O
Run Number:  /Q»-6 /  Date:  5T-
                      cfm
               Sample Type:
               Pbar  £3.90
               CO2:   __
Pretest Leak Rate: tCCt\
Pretest Leak Check: Prtot:
   // in. Hg.
Orsat:
                Ps:
     	02:.
Probe Length/Type:  /
Stack Diameter:   )S
                                                             Operator:
                                                               -Q.B2.
                  Nozzle ID:
                 Assumed Bws: —
                 Thermocouple #:
                 Filter*:  —
   Pilot #: 5T3
As:
Meter Box #:  /^  Y: /
Post-Test Leak Rate: ,OCO cfm @ /pin. Hg.
Post-Test Leak Check: Phot:      Orsat:
TravwM
Point
NuniDfc
















.










Sampling
Tin*
(min)
0
/o
90
3n
"Vo






















OoCfcrtOM
(24-hour
dodc)
fe&o
ILI&
lt»£k
Halt*
\U> ^L






















Gas Meter
Reading
(Vm)ft3
O5<,-2>d3
333,36
SHJ .^o
•^H^/^O
35-7 *tl<




••
*»/
^O
^
(5
^-
c:^
/
JK-
-








Valocity
Head (Ap)
lnH2O
Oriica Pressure Ditterential
(AH) in H20
Desired | Actual
Stack
Temp.
(Ts)
Temperature
/•':"°F
Probe
Filter
Impinger
Temp.
°F
Dry Gas Meter Temp
Inlet
(Tm in°F)
Outlet
(Tm out°F)
Y////////////////////^^^







\J&£tt£
— • i i

















j*$b
t>f$
t, &
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^








































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^*
^f
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i










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/on
97
t^
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/Cd>
^7
?•-?
9^






















Pump
Vacuum
(in. Hg)
7/7,
"3
•^
'^
*3






















                                                 AH= /
                                                                                                       -
-------
Ir-1	
                            SAMPLE RECOVERY DATA
PLANT
                                                   Run No.    10 -
DATE  5~-
                        Sample Box No.
SAMPLE LOCATION
     TRAIN PREPARER
     SAMPLE RECOVERY PERSON
     COMMENTS

     FRONT HALF
     Acetone
     Container No.

     Filter
     Container No.

     Description of Filter
     Samples Stored and Locked

     RACK HALF/MOTSTTTRE
     Container No.        	
     Liquid Level Marked
                            Liquid
                            Level Marked
                                                   ;0b No.    ^ 4-
                                                   Filter No.
                                               Sealed
                                                Sealed
                                                Sealed
         IMP. NO.
                CONTENTS
                           INFTIAL VOL
                              (ml)
                                                       WEIGHT fgramsi
                                             INmAL
                                                      FINAL
                                                                       NET
                      Hio
                             (o
                                  1 0 o
                                   0
                                             . 3
                                                                   0.3
                TOTAL
-------
                 GAS VELOCITY AND VOLUMETRIC FLOW RATE

Plant:  LASCG       	  Date:  g-tf  ?. o   Pitot Tube, Cp:_^
Stack Dimension, in.  Diameter or Side 1: I'S	Side 2:	
Wet Bulb, °R.
   Tr«v«rM
    Point
   Number
  /;
       6
 A-  /
      JT
               Velocity
                H««J
               in. H2O
               1  / (0
                 Q 1
                               Dry Bulb, °F:.
Stack
T«mp.
                           On
                          2-31-7
Md - (0.44 x %CO2) + (0.32 X KO?) + (0.28 x %r4j)

Md - (0.44 x     ) + (0.32 X    ) + (0.28 X     )

Md -
                                                  % HO      % HO   /f—
                                        M«- Mdx(1 - 	—) -t- 18 (	— )
                                                    100        100
                                        P«-Pb
                                                13.0
                                                                13.0
                                                     =  .1   TS(°R)
                                        Vi • 05.4B x Co X
                                         V« • 65.40 x (
                                                              Pax Ma
                                                         ) x (
                                                                xM
                                         Qs ^=0t x 17.647 x—— x(1	_)
                                           •**           ?•      100
                                                     X 17.047 X-
                                                                            100
-------
Plant-
"ty^ S^-O Sample Type: /V'9 Operator: fifK/tf/'-,
Sampling Loci
Run Number.
itk>n diljM/ •**" /O Pbar ^5?x?O Ps: "" ^ ^ 1
f0-£ 3 Date: ^ / in. Hg. Probe Length/Typi
Pretest Leak Check: Pitot: • — Orsat: 	 Stack Diameter:

Point
Numb*
























<.



Sampling
ThTM
(mln)
O
16
So
•30
s^5























dock Time
(24-hour
dock)
itf'f'3'7
|6)X7
1^1
Od>;*7

•an
32$'
«=?a'9
f^^1 y
&& t
^9!T



Stack
Temp.
(Ts)
Nozzle ID: Thermocouple #: U "^
Assumeo
Meter Bo
Post-Tes
PostTest
Temperature
°F
Probe
Filter
Bws: 	 niter*
x*: /^
tUakRa
LeakCh
Impinger
Temp.
°F
///////////////////////








C>t"7*-
• — .













,










Q
:^HI^B^B^_^B«*
M4 -
Ms -
p5 -
i/s =
H
&.&
j'/sy
/4i?










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^~" O^
-^5
4T^






















: , 	
Y— $^fc AH@ /^AO
te: 0>>0
eck: Pitot:
cfm @ ID
in. Hg.
££L Orsat: -^-2-

Dry Gas Meter Temp.
Inlet
(Tm in°F)
OuHet
(Tm out°F)
s////////////
?Y
O ^
^ 3k
^i5






















Atf_ *^ / ^ 1 ^ .A"Z ^IjCt \ TT7 / CV« y ^'Vi- */— 9 	 O £
flvrn™ j I ' v I j VAp= ' ~ j | AH= 1 { OU !•= o*y*^~ • *^ Tm= ^ -^
^V
?3>
^s
9S'






















'r^JA
Pump
Vacuum
(in. Hg)
9
7
^
-------
                       SAMPLE RECOVERY DATA
°<-V\
PLANT _

DATE  	

SAMPLE LOCATION	

TRAIN PREPARER    PAUL
                                              Run No.    1 Q ~ (a -
                       Sample Box No.  M~7     Job No.
. oo3>
                        QvTvlaA  Filter No.
                                                            NJ
SAMPLE RECOVERY PERSON
COMMENTS

FRONT HALF
Acetone
Container No.

Filter
Container No.

Description of Filter
                            Liquid
                            Level Marked
                                  Sealed
                                              Sealed
Samples Stored and Locked

BACK HALF/MOISTURE
Container No.        	
                                              Sealed

IMP. NO.
I
2
3
4
5
6
CONTENTS
fcT HxO
T^X V^O
Ewc«V«-j
SIUICA. <^£l—


TOTAL
INITIAL VOL
(ml)
/to
/eo
—
2SD



WEIGHT (grams)
INITIAL
»*4
t,tsn
sn..
-------
         EPA METHOD 4 MOISTURE CALCULATIONS




PUNT:	!=££^0	SOURCE/RUN #: lf>U-?» DATE:



1.  Leakage Correction for Volume Metered



    vmc=vm-(Lp-La)x6



    vmc=vm-(Lp-0.02)xe



    Vmc = (       ) - (        - 0.02) x (       )



    Vmc= 31.7.15  .ft-a



2.  Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)



                           Phar-MAH/13.6)N
                            oar*        •'
      lsw- ".D«XVmcXYX
V
                                                        /13.6)
                                              (  553  )
3.  Volume .Water Vapor Collected, Standard Conditions



    Impingers & Silica Gel = V ^  = 0.04707 x (W - W }
                         wstd          v f   i7
                           s              scf


4.  Percent Moisture, by Volume



    B   -

        "
             Vw   + Vm
              wstd    mstd
          /

          (0.54^




                ftr.- I fl
-------
                                METHOD 18 FIELD DATASHEET
         Plant: U5£Q
         Date:_^ii±£
         Location:.
         Run #;   Noft^-\
Stack I.D.:  .sr*
Pbar:    Zfe.ftM
                         \ve
Sample Tube #:.
Operators:   ss
                           - t.-itv
Leak Check: Pre:
                                Post:
V- IT-
            TravcrM
             B^la»*
             Kotnt
            Numbor
               Velocity
                H
               In.
Stack
T«mp.
 °F
                                       Tested Analyte:   S-ki*.^
                                       Orifice Tank #'•       —
            Pump/Rotometer #:  .PJ
            Pt:  Pretest (mm Hg)'	
                Post-Test (mm Hg):_
            Tt:  Pretest fF):	
                Post-Test f F);	:
            Time: Start:IhftS
            W/B:_Z_D/B:_n
Time
1 11*0.01
IHloZ>
*V<.&, ou
i U / "1 / L/ ~
• T v * * LA i
^10 .Z^
y ^7^,7-^
11/15,^
Gauge
Vacuum
(Hg)
/
I
/
-••• • i
/
/
i
Row
Setting
Zj
~L\
l\
7.1 ::
Z(
^1
2.(

K
/(X)
>2ULL_C02:><
                                                Md • (0.44 x %CO2) + (0.32 X %O2) + (0.28 x %l^)


                                                Md » (0.44 X    ) + (0.32 X   ) + (0.28 X
                                                                               : LO
                                                          %HO
                                                           %
                                                                100
                                                                          100
                                                       C D
                                                         '
            Ps-


            &-


            Vs - 65.40 X Cp X



            Vs » 65.40 X (


            Vs-


            A*-
                                                   In. Hg
                                                        Y-?
                                                                    Pa x Ms
                                                                )x(
                                                             ft/8


                                                              2
                                                Qs - Vs x As x 60 s/m
                                                Qs -

                                                Qs -
                                                     acfm

                                                      Pa
                                                              x 60
                                                                      %H,0
                                                                      - —
                                                                       100
                                                Qs

                                                   X 17.847 x-


                                                    dscfm
                                        •x(1	)
                                              100
-------
                                  METHOD 18 FIELD DATA SHEET
/•W
Plant: LMtD
Date: T-/*-^
Location: A^DA
Run#: AJDA-k-^
Stack ID.: V-H - M>*
Pbar: z-s-.y-y
Sample Tuba #• AJOA - inn
""• is • uu

aid 100

Qsjtd™ dscfm
-------
          APPENDIX A. 1.8

             Condition 7
(includes flows, moistures, and Method 18)
-------
                       METHOD 18 FIELD DATA SHEET
         -
Plant: Li&LD
Date:.
Location:
Run #:
Stack I.D.:
Pbar:_
Sample Tube
Operators:.
Leak Check: Pre:
                       Post:
Time
iiA). 5V
:s//. oo
2V 1.1 1
Z3/2- 60

.= ^..3*2-

Gauge
Vacuum
(Hg)
/
/
/
t



Flow
Setting
L^Ot.c.
/.-t.
i£6{.(L
)•/ Total:
W/B:  <^8 D/B: ?V O2: z./  CO2:

Md - (0.44 x %CO2> -i- (0.32 x ^.O^ + (0.28 x %r^)

Md - (0.44 x &  )
                                        Md-
                                                  %H2°,

Traversa
Point
Number
t
i
3
2.
.±1
.30
•V3
.51
.2>t








Stack
Temp.
W
W
7-V
?V
T^V
^•^/
?«v
71

7H
25
^<
5r_T
>^
W
?V
?'/








                                        Ts-
                                        Ps -
                                                13.8

                                              ", 92.   In. Hg
                                                               13.8
 Vs - 65.49 x Co x


 Vs - 85.40 x ( ,'

 V.. 3^T

         10.0*

 Aa-  ''6~7    ft


 Qs« VsxAsxOOa/m


 Q*«

 Qa«
                                                             Pax Ms
                                                                  )x
                                                                xeo
                                                      acfm

                                                        p.
                                              Q« XI 7.847 X - x(1
                                                        Ti
                                                                100
                                                     X17.B47X-
                                                                           100
                                         Q«atd-
-------
Plant:
Site:
           WET-BULB/DRY-BULB MOISTURE CALCULATION
             	Location:  /^.^ £>k-. ^5^
                       Operators:  .T/-f     Run #\
                                                           Date:
                              ~  13.6
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack =   Pbar
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2Q at Tw (from Table) =   Pvw =
                                   (Ps - Pvw) x (AT)
Vapor Pressure of H2O = Pva = (Pvw) -'•-
                                   2800 -(1.3xTw)
                       2800 -(1. 3 x
Proportion of Water Vapor by Volume = Bws
                                                        l.g
(Ps)
Tamp.
OF
0
10
20
30
40
50
60
70
80
90
100
110
120
130
140
150
160
170
180
190
200
210
220
230
240

0
0.0376
0.0631
0.1025
0.1847
0.2478
0.3826
0.5218
0.7392
1.032
1.422
1.932
2.598
3.448
4.525
5.881
7.589
9.652
1240
1549
1941
2347
28.75
3940
4241
5044-

1
3.0398
0.0660
0.1080
0.1718
0.2576
0.3764
0.5407
0.7648
1.068
1.467
1.992
2.672
3.943
4.647
6.034
7.799
9.885
12.48
19.63
19.42
2346
2943
3948
43.11
91.76
Pbar =
Pg =
Ps =
Tw =
Td =
AT =
Pvw =
2
-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: Ln^LO Date: 6-zo—n
Sampling LOG
Run #: /A £ -
atinn- ^v, .r £vU,L.t-f- • Clock Time: /7?j
~7 ^ft - "2- Onflraror?' -^/5-s
Barometric Pressure, in. H
Moisture, %: /. 5
Stack Dimens
Wet Bulb, °F
TrovarM
Point
Number
1
7
3
4
5
L>
. 1
_
3
/|
3
o
7
%









q: ~>%.0\~> Static Pressure, in. HUO: .02-
Molprularwt. Drv: ^.<4 	 Pitot Tube, Cp: ., zJ
t^fj
?5
5~?3
93
£2>
8*"^
g-3

?^
S7^
3 .>
^3
^^
^
lb
7i








fii- *?3
1: !"7 5 Side 2: -
nlh,0p 9-5
Md - (0.44 x %CO2> * (0.32 X %O2> f (0.28 X %N2>
Md - (0.44 x G ) -f (0.32 x :v ) •(• (0.28 X 7V )
Md •• "2.^ CV
% H.O % HO
wa-Mdxd 100 ' '1Dl ,00 '
M.-,o.v.W )X(1- -Lu|L_> + 18<-^S->
T;. ^0, 0F. ^^> °R(°F.460)
13.8 '3.8
Pt. 15.^);. In. Hg
^SF =• , 5C 5G
— / Ts (^R)
Va-«5.4gxU>x JS? x ^ p,xM8


Va • 3»-"'/ ft/a

Aa«).C/*l ft2
Qa • Va x Aa x 60 a/m

••tf TA / / ^ —
Qt • J8,fJ x /. l> / xOO
Qa • Z?0 0 \ adm
i
p, HH20
atd° ' T, 100
-28 fZ /.-6
aid i ' 5*-f ^ 100
                   OHM-
-------
  ?lant:
  Site:
             WET-5ULE/DRY-5ULH MOISTURE CALCULATION
                	-ccaticr.:   /VV.A £*h«»sS-
                               cerators:
                                                                       Gate:   5-
Barometric Pressure, in. rtg =
Static Pressure, in. H2O =
Absolute Pressure ot Stacx =   =bar
Wet-Bulb Tamoerature. °F =
Ory-Bulb Temoerature. °r =
Temoerature Difference. Td - Tw =
Saturation Vaoor Pressure ot HTG at fw (from fabie» =
?bar = _Z
Pg =
Ps =
Tw =
Td =
..?.?£ ,n.Hfl
^T (j
-------
                                  METHOD 18 FIELD DATA SHEET
          Plant:
        I ocatiorv   /Vw.A  E,
        Run *:  ME-7-3
        Stackl.D.:_
        Pbar:   2^.9?
                          . 5
          Sample Tube *•  Mg.
          Operators:  ?A-
          Leak Check: Pre:
                                Post:
I
if

23   •
zi   j


L'-n
              TravarM
               Point
              Number
                        Velocity
                         H««d
                        In. H20
                            JO
                           .vz.

                            1,7,
Stack
T«mp.
 °F
            Tested Analyte:    -^
            Orifice Tank #:	1
            Pump/Rotometer #:_
            R:  Pretest (mm Hg):	
                Post-Test (mm Hg)L
            Tt:  Pretest
                                                    Post-Test fF):_
                                                Time: Start: , ?/3 Finish: /?** Total:
W/B: 6V  D/B:
           O2:<
                                        CO2:  o
0
5
'6
$
Time
2.3i2.,fO
z.3/^67
i3/V, 3^
Z3/5, /O



Gauge
Vacuum
(Hg)
/
/
/
/



Flow
Setting
i&O <• f-
t<,2) + (0.32 X%Cy -H (0.28x%N2)


                                                  •Md-(0.44x «3  )+(0.32x -' )-l-(0.28x 7?-


                                                   Md -  if. S^V
                                                             %
                                                                        % HO
                                                   M.


                                                   Ta
13.8
                                                                           13.8
                                                                in.Hg
                                                 Va - 85.48 X Cp x



                                                 Va-85.48X(  . ^


                                                 V..  •J?.^'    n/.


                                                 A.-   -\.U~\    n2


                                                 Qa - Va x Aa x CO a/m
                                                    Q.-
                                                                —    I   Ta(°R)
                                                                         Pax Ma
                                                  Qt
                          x 17.647 X-


                           dscrin
                                                                                   (i
                                                                                       100
-------
         WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: L^,b
Site: jOdu^^^^,^ Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack = Pbar + -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw
Vapor Pressure of H/>O - Rva - (Pvw) -
Pva=( ,^ } < wt •<«»'
Location: n/u:* u,._.,i
r.i Run ff: w^.-j-'b Date:
Pbar = ^a.^-L
Pq = . "'*>
-^- PS= T*.?
(Ps - Pvw) x (AT)
2SOO-(1.3xTw)
* )x( ,
-------
   as a. 3
                           METHOD 18 FIELD DATA SHEET
__ '-s /9
Plant: L/tSCO TesteH Analyte- Si^^^_
Date: o'-lo-'n Orific« Tank *• —
Location: .^o/* £,)«.,, <..L Pump/Pntnmeter #: i/W* /
Run*: fte-T-i Pt: Pret«st (mm Hg)-
Stack I.D.: z&" i ^ '' Post-Tact (mm Hg):
Pbar: ?4 ?2_ Tf Pr«*««t fry
Sample Tube
Operators: -n/
#-R6-*)-lfl /?/=- 7-/A Roct.Toct CF)-
H Tims: Start: ^* Finish:/^ Total: 3^>_
Leak Check: Pre: / Post: S W/B: -3 _D/FV i f 00: i/ CO0: o
•

Gauge
Time Vacuum
(Hg)
mi, ^6 /
-D3&91 '
1110. -z.1 1
ilTH. L*5 1

M.i0!

5^;
Travaraa
Point
Numbar
I
•i
-*i
•j
.r
U
I
2.
~/
V
7
«.
/
7
5
f
S
6.
I
1
•5
«f
5
o

Flow
Setting
S£o<^^
/30d-
,30 cc.
;<,£»- -

five. -

N^ — j 0 5
Vatocrty
Haad
In. H^O
,06,
.o6»
oT
^7
, o;7
.0^
,//
,0*1
O(f
;OS
o5
^
II
.0^
.06,
,0^
•OCf
• i -L
•06»
.07
0.5
o5
.w?
.1 /
f~o.cn if
Stack
Tamp.
°F
7<*
77
-77
77
7")
T?
-77
-)1
71
-77
-»T
-77
-77
-77
•71
IT
11
TT
TT
7~7
-77
-71
-7 7
11
-7-7
Md - (0.44 x %CO2) + (0.32 X %O2> + (0.28 X %l*j)
7/
Md. ^=7
% H.O % HO
1| Ma-Mdx(1 100 ' *1B( ,00 '
17- Ma-(^)'rl" )x(1- _L_!_) + 18(-L_L)
1 ' 100 100
_,, M.- gS-S "g
Ts- "J-? ^-^O °R(°F^4«))
D- DU ^ S.P. _ , -^ _ , . - "^S"
P8 b HT ' S '-' . 13.0
Pa- D^.^"""? In.Hg
^P - o 5Cp-)V

— J Ts ("R)
Va - es.4* x 
-------
               WE7-3ULE/DRY-5ULB MOISTURE CALCULATION
Plant: (_q $> 0
3ite: ^DO^X, r^^O- Coerators:
3arometnc Pressure, in. rtg =
Static Pressure, in. H2Q =
Absolute Pressure of Stacx = Pbar - -
Wet-Bulb Temperature. °r =
Dry-Bulb Temperature. °r =
Temperature Oifference. Td - Tw =
Saturation Vapor Pressure of H«C at Tw
Vapor Pressure of K,Q = PVa = iPvwi -
Pve.=< . Q0?c; j ( 3S--S-7- So
-scaticn: • ° '
^/•rA "^n ?r '2^'^~> - 1
?bar =
Pg =
-^_ Ps =
' T C 3 -^
> J.o
Tw «
Td =
AT =
drom Table) = 3vw =
'Ps - P'/w» x (^T)
2800 -X( i ^ ) '
T JV\ t.^ d
Date:
?«?,.? 2.
-,6.S
3^-
-------
              GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:  LMco
 Date:   5-20-41
Sampling Loc
Run #: 7^ E
ation: ^rrii^ Ar.i,,.llf,f Clock Time: /7/0
- 1-Z Onflrfrrni's- -rAI5S
Barometric Pressure, in. H
Moisture, %: "O- ft
Stack Dimens
Wet Bulb, °F
Travaraa
Point
Numbar
l
L
3
^
<
0
1
^
-3
if
5
t-
i
2-
•?
M
4
L
t
I
<^
1
q: Z^ 9 7 Static Pressure, in. HUO: •"",£•'?>
Molpnilarwt Hrv ^? ?w PHotTube, Co: .7? .
lion, in. Diameter or Side
-£& Dry E

Vatocny
Haad
in. H2O
.0(9
0^?
• ol
01
.07
.o«
. u
oy
.01
.OS
.06
, /O
.//
J/
•01
OG»
OG
.11
M
,°%
ct*
• OS
Stack
Tamp.
°F
76.
lt-^
7G
7^
-70
-70
^7
11
-T7
71
H
11
11
71
17
11
T7
11
7~1
11
n
7-)
1: Z5 Side 2: Z.V
lnlh.Op. 11
Md - (0.44 x %CO2) ••• (0.32 X %O2> + (0.28 X %*%)
Md-(0.44xO ) + (0.32 x i ' ) -t- (0.20x7 V )
% HO % HO
100 *k °° •&&-
Jr Off
M.-( 2«.^ )x(,.^_).ie(^-)
« p • -•"• / , 2j
13.8 13.8
Pa - 7-$.$n In. Hg
&P- •7-"'"?
— 1 Ts f-'R)

i «r"T"7


v«. /?,jS^1vi

A«« ^iCl ft2
O« av Va « AA v rtO ft/m

Q^ _ (TS'O %^ y j 'Vy ' w QQ
• Qt- 'S^JS^L- «Hm 5^2.^1
X 17.847 X-
 8i
 dadm
                                                                100
-------
            WE7-5ULE/DRY-5ULS MOISTURE CALCULATION
Bite:
                            cerators:

                                                                     Date:  ---<
Barometric Pressure, in. hg =
Static Pressure, in. H,O =
Absolute Pressure ot Stacx =
Wet-Bulb Temcerature. °r  =
Ory-Sutb Temoeratura. °F =
Temoerature Difference. ~d • 7* =
Saturation Vaoor Pressure ot H-G at Tw itrom  Table)  =
                                                       =bar
                                                        pg
                                                          d =
                                                                          -7T
Vaoor Pressure ot hUG = Pva =
Pva
                                         •Ps - f=«/wi x
                                         2800 - n.3x Fw>
                                            .  253Z
                           2BOO-(i.3x
Proportion ot Water Vaoor oy Volume
                                      5ws
Bws =

                           VAPOR PRESSURES OF WATER
                                  In Inenn ot Mercury
  0
  •o
  :o
  30
  «o
  so
  ao
  70
  00
  00
 100
 MO
,120
'l30
 14O
 190
 180
 170
 180
 180
 208
 210
       3
     '.0378
     :083t
     :.103S
     0.1847
     0.2471

     o.uta
     0.739S
      1.032
      1.422
      1.032
      2JM
              :.ioao
              3.J718
              OJ37B
              OJTB4
              0^407
              0.9
               i.e
               1.

               2J7I
                        2
                        O417
 .1127
a.taoa
3^877
ojeoa
O.M01
0.7812
 1.102
 t.913
  3
3.0441
3.0728
3.1186
3.1878
0.2782
0.4082
0.9802
04189
 1.198
 1.981
 2.114
      SJtl


      1
                       2.740
                       3443
                       4.773
'0788
:.i24*
3.1898
3.2881
3.4
O.fl
O.J
 t.178
 1.810
 2.178
 2J11
  a
3.0317
3.0844)
3.1370
                                3.744
                                4J
04120
0.4820
04443
04048
 1.2S3
 1.712
 2410
 3481
 4J
  7
3.0341
3.0882
3.1428
3.2203
04240
0.4
                                                      a
                                                    3 0371
              7.7»
                       1X77
                       !(
                       II
                                8.180
                                1840
                                1347
     2X17
     2UI
         2447
         301
         3fl
                 J4S1
                 9413
                 6481
                 1041
                 1347
                 18JO
                 20JD
                                                9.109
                          8J07
                          11.12
                          1340
                          174*
                          2140
04382
 1.283
 1.789
 2470
 1180
 4.174
 1442
 7.0M
 8481
 1148
 \t
 174
:.isoa
3.:
3.4
3.4
0.1
OJ
 t.a
 1.810
 2444)
 3490

 3488
                                   1U
                                   14
                                   1841
                                                                  2747
                                       31.10
                                                            in. Hg
                                                            in.r^Q
                                                            in. Hg
                                                            °F
                                                            °F
                                                            °F
                                                            m. Hg
                                                                                  in. Mg
-------
cza
              GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: ut^o Date: 2-^>-^
Sampling Loc
Run#: KE-
ation: fy>wi e*kur/- Clock Time: ' ?V ?
7-~^ Oneratorr •rt/f*
Barometric Pressure, in. H
Moisture, %: /- *
Stack Dimens
Wet Bulb, °F:
TrmrM
Point
Numb«r
i
^
3
V
5
0
/
7
->
V
1
U
1
z
•5
1
5
o
i
i
3
M
5
0


q: ef.9z. Static Pressure, in. HUO: —.^3
Molecular wt.. Drv: 7ff ?V Pitot Tube, Cp: -2Z_
ion, in. Diameter or Side
•** DrvB

Velocity
H.td
in. H20
,06
•o7
,O(D
,OG
ol
-08
.09
8
.oCn
.(^5
,05
./O
/2>
<0^
•OG
,05"
,0^
>/0
,IO
•°1
,05
.0^
,06>
./o

«F-,Zd52
Stack
T«mp.
°F
17
77
")?
-)7
1U
^7G
-71
77
if
11
71
1G
7^
^70)
'16»
7 * (0.32 X %O2) t- (0.28 X %N,j)
Md-(0.44x 0 )> (0.32x^.1 )*(0.28xTl )
Md- 2-*.^
% HO % H20
Mc-M«iJi(l • 1QO ) io< 10Q I
M.-(^.^ )xd- -^35- >* ie(^TS5->
M.- -i8-"13
T;. n °F- 531 °n (°p*4«3)
Pt - Pb + SP' - (l&tf'i. ) + 	
13.0 '3-8
P«- Z^.^l In. Hg
^P . , Z6 5 2-
— . | Ts (^R)
Vi-«b.4«xCpx VAH x \j p,xM8
- 1 — I i>"2T
V«- 85.48 x( .9? )»(.165Z. )XA 	 i£J 	
V T^.D A-Z.f.~»3
v« • /?.oG> ft/i

Aa.^.^T ft2
Q* • V« K AA v 6O ft/m

Qt. ,f.OO x -V,C ' X«>
0.. ^00 .dm
P« %«z°4
Q.itd=Q.Xl7.647x — x(1--^-)
•«^-fl /.o
0.^.5000 xir.e47x_2T-_x(1.-jS-)
-------
200.,
        Plant:
        Site:
                  WET-BULB/DRY-BULB MOISTURE CALCULATION
                                        Location:
Operators:   fft.     Run
                                                  ~ 7 -
                                                                   Date: s~--
                                                      Pbar =
                                                        Pg =
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of StacK =  Pbar
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =                          Td =
Temperature Difference, Td - Tw =                    AT =
Saturation Vapor Pressure of H2O at Tw (from Table) =   Pvw =
                                    (Ps - Pvw) x (AT)
                                                                  /9
Vapor Pressure of H20 = Pva = (Pvw) -

Pva=( ,
                                           2800-(1.3xTw)
                                          2) X (   ,?     )
                               2800-(1.3 x
        Proportion of Water Vapor by Volume = Bws
(Ps)
Tamp.
OF
0
to
20
30
40
50
60
70
80
90
100
110
120
130
140
150
160
170
180
190
200
210
220
230
240

0
0.0370
0.0631
0.1025
0.1047
0.2476
0.3626
0.5216
0.7392
1.032
1.422
1.932
2.596
3.446
4.529
5.681
7.569
9.652
12.20
1520
19.01
23.47
28.75
35X0
42.31
5044-

1
3.0398
0.0660
0.1080
0.1710
0.2576
0.3764
3.5407
0.7648
1.066
1.467
1.992
2.672
3.543
4.647
6.034
7.759
9.865
12.46
15.63
19.42
23.98
29.33
35.68
43.11
51.76
                                                                       ,,0
                                               in. Hg
                                               in.
                                                                              in. Hg
                                                                              o.-
                                               °F
                                               in. Hg
                                                                              in. Hg
( TJ-.tl )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
15.99
19.84
24.48
29.92
3647
43,92
52.70
3
0.0441
0.0728
0.1186
0.1 B78
0.2782
0.4052
0.5602
0.8183
1.138
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.36
13.07
16.34
2027
24.97
30.52
37.07
44.74
53*5
4
0.0463
0.0768
0.1248
0.1955
0.2691
0.4203
0.8009
0.6462
1.175
1:610
2.178
2.911
3.848
5.031
6.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.57
54.62
5
0.0469
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2243
2.553
3.S5&
5.SS3
6.660
8.557
10.66
13.67
17.07
21.14
26.00
31.75
38.50
48.41
5540
a
0.0517
0.0646
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.650
8.767
11.12
13.98
17.44
2149
2643
3248
3924
4727
5640
7
0.0541
0.0692
0.1429
0.2203
0.3240
0.4666
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.981
11.38
14.30
17.82
2245
27.07
33.02
3949
48.14
5741
9
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.819
2.449
3.259
4.269
5.585
7.202
9.200
11.65
14.62
1821
2242
2742
3347
40.75
4843
5843
9
0.0598
0.0962
0.1567
0.2383
0.3493
0.5035
0.7144
0.9989
1.378
1.875
2.521
3.391
4.406
5.732
7.384
9.424
11.92
14.96
1841
2249
28.18
3443
4142
4043
9947
-------
,  c
 *3
K
    ?l
       Plant:
       Date:
                      - 9 *?
         Location:  CiMf/v1
         Run *:  90- I
 METHOD 18 FIELD DATA SHEET
	    Tested Analyte:_
	    Orifice Tank #:_
                Pump/Rotometer
         Stack I.P.:   i S'
         Pbar:.
         Sample Tube *r 9-7-M   ir o  Post: .
Time
IS*-/*}
/scq
IS l^
^"IV
/5'^


Gauge
Vacuum
(Hg)
O
O
O
O
O


Row
Setting
^Td; ^A*,





\
— 7-



^
/ ^
              Point
             Number
                 5
                      V«lodty
                       H
                      in.
                         ,0*1
                                             Time: StartLL!i^Finish:jii£Tota!:_££_
                                             W/B: —  D/B:  — O2:  —  CO


                                             Md - (0.44 x %CO2) + (0.32 X %O2) + (0.28 X %Nj)


                                             Md - (0.44 x    ) -t- (0.32 X    ) + (0.28 X
                                                                   %HO
                                                                   —-
                                                             100
                                                                       100
                                                I.-
                                                         SB
     Stack
     T,mp.
                                    i(o

                                    //.. V
                                      o")
                                                V« • 65.48 x Cp X
                                                V« « 85.40 x (
                                                         fir*^-lZ

                                                             )x(
                                          )x
I
                                                 Qs-
                                                                    xflO
                                                 QHW—
                                                                                      - /. 2 ^
                                                                                  100
                                                                                           Ifi.
-------
Plant	
Sampling Location  g)U (Ov
Run Number:
     FIELD DA IA SHEET
Sample Type:  flj- V   Operator:^ S/G
                                                           fc-
                                                                                   Nozzle ID:
Pretest Leak Rate:
Pretest Leak Check: Pilot:
Date:
 cfm
                                                         Ps:  —
                                                         02: -^
                                                                 Assumed Bws:
                                                                              Thermocouple #:
                                                                              Filter #:  — - —
                                                                 Meter Box #: )  cfm @ ^£ in. Hg.
Stack Diameter:  /J'      As:  /.Z5-/V*      Post-Test Leak Check: Pilot:  — Orsat: ~
TrwwM
Point
Numtwr




	





















Sampling
Tim
(mln)
r>
/ft
OA
•1°
V,






















dock Tim*
(244iour
dock)
/ty^t,
I$QO
K/a
i< 3>ft
j<^n






















Gaa Meter
Reacfing
(Vm)tt3
N9I/6*
^»S.5&
V^.-vs"
i/K <^
*<63.^i<






















V.locrty
Head (Ap)
lnH2O
Orifice Pressure Differential
(AH) in H20
Desiied | Actual
Stack
Temp.
(Ts)
Tempeiature
°F
Ptobe
Filter
Impinger
Temp.
°F
Dry Gas Meter Temp.
Inlet
(Tm in°F)
Outlet
(Tm out°F)
Pump
Vacuum
(in. Hg)
Y/////////////////////M


























l.fL
(.$&
/x§6
j, e^>










































































'••





.-•"" .'


•'. '








r:

































^«
srt
-------
                       SAMPLE RECOVERY DATA
PLANT
DATE
            tMa>
                                             Run No
.?-?-/
                      Sample Box No.
                                             loh No.
SAMPLE LOCATION
TRAIN PREPARER
SAMPLE RECOVERY PERSON
COMMENTS

FRONT HALF
Acetone
Container No.

Filter
Container No.

Description of Filter
Samples Stored and Locked

RACK HALF/MOTSTTfRF
Container No.        	
 Liquid Level Marked
                           Liquid
                           Level Marked
                                             Filter No.
                                             Sealed
                                             Sealed
                                              Sealed
    IMP. NO.
               CONTENTS
          TOTAL
                          INITIAL VOL
                             (ml)
                            /(*>
                           to
                                                WEIGHT fgramsi
                                       INITIAL
                                                    FINAL
                                                  010.3
                                                                NET
                                                                0.  S
                                                                            /A III
-------
        EPA METHOD 4 MOISTURE CALCULATIONS


PLANT:   U<^o _ _ SOURCE/RUN #: JL2^L_ DATE:


1 . Leakage Correction for Volume Metered
    Vmc=(       )-(        -0.02) x(
    V   = _      ft
    vmc  - ll
2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)

                          Pbar+(AH/13.6)N
    Vm   = 17.64 xVmrxYx
       std         mc            Tm
    Vm   = 17.64x(
      mstd         v
     v
      mstd
3. Volume Water Vapor Collected, Standard Conditions


    Impingers & Silica Gel = V...   = 0.04707 x (W. - W.)
                         wstd            T   '


                          'std
                          rstd

                        Vw   = 0.04707 X(
                       V   =_ili§_scf

4. Percent Moisture, by Volume
                          w
                          wstd
              v    ,  v
               wstd   mstd
         -
      ws~
-------
3-B.a. cia
                    GAS VELOCITY AND VOLUMETRIC FLOW RATE
Pi^nr /flWr, . Date: A-.90-?9
Sampling Loc
Run#: £'7-
ation1 OlfS.f\J ** <9 Clock Time: /$tPG
-7 Operate"^- £)&Y/<3G ,
Barometric Pressure, in. H
Moisture, %: "~
Stack Dimens
Wet Bulb, °F:
TravanM
Point
Number
/9- \
3
3
- Static Pressure, in. H«O: • ~£ft
Molecular wt.. Drv: — Pilot Tube, Cp: , ?£.
ion, in. Diameter or Side
DrvB

Velocity
in. H2O
< 11
••19
, l'~>
»• ^"t)
/^ 3H
, Qf5

, 1 1
, 9o
Q.9
- 9o
.30-
. 91











Stack
Temp.
°F
/6t
iG'~)
Ib^
.00
//& -t- (0.28 X S,!^)
Md - (0.44 X j } ••- (0.32 X ~i\ ) f (0.28 X~l 5 )
Md » '>£•'? H
% H.O % HO
4Wi 1ft/ ^
• JA V W » ^& f
^ 13.8 13-8
Pa- 7
-------
                  FIELD DA IA SHEET
Plant:
LA^db Sample Type: /V\ - M Operator: b&/C&
Sampling Loci
Run Number:
ition OlDifA) *^ Pbar 0  '
y-")-^ Date: 5'3Cr9"7 CO2: 	 O2: 	
Pretest Leak Rate: , Cfin cfm @ /$ in.
Pretest Leak Check: Pitot: — -Orsat: —

Point
Numbe



























Sampling
Time ;
(rrtn)
DO
/°
9C,
i 0
|c






















dock Time
(244iour
dock)
/^l\
\QS\
IS '31
1^4-1
i°i*5 )






















Hg. Probe Length/Type
• 	 Stack Diameter: _/
j; j 's'^ Pilot #: S" 3
S'1 As: 1,23-ft2
•
Gas Meter
Reading
(Vm) ft3
V£S. 6V<5
4^1 .1 '>7.3
^•Q J ,4-13
•S*c.*?, 4-"7_J
5^-j 9<9





Xl-i
.3
.•^
V

^

n ' ^
o
^
^
r
b




Velocity
Head (Ap)
inHZO
Oriioe Pressure DirlerentuU
(AH) in H2O
Desired
Actual
Stack
Temp.
as)
Nozzle ID: •— Thermc
Assumed Bws: ' Filter #
Meter Box #: / ^
Post-Test Leak Ra
•couple »: VA
Y:/9£kAH@: /..(7-'=i
le: (SXl)'>
Post-Test Leak Check: Pilot:
Temperature
°F
Probe
Fater
Impinger
Temp.
°F
cfm @ i^ in. Hg.
	 Orsat: — •

Dry Gas Meter Temp.
Inlet
am in°F)
Outlet
am out°F)
y///////////////////////////////////////////^^







\}&.LC£rf

,O°i
( \ 3
r I*"?
'
y 4.


















-•~



y/f
S>¥
\j --7
^^ X
J '7






















^^ i?
o o
5^7
9o










«











Pump
Vacuum
(in. Hg)
-/^
3
3
3
2>






















AVm-
Tm=
JJ
-------
t	
                             SAMPLE RECOVERY DATA
     PLANT
DATE
                             Sample Box No.
SAMPLE LOCATION
     TRAIN PREPARER
                          ^ T Ou
     SAMPLE RECOVERY PERSON
COMMENTS

FRONT HALF
Acetone
Container No.

Filter
Container No.

Description of Filter
      Samples Stored and Locked

      RACK HALF/MOISTTTKF
      Container No.         	
      Liquid Level Marked
                                  Liquid
                                  Level Marked
                                               Run No.

                                               Job No.

                                               Filter No.
                                                       •  /
                                               Sealed
                                                     Sealed
                                                Sealed
         IMP. NO.
                CONTENTS
                    Ox H2o
                         N
                TOTAL
                           INITIAL VOL
                              (ml)
                              (00
                                                        WEIGHT (grams)
                                              INITIAL
                                                      FINAL
                                                                        NET
                                                                ' \
                                                                                   ./(I!
-------
        EPA METHOD 4 MOISTURE CALCULATIONS



PLANT:   U
-------
J ag
                   GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: £/?SC°>
.. 9^
, QQ
,os








Stock
T«mp.
°F
DPS'
^>£9
99^ -S'
3 ,5kO
9>9£>
P9S'


3P
Md - (0.44 x O ) -f (0.32 X 1,\ ) f (0.28 X "71 )
Md- ^T'^Y
% HO % H.O
M. -Mdxd IOQ ) * 1B< IOQ )
1,7 t>>
M.-(»<.1^)x(1--T—- )*l8(-j— -)
Ms- 9^ -TO
71- 33n °F- l*^6? 0R(°F*460)
Pa — Pb * = ( 3 i* Q3) +• ^— 	 	 ' —
™ i3.a su.q?; ,3B
p.. 9^-^ in.Hg
^- .HZI
— , | Ts ^R)
vi-«6.4yxcpx ^SP x ^ '"'p;;1^

V.-05.48X( TT )x(.-n\ '^35.^^
V.-^5'50 fM

A.- 1-3? n2


oc. l»-^<> x \-^^ xeo
Qt- ^31"? adm
Pt *H,°
Ot^- Q« XI 7.847 X 	 x(1- -—^-)
•» j, 100
•yy.%0, V.3
Q-rtd- »?^Ki7Jir« — ^Y"'0*"^
-------
ago eg
                       METHOD 18 FIELD DATA SHEET
Plant: L/)^jO T«st«H Anaivte- Srv/teA1* :
D
L
R
S
P
S
C
L

2%fS'
^0/60
3^-11
3^'93
t/ -^
2,%'^
Hi. <°
ft.b*
\2^L
ate: S'-^c- '-) 9 Orifico Tanir 4- 	
acation: OUZ/U X*-/0 Pump/Pntnmfiter #: - -
un #: /tf - 7 - .X Pt: Pret«c* (mm Hg)- -
tack I. D.: JS " Post-Test (mm Hq); —
bar: £S#9 Tf Pmtoct (°P)' —
ample Tube
Jperaiors: D
#• )C -7 - 5.^ /O f-9 A Po«t-Tflst <°R • - —

eak Check: Pre: -aco Post: • oco

to ^L  ^>
1-73^ o
11^3 O
1 ~> S"3 0
/ 6 6*3 0
Flow
Setting
?&ct/n
• ' ' i



y
\ x
^TATI(L ~~ • PI
Traverse
Point
Number
fl-»

_y
^
f
c

.A-;
o>
^7
*y
<;~
ds












Velocity
. /^)
' / "5
I L->
90
- £c'
^ Q ^7

' ^ 6,
, 55
C3 1
, I ^
'0O
»<9V










<^—
WfcP X«V^
Stack
Tamp.
95? l
;9^7/
.9 s? •£
.5»9V
&3(3
g Si. C(

5-3O
^SS"
0 "V?
?P '? 5?
J^? tf
9$'%











ftSlS
Time: StartLLlsi_Finish:j8o2__Total:_(46 — ^
W/B: — D/B: — O2: — CO«:— ~^
Md - (0.44 x ttCOj) + (0.32 X %O2> + (0.2B X %N2>
Md-(0.44x ^ J-M0.32X Zf ) •»- (0.28 x"7? )
^ V ^ % H-O % H20
•fe/^ -3 V'? '"^
W-T'" 39e) °fr-(i'XAI


A. _ V« ^J **


Qa • Va x Aa x flO a/m
•7 J JJ a-7
Qg-O'l'Q^x I- »)XflO

Q*_ ^.tj^-j •**"
P« SHjO


D*.*<, _ ( • J .


^^•_|gjfjaj 1 (J ^ 1 OflflVD
-------
                                     FIELD DATA
Plant U\>CO
i •
Sampling Location duiCH & )£,
Run Number: 1 C -7- 2 Date:
Pretest Leak Rate: , OCO cfm @ / 1>' in. Hg.
Pretest Leak Check: Pitot: 	 - Orsat: — -
Sample Type: f^\ ' I
Pbar 2-&&1 Ps:
CO2: 	 	 O2:
Probe Length/Type: /
Stack Diameter: /,}' "
Operator: P#ty Pilot*: ST-3
As: I • M -ft*
Nozzle ID: 	 	 Thermocouple #: n u
Assumed Bws: — Filter*: 	
Meter Box #: ;
-------
                        SAMPLE RECOVERY DATA
PLANT """^ * c ° ¥f°'d v cr
DATE ^-^-«!\ Sample Box No. *
SAMPLE LOCATION ^\0 ^oc^ ^ ;obNo Vi'l.oo?
Filter No. /VA
TRAIN PREPARER
SAMPLE RECOVERY PERSON

COMMENTS
                                    4 r>U
FRONT HALF
Acetone
Container No.

Filter
Container No.

Description of Filter
                            Liquid
                            Level Marked
Samples Stored and Locked

RACK HALF/MOTSTTIHF
Container No.         	
 Liquid Level Marked
Sealed
                                                Sealed
                                                Sealed
IMP. NO.
1
2
3
4
5
6
CONTENTS
0* Uno
or wto
^•I v~(^
S , 1 ( <"„ CjAJL


TOTAL
INITIAL VOL
(ml)
[;OW
1 OC?
-
390



WEIGHT (granui
INITIAL
GlG^
6o(?J
4*71-3
^SU



FINAL
63^-7
L^oo,6
^.1
"l^G.y



NET
' 2.1
o.g
&M
573


%3
-------
        EPA METHOD 4 MOISTURE CALCULATIONS


PLANT:  Laj-'2-  DATE:


1 . Leakage Correction for Volume Metered
    Vmc=(       •)•(        -0.02) x(       )


    V   = _ ft3
    vmc  - ll


2. Volume Metered, Standard Conditions (68  F, 29.92 in. Hg)


                           Pbar-MAH/l3.6)N
    Vm   = 17.64xVmrxYx
      mstd          mc
                                  m
     v
      mstd
 3. Volume Water Vapor Collected, Standard Conditions


     Impingers & Silica Gel = V w   = 0.04707 x (Wf - W.)


                         Vw   = 0.04707 x( *r
                           rstd
                         vw   =  -        scf
                          wstd
 4.  Percent Moisture, by Volume

                 V,
           	wstd
     BWS=       ~
                wstd    mstd
     B   -
     DVVS-
      '**—-	                                             /»»
-------
                 GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: _

Sampling Location:  QU<£A*'

Run#:J^> 3>
                     Date:   $ - 9C - 9 1

                     Clock Time: Q&&O
                                             Operators:.
Barometric Pressure, in. Hq: £>fr'.93	  Static Pressure, in. HgO: 	

Moisture, %:               Molecular wt., Drv:   ""       Pitot Tube, CD:  , 9S
Stack Dimension, in. Diameter or Side 1:   15 ''	Side 2:		
Wet Bulb, °F:
Bulb,°F:.
Trovara*
Point
Number
/M
•^
^
V
f
&

A- /
.0
^
H
<
6













Velocity
Head
in. H2O
' /O
MS
M
.l^
,95'
r^^

.. 3rt
/- 5 i
..0)
,/<5
.9'
, yH













Stack
Tamp.
°F
35? "I
9^0
937
ST79
2.9.?
2 $7

asi
atj f (0.32 X %O2> * (0.28 X %NZ)



                                       Md - (0.44 x ^  ) + (0.32 X ~*~\  ) -t- (0.28 x"? T  )


                                       Md.   3*-«lf


                                                  % HO      % HO
                                       Mt . Mdx(1 - 	—) •*• 18 (	— )
                                                   100         100
                                                        100
                                          . 3-8.10
                               liL_
                                100
                                                             °R(°F+430)
                                               oa             _ «I
                                             + -i-^-^ ( >30
                                            =Q« xi 7.647 x - x(l- - — )
                                                       T«       100
                                        Qt-M-  ?5"3? X 17.647 X-   ,
                                         «W                   6.1-2,
                                                     dwtm
                                  •xd
                                        100
                                                                                  .///f
-------
•3-3 Q 3
u-ac=;
METHOD 1 8 FIELD DATA SHEET
Plant: ^iO Tester! AnaK/t«- $A/ «.^«_
C
L
F
S
F
£
C
L

t4So o
g'S'O ;o
i S ^ aft
/ "S 2.&> i°
fe*o Ql
_ '*y« si
/5*to
^\): (b.oZ.
%--B%
Jt
)ate: ^-Zfl-'H Orific« Tani< *• -
.ocation: MDft Pump/Rntnmeter ^: v*0^^ * a-
iun #: NDA-1- 1 Pt: Prefect (mm Hg)-
Jtackl.D.: 52"xi2T>11 Post-Test (mm Hg): -
sbar: ^it Tt: Prfitset <°R-
sample Tube
Operators: •«
*!A;nfl-l-»fl MOA-1-/R Post.Teet (°R: ~
»-55
.eak Check: Pre: // Post: ^


Gauge
Time Vacuum
(Hg)
14 ^5^-7 ,
' ^ -?•? . so r
«?qn-7l^ '
,^3.2, /
/ ^s- , ^ i
•.IW.IS I
\ 5oo0 t»7 1
Flow
Setting
2.1
2.1
1-\
2 /
^.i
Z/
3^

Trav«re«
Point
Numbar

























Vatocity
Haad
In. HjO

























Stack
Tamp.
°F

























Time: Start^sb Finish: Jl5& Total :J^6 	
W/B: — D/B: - O£: -Li CO2: ^3
Md • (0.44 x -fcCOj) -f (0.32 X %O2> + (0.28 x %^)
-r*
/ A\ u j /<» 4^ „ \ j. /rt ^9 v ^ ^ fO 5B x 1
?3
w Md-
% KLO % HO
^ M.-Mdx(1.^-).18(-i^-)
^ Ms " ( )x(1- 	 )-i-18( 	 )
^ 'M 100 100
c|/ M«-
Q3 Ts- °F- °R(°F + 4flO)
o p
D« . DK i °'' ' -, / \ J.
13.8 13.8
Pa - In. Hg
V5p-
s= J Ts ^R)
V» - 65.W x Cp x V^ A y p8 x Ma
Va - 65.40 x ( ) x ( ) x Al
Vs- ft/a
A.- n2

Qa-VaxAaxeoa/m

Qt- x x80

Qa - acfm
Pa *«2°
Qa^.- Qe xl 7.047 x 	 x(1- — -2- )


Q^rtd" xi7.e47x x(i- iflo )
•
Qtttd" dacfm
-------
                                 METHOD 18 FIELD DATA SHEET
          PlantL
          Date:_
         Location:_
         Run #:_M
         Stack I.D.:_
          Sample Tube *; /\/nft-i-zA~/7pfe-7-23
          Operators:   ^5     	
          Leak Check: Pre:  /    Post:  .^"
                                          Tested Analyte:_^
                                          Orifice Tank #:	
                                          Pump/Rotometer
                                          Pt:  Pretest (mm Hg):	
                                               Post-Test (mm Hg)L
                                          Tt:  Pretest (°F):.
                                               Post-Test fF)L_r_
    13
\ •->
z*
Time
\ SCJO.^-JL
i So 5 . 3-7
/ .56 5. . Finish: ^^iTotal:.
                                           W/B: —  DIB: —  O2: a  CO2:


                                           Md - (0.44 x %CO2) + (0.32 X %O2) + (0.28 X %N2>
                                                 Md - (0.44 x
                                                 Md
                                                         (0.32 X
                                      (0.28 X

                                %H20

                                  100
                                                                  100
                                                                            100

                                                         e p
                                           Pa-


                                           &-


                                           Va • 65.48 x Cp x



                                           Va - 65.40 x (


                                           Va«


                                           Aa-
                                                              in. Hg
                                                                   Y-STsr
                                                                  )x(
                                      )x
f
                                                               ft/a
                                                  Qa-VaxAaxeOa/m
                                                  Qa-

                                                  Qa-
                                                                         x00
                                                         aefm
                                                  Qt ...iQex 17.647 x-^-x(1- —•*-)
                                                    •tn           Tg      100
                                                  Q«atd"
                                                              X 17.847 X-
                                                         dacfm
                                                                        •x(1
-------
          APPENDIX A. 1.9

             Condition 8
(includes flows, moistures, and Method 18)
-------
DQC7
         Plant: L /Ud£>
         Date:.
               5-z^-n
 METHOD 18 FIELD DATASHEET

	     Tested Analyte:_
	     Orifice Tank #:_
                                                                 <>V,/,~/v>.
        Location:.
        Run #:  /vig-
        Stack I.D.:
        Pbar-
       Sample Tube #:
       Operators:  fA
        Leak Check: Pre:
                               Post:
of «?•/

oS '3
     /o
                  Pump/Rotometer #:  ./ - 18 ( 	 i
                              100         100
                                                                1.2
                                                                100
                                                                           100
^y, 1 • <_ - ,o7
Travarse
Point
Number
i
2
T
V
•f
6
1
1

1
I
3
H
5
/,
1
tf







TSu -
Velocity
H«aa
in. H^
-Z.-7
^/
j,3
, ^3
. b'-f
. 2~J
•^ "i
. */ ?>

18
. 30
- 12
. 51
,32
32
• )>3
.32-







O.5>il
Stack
Tamp.
°F
-rJ
-73
w
"I'-f
7V
"?y
7T 2-H  dadm
                                                                        x60
                                                                        %HgO

                                                                         100

                                                                        Z9 5
                                                                        S3V
                                                       i.q
                                                       100
-------
         WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: i-^(o
Site: M/VIM &u>titf,r- Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of Stack = Pbar ± -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw
Vapor Pressure of K-.O - Pva = rPvwt -
Location: . r?tjur.,
ME,
T^ Run #:££-Date: ;'-z?-4-i
2^-5" in. Ha
• * 2- in. HnC
2
zf-5 in. Ha
r? °F
T*V Op
/5 °F
. -To 3 .r in. Ha

                               2800 - (1.3 X Tw)
Pva =(   503. s  ) -
                  2.1. S
                                                     30
                    2800-(1.3 x  «;

Proportion of Water Vapor by Volume = Bws

                      (  .i
                                                1-2.%
                    VAPOR PRESSURES OF WATER
                         In Inches of Mercury
in. Hg
Tamp.
OF
0
10
20
30
40
50
60
70
80
90
100
110
120
130
140
150
180
170
180
100
200
210
220
290
240

0
0.0378
0.0631
0.1025
0.1647
0.2478
0.3028
0.5218
0.7392
1.032
1.422
1.932
2.506
3.446
4.52S
5.881
7.560
9.652
12.20
15.29
10.01
23.47
28.75
35.00
42.31
5044-

1
0.0398
0.0660
0.1080
0.1716
0.2576
0.3764
0.5407
0.7648
1.066
1.467
1.002
2.672
3.543
4.647
6.034
7.750
0.885
12.48
15.83
10.42
23.06
20.33
39.88
49.11
51.78

2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.740
3.642
4.772
6.100
7.052
10.12
12.77
15.08
10.84
24.46
20.02
36.97
49.02
52.70

3
0.0441
0.0728
0.1186
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.820
3.744
4.000
6.350
8.150
10.38
13.07
16.34
20.27
24.07
30.52
37.07
44.74
5945

4
0.0463
0.0768
0.1246
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.176
2.911
3.848
5.031
6.513
8.351
10.61
13.37
16.70
20.70
25.48
31.19
37.78
45.57
54.62
	 j
5
0.0489
0.0810
0:1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.005
3.054
5.165
6.680
8.557
10.86
13.67
17.07
21.14
28.00
31.75
38.50
48.41
5540

8
0.0517
0.0846
0.1370
0.2116
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.650
8.767
11.12
13.08
17.44
21.50
26.53
3248
39.24
47.27
58.80

7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4666
0.6669
0.9352
1.293
1.785
2.370
3.160
4.174
5.442
7.024
8.081
11.38
14.30
17.82
2245
27.07
39.02
3040
48.14
5741

8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4856
0.6003
0.9666
1.335
1.819
2.440
3.250
4.280
5.585
7.202
9.200
11.65
14.62
18.21
2242
27.62
39.67
40.75
4049
5849

9
0.0596
0.0082
0.1567
0.2383
0.3403
0.5035
0.7144
0.0080
1.378
1.875
2.521
3451
4.408
5.732
7.384
9.424
1142
1448
1841
2240
28.18
9449
4142
4043
5047.:
                                                                   J.
-------
^^m ^M
 aca
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: LA&6' Date: S-zz.-'n
Sampling LOG
Run #: «*=
ation: /v»^;/, /r-v/wA Clock Time: -"^-s-
- ion, in. Diameter or Side
d.3 DryE

Velocity
Heed
in. H2O
,zy
, >/
. S2
?>/
*£,
-3S
.Vd;
,v */

,iS
.i7
17
7?
7T
71
77
77
-7 7

-7-7
•7"?
^^
11
"77
-77
77
71









1: /7 ^ Side 2: —
ulh.op- 71
Md - (0.44 x %CO2) -t- (0.32 x %O2> + (0.28 x%r^)
Md»(0.44x & )-t-(0.32x^/ ) + (0.28 x ' r ) .
Md - Z.S'S'''
% HO % HO
M< - "2^, ^0
1~3.8 13.8
Ptm 2. n2
Q> • Vs x AB x 00 s/m

Q« - i+y^tS x / " "7 xOO
Qt- ^5^^ aefmfttsT)
P.^ %H,0
0,itd-Q.xl7.e47x — x(1.-j^-)
K4,trh <^/ 2*'^ . . '»-5
nd 5 3 -7 100
-------
 Plant:
 Site:
           WET-BULB/DRY-BULB MOISTURE CALCULATION
                 	Location:  /vie -i^L-   /n<;,
                 C^A.  Operators: rA    Run #:  ,
                                                      -.S in. Hq
^\ (. -S °F
-7~» 0P;
AT= 1* °F
Pvw =
• 5*t>    =        (
T*mp.
 OF
 o
 10
 20
 30
 40
 50
 60
 70
 80
 90
 100
 110
 120
 130
 140
 150
 160
 170
 160
 190
 200
 210
 220
 230
 240
(Ps)
0
0.0376
0.0631
0.1025
0.1647
0.2478
0.3626
0.5216
0.7392
1.032
1.422
1.932
2.596
3.446
4.525
5.881
7.569
9.852
1220
1529
19.01
23.47
28.78
35.00
4241
5044-
1
0.0398
0.0600
0.1080
0.1716
0.2576
0.3764
0.5407
0.7646
1.066
1.467
1.992
2.672
3.543
4.647
6.034
7.789
9.885
12.48
18.83
19.42
23.98
2943
35.88
43.11
51.78
                                                                        in. Hg
( it.; )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1603
0.2077
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
15.98
19.84
24.46
29.92
36.37
43.92
52.70
3
0.0441
0.0728
0.1186
0.1876
0.2782
0.4052
0.5602
0.6183
1.138
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.36
13.07
16.34
2027
24.97
30.52
37.07
44.74
5345
4
0.0463
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.176
2.911
3.848
5.031
6.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
48.57
54.82
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.660
8.557
10.86
13.67
17.07
21.14
26.00
31.75
38.50
48.41
5540
8
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.650
8.767
11.12
13.98
17.44
21.59
26.53
3248
3924
4727
5840
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.981
11.38
14.30
17.82
22.05
27.07
33.02
3949
48.14
5741
8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
•1.819
2.440
3259
4.289
5.585
7.202
9.200
11.65
14.62
1821
22.52
27.82
33.87
40.75
4943
5843
9
0.0598
0.0982
0.1567
0.2383
0.3493
0.5035
0.7144
0.9989
1.378
1478
2.821
3.381
4.608
£.732
7.384
9.434
1142
14.96
1841
2249
28.18
3443
4142
4043
9047
                                                                                  J,.
-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: t-(\•"/ F
ation: \ })c. ;,v r x h c, ,„ r Clock Time: y^ o 3
S '- 7 Onerator^' "?# / ss
Barometric Pressure, in. H
Moisture, %: 1'$
Stack Dimens
Wet Bulb, °F
Travara*
Point
Mum bar
/
t
^
V
5
G
-7
J'

/
T_
i
4
5
t,
1
tf









q: ~>Q, <$ Static Pressure, in. hUO: cz
Molecular wt.. Drv: *-*-W Pitot Tube, Cp: .-*?
.ion, in. Diameter or Side
67 DryE

Vatocrty
Haad
in. H2O
, ^2^
. ^'
!>3
, i3
. 3G
.i?
. *//
.^/Z.

26
7 4
' ^- ^5
,26
.32.
,30
,3>3
• ^
,33







Stack
Tamp.
C^"2>
90
.50
5'0
gro
8*0
T^
f^)

-------

         WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: L$6(J)
Site: MO^* <2skfaJJr Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack = Pbar ± -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of HpO at Tw
Vapor Pressure of H/jO = Pva = (,Rvw) -
( 2*.£ -?i S?<
Pva=(,5£6i. ) 	 — 	
Location: M** -zt'tw Post-Test (mm Hg):
Pbar: H.* Tt: Pretest fR-
Sample Tube
Operators:
#'.AIZ-*-I A fir-S-l* Post-Test fF):
Trl- ' Time- Start: cy-sy Finish: «"# Total: 3c7
eak nherk- Pre- :/ Pnsr^X W/R- <4i n/R: •?/ On: 2 ' CCV o


Gauge
Time Vacuum
(Hg)
T7s/riy <
77^3, 2 Z /
1-1^,95 /
-nnL.^0

l/;n- >/,% ^

Flow
Setting
/ •>£><"-
/ !?O f <•
T
/ 1
,/'
,0(j>
.^6
. oi
.Of
Stack
Temp.
°F
~\l
T 1
Tl
Tl
Tl
Tl
11
1 '
70
-70
70
70
-1 /
11
-I/
T
I (
-l'
Tl
->/
^>
^/
T
Md = (0.44 x %C02) + (0.32 X %02) f (0.28 x roNj)
^5 ,> c^
Md = ' "
V?
% H,O % HO
0 ' 100 100
'/""5 Ms - ( "ifr. W ) x (1 - 	 '• 	 ) -r 18 ( — i 	 )
^ ( ' ( 100 100
Ms « T-? . -\ 3
^^
T, . -!< °F= S-5/ °R (°F.460)
_ p. S.P. , 7« £ , . ~ .^X
13.6 13.6
Ps= -z.'J.V^ in. Hg
^P = 2-6 26
-= 1 Ts <°R)
Vs » 6b.49 x Cp x 
-------
           WET-BULB/DRY-BULB MOISTURE CALCULATION
Plam:  Lfa£0   	Location:  fig - f- \    n<
      	      Operators:  _>   Run #:
                              -  13.6
Site:	
Barometric Pressure, in. Hg =
Static Pressure, in. HgO =
Absolute Pressure of Stack =   Pbar
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H^O at Tw (from Table) =   Pvw =
                                   (Ps - Fvw) x (AT)
                               Date:  5-&->
Pbar = 7.9. S
Pg = ~,0-Z-
Ps= 11. 45
Tw = _-?C
Td= ' T
AT = &
Pvw = . VS 2-0
in. Ha
in. HO
2
in. Hq
°F
°F
°F
in. Hq
Vapor Pressure pf H2O = Pva = (Pvw)

Pva =(  _^
        2800 -(1.3xTw)
- .  fsu) )x(   if    }
                       2800-(1.3 x
Proportion of Water Vapor by Volume = Bws
                         (
                                                      l.O
(Ps)
Tamp.
op
0
10
20
30
40
50
60
70
80
90
100
110
120
130
140
150
160
170
180
190
200
210
220
230
240

0
0.0378
0.0031
0.1025
0.1047
0.2478
0.3828
O.S218
0.7392
1.032
t.422
1.932
2.598
3.444
4.525
5.881
7.589
9.852
1250
1559
19.01
23.47
28.7S
35.00
42.91
50.84-

i
3.0398
0.0880
0.1080
0.1710
0.2578
0.3764
3.5407
0.7648
1.088
1.467
1.992
2.872
3.543
4.647
6.034
7.7S9
9.88S
12.48
18.83
19.42
2340
29.33
3540
43.11
51.76
                                                                     in. Hg
( i*.y5 )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0896
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.842
4.772
6.190
7.952
10.12
12.77
15.98
1944
24.48
2942
3647
4342
52.70
3
0.0441
0.0728
0.1160
0.1676
0.2782
0.4052
0.5802
0.8163
1.138
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.38
13.07
16.34
2047
2447
3042
3747
44.74
CT.B3
4
0.0463
3.0766
0.1248
0.1955
3.2891
0.4203
0.6009
0.6462
1.175
1.610
2.178
2.911
3.848
5.031
9.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
4547
54.62
5
3.0489
3.0810
3.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.680
6.557
10.86
13.67
17.07
21.14
26.00
31.75
38.50
4641
58.60
6
0.0517
0.0846
0.1370
0.2116
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.850
8.767
11.12
13.96
17.44
2149
2643
3248
3944
4747
5640
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6869
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
6.981
11.38
14.30
17.82
2245
2747
38.02
3949
46.14
5741
a
0.0571
3.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1841
2242
2742
3347
40.75
4948
5643
9
0.0598
0.0982
0.1 907
0.2383
0.3493
0.5035
0.7144
0.9989
1.378
1.878
2.521
3451
4.406
5.732
7.384
9.484
1142
1446
1841
2249
28.18
3449
4142
4949
5947
-------
Plant:  L
                 GAS VELOCITY AND VOLUMETRIC FLOW RATE

                	  Date: 5 -
Sampling Location:
     E;   f?/£-fr-Z.
                                                      Clock Time:  
Moisture, %:    (. o	Molecular wt., Dry:   zftg*/    Pilot Tube, Cp:  . ??
Stack Dimension, in. Diameter or Side 1:     ^^1e$  if?"  Side 2:.
Wet Bulb, °F:	
Dry Bulb, °F
                                       °
Trovare*
Point
Numb«r
\
-i
•j.
>
y
5
i/
;
2.
*
V
5
6
/
2.
3
4
5
6
;
z.
3
^
5
^


Vttocity
H*«d
in. H20
.OB
-06
.01
• 0'7
«0g
.0%
.10
/O
. oi
. O(s
,06
. ./a
,'3
.09
.01
,d>6
.ol
. 11
./i
,o -i- (0.32 x ^.O^ -t- (0.28 x %^)


                                                          -V  ) -t- (0.28 X 1
-------
              WET-BULB/DRY-BULB MOISTURE CALCULATION
 Plant:   l^U)                                Location:  2... ..;=./.- J
Site: &.w frUurf- Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack = Pbar + -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td • Tw =
Saturation Vapor Pressure of H2O at Tw
Vapor Pressure of H00 = Pva = fPvwi -
yii. Run *: ££££&-**&
Phar= ^'^
Pg= ~-M
_P2_ Ps = Z«.*tf
13.6
Tw = $6
Td = -Tf
AT= ;5"
(from Tahlp) = Pvw = , 7^°_
(Ps - Pvw) x (AT)
i: 5-2^-47
in. Hg
in. H_O
2
in. Ha
°F
°F
°F
in. Ha

 Pva = (   n 5 2.0
                       (  *«*
                                    2800-(1.3xTw)
                             •«**)*("  ,<      )
                            2800 -(1. 3 x    S(,

 Proportion of Water Vapor by Volume = Bws
 Bws =
     (Pva)
     (Ps)
Tamp.
 °F
 o
 10
 20
 30
 40
 50
 60
 70
 80
 90
 100
 110
 120
 130
 140
 150
 160
 170
 180
 100
 200
 210
 220
 230
 240
  0
0.0376
0.0631
0.1025
0.1847
0.2478
0.3626
0.5218
0.7392
 1.032
 1.422
 1.032
 2.506
 3.446
 4.525
 5.881
 7.560
 9.652
 1220
 1520
 10.01
 23.47
 28.75
 35.00
 4241
 50.84-
  1
0.0398
0.0660
0.1080
0.1716
0.2578
0.3764
0.5407
0.7648
 1.066
 1.467
 1.002
 2.672
 3.543
 4.647
 6.034
 7.750
 0.885
 12.48
 15.63
 10.42
 23.06
 2843
 35.68
 43.11
 51.76
                                                                           in. Hg
( M.«f )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0096
0.1127
0.1803
0.2077
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.740
3.642
4.772
6.180
7.852
10.12
12.77
15.08
10.84
24.46
28.82
36.37
43.82
52.70
3
0.0441
0.0728
0.1180
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.629
3.744
4.000
6.350
8.150
10.36
13.07
16.34
2027
24.07
30.82
37.07
44.74
83.85
4
0.0463
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
6.513
8.351
10.61
13.37
10.70
20.70
25.48
31.13
37.78
4847
54.62
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.054
5.165
S.660
8.557
10.86
13.67
17.07
21.14
26.00
31.75
38.50
46.41
5540
a
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.083
5.302
6.850
8.787
11.12
13.08
17.44
21.50
26.53
3248
3024
4727
56.60
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.370
3.160
4.174
5.442
7.024
8.881
11.38
14.30
17.82
22.05
27.07
33.02
30.80
48.14
57.61
a
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
•1.819
2.448
3.259
4.280
5.585
7.202
0.200
11.65
14.62
1821
22.52
27.62
33.67
40.75
40.03
5843
9
0.0598
0.0982
0.1567
0.2383
0.3403
0.5035
0.7144
0.9080
1478
1.875
2.521
3.391
4.406
5.732
7.384
0.424
11.82
14.86
1641
2248
28.18
5488
4142
4043
5847
-------
                 GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:.
Sampling Location: _n
Run#:  ,-f^- 6-
                                                      Date:
                                                      Clock Time:   //,<
Barometric Pressure, in. Hg:   £? 5"	  Static Pressure, in. H2O:_
Moisture, %:     -1 *       Molecular wt., Dry:  ?.*.*$    Pilot Tube, Cp:.
Stack Dimension, in. Diameter or Side 1:     z e"
Wet Bulb,°F:      5*1         Dry Bulb,°F:	
                                                      Side 2:
Travare*
Point
Numb«r
/
7.
3
-y
s
Lf
i
2.
J
4
^
/•»
,
^
3
.f
5
C
r
i
•b
H
5
(^


V«tocrty
H««d
in. H2O
co>
,07
.66
.OU
.0%
.07
i/O
,09
,^7
,C*e
.oT
: ^>^
i/ 3
, ^o
.C?Ca
,^>G
,07
, //
./o
.063
0(,
.oi,
.^7
JO

Stack
T«mp.
°F
7V
•?«-/
7V
"7^
-7V
"7-V
7V
~IL\
7V
74
7V
-7V
7V
•7V
7^
7^/
-?*y
-7V
-7V
"7V
74
-7V
74


^P. .ai6?|rl- IV
                                       Md - (0.44 x ttCOj) + (0.32 X %02> +


                                       Md - <0.44 x CJ   ) +• (0.32 X  Zt ) + (0.28 X

                                       Md -  ^ ^_y
                                        Mt -
                                                   P-
                                               13.8
                                                          ) +
                                                              -Av
                                                               13.0
                                        Pa-
                                                    in. Hg
                                        V« - 85.40 x Cp x



                                        Va - 85.40 X (  •'' ^
f
                                                             T3(°R)
                                                             Pax Ms
                                        A..   ,        n

                                        Q« • VsxAaxeoa/m

                                        »-

                                        Qg.
                                                      aefm

                                                        Pi
                                             .Qtxl7.e47x	X(1
                                                        Ti
      X00



     SHgO

      100
                                                     X17.047X-
                                                                           •n
                                                                           100
-------
Plant:
Site:
           WET-BULB/DRY-BULB MOISTURE CALCULATION
          L-'J ^ •- ••*	              Location:   P
                                                     > i//\
                                           (A
                                                               "iJ
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack =   Pbar
^X— Operators: TA/SS   RUn #:  ££'$-3
                             Pbar =	
                              Pg = _
                              Ps =	
                              Tw =	
                              -  13.6
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =                         Td =
Temperature Difference, Td - Tw =                    AT =
Saturation Vapor Pressure of H^O at Tw (from Table) =   Pvw =
                                 ,,.. (Ps-Pvw)x (AT)
Date:   S'/^.z/ ° 7
       	 in. Hg
       	 in. ^0
       	 in. Hg
                                                        -.c-V
                                                          \ 1
Vapor Pressure of H2O = Pva =
                                   2800-(1.3xTw)
                                   )*(   O     )
                       2800-(1.3 x   $"-7
Proportion of Water Vapor by Volume = Bws
(Ps)
Tamp.
OF
0
10
20
30
40
50
60
70
80
90
100
110
120
130
140
150
160
170
180
180
200
210
220
230
240

0
0.0376
0.0631
0.1025
0.1847
0.2478
0.3628
0.5218
0.7392
1.032
1.422
1.932
2.596
3.446
4.525
5.881
7.569
9.652
1250
1558
18.01
23.47
28.75
35.00
4241
5044-

1
0:0398
0.0660
0.1080
0.1716
0.2570
0.3764
0.5407
0.7648
1.066
1.467
1.882
2.672
3.543
4.647
6.034
7.758
8.885
12.48
15.83
18.42
23.86
2843
35.68
49.11
51.76
                                                    °F
                                                    in. Hg
                                                                      in. Hg
( 
-------
i~==
                    GAS VELOCITY AND VOLUMETRIC FLOW RATE



      Plant-  //><(*' (^                                 Date:  fc 5^3 -
Sampling Loc
Run #: 9- X
ation1 OOfAr&. *? Clock Time: /T-.f7.?^
- / onerarnrs- -/Y^ /<$*
Barometric Pressure, in. H
Moisture, %: -- 	
Stack Dimens
Wet Bulb, °F:
Trov«rM
Point
Number
A - i
Q
' •>
w



fir )
3
3
f
<
6









•



q: ^°i. ^ Static Pressure, in. HUO: - .is>°l
Molecular wt.. Drv: " Pitot Tube, Cp: r jL*i
ion, in. Diameter or Side
'" 	 Drv B

Velocity
in. H2O
- l9
. ,5/
- 23
- 33
• 22
90











Slack
T«mp.
°F
fff' '
it,"2*
/&>4
Ha?
j(j£

j£>'2y
/(&n
1'7L?
Ik a
no
J ' fo*7











i

1: ft" Side 2: -
nlh,0p- 	 	
Md - (0.44 X %C02) -t- (0.32 X %O2> * (0.28 X%Nj)
Md - (0.44 X ) * (0.32 X ) t- (0.28 X )
M Md «1 %"2°> 18(%H2Q)
100 100 ,
Ma- Zfc.lrl*
e p
Pa - Pb * b'K = ( ) + 	
13.8 13.8
£P = .^°
— | Ts I^RJ
V» « 85.4B X Cp X VAP x U p, x Ma
, /

Vi- 32.. ^^'o «/•
I Z2.T- ^
A..^^, ft
Qs • Va x At x 80 a/m

Qs ~ J?3 \t^~~ x x *
Q> • ~L-'&0?) aefm
p. %HjO
«W T, 100

«td .. * * too
-------
a a
                      METHOD 18 FIELD DATA SHEET
.,
1
l/dvJA^
<6 34>
*><*>'"
•(*>*>*
6ft •'n
(0(0 A\
•6gS*
X7^3
&*
^ *
Plant: £/Kff
Date: ^-^-9°
Location- C9i' £j^ * 9
=lun#- 9-.V-.9v
Stack I.D.: />
. Ou
. QH

^ /•?
• 9 /
, y;}
rQ3
' ,9^5
O 3-










)^
/4P rVVO
/




/

Stack
T«mp.
°F
/^/
' t
l(a
L,
it'j
,(t<*
Tk9
//, .^r

/ fc
/ to
^
7
/^s
nn
; 6,
7
; d><


m








l&t>
Time: Start;c^;( Finish:^o^iTotal:_^l.
W/B:_z^D/B:^^02: — COgiJrz^.
Md - (0.44X%CO2) + (0.32X%02) + (0.28 x*^)
Md - (0.44 x ) -I- (0.32 X ) ••• (0.28 X )
£o/ro
1 Md - .05 C-< .
^» %H,0 ,H20 p^
^Mt-Mdxd 	 i_) + 18 <—-£-) \- '
3A(S3 100 100
PV u. , \»M ) + 18( 	 )
mv' 10° 1°°
^ M,. zi-^
T«- ILU °F- I.Z.U °B(°F-K4ao)
s p . - i/'i
p.-pb*^Il-- + — Zk —
13.8 13-8
P.. ^.H^ In. Hg
fiF - o-4MO
— J Ta^R)
V«-«5.4QxCpX VAP X W p8xM«

Va- 3Z.6?/ n/«
A.- |.2^| n2
O«- VaxA«xoOa/m
Qs- x xeo
0*- 2.3H ufm
Pt %H7°
Qs ..»Q«x 17.647 X— x(1 • — -— • )

Qi^- X17.047X 	 X<1« 1fl0 )
QHtd- )^iZV dMfen
-------
Plant  tA$£G	
Sampling Location ®j£rJ * 9
Run Number: 7"§* ^  Date: J>
Pretest Leak Rate:  .«oz-   cfm @
Pretest Leak Check: Pitot: -—Great:	
              FIELDDAiASREET
                        JjJ/_ Operator: D
                                       -
Sample Type:
Pbar    '
CO2:
                         Ps:
                         O2: —
Nozzle ID:  -~—
Assumed Bws: —  Rlter #:
Meter Box #: /£    Y:,
                                  Thermocouple #:  V (3
in. Hg.    Probe Length/Type: / ' 5 <>    Ptot *: Tg-^   Post-Test Leak Rate: ..-»>»  cfm @ JT in. Hg.
         Stack Diameter:
As:
                                        Post-Test Leak Check: Phot:  	Orsal:
Point
Number



























Sampling
Tim*
(mln)
O
10
^tfl
*^^^\
\ f}
1+ «*J
^-i^—




















dock Time
(244iour
dock)
0994L
B <• Q '•>
01^7^

£>y$"3-
r*Gd> •>-
/oo 5^





















Gas Meter
Reading
(Vm)ft3
^V9, ^7<
$"£?,. ^51
S &&/ 1 O C*
S 73 > V o
* 	 ' 	 1

*




















Velocity
Head (Ap)
lnH20
Y////////


























Orif ce Pressure Differential
(AH) in H2O
Desired
'//////,
I-3L
1 ft*
/<$£
*.*•<*






















Actual
Stack
Temp.
fTs)
Temperature
°F
Probe
Filter









































































































Impingei
Temp.
°F
'/////
£>Q
L/6
£~Q
£ 1






















Dry Gas Meter Temp.
Inlet
(Tm in°F)
'/////,
?3
?3
^3
^Y






















Outlet
(Tm out°F)
Pump
Vacuum
(in. Hg)
///////////.
9$
S (&
& ^"}
ff^






















-------
355
                           SAMPLE RECOVERY DATA
PLANT

DATE
                                                  Run No.
                    HI	Sample Box No.  A/-O     Job No. _

    SAMPLE LOCATION    M °\  Qu^o 
-------
         EPA METHOD 4 MOISTURE CALCULATIONS


PLANT:  JA^D _ SOURCE/RUN #:_L_^lL DATE:


1 .  Leakage Correction for Volume Metered
                    (        -0.02)x(


                   ft3
2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)


                           Pbar+(AH/13.6f
            17.64 xVmcxYx

 3. Volume Water Vapor Collected, Standard Conditions


     Impingers & Silica Gel = V w   = 0.04707 x (Wf - Wj


                         Vw   = 0.04707 x( ii.
                           'std

                         Vw    =  5-?^    scf
                          wstd
 4. Percent Moisture, by Volume

                 V,
     R             wstd
     bws
                wstd    mstd
                                                               M.A
-------
                 GAS VELOCITY AND VOLUMETr.iC FLOW RATE
Plant:
Samoung Location:

Run #•  9 -
                                      Date:  $'99>^~)

                                      CIocx Time:   / *,'/ ^
Barometric Pressure, in. Hq:  ^,3'Q        Static Pressure, in. HgO:^

Moisture. %:	        Molecular wr.. Dry:	Pitot Tube. Cp:

Stack Dimension, m.  Diameter or Side 1 •   /5"'	Side 2~  •	—
Wet Bulb. °F:    	
      .1
               '/•teeny
               n M,
                 3
                 l'/
-«-'
                XT.
                            •mo.
                            ' a _
                          If.
          f. 4-
                         ILL
        AC;
                       Md • 10 44 K %CO.) ^ '0.32 X %CX) - (0.28 X %»*,>




                       Md»i044«    :  •• <0.32 x     > . (0.28 X
                                          • Md i n
. M,O      % H,O


 lOO        100
                                                 i x ( i
                                                        10O  '       100
                                       M*.
                                               SP.

                                               13.8
                                                               1 3.8
                                                    [

                                        /• - A3.4U K Co X «AP x  \
                                                            PllM*
                                       V« - 09.40 I|
                                         - 32.. <
                                                        ) a (
                                       ot.
                                                       Pi      %H.O
                                       Q8.M-otair.e4TK — «o-   ^
                                         •"            T»       tOO
                                        °---
                                   X 17.647 X<
                   r|l«
 (M*.  «




 '^tti

^n^Kw
                                                                          108
-------
f
      VA
                                   METHOD 1 8 FIELD DATA SHEET
Plant;.
Date:
                        c
                     - .3
                        /O
Location:
Run #:  / 0 - y - /
StackI.D.:  If"
Pbar:
                       o«/7* <•
            Sample TubAe
            Operators:.
Leak Check: Pre:_
                                   Post:
                 Time
                Trovcre*
                 Point
                NumtMr
                 -1

      ±
                 Gauge
                Vacuum
                  (Hg)
                             0
                             c
                             o
                              o
                V«lodty
                 HMd
                In.
                  \
                             IS
                             9
                            Row
                          Setting
                         ,95'0
                            Stuk
                            T«mp.
                             °F
                                       Q/ V
                                       •3 ?
                                             ^t>>

                                          9m
                                       Tested Anaiyte:.
                                       Orifice
Pump/Rotometer #: •	
Pt:  Pretest
                                                       Post-Test (mm Hg)L
                                                   Tt:  Pretest
Time: Start: Q?kvnnish:'(Qf»fe Total: S~&



Md • (0.44 x %CO2) + (0.32 x XCty + (0.28 x %r^)


Md - (0.44 x     ) + (0.32 X   ) + (0.28 X
                                                            %H_0

                                                       *ia(^->


                                                       llb-**18'-^1
                                                            °R(°F*460|
                                                      -Pb+-±l_-
                        13-e
                                          • ^a  ^j^   In. Hg


                                           - D-H53


                                        Vl - 85.48 X Cp X JE? X Y



                                        Vs - 65.48 X (


                                        Vt- -SM.IM.3)   W«
                      Pax Ma


                 )x(        )x
                                                                                ^
                                                                           xM
                                                     OB.. - Qt x 17.047 x -^- x (1 -
                                                      •«           T«       100
                                               Hlft
                                                                                          .//./»
-------
                                              FIELD DA IA SHEET
Plant:  LA$CO
Sampling Location    >Q
Run Number: JO-?- I   Date:
Pretest Leak Rate:  ,OO 1  cfm
Sample Type: ;*) - 4-   Operator:
Pbar 3*j 3^    Ps:   -o.ftz
CO2: •*	      O2:	
Pretest Leak Check: Pitot:
                             )£ in. Hg.
                         Orsat:  ^1
Probe Length/Type: t'
Stack Diameter.   jlS'"
   Pitot #:
As:
Nozzle ID:	^
Assumed Bws: _
Meter Box #:  | ^   Y: ^
Post-Test Leak Rate:
Post-Test Leak Check: Phot:
                                                                                                   Thermocouple #:
                                                                                                   Filter
                                                                                                           AH@:
@ '7 in. Hg.
 Orsat: —
Traverse
Point
Number



























Sampling
TbiM
(mln)
0
10
ao
?>0
40
la





















OocfcTfcns
(244iour
dock)
?T54-
GSkrf)tf
OtlM
O^^
O^^
®8T^





















Gu Meter
Reading
(Vm)«3
rn.^sf
^.•3s /^
5" 33 .- ^o
^^/ / 10
	 	 —
^V73'0





















Vtkxaty
Head (Ap)
lnH2O
Oriica Pressure Dtftorential
(AH) in H20
Desired
s //////'/////////

























•
}.Jt>
l'$b
l/?b
I/ ^6






















j Actual
Stack
Temp.
(Ts)
Temperature
°F
Probe
| Filter
Impinger
Temp.
°F
//////////////////////////////








































































































KO
51
5^
56






















Dry Gas Meter Temp.
Inlet
(Tm in°F)
'/////,
-75
oa
-7*r
70


















.-.' '•.•.;:•'-' '



Outlet
(Tm out°F)
/ f / / / /
~> ~>
?
-------
                       SAMPLE RECOVERY DATA
PLANT
DATE
                                              Run No.
                                                         0- ?-)
                       Sample Box No.  V-/     Job No.
                                                              OO3
SAMPLE LOCATION   ' # IP
                                     oTi«rT   Filter No.
TRAIN PREPARER   ___

SAMPLE RECOVERY PERSON  	

COMMENTS            MM"   P\h?iUtE.
FRONT HALF
Acetone
Container No.

Filter
Container No.

Description of Filter
                            Liquid
                            Level Marked
                                               Sealed
                                               Sealed
 Samples Stored and Locked

 RACK HALF/MOISTURE
 Container No.        	
 Liquid Level Marked
                                               Sealed

IMP. NO.
1
2
3
4
5
6
CONTENTS
03T H,C)
nr J-LO
•^-i*p/\j
/
3:/;* r~l


TOTAL
INFTIAL VOL
(ml)
^oo
,06
• 	 .
"Z4O



WEIGHT (grams)
INITIAL
t,3?<7

1^,1
•756,4


H^C.5
FINAL
C^/.o
^•^t y
t^.7
9GI.5


"i^ofz.
NET
• ;*.;
- p.f
. L.
r. /


f6
-------
        EPA METHOD 4 MOISTURE CALCULATIONS



PLANT:  /. &*._n _ SOURCE/RUN #' io -&*\  DATE:


1 . Leakage Correction for Volume Metered
    Vmc=(       )-(       -0.02) x(


                   ft3
2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)




          = 17.64
                   11 iu    \        ^
                                  m


                                   )x
    Vmstd=    '^    dscf


 3. Volume Water Vapor Collected, Standard Conditions


    Impingers & Silica Gel = V...   = 0.04707 x (W. - W.)
                         wstd             f    '

                        Vw   = 0.04707 x(
                           rstd


                           'std
 4. Percent Moisture, by Volume




     B           VwStd
     °WS-    w    + w

               wstd   mstd
     B   -     (
     Bws—;	
-------
                GAS VELOCITY AND VOLUMETr.iC FLOW RATE
Plant:
Sampling Location: j^
Run
                            Date: __5	
                            Clock Time: /'QgQ
Barometric Pressure, in. Hq: P9 ,• f 0
Moisture. %:
                                         Ooerators:.
  Molecular wt.. Dry:.
                   Static Pressure, in. HoQ:  ~
StacK Dimension, in. Diameter or Side 1:
Wet Bulb. °F:   •	
    Point
  0-  /
              v.iocnv
               Ii
   Stack
  I/O
                          It
                        9/C,

                        '313
on
Pilot Tube. Co: /9^
Side 2:	
                                     Md - <0.44 • %CO.l •>• (0.32 X %O,) ~ (0.
                                     Md - <0.44 x    )  * 40.32 X    i - (0.2B X    )
                                     Ms • Md x (1
                                                ioo
                                                  .; . ie<
                                                    too
      iH3O

      100
                                                              too
                                            S.P.
                                            13.8
              P..
                          ,„.«,
                                                          \cm
                                     V« • 0S.40 X (       ) » (       IX


                                     V.. JHJ1    */•


                                     A..  |.227   n2
                                        t
               Qs-

               Q*«


               °-dd-
                                                           xM
                                                             ,
                                                           108
                                                 X17J47X-
                       •\tv
-------
FIELD DA IA SHEET
Plant:
L43G.O Sample Type: AV ll Operator: /^ )/Ci6
Sampling Location GOi£/U it- Jfi Pbartt)<^v5o Ps: *-« ff ?) 7
Run Number:
/0.K.3 Date: S"->7-9"7 CO2: '- 	 O2: 	
Pretest Leak Rate: p>? cfm @ /5 in
Pretest Leak Check: Pitot: - — Orsat: —
1
Traverae
Numb*



























Sampling
Time
(mln)
O
;0
£h
'^0
*/r>






















Clock Tfcne
(24-hour
dock)
HMO
M SC
)9CO
jO/fj
I-1A6






















Hg. Probe Length/Typ<
— Stack Diameter: )
3. / '55 Pilot*
.^*j-* .*..
S" As:/.2i^' ^

Gas Meter
Reacting
j«r A ^ ^ftdw)
Ti? V f f ^rTrT^
^^/ ,6/0
§99 - &£>
too?/ H"7
CK. 5c4-





/i __ I
/^i
. b
"L
5^
&>

•A 1
•3
*3
£ i

« XT-
1-5




1 $•/
f < ff y3
; . '§£,
( •• &h
t< 9 6



j

























§f/^<2 <

























. '"IV^Vi

Z/Ci
rj S
ai^-
>/5
i l-f
7/5

7 Jv
•> lr
> yj'
''U
')((,
J't











?
-•


























>/ :

^ -

^T-.O"



*








r^O
<>&
^'t,
r.s





>l.^l

jb^i,

l&SH








• •."



^S^
ps
i^r^
$>±





fp>

«C-frH

db «-.-f m.








-: -



Outlet
(Tm out°F)
^/yT/s
£&
5>.p
f? C
if 7


















••••••



Pump
Vacuum
(in. Hg)
^
gf'S
'£
-s-






















                                            . .
-------
        EPA METHOD 4 MOISTURE CALCULATIONS


PLANT:  LA-g^-b _ SOURCE/RUN #: J£JL


1 . Leakage Correction for Volume Metered
    Vmc=(       )-(        -0.02) x(

         ^^l - ft3
2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)


                         /Pbar+(AH/13.6)N
    V^ 17.64 xVmcxYx^	—



    Vmstd=17.64x( 3,.u^ )x(  /?OW  )x



    Vm   = 2 H7_   Hsrf
      mstd       "

 3. Volume Water Vapor Collected, Standard Conditions


    Impingers & Silica Gel = V w   = 0.04707 x (Wf - W.)


                        Vw   = 0.04707 x(  34.2.
                         wstd


                         wstd

 4. Percent Moisture, by Volume

                 V,
     n   _ 	WStd
     Bws-    ^7
               wstd   mstd
-------
                        SAMPLE RECOVERY DATA
PLANT

DATE
                  "7
                        sample Box No.
                                               Run No.   I Q -

                                               Job No.
SAMPLE LOCATION
TRAIN PREPARER
                      /O o^J
                                               Filter No.
SAMPLE RECOVERY PERSON
COMMENTS

FRONT HALF
Acetone
Container No.

Filter
Container No.

Description of Filter
                             Liquid
                             Level Marked ' "
                                                Sealed
                                                Sealed
Samples Stored and Locked

BACK HALF/MQrSTTTKF
Container No.
 Liquid Level Marked
                                                Sealed
    IMP. NO.
                CONTENTS
           TOTAL
                           INFTIAL VOL
                              (ml)
                                                   WEIGHT (grams)
                                         INITIAL
                                        G57.0
                                                      FINAL
                                                                   NET
-------
ooa
                              METHOD 1.8 FIELD DATASHEET
        Plant:.
        Date:
                                              Tested Analyte:
                                              Orifice Tank #:
       Location:  AJ.DA-
       Run #:_
       Stack I.D.:.
       Pbar:	"•
       Sample Tube #-.
       Operators:    rrt
                                                Pump/Rotometer #:_
                                                Pt:  Pretest (mm Hg):	n
                                                    Post-Test (mm
                                                Tt:  Pretest fF):_
                                                                         •**
                                                    Post-Test fF):_
       Leak Check: Pre:
                                Post:
                                                                         •• Total:
                                                                          CO,
0? 13
»
Ji
.fa
Time
)t\ S.$*
,s /? . 11
ifzi, -*>•?-
l5i-s. i-x.
\ ^ 2Ce. H'?
/$^q,os
\/*^ » J. ;o
Gauge
Vacuum
(Hg)
/
,
,
i
I
/

Flow
Setting
11
x.
r /
^l
-»-i
^'
X
    Time: Start£7_£s_ Finish:.
    W/B:  -  DIB:-	O~:
                                              Md = (0.44 x %C02) 1- (0.32 X %O2) T (0


                                              Md = (0.44 x     ) -»• (0.32 X    i * (0.28 X


                                              Md =
7£>   Ms = Md x (1


     Ms •= (


     Ms-


     Ts-
                                                            H.O
                                                             £_;
                                                            1 00
                                                                   % HO
                                                                   - —
                                                                    1 00

                                                                         100
                                                                   °R (°F.460)
                                                      S.P.
Trav«rs«
Point
Number


























Velocity
Head
in. HjO


























Stack
Temp.


























13.6 13.6
Ps - in. Hg
_
VSP =

1 T /Oai
	 1 Ts rn)
V3 - 03.»» X >-p X ^U-- t \| P3 X MS


u
Vs - ft/S


AS • n

Qs - Vs x As x 60 s/m

Q( m X X 60

Qft — acfm
Ps *HiO
Q$ .= Qs X 1 7.647 X 	 x (1 • )
8td T. 1 QO
""• IS i uw



Q«ttd" dsdm
-------
                                     METHOD 18 FIELD DATA SHEET
Plant: t-"5<& Kr.Jv/cA
Date: waa/
Run #: /s/D^-9-7. A^
Stack I.D.: 0 .5" * >2"
Pbar: zi.3
Sample Tube #: AiDA *'-z^, /i/afl .s-2&
Operators: H / r/\
Leak Check: Pre: ./ Post: iX
Tested Analyte: Siyj-f^
Orifire Tank *• -
Pump/Rotometer #: t^st rt"
Pt- Pretest (mm Hg): -
Post-Test (mm Hg):
Tt- Pretest <°R:
Pnst-Test rF): —
Time: Start: of 2* Finish:/^-' Total:_
W/B: — D/B: - O«: ^ CO^:


>




oo
o
    O
    100«
   1 « V|
»<»

~L°
          40
Time
IS^ iH
-------
          APPENDIX A. 1.10

             Condition 9
(includes flows, moistures, and Method 18)
-------
                            METHOD 18 FIELD DATA SHEET
Plant:j
Date-
            -2z-C(_
,J0S<-



^
6«
Gf'
li
13
            Time: Start:'€os  Finish: '<*# Total: ^
            W/B: CC,  D/B: ff  )-t-(0.28x7?  )

            Md =  2-2
                                                 Mdx(1
                                                    100

                                                    x(1 •
                                                              )00
                                 % H2O

                                   100

                                •) •- 18(
                                             Ms «= (
                                             Ts-
Ps - Pb +-1L. = &. zf, )+  •c~i-
        13.6              13.6
                                                                         100
Ps= 29.
                                                           m.Hg
                                              Vs-
                                              Vs - 85.49 x ( . ^ t   ) x (
                                                                   )x
                                         ^
                                              Af
                                              Qs » Vs x As x 60 s/m
                                              Q» -
                                                              Ps
                                              Q»..j= Qs x 17.847 x	
                                                8td            Ts
                                                                 x 60
                                                                %H20

                                                                 100
                                                           X 17.847 x-

                                                   3k)*
-------
Plant:
Site:
           WET-BULB/DRY-BULB MOISTURE CALCULATION
                  	.	 Location:    |Mftm  t
                       Operators:  TA    Run #:
                                 13.6
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of Stack =   Pbar t
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H20 at Tw (from Table) =   Pvw =
                                   (Ps - Pvw) x (AT)
                                                          Date:   ,^-A-<
Pbar= M-2-B
Pg = O.tl
Ps= 2Llt
Tw = UC>
TH= ^
AT= IS
Pvw = v>. u^2_
in. Ha
''in. H,0
in. Hg
°F
>p. •
°F
in. Ha
Vapor Pressure of H2O = Pva = (Pvw) -
                                   ,2800-(1.3xTw)
Pva =(
                )-
                  (
                                                             &
^'13
                       2800 -(1. 3 x
Proportion of Water Vapor by Volume = Bws
in. Hg
                                                0
                                                               I • 6/0

         (Ps)
                       VAPOR PRESSURES OF WATER
Tamp.
°F
0
10
20
30
40
50
60
70
80
90
100
110
120
130
140
150
160
170
180
190
200
210
220
230
240

0
0.0378
0.0631
0.1025
0.1847
0.2478
0.3826
0.5218
0.7392
1.032
1.422
1.932
2.596
3.448
4.525
5.881
7.569
9.652
1220
1529
19.01
23.47
28.75
35.00
4241
5044-

1
0.0398
0.0860
0.1080
0.1716
0.2578
0.3764
0.5407
0.7648
1.066
1.467
1.992
2.672
3.543
4.847
6.034
7.759
9.885
12.48
18.83
19.42
2348
2943
35.88
43.11
51.78

2
0.0417
0.0698
0.1127
0.1803
0.2877
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.842
4.772
8.190
7.952
10.12
12.77
15.98
19.84
24.48
2942
3847
43.92
52.70

3
0.0441
0.0728
0.1188
0.1878
0.2782
0.4052
0.5802
0.6183
1.138
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.38
13.07
16.34
2027
24.97
30.52
37.07
44.74
53.65

4
0.0463
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
6.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.57
54.82
IQIWUI y
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.660
8.557
10.86
13.67
17.07
21.14
26.00
31.75
38.50
46.41
5540

6
0.0517
0.0848
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.083
5.302
6.850
8.787
11.12
13.98
17.44
21.59
28.53
3248
3924
47.27
58.80

7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.981
11.38
14.30
17.82
22.05
27.07
33.02
3949
48.14
5741

8
0.0571
0.0932
0.1502
0.2292
0.3384
0.4858
0.6903
0.9666
1.335
1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1821
22,52
27.82
33.87
40.75
4943
5843

g
0.0598
0.0982
0.1567
0.2363
0.3483
0.5035
0.7144
0.9989
1.378
1.875
2.521
3.351
4.408
5.732
7.384
9.424
11.92
14.98
1841
2249
28.18
3443
4142
4943
-------
'*6 3
                               METHOD 18 FIELD DATA SHEET
        Plant:.      	
        Date:   f>-2z-n
                                        Tested Analyte:.
                                        Orifice Tank #:_
        Location:  (Voc,/n /?
        Run #:  ftc- 3- i
Stack I.D.:
Pbar:   '^, ZQ
                    z-6" .< -2.^ ••'
Sample Tube
Operators:
Pump/Rotometer #:_
Pt:  Pretest (mm Hg):	
    Post-Test (mm Hg):_
Tt:  Pretest fF):.
                                   H  --
Leak Check: Pre:
                                Post:
Time
-?n%,L,6
1^7, 15
77V?, 2/
77^o. ^V



Gauge
Vacuum
(Hg)
,
i
/
l



Flow
Setting
'^c<_
/ •€£? ^ ^_
/.«» ^
iSdrt.

MlG?

/(-.
I/
Traverse
Point
Number
i
-L
1
H
<,
V
/
Z-
1
H
S
(j
.
^
•>
n
A
it
1
1
•}
1
f
u

Velocity
Head
in. HzO
. ^T
• &~1
•OG
. O&
. oC.
. ^o
.0-7
0-7
OC/
.O^J
X5C*
oY
.;i
.9
79
T*

    Post-Test f°F):_
Time: Start:,**3 Finish: ^J2_Total:.
W/B: g*7  D/B: 1? O~:  z/   CO
.02:^
                                                                                2'-
                                         Md = (0.44 x %C02) f (0.32 X %O2) -r (0.28 X "/oN^


                                    •^" Md = (0.44x  O ) + (0.32X1-1  )  +• (0.28 X 7 7


                                         Md =   *.&• **
                                                           % H2O

                                                            100
                                                                 100
                                                              % H2O

                                                               100
                                                                        18 (
                                                                            100
                                                 Q_ _ QL_ ^ S.P.   (^ A J I  \ .   ^C^ O
                                                 r9 • rD -f ««<^^ •= ( c'i *-v  } +  «••_—««
                                                        13.6             13.6
                                                             ^Px|
                                                                      Ts(°R)
                                                 vs - 85.49 x ( . yy   ) x (
                                                                    )x
                             I-
                                                      M.bT-     ft2
                                                  Qs • Vs x As x 60 s/m
                                                  Qs
                                                                 X 60
                                                  Q« w= Q« x 17.647 x -^— x (1
                                                         Ps      %H20
                                                        	x(1- —-f-)
                                                                               •x(1-
                                            c^
                                         : Si*^,
                                                                                     100
                                                               dsdm
-------
           WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant:
Site:
                       Operators:
Location:
Run #:
                              -  13.6
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of StacK =  Pbar
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of HpO at Tw (from Table) =   Pvw =
                                   (Ps - Pvw) x (AT)
R£.-q-\ Date: 5"-Z2 -«1
Pbar =
Pg =
Ps =
Tw =
Td =
AT =
Pvw =
JM.2P
-0 £
Jl
£>-MU>fcU
in. Hq
in. H O
in. Hg
°P
°F
°F
in. Hg
Vapor Pressure of H2O = Pva = (Pvw) -
                                   2800-(1.3xTw)
                                   )x(  X.)      )
Proportion of Water Vapor by Volume = Bws
                         ( .
(Ps)
T«mp.
°F
0
10
20
30
40
50
60
70
60
90
100
110
120
130
140
150
160
170
180
190
200
210
220
230
240

0
0.0378
0.0631
0.1025
0.1647
0.2478
0.3826
0.5218
0.7392
1.032
1.422
1.932
2.596
3.446
4.525
5.881
7.569
9.652
12.20
13.29
19.01
23.47
28.75
35.00
42.31
5044-

1
0.0398
0.0660
0.1080
0.1716
0.2570
0.3764
0.5407
0.7648
1.066
1.467
1.992
2.672
3.543
4.647
6.034
7.759
9.885
12.48
15.63
19.42
23.96
29.33
35.68
43.11
51.76
                                                                     in. Hg
( 2<\.2-> )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1803
0.2877
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
8.190
7.952
10.12
12.77
15.96
19.84
24.46
29.92
36.37
43.02
52.70
3
0.0441
0.0728
0.1186
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.36
13.07
16.34
2027
24.97
30.52
37.07
44.74
53.65
4
0.0463
0.0768.
0.1248
0.1955
0.2091
0.4203
0.6009
0.8462
1.175
1.610
2.178
• 2.911
3.848
5.031
6.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.57
54.62
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.680
6.557
10.66
13.67
17.07
21.14
26.00
31.75
38.50
46.41
5540
e
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.850
8.767
11.12
13.98
17.44
21.59
26.53
32.38
3924
47.27
56.60
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.981
1 1 .38
14.30
17.82
22.05
27.07
33.02
39.99
48.14
57.61
8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1821
22.52
27.62
33.67
40.75
48.03
5643
9
0.0598
0.0982
0.1567
0.2383
0.3493
0.5035
0.7144
0.9989
1.378
1.875
2.521
3.351
4.406
5.732
7.384
9.424
11.02
14.96
18.61
2249
28.18
3443
4142
4848
5847
-------
METHOD 18 FIELD DATA SHEET
Date: $~-,93-<3p nrifjre Tank #• 	 	
-OcatiorvO^ew *• ^ P.-mp/Rotometer *: 	
Run#: °-V~; Pt- Pretest fmm Ha): —
Stack I.D.: )S" Pnsr-TesUmm Ha): —
Pbar: 39, 0
r «••?
,«9

^/-7
.,a/^
,l\
,91
&'
;V*











='^rl
Flow
Setting
194; r-e/^
]



/
Y
,/
i/. «a
/^a
//* o
/^Q

i4
&/*?„-, ,,„ ^ , .,, -i-s ,
f*K '" '"
$r- J8 ^
Ts- \U>T> °F- ^2^ °H(°F.460)
^•^ . 0
_ _. S.P. . oa - . -. tofe
p9-Pb*T5T^2^ ^^Ta-
Ps- ^.MS' in.Hg
^p - DM2 n2
Qa • Vs x As x 60 t/m
#
0« - g x x 60
o.-^2.n «*"
Ps %H-0
Qt^^-QmxiT^Tx 	 x(l 	 i-)
•» T« 100

0.^- X17.847X 	 «(1--lo7^

QHW--\®^ d-to
-------
                        FIELD DA IA SHEET
Plant IfclXlO
Sampling Location _
Run Number: *?~9
Sample Type:
Date:
                              9 3 •
Pretest Leak Rate:  iQo [_ cfm @ /< in. Hg.
Pretest Leak Check: Pitot:  —Orsat:   —'
                                                                                  Nozzle ID:
                                                                             Thermocouple #:  *~\ f}
                                                            Assumed Bws: — •  Filter #:
                                         Probe Length/Type:
                                         Stack Diameter:
Pitot #: 5T- 3
                                           As:  /• 23 A
                                         Meter Box #:  /^  Y:
                                         Post-Test Leak Rate: .ex.to cfm @ j_^"i
                                         Post-Test Leak Check: Pitot:  — -6rsat:
                                                                                               Hg.
TravwM
Point
Number























. ; ;



Sampling
TbiM
(mln)
^
/G
56
ft>
frfc






















OockTkm
(24-hour
dock)
It&f
/f/V
/^^
^3^
/<*•#'






















Gas Metar
Reatfing
(Vm)ft3
£/5''£?
f-7
?f






















W
Pf
£*
9<






















Pump
Vacuum
(in. Hg)
7/7,
^
3
S
_3_





















                            AH
                                                                          Tm
-------
a DC
PlantL

Date:
                 <0
            r- a a-
 SAMPLE RECOVERY DATA

	  Run No.:

                    ^"k  Job No.:
                     Sample Box No. :
Sample Location:.
                                    ov7t«r
      Sample Type;   m -
                                             Filter No.:
      Sample Recovery Person:

      Comments:
      FRONT HALF

      Acetone
      Container No. L
                          Liquid
                          Level Marked:.
      Filter
      Container No.:_
                                             Sealed:
                                             Sealed:
      Description of Filter:
      Samples Stored and Locked:

      BACK HALF/MOISTURE
      Container No.:.
      Liquid Level Marked:
                                             Sealed:
                                                        9-1-

IMP. NO.
1
2
3
4
5
6
CONTENTS
WLO
Hv0
^PTt
S/L


TOTAL
INITIAL
VOL (ml)
loo
ID*
—
*$„



WEIGHT farams)
INITIAL
v i / 7
V «J l| \M^
^i ^^
7^;.i


n A.14 S?
/*T *()• v
FINAL
6I/,?
G>.5
1-J-C.o
7^-0


^W.f
NET
i ^
x^
•—
>*-\


*«*>
Description of Impinqer Catch- -— -
-------
        EPA METHOD 4 MOISTURE CALCULATIONS


PLANT:   LfVaCD _ SOURCE/RUN #:_3l3lL DATE:  S'ZZ'T7


1 . Leakage Correction for Volume Metered
    vmc = V (Lp - 0.02) x 0


    Vmc=(       )-(        -0.02) x(
2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)


                          'Pbar-MAH/13.6)N
      rnstd



     Vmstd
                                  'm


          = 17.64 x (31. oo-v )X(o/*loV,  )X
 3. Volume Water Vapor Collected, Standard Conditions


     Impingers & Silica Gel = V w  = 0.04707 x (W. - W. ) .
                          wstd             '   '

                         Vw  = 0.04707 X ( 2B.
                            std       -
                         Vw  =  MF-    sef
                          wstd
 4.  Percent Moisture, by Volume


                   wstd
              w      w

                wstd    mstd
     B
-------
P'ant:
Samonna Location:  J  '
Run x-fQ-^' J
                 GAS VELOCITY AND VOLUMETr.iC FLOW RATE

                                                      Date:  m g-29-9i
                                                      CIocK Time:	
Barometric Pressure, in. Hg:_o	
Moisture. %:   -^         Molecular wi.. Cry:
StacK Dimension, in. Diameter or Side r
Wet Bulb. °F:^
                                            Static Pressure, in. l-^O:
                                            x'
««MI W. III. 1 *O ^^« _^^^^^*^_
Pilot Tube. CQ:  ,?9

Side 2:
                                       Md • 10.44 • %CO,J » iO.32 X %CW » (0.28 X %M,>


                                       Md • IO.44 •     ! «• (0.32 X     < « (0.28 X
                                                  . M,O      S H,O

                                                   100   *      100
                                                                  100
                                       Ml • Md 111 •

                                                        100
                                       P« - Pb »-!£_-.<      I* 	
                                               13.0              13.0
                                       »• -
                                                    -n. H.
                                        •/• . «s.«o K Co «  Ma



                                                                   ^
                                        Q«
                                        0%^- «• «17.84T X «^— « O



                                        °«-d-
                                                               xoo
                                                             %H.O
                                                      Ti       tOO

                                                    Kt7J«y«
               Ki-
                          ^
-------
ODCZJ
                        METHOD 18 FIELD DATA SHEE1
    0
- fe
=lant: ^HSCtf Tested Analyte: S' -1 v *->--<
Date: s-zz-tft Orifice Tank #: 7-
_ocation: WA Pump/Rotometer #: ^^-^/ * *?
=lun#: NDfl-1-l Pt: Pretest ; -rim Hg): -
Stack I.D.: ^-6^^ £2V 12.0" Post-Test (mm Hg): '
3bar: 2-1 -3D Tt: Pretest <°R:
Sample Tube #
Operators: fA/
• /vOfl-l-i Post-Test (°F):
^ , Time: Start: «B02L Finish: ife^Z Total: 3O
_eak Check: Pre: ^ Post: ^ W/B: — D/B: - O0:^> CO0: <=>

Time
, 5f **•$>,
Gauge
Vacuum
(Hg)
/
/
i
i



Row
Setting
*./
it
il
2-!




Traversa
Point
Number

























Velocity
in. H2O

























Stack
Temp.
°F

























Md = (0.44 x %CO2) 1- (0.32 X %O2) -r (0.28 x "/oNj)
J^~y Md - (0 44 x ) -t- (0 32 x } *• (0 28 x )
-------
          APPENDIX A. 1.11

             Condition 10
(includes flows, moistures, and Method 18)
-------
METHOD 18 FIELD DATA SHEET
Plant: LfeCO TestPri Analvte: 5A/^,~a
C
L
F
S
F
c
C
L

?fc/o
ul/5-
\L l;o
V l.j

)ate: 5-iz--^'' Qrificp Tank #• —
ocation: /vui~ c-au^f Pump/Rotometer #: U9«,f- •* -i-
un #• /riif- /o-< Pf Prefpst (mm Hg):
tackl.D.: I-*" Post-Tpst (mm Hg): -
'bar: IA.I* Tt: Pretest (°R: —
>amp!e Tube
Dperators:
#:AI.->*. *••*-»-/ •» Post-Test (=F): -
fKl- Time: Start: /?£ Finish: '?r/ Total: •• r
eak Check: Pre:_4^_ Post:_tx^__ W/B: 6^ D/B:*^2- O0:_2j_CO0:_j2_


Gauge
Time Vacuum
(Hg)
2->2/,S7 /
^^2. b' /
z'b-ig.1?!- . /
11,13,^-5 /



-h >03
Traversa
Point
Number
;
2
5
4
5
u
1
fi

1
1-
3
<.<.
l$o<^
. 50 'V_
,*>«.
M(y\-



Stack
Temp.
°F
77
S^
ft
g-z.
?^
S^-
fft
^t-

^2-
^2.
#2-
9-2-
^2.
?2-
^2.
?~2~



ft1,«p ,,/
c^m »ift



	 ^ fc
Md = (0.44 x %C02) * (0.32 X %O2) -r (0.28 x "/oNj)
— KJ — in AA V ,-• ^ J. (f) "V3 t 2.1 1 4- (O ?S K ~7^ 1
Md = -^ ^ ^
~\ ' Ms = Md x ( 1 • 	 — ) - 1 8 ( 	 i
1 00 1 00
"»* M.«. )X(1 ''4 ).18( ''M-)
1 00 1 00
70
Ms » ^^- ^^
Ts- °F- °R (°F *460)
c p
Q_ — OL- . J-r- i \ .
13.6 13.8
PS = "23 2?> '"• ^
J&P ~ 0 ^jU~ya

VS - 03.<»» X UP X «jr X ^ ps x Ms
Vs - 85.49 x ( ) X ( ) X A I 	

A. , . 1 *2
1 L 1 "

Qs - Vs x As x 60 s/m

Q«« x X60

Qs • yo 7 » acfrn
Ps ^ V2
Q* . .= Qs x 1 7.847 x — - x (1 • )
Std T_ 1fM

..
aid 100

^•>*0l(J y^K^^v 8*iIIII
-------

         WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: L/\S<_c?
Site: ^A/H&) GxkAtt^ Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H20 -
Absolute Pressure of Stack - Pbar + -
Wet-Bulb Temperature, °F -
Dry-Bulb Temperature, °F =
Temperature Difference, Td • Tw -
Saturation Vapor Pressure of H2O at Tw
V/annr Procci iro r\i W C"\ — Dwa — /D\AA/\
Pva-/ h i,tc4 \ , .^"2J, "ruc"q
Location: MAH-* ddi-^Au-^T"
TA Run #: rue-to-^ Date: 5-2
Pbar= >??.^ft
Pa = +o.t3
-SSL, Ps= Z«.*fc .
Tw = 04
Td= &2.
AT= \3
(frnmTflhlP)= PVW = D-UOo^
(Ps - Pvw) x (AT)
2800 - (1 .3 x Tw)


in. Hg
in. H20
in. Hg
°F
°F
°F
in. Hg
in. Hg
                   2800-(1.3 x
Proportion of Water Vapor by Volume = Bws
   _   (Pva)
(Ps)
Tamp.
op
0
10
20
30
40
50
60
70
80
90
100
110
120
130
140
150
180
170
160
190
200
210
220
230
240

0
0.0370
0.0631
0.1025
0.1647
0.2478
0.3026
0.5218
0.7392
1.032
1.422
1.932
2.596
3.440
4.529
5.881
7.569
9.652
1220
1529
19.01
23.47
28.75
35.00
42.31
50.84-

1
0.0398
0.0660
0.1080
0.1716
0.2576
0.3764
0.5407
0.7648
1.066
1.467
1.992
2.672
3.543
4.647
6.094
7.759
9.865
12.48
15.63
19.42
23.96
29.33
3S.68
43.11
51.78
)
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
15.98
19.84
24.46
29.92
36.37
43.92
52.70
3
0.0441
0.0728
0.1186
0.1878
0.2782
0.4052
0.5802
0.8183
1.136
1.561
2.114
2.629
3.744
4.900
6.350
8.150
10.36
13.07
16.34
2027
24.97
30.82
37.07
44.74
53.88
4
0.0463
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
6.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.87
54.62
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.660
8.557
10.66
13.67
17.07
21.14
26.00
31.75
36.50
46.41
5540
6
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4,063
5.302
6.850
8.767
11.12
13.98
17.44
21.59
20.53
3248
3924
4727
56.80
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
6.981
11.38
14.30
17.82
22.05
27.07
3942
39.99
48.14
5741
a
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1821
2242
27.82
3347
40.75
4949
5849
9
0.0598
0.0982
0.1567
0.2383
0.3403
0.5035
0.7144
0.9989
1.378
1.875
2.521
3.351
4.408
5.732
7.384
9.424
11.92
14.96
1841
2249
28.18
9449
4142
4049
5047
-------
                        METHOD 18 FIELD DATA SHEET
Plant:.
Date:_
                                         Tested Analyte:_
                                         Orifice Tank #:_
Location:.     	
Run #:   fte'-fo-i
Stack I.P.: 2g" /
Pbar:     2.<
Sample Tube #• *e -/*   $>=.-'<>->
Operators:   rA-
                                         Pump/Rotometer #:
                                         Pt:  Pretest (mm Hg):
                                             Post-Test (mm Hg):
                                         Tt:  Pretest
                                                                     Total:
Leak Check: Pre:
                        Post:
Time
77SO.?(,
1752. 3Z.
->1^^
-7 -) 55 ^ 3,



Gauge
Vacuum
(Hg)
1
,
f
1



Flow
Setting
/soco
/So«
/5*rc.
.^.-^

ArVJU"

Md = (0.44
Md = 1i
~[l Ms = Md x
•)
_ i Ms - /
Ts-
    Post-Test (°F):
Time: Start:_i£*
W/B: sV  p/B:
                                         Md = (0.44 x %C02) -t- (0.32 X %O2) -r (0.28 x "/oNj)


                                         Md = (0.44 x o   ) + (0.32 X 
1
6
<,
1
i
!>
H
1
i.
i
z.
3
^
5
t>

Velocity
Head
in. H^
, 3G
-0(j>
,o5
. o^-
.OCa
•0~T
. °e
,01
d?5
.o5
.05
• 01
. //
•07
.0-5
,04
.00
o<7
,/o
.05
;t?5
.05
lOT
, /o

Stack
Temp.
°F
'10
-((a
10
ni.
-76
-It.
-J6,
~>6
~l(/
If
-)<*
10
-,U
!(!>
10
Ifr
-I*
-7£/
-|U
l^
1*1
1(J
-16
To

                                          Ps - Pb +.
                                                 13.'
                                                                 13.6
                                          Vs « 85.49 x Cp X


                                          Vs - 85.49 x (


                                          Vs- |>- ll/


                                          AS - M. vrv     n


                                          Qs • Vs x As x 60 s/m
                                                               Ts(°R)
                                                               PsxMs
                                                          ) X (
                             4
                                                        ft/s


                                                         2
                                                                  x60
                                                        acfm
                                          Qs . .= Qs X 17.847 X
                                                          Ps      *H,0
                                                         	x(1- —2-
                                                                  100
                                                       X 17.647 x-


                                                        dscfm
                                                                              100
-------
            WET-BULB/DRY-BULB MOISTURE CALCULATION
 Plant:   LAf>cr?	_	Location:     fc.^  g;
 Site:
                         Operators: —^     Run #:  £e-.o-s     Date: .5-
 Barometric Pressure, in. Hg =
 Static Pressure, in. HgO =
 Absolute Pressure of Stack =   Pbar i —r=~s
                                   I J.O
 Wet-Bulb Temperature, °F =
 Dry-Bulb Temperature, °F =
 Temperature Difference, Td - Tw =
 Saturation Vapor Pressure of H2O at Tw (from Table) =   Pvw =

                                     (Ps - Pvw) x (AT)
Pbar= 23.23
Pg = -0. ^^
PS = ^<^.23
TW = 54
Td= >c»
AT= zz
Pvw = oH"i*^
in. Ha
in. HLO
in. Hq
°F
°F
°F
in. Ha
 Vapor Pressure of H2O = Pva =
''il,

 Pva = (
                                     2800-(1.3xTw)
                                                          0.
                         2800-(1.3 x

 Proportion of Water Vapor by Volume = Bws

 Bws =
Tamp.
 °F
 0
 10
 20
 30
 40
 50
 60
 70
 80
 90
 100
 110
 120
 130
 140
 150
 160
 170
 180
 190
200
210
220
230
240
(Ps)
0
0.0376
0.0031
0.1025
0.1047
0.2478
0.3020
0.5218
0.7392
1.032
1.422
1.932
2.596
3.446
4.525
5.881
7.569
9.652
1220
1529
19.01
23.47
28.75
35.00
4241
5044-
1
0.0398
0.0600
0.1080
0.1710
0.2570
0.3764
0.5407
0.7648
1.066
1.467
1.992
2.672
3.543
4.647
6.034
7.759
9.885
12.48
18.63
19.42
2346
2943
35.68
43.11
51.76
                                                                        in. Hg
( 2li* )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0096
0.1127
0.1803
0.2077
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
15.96
19.84
24.46
2942
36.37
43,82
52.70
3
0.0441
0.0728
0.1186
0.1878
0.2782
0.4052
0.5802
0.8183
1.136
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.36
13.07
16.34
20.27
24.97
30.82
37.07
44.74
5345
4
0.0403
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.176
2.911
3.848
5.031
0.513
8.391
10.61
13.37
16.70
20.70
25.48
31.13
37.78
48.87
54.62
5
0.0469
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.660
6.557
10.66
13.67
17.07
21.14
26.00
31.75
38.50
46.41
5540
6
0.0517
0.0646
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.850
8.787
11.12
13.98
17.44 .
21.59
28.53
32.38
3924
47.27
56.60
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
6.981
11.38
14.30
17.82
22.05
27.07
33.02
39.99
46.14
57.61
8
0.0571
0.0932
0.1502
0.2292
0.3304
0.4858
0.6903
0.9666
1.335
1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1821
2242
27.82
3347
40.75
4949
5843
9
0.0598
0.0962
0.1567
0.2383
0.3493
0.5035
0.7144
0.9969
1.378
1.875
2.521
3.381
4.408
5.732
7.384
9.424
11.92
14.96
1841
2249
28.18
3443
4142
4843
5847
-------
Plant:
Samoima Location:
Run*:  <* -JO ^
GAS VELOCITY AND VOLUMETRIC FLOW RATE

                                    Date:  5^-9?
                                    CIocx Time:
                                          /dA
Ooerators:.
Barometric Pressure, in. Hq: 5>?.fTo	  Static Pressure, in. HpQ:  ~,
Moisture. %:	       Molecular wt.. Grv;   —"     Pilot Tube. Cp:^;
Stack Dimension, in. Diameter or Side 1 •    IS'/f	Side 2:
Wet Bulb. °F:
    3otm.
   A-  (
   6
               ,30
                O/'i
                           o_
                          UL
                         1(0$
                      Md - (0.44 i %CO.) » i0.32 X %CUi * (0.28 X %N*)


                      Md • to.44 •     ! - (0.32 x    : . 
-------
METHOD 18 FIELD DATA SHEET
Plant: C74SHG
Date: ^-oia-q-/
Location: &V & ^ <*• 1 n
Run#: /0-/t?-/
Stack I.D.: ;esv^A
Leak Check: Pre: , got' Post:
Gauge
Time Vacuum
(Hg)
3onn rj
£b Je> 0
sfcac 0
Stoic* f)
2c
3. OS
aia
:3 ^W

^
k?^




-






Oj^330
Time: Start:0
Qi^-QiX 17.847 X 	 x(1- 	 2_)
•» T« 100
tf-
°NW- f-70^ 
-------
FIELDDAlAWlEET
Plant Cx/jS^O Sample Type: fl\-*^ Qpeia[oi:(^/d&
Sampling Location Ct)C^ f> /C Pbar £^.^>O Ps: — , 3)
Run Number: ft -16- Date: 5'92-9d CO2: 	 O2: 	
Pretest Leak Rate: ,£#£ cfm@/<" in
Pretest Leak Check: Pilot: -~ Orsat: —

TMMMM
Point
Numb*



























Sampling
Time
(mln)
On

9C
3&
*iO






















dock Tim*
(24-hour
dock)
8000


























Hg. Probe Length/Typ
Stack Diameter:
K I 'S^ Pta**:Sf'3
}^'' As: 1 23-
rji

Gaa Meter
Reading^
£?V4 • £3&
k?&>£ . ^6
6> 70,' .^o
(j,^ ^ . 35(i






















Velocity
Head (Ap)
inH2O
Oriice PrMOura Diflwential
(AH) in H2O
Desired
Actual
Stack
Temp.
(Ts)
Nozzle ID: " Thermocouple #: *Y /3
Assumed Bws: - — • Filter #: *"
Meter Box #: /fr Y: . 9<^
Post-Test Leak Rate: 6(it>
Post-Test Leak Check: Phot:
Temperature
°F
Probe
Filter
Impinger
Temp.
°F
6 AH@: 1-S-&3
cfm @ g" in. Hg.
- — Orsat: — —

Dry Gas Meter Temp.
Inlet
(Tm in°F)
Outlet
(Tm out°F)
'////////////////////////////////////////////////////////s


























1 F6.
/,$>£,
/<-"¥£,
\ t S&






























































































































^0
3"?
5"-^
5"r^>
.$"4^





















£6
^^
^ "^
&"3
S^^>





















^'3
PV
-------
OD
a
Planti

Date:
                        SAMPLE RECOVERY DATA

                       	.	   Run No.:

                       	Sample Box No.:   ^^    Job No.:
      Sample I oration-

      Sample Typfl-
                                            Rlter No.
      Sample Recovery Person:

      Comments:	l"n-
      FRONT HALF
      Acetone
      Container No.:
                          Liquid
                          Level Marked:.
      Filter
      Container NO.L
Sealed:
                                            Sealed:
      Description of Rlter:
      Samples Stored and Locked:

      BACK HALF/MOISTURE
      Container No.:	
      Liquid Level Marked:
                                             Sealed:

IMP. NO.
1
2
3
4
5
6
CONTENTS
flto
W^o
CrtiPry
5/6


TOTAL
INITIAL
VOL (ml)
(Oo
> oo
*~~
Mu



WEIGHT (arams)
INITIAL
6*;, /
C/&-9
4"oG. I
*)/t.3


35 (bQ.<^
FINAL
W?.5l
6^G,&
•ToC^
7-^-7


r^on
NET
/, I
- .5
- ,/
fy*^


ll,3
Description of Impinqer Catch- . — "
-------
        EPA METHOD 4 MOISTURE CALCULATIONS


PLANT:  L/V5£p _ SOURCE/RUN #: J2l/i±. DATE:


1 . Leakage Correction for Volume Metered


    vmc=vm-(Lp-La)xe
    vmc=(       )-(        -0.02) x(
2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)


                          'Pbar-MAH/13.6)N
          = 17.64 xVxYx
                   me-     v       T
                                  'm
    vrrw = 17-64 * (et"«H   ) x (  .%<•   ) x
                     dscf
 3, Volume Water Vapor Collected, Standard Conditions


     Impingers & Silica Gel = V ...   = 0.04707 x (W. - W. )
                                          '   '
                        Vw
                          wstd
 4. Percent Moisture, by Volume




     R  -       VWSW
     DW/C — -
              Vw   4- Vm
               wstd   mstd
     B         (          )
     °ws—/	•	



        .- D.OOL  31
-------
aaci
                                METHOD 18 FIELD DATA SHEET
!<»?")




I 1 */-
Plant: t-^-»cy
Date: */i-/-/*7
Location: ^0,9-4
Run*: VPA -•/«-/
Stack I.D.: 3&"MM>"
Pbar: 29-. is
Sample Tube #•
Operators: S^/TA
Leak Check: Pre: \/ Post: ^
Tested Analyte: ?H'-
                                                  Md = (0.44 x %CO2) * (0.32 x %O2) T (0.28 x





                                                  Md = (0.44 x    ) •*• (0.32 x    ) + (0.28 x
                                                             ?'» HO
                                                                          HO
, fn 2o
^0
.
* r
- ^ gO
TrfT ^ '



























/r^5, 7~
i^1^^, 3C




Traverse
Point
Number



























7































/
t




Velocity
Head
in. H;>O


























1J C

M(A*



Stack
Temp.
°F


























' ' ~ 100 100
Ms » ( )x(1- 	 )^18( 	 )
100 100
Ms -
Ts- °F- 0R(°F.460)
^ P
O. _ OU j. -J-r. ^ » _
13.6 13.6
Ps = in. Hg

jfip =



V

Vs - 85.49 x ( ) x ( ) x \l 	

Vs * ft/8

A.. ft2


Qs - Vs x As x 60 s/m

Q« • x x 60

Qs - acfrn
Ps %H,0
Q, -0.x 17.647 X x(1. )

,


Qsgfcj* dscfrn
-------
          APPENDIX A. 1.12

             Condition 11
(includes flows, moistures, and Method 18)
-------
r
I
o? /tf

 0f- /
                                METHOD 18 FIELD DATA SHEET
                               	     Tested Analyte:	
                               	     Orifice Tank #:	
                                         	     Pump/Rotometer
                                                                 ?/y/"<-
        Stack I.P.:   H. S
        Pbar:	2j
        Sample Tube #:.
        Operators:  -rA
          Leak Check: Pre:
                               Post-
                                                  Pt:  Pretest (mm Hg):    —
                                                      Post-Test (mm Hg):	ZL.
                                                  Tt:  Pretest fF):_
0
S
/*
Time
232?. 5=7
iS2v. }*-
n-zv. 7-z-
•2-375-. V3



Gauge
Vacuum
(Hg)
/
/
I
,



Flow
Setting
/**'<•
/«rd
/f*«-
/&>*<-



7*
sc,
SI
                                                    Post-Test (°R:      		
                                                Time: Start: ov* Finish: <*?* Total:  /«
                                                W/B: Ji£^ D/B: J?J_O2:_2_L_ CO2:_d_


                                                Md = (0.44 x %C02) i- (0.32 x %O2) * (0.28 x "/oN^

                                                Md = (0.44x  O  )+(0.32 X?'  ) •(• (0.28x7*  )

                                                Md = ~Z
                                                          ••', H,O      % HO
                                                Ms = Md x 1 1 -  - i— ', - 1 8 ( -
                                                           '.00  '      '00
Traverse
Point
Number
I
1
3
^
4
V
7
/

i
i
3
V
^
c,
1
f








Velocity
Head
in. H^
. 25
31
3-1
. 23
.*£
?/
• Vd
W

.71
.»o
.21
.31
.31
JZ
.VL
,3O


ID. 57f)f





Stack
Tamp.
°F
77
77
77
77
.,-7
"77
•7 7
7-7

77
•77
77
77
77
Tt
77
77


77





                                                   Ms-


                                                   Ms-


                                                   TS-
                                                   Ps - Pb + Jl -.
                                                          13.6
                                                                100
                                                                     - 18
                                                                           100
                                                                   ) + —
                                                                       13.6
                                                Ps«»  •e.4/*''   in. Hg
                                                        s^.
                                                     O-
                                                                     Ts(°n)
                                                Vs-85.49 xCpxv'AP x \l   pgxMs
                                                Vs - 65.49 x (
                                                Vs-
                                                As-
                                                                ft/8
                                                 Qs - Vs x As x 60 s/m


                                                 Qs -         x  /• 6 "7   x 60
                                                 Qs-
                                                                 aefm
                                                                Ps
                                                 Qs . .= Qsx 17.647x —— x(1
                                                  «W            TS       100
                                                 Qs

                                                               x 17.847 x-
                                                                              •""•-sr*
                                                                                             JW
-------
           WET-BULB/DRY-BULB MOISTURE CALCUU\TION
Plant: LAs><^> VLvJ? ^t^JLjrr Location: f%*^~c^ fc^-
Site: A^ £xL~**- Operators: -^/^ Run #:
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack = Pbar + PV
l o.b
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H20 at Tw (from Table) =
(Ps - Pvw) v. <
Vapor Pressure of K-.O - Pva - (P\w\ 	
fa* -II- I Date: ^
Phar= 14. ft
Pg = '+ ><> *- '
Ps= 14,«ft
Tw= ^"2-
Td= 77
AT= /£*
Pvw = 0' Zkol
:AT)
fiV/V7
in. Hq
in. HP
2
in. Hg
°F
°F
°F
in. Hq

                                   2800-(1.3xTw)
                                                      O.
                      2800-(1.3 x  ^

Proportion of Water Vapor by Volume = Bws
        (Pva)    _       (  0,
-------
3 a
       Plant:
       Site:
           WET-BULB/DRY-BULB MOISTURE CALCULATION
           /./fe&?   fi~J?  .^uJL/r-Locati
                   -   Operators: -f^-fa  Run 4
                                                                  Date:
                                     ~  13.6
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of Stack =   Pbar +
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H^O at Tw (from Table) =
Pbar = % ye
Pg= r6.03
PS = 27. VB
Tw= &(e
Td= 7?
in. Ha
in. HnO
2
in. Hg
°F
°F
AT= /3 °F
Pvw = £>,£, V2_
in. Ha
       Vapor Pressure of H2O = Pva =
Pva =i
                                   (Ps - Pvw) x (AT)
                                   2800 - (1.3 x Tw)
                                    x(    (3    )
                              2800 -(1. 3 x
                                                                            in. Hg
Proportion of Water Vapor by Volume = Bws
«,...._   (Pva)     _       (   C
(Ps)
Tamp.
°F
0
to
20
30
40
50
60
70
80
90
100
110
120
130
140
150
160
170
180
100
200
210
220
230
240

0
0.0376
0.0631
0.1025
0.1647
0.2478
0.3626
0.5218
0.7392
1.032
1.422
1.032
2.506
3.448
4.525
5.881
7.560
9.652
1220
15.20
10.01
23.47
28.75
35.00
4241
5044-

1
0.0398
0.0660
0.1080
0.1716
0.2576
0.3764
0.5407
0.7648
1.068
1.467
1.092
2.872
3.543
4.647
6.034
7.759
9.885
12.48
15.63
19.42
2346
2943
35.88
43.11
51.78
                                                          &> 0 (1
in *
( isw* )
VAPOR PRESSURES OF WATER
* V
37+1 ,_ ^
In Inches of Mercury IT) ( i{ ^'
2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
15.98
19.84
24.46
2942
3647
49.92
52.70
3
0.0441
0.0728
0.1186
0.1878
0.2782
0.4052
0.5802
0.8183
1.136
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.38
13.07
16.34
2027
24.97
30.52
37.07
44.74
53.65
4
0.0463
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
6.513
8.331
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.87
54.62
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.680
8.557
10.86
13.67
17.07
21.14
26.00
31.75
38.50
46.41
5540
6
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.850
8.767
11.12
13.98
17.44
21.59
28.53
3248
39.24
4727
58.60
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.370
3.160
4.174
5.442
7.024
8.081
11.38
14.30
17.82
22.05
27.07
33.02
30.99
48.14
5741
8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1821
22.52
27.62
3347
40.75
4943
5843
9
0.0598
0.0982
0.1567
0.2383
0.3493
0.5035
0.7144
0.9989
1.378
1.875
2.521
3.351
4.408
5.732
7.384
0.424
11.92
14.98
1841
2249
28.18
3449
4142
4943
5947
-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:
                                Date:
Sampling Loc
Run#: t<\&-
:ation: AU,;, Fv/^W Clock Time: /t<»5-
- I/-"* Onnrators: T^/55
Barometric Pressure, in. H
Moisture, %: ^ U
Stack Dimenj
Wet Bulb, °F
Travaree
Point
, Number
(•
.?_. ••-.. ;
"b
V '
5
c,
7
^

f
i
3
ion, in. Diameter or Side
£5* DrvE

Velocity
Head
in. H2O
•IS
.11
.-3/
/*,!
35
,31
."M
/





Stack
Temp.
°F
f;
ft
ti
V
fl
$1
?r
r/

?i
21
tl
*/
10
n
d
tl





1: /7-<5 Side 2:
ulb.op f/
Md_(0.44x O)+(0.32X11 )-t-(0.28x "Jf )
Md - Z* ^'/
%HO %HO
Me-Mdxd ,00 ' ' 100 '
Ma - /^V ^
Pa • pb -t- = ( ^' *^ ) •»• 	
13.8 ' 13-8
Pa . 2 f. 2 f in. Hg
fip = D ,^>6^^
— | T3f1R)
Va - 85.49 x Cp x ^P x W 	 Rs x Ma —
f
Vs- 85.49 X( . f f )x( ) X A! 	
°
Aa- /,(,-? n2
da • Ve x Aa x 60 a/m

Q.. X l.(,-\ X80
Qt-^RV2) acfm
                                      *"°
                              X17.B47X-
-------
         WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: / ASCh
s'te: 1Aflf** i^h^,/- Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack = Pbar + -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw
Vapor Pressure of HoO = Pva = (Pvwi -
Location: MAIM £"* MAIA^-I-
T/*/s& Run #
Pg
13.6
(from Table) =
(Ps - Pvw) x
: ME -f
.05*
.»<•
.«1
00
e-T
.«6
.t>S
OU
.«1
.//
.4*
• *s
OS
,o*
.11
.tA
.01,
QS
.*s
.Off
.11
6,1f«(
Stack
Tamp.
°F
7Z
7r
7T
7t
•»*•
Tt
7t
7t
T7
•?•»•
7«
tt.
72
7?
•7t
7t
71
7*
7*
Tt
It
7t
11
-n
71
                                       Ms =


                                       Ms -


                                       Ts-
                                       P9 - Pb t- -^. =
                                               13.6
                                                            1 00
                                                                      1 00
                                                                   13.6
                                       Ps
                                                         in.Hg
                                                         =
                                            Vs - 85.49 x Cp x VAp
                                                                   (°R)"
                                                                 PsxMs
Vs - 85.49 x (
                                                       ) x (
                                                                    \  ) x
                                             Qs - Vs x As x 60 s/m
                                        Q.-

                                        Q« -
                                                                   X60
                                                  l\<% $0
                                                            Ps
                                             Qs x 17.847 x - x (1
                                                      Ta
                                                                   100
                                             Q»atd-   '^"l */ efscftn
                                                                               100
                                                                                    IB'
-------
go
F
Plant:   	|
Site:   E-atAvx
           WET-BULB/DRY-BULB MOISTURE CALCULATION
                                    	Location:
                                    r<    Run #:
                                Operators:
         Barometric Pressure, in. Hg =
         Static Pressure, in. H20 =
         Absolute Pressure of Stack =  Pbar i
         Wet-Bulb Temperature, °F =
         Dry-Bulb Temperature, °F =
         Temperature Difference, Td - Tw =
         Saturation Vapor Pressure of H2O at Tw (from Table) =   Pvw =

                                             (Ps - Pvw) x (AT)
fce-u-i Date: £/??/?-?
Pbar = ^T.^
Pg = — n 6-Z
Ps= ^7 13
Tw = ^
TH= ^
in. Ha
in. HO
2
in. Hg
°F
°F
AT= '<~7 °F
PVW = <• 4 3 S ~
> in. Hg
Vapor Pressure of H20 = Pva = (Pvw) -

                   (->*,.,   .   UK
Pva=( .^5=,    ) A
                                             2800 - (1 .3 x Tw)
                                             ) x (  '. 7     )
                                 2800 - (1.3 x   $^-

         Proportion of Water Vapor by Volume = Bws
                  (Pva)    _        (    ^5?   )
                                             )
        Tamp.
         °F
         o
         10
         20
         30
         40
         50
         60
         70
         80
         90
         100
         110
         120
         130
         140
         150
         160
         170
         160
         190
         200
         210
         220
         230
         240
(Ps)
0
0.0376
0.0631
0.1025
0.1647
0.2478
0.3626
0.5218
0.7392
1.032
1.422
1.932
2.596
3.448
4.525
5.881
7.569
9.652
1220
1529
19.01
23.47
28.75
35.00
4241
5044-
1
0.0398
0.0660
0.1080
0.1716
0.2576
0.3764
0.5407
0.7648
1.066
1.467
1.992
2.672
3.543
4.647
6.034
7.759
9.885
12.48
15.63
19.42
23.98
2943
35.68
43.11
51.76
                                                                        in. Hg
( ?i.*M )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
15.98
19.84
24.48
2042
36.37
43.02
52.70
3
0.0441
0.0728
0.1186
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.629
3.744
4.900
6.350
8.150
10.38
13.07
16.34
2027
24.97
30.52
37.07
44.74
53.65
4
0.0463
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.6462
1.175
1.610
2.178
2.911
3.848
5.031
6.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.57
54.62
5
0.0489
0.0810
0.1302
0.2035
Ji.3004^
(1X4359^)
08222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.660
8.557
10.86
13.67
17.07
21.14
26.00
31.75
38.50
4641
55.60
6
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.850
8.767
11.12
13.98
17.44
21.59
26.53
3248
3924
4727
56.80
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.981
11.38
14.30
17.82
22.05
27.07
3342
3940
48.14
5741
8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
•1.819
2.449
3259
4.289
5.565
7.202
9.200
11.65
14.62
1821
2242
27.62
33.67
40.75
4943
5843
9
0.0598
0.0982
0.1567
0.2383
0.3493
0.5035
0.7144
0.9989
1.378
1.875
2.521
3.351
4.406
5.732
7.384
9.424
11.92
14.96
1641
2249
28.18
3443
4142
4049
5047
-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant: L(\y$ Date: 5-7l*-'fl
Sampling Loc
Run#: $6
ation: *^.-v £,h^y.Z Clock Time: f&v4
-»/-?_ Dnfirators: 7^/5*
Barometric Pressure, in. H
Moisture, %: 6. 1 %
Stack Dimens
Wet Bulb, °F
TravarM
Point
Numbar
,'
T
V
H
5
i.
1
^
--,
^
5
c.
i
-
*
H
j
o
1
Z.
3
H
5
0.


q: z*?. ^ Static Pressure, in. HoO: -. Cl
Molpnilarwt Hrv ^Wl Pitot Tube, Cp: ,- ?*
>ion, in. Diameter or Side
5iC. Dry E

Vatocrty
in. H2O
.Ots
.0*1
.•<*
oL,
.61
.«7
,6
^JO
O^T'
,0«
tf-T
.ott
• ^F ^T
.05
.0*
.6t
.61+
.«$
-06
.6£
-01

1 A fi ^ O £llf
•/w^ •* y i,^ \ t
Stack
T«mp.
°F
7*L
7V
7V
11
•»v
7V
7V
7V
iy
^'
-"/
7V
1^/
7V
7V
7^
7V
7V
7V
^Y
7f
7V
7V
7«|

fi. "?4
1: 28* Side 2: ^'
nlh.OF- 7V
Md - (0.44 x %CO2) + (0.32 X %O2) -t- (0.28 X %N^)
Md - (0.44 x ° ) •*• (0.32 X c^ i ) * (0.28 X~) '5 )
Md- P'sVf'r
%H20 %H20
100 100
Nfc-O-?.'^ )xd- 10Q > *18( 10o '
13.8 '^l-HJ' 13.8
Pa. Z^V4/ in-H8
VSp- 39,(
— 1 Ts (^R)
vt-as^BxCox^Hx )| P9XM8
|
Vs - 85.49 x ( ' ^1 ) x ( . 35 (Q., ) X V 	
V.- llo-S}- ft/i

A*- V.6~i n2
Qs » Vt x Aa x 60 a/m

Q|v X ' ,(j\ XOO
Ot- HW- achn
p, %H-0
Qs . .= Q« x 17.847 x 	 x (1 • — •*- )
•td Tt 100

^rtd" XI7.847X K(l- 1QO )
                                                       //ft
-------
         WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: U.?/?->
2 "7 ^r in. Ha
— .61 in. HO
22 ^ in. Hg
£b °F
/V °F
/8 °F
0. WD in. Hq

                              2800-(1.3xTw)
Pva =i
    '   '       '      2800-(1.3 x
Proportion of Water Vapor by Volume = Bws
   =  _J?ya)
(Ps)
T«mp.
°F
0
10
20
30
40
50
60
70
60
90
100
110
120
130
140
150
180
170
180
100
-200
210
220
230
240

0
0.0370
0.0031
0.1025
0.1047
0.2478
0.3020
0.5218
0.7392
1.032
1.422
1.032
2.508
3.446
4.525
5.881
7.588
0.852
12.20
1550
10.01
23.47
28.75
35.00
42.31
50.84-

1
0.0398
o.oeeo
0.1060
0.1710
0.2570
0.3704
0.5407
0.7848
1.086
1.487
1.002
2.872
3.543
4.847
8.034
7.759
9.885
12.48
15.63
19.42
23.06
29.33
35.68
43.11
51.76
                                              0.6 >o? -i
                                                            in. Hg
( Z«.Vy )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0090
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
15.98
19.84
24.46
2942
36.37
4342
52,70
3
0.0441
0.0726
0.1166
0.1878
. 0.2762
0.4052
0.5602
0.8163
1.138
1.581
2.114
2.829
3.744
4.900
6.350
8.150
10.38
13.07
16.34
2057
24.97
30.82
37.07
44.74
53.68
4
0.0463
0.0768
0.1248
0.1955
0.2691
0.4203
0.0009
0.6402
1.175
1.010
2.178
2.911
3.848
5.031
6.513
8.351
10.61
13.37
18.70
20.70
25.48
31.13
37.78
45.87
54.62
5
0.0469
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2543
2.995
3.954
5.185
0.080
8.557
10.88
13.67
17.07
21.14
26.00
31.75
38.50
4641
55.60
6
0.0517
0.0846
0.1370
0.2116
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.850
8.787
11.12
13.98
17.44
21.59
26.53
32.38
3954
4757
56.60
^LL^Jt
£7-Z7.
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.785
2.379
3.169
4.174
5.442
7.024
8.981
11.38
14.30
17.82
22.05
27.07
33.02
39.00
48.14
57.61
8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.819
2.449
3559
4.289
5.585
7.202
9500
11.65
14.62
1851
22.52
27.62
33.67
40.75
4043
58.63
9
0.0598
0.0962
0.1567
05383
0.3493
0.5035
0.7144
0.9980
1.378
1.875
2.521
3.351
4.406
5.732
7.384
0.424
11.02
14.06
16.61
2240
28.18
. 3443
41.82
4043
8047
-------
                        METHOD 18 FIELD DATA SHEET
Plant:.
Date:_
Location: *^.~ ,S>
Run #:_
Stack I.
Pbar:
Sample Tube #•
Operators:_jol
Leak Check: Pre:
                         Post-
    Traversa
     Point
    Number
                 Velocity
                  Head
                 in. H,O
Stack
Tamp.
                                          Tested Analyte:.
                                          Orifice Tank #:_
                                          Pump/Rotometer #:_
                                          Pt:  Pretest (mm Hg):	
                                              Post-Test (mm Hg):_
                                          Tt:  Pretest
                                              Post-Test fF):_
Time
i^zfl'e t_
132^. /3
2.3.30. 0*
i-b^i. ^•L



Gauge
Vacuum
(Hg)
/
/
1
1



Flow
Setting
l&c*.
>*>«.
.*•'(-
,40tt.



^
95
fV
             Time: Start:/-**/  Finish:/?>/  Total: J'
             W/B:   —B/B:  — O2:  *•>  CO2:..Q_


             Md = (0.44x%C02) *• (0.32 x%O2) -r (O^Bx0/.,^)


             Md = (0.44 x  &  } •>• (0.32 x Z.«   ) t- (0.28 x T^  )

             Md =  "*•*'*
                                                     % HO      % HO
                                      f«/  Ms = Md x 11 - 	=— i  - 18 (
                                                       • 00
                                                                  1 00
                                          Ms o ( 2.1


                                          Ms =


                                          Ts-


                                          Ps- Pb
                                                            100
                                                      _
                                                      F ™
                                                                       100
                                   °R (°F *460)
13.6
                 13.6
                                                        in. Hg
                                           Vs - 65.49 x Cp x



                                           Vs - 65.49 x (


                                           Vs«


                                           As-
                                                                 Ts(°R)
                                                                 PsxMs
                                                                      )x
                                                         ft/8
                                           Qs » Vs x As x 60 s/m
              Q«


              Qs


              Qs
                                                                    x60
                                                          acfm
                                                           Ps
                                              . .  Q8X17.047X - x<1
                                             •W            Ta
                                                                    100
                                                        X17.847X-
                                                          dscfm
                                                                          >x(1
                                                                                 100
-------
                       METHOD 18 FIELD DATA SHEET
Plant:
Date:
Location:.
Run #:&*••
Stack l.D.:.
Pbar:   **
Leak Check: Pre:
                       Post:
                                       Tested Analyte:
                                       Orifice Tank #:
Sample Tube #•&•»-**,  
Time
T76Z. f ^
llLV. iS
•—> — > / IT t/*1
7 ' C* -X • I
TlU,. (,3



Gauge
Vacuum
(Hg)
;
f
1
/



Flow
Setting
/$*£«.
!**«.
,6ffct.
,4*'*



T*.
7*J
-ic
7^
tr
Traverse
Point
Number
i
Z
^•
y
i
(.
r
c
3
V
.*
V
/
t
3
»
4
V
f
1
3
ft
>
U

Velocity
Htad
in. H^
.tf*'
.ot
«6
. ffC*
.01
Ofi
.df
.09
.oT
• oc
.46
.Of
.10
• «f
,ftO
.^5
.oC/
.10
.»1
-------
Plant:
Site:
           WET-BULB/DRY-BULB MOISTURE CALCULATION
         LA'S Co     	Location:     '&=>»,
                       Operators:  TA    Run #:  £F - H-5
                                                           Date:  :5^5-?>
                                 13.6
Barometric Pressure, in. Hg =                       Pbar =
Static Pressure, in. H20 =
Absolute Pressure of Stack =   Pbar i
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td • Tw =
Saturation Vapor Pressure of H2O at Tw (from Table) =   Pvw =
                                   (Ps - Pvw) x (AT)
Ps=   2.1.20
Tw = _
Td =
Vapor Pressure of H2O = Pva = (Pvw) -
Pva =i
                                   2800-(1.3xTw)
                                     X    Z.
                                                   _   £'•
                       2800 -(1. 3 x
Proportion of Water Vapor by Volume = Bws
    -    
-------
- jaa ca
                       GAS VELOCITY AND VOLUMETr.iC FLOW RATE
       Plant: _
       Samonng Location: _0CMLAJ  #
       Run #•   ~*    '
            -  n  —  i
                                                      Date:  .S"-33«n
                                                      CIocx Time:   ) o /
       Barometric Pressure, in. Hg:
       Moisture. %:	
                                                   Ooeratars:
                                    	 Static Pressure, in. HpO:  ', 69
            	  	.vt.. Cry:  -         Pilot Tube. Co:    t *H
StacK Dimension, in. Diameter or Side 1 •    IS>"	Side 2:
Wet Bulb. °F:	
 ?ofcn
NumMr
         L
                      -••a
                      n. M.Q

                           SIAUC
                           "•mo.
                                   ^ ,0.28 1 %N>
                                       Md - iO.44 •     : - (0.32 x      - (0.28 X    )
                                                  ^ M,O      S M,O

                                                   100   *     100
                                                              too
                                                                         100
                                                      13.8 "*            '3.8
                                              P. -
                                                  65.49 « Co «

                                                                    i cm


                                                                          i
                                                            «*

                                                             2
                                              QB.M-Oai17.e47X — i<1
                                                •*•
                                                           117^71
                                                                     100
                                                             Pt     *H.O
                                                                                 
-------
                          METHOD 18 FIELD DATA SHEET
           Plant:
           Date-

           Run #;9-//-3
           Stack I.D.:   it"
           Pbar:_b
   Sample Tube*: 4 -/I-. a/1 -  9- ,1-3 A
   Operators:
   Leak Check: Pre: .000  Post:
                  J5TT
Time
/03^
/.Q*it
IOZ8-
not
n \s
I I 80

Gauge
Vacuum
(Hg)
CD
O
*>
O
O
O

Row
Setting
3SO CC/W




\




f

<\>3f
1$ fn>ri d
€J
       Traverse
        Point
       Number
      A  ' L
           3
             + (0.28 X ^h^)


                                           Md - (0.44 x    ) + (0.32 X    ) -•• (0.28 X


                                           Md-  IK M
                                                     % H0

                                                           100
                                                                       %H_O

                                                                      'H3-
                                                                     100
                                           Te.
            P..
                                                         . HO
                                           V« -
                                           v« - es.49 x <
                                                                Pax Ma
                                                         ft/I
                                            Qe- VaxAaxflOa/m
                                            Oe-
                                                -0. K17.B47X
                                                                   x00
                                                                  %K,0

                                                        X 17.847 X-
                                                                              100
-------
Plant
Sam|
Runl
Prete
Prete
Tr«v*r*4
Mnl
NumbM

























|

: b~pfaGb - — r Ifivc^vt «-.i San
ilingLoc
^umbflr:
si Leak F
si Leak C
Sampling
Tkm
(rrtn)
<96
-ifl_
PO
30























abbn 0(5 fi' it- Ji ^ Pba
9-/y-^- Data: S-Z^-^7 CO;
late: ,OOlP cfm @ )L in Hg Prol
Jheck: Phot: — - Orsal: 	 Slac

dock Tim*
(24-hour
dodi)




























GM M«l«r
Rcadng
-9/0. PH 3-
7/)
inH2O
X/X ^'' ^













	












Nozile ID:  -
Assumed Bws:
Meter Box #:
                                     Thermocouple
                                     Filter #:  ^^
                                     Y:
	Pilot #: ST- 3   Post Test Leak Rale: /coo cfm @^y in. Hg.
 As:	—       Posl Test Leak Check: Pilol:	 Orsal:  	
Oi6c« Pr«»Aui« Oitt»«nliaJ
(AH) in ICO
D«s»*d | ActjaJ
Stack
Temp
0*1
lampeiatur*
°F
Piobe | Fdtec
knpingai
T»mp
°F
Dry Gas Metal Temp
(TnT^F)
OuBei
(Tm oul°F)
Pump
Vacuum
(in.Hg)
'•'V//''//////////////// ",• • v/////// ///////. 'V//////,y,
Iff (&
/ f ^Typ
/ 1 ?£>




























































































_..


























&J)
H (o
^£
-------
                       SAMPLE RECOVERY DATA
PLAiNT
DATE
SAMPLE LOCATION
TRAIN PREPARER
                       Sample Box No.

                       °]
                   Run No. .

                   Job No. _

                   Filter No.
SAMPLE RECOVERY PERSON
COMMENTS

FRONT HALF
Acetone
Container No.

Filter
Container No.

Description of Filter
 Samples Stored and Locked

 BACK HALF/MOISTTJKE
 Container No.        	
 Liquid Level Marked
                                               Sealed
\
Liquid \
Level Marked \
\


Sealed

Sealed
    IMP. NO.
               CONTENTS
INITIAL VOL
   (ml)
                                                  WEIGHT (gramsi
                                        INITIAL
                                                     FINAL
                                                                  NET
                                                   Co|.4-
                            130
           TOTAL
-------
3 at
              EPA METHOD 4 MOISTURE CALCULATIONS


     PLANT:   LA^rJZ _ SOURCE/RUN #:.2l/tL_ HATE:   5 -ZV.37


     1 .  Leakage Correction for Volume Metered
          vmc=vm-(Lp-0.02)xQ


          Vmc=(       )-(        -0.02)x(


                         ft3   ,,
      2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)


                                Pbar-MAH/13.6)N
          Vm   =17.64 xVmcxYx

             std
                = 17.64 x ( j\flia )x(0fltb  )x
                                                         i.at,/13.6V
           •"std         ^^^•..~ ,   i~.,v*,  ,  y       ^ 545



          V"std = ^'UZ  dSCf

      3. Volume Water Vapor Collected, Standard Conditions


          Impingers & Silica Gel = V...  = 0.04707 x (W. - W.}
                               wstd             f    '

                              Vw  = 0.04707x(  3.0   )
                               wstd
                              Vw   •  Q.I4I
                               wstd
4. Percent Moisture, by Volume

                V,

    BWS=    rr-
                        wstd
                     wstd    mstd
           j  -  _  (  0-l4f   )
           'W8	7^
                          gwO.5%  Hbid'We '                       A

-------
                GAS VELOCITY AND VOLUMETr.-C FLOW RATE

Plant:   £f\^<->  •	Date: 5^3-?-?

Rm * ^ ?C'C/T°n: ^U^^q	 CIOCK Time:  'SO^
                                         Static Pressure, in. HpQ:  —,
Barometrjc Pressure, in. Hq: d<$.
Moisture. %:^=^_	Molecularwt.. Crv: 	      Pilot TubeTCo:  ,99
Slack Dimension, in. Diameter or Side 1:   JS "	Side 2:
Wet Bulb. °F:
                                     Md • I0.4A • %CO..) -r .0.32 x %O.> «
                                                           - <0.28X
                                                                         fft  .
-------
                       METHOD 18 FIELD DATA SHEET
Plant:   ^-*s «•
Date:    ,r-> -
Location:_
Run #:  /J
Stack I.D.:
Sample Tube
Operators:
                            /0-M-
Leak Check: Pre: >^«/    Post:
1^,36
  / CO , *to
• o-y  <^
™OC:^
                                                  Tested Anaiyte: $''T/X£*JiL
                                                  Orifice TanK #:      :.	
                                                  Pump/Rotometer #:  	
                                                  Pt:  Pretest (mm Ho^:	
                                                      Post-Test (mm Hg):	
                                                  Tt:  Pretest fF):.
Post-Test fF):_
                                                  Time: Start:c>9/3Ftnisn:/gyg Total:  £?o
                                                  W/B>	D/B: -— O,.: —
Gauge | FIow
(H^ Settin9
ffit-3 0 l-xo/itf/j
OS 9? 1 o 1
^^7'?P- 1 (9 1 1
f,QH'^ 10 | I
#5'2 C
0$OA 0 |
/6JO O 1 V
 rl flw
TrovcrM
Point
Number
A /
2.
5
f
f
&
ft 1
>
i
f
/
(i













Velocity
H«M
m.H^J
. i-3
/q
./sr
HH
,9
.Q3'3
.^Jiy
9'?':5
^y-3/












A,^ S3 1
                                       Md - 10.44 x %CO,) - (0.32 x %O,J ^


                                       Md = i0.44 x    ) - (0.32 x   ;  * (0.28 x
                                    '»
                                       Md -
                                       MS - Md x (
                                     fr
       i H,O      % H,O
       	1_. - 18 ( 	i— 1
        i00        i00

       xd- _£!_»-,8(_2!
            100         100
                                                      2i\    F-  bll    R ( F»460)

                                                      Pb +-IL.- ( ^.Ufe ) * '-&'
                                                          13.8     '         13.8
                                       p.- ;i,(
                                       Vs - 85.49 x Co x V$P~ x '\
                                       Vs • 65.49 x I


                                       Vi- 3-
                                                                  )x(
                     )x
i-
                                                    ft/»
                                       Q« • VsxAaxeOs/m
                                       Q« -
                                                              xflO
                                                      Pa      *l
                                       Q>.M=lQlxt7-847x	««	*— )
                                         •W           T«       100
-------
     FIELD DA I A SHEET
Plant:  c"* S c 6	
Sampling Location -ft /O oo«~»
Run Number: |0~M\   Date:
Sample Type:
Pbar  3*M
CO2:
Ps:  -
02:
                                                           Thermocouple it:
                                                           Filter #:  	
Pretest Leak Rate:  .^p I  cfrni® \s in. Hg.
Pretest Leak Check: Pilot: _J/Orsat:  *•••%
Probe Length/Type:  /X
Stack Diameter:  ^ $ "
                           Pilot #: Sr- 3
                        As:
Nozzle ID:	
Assumed Bws: —
Meier Box #: y 4-
Post-Tesl Leak Rate: . Ope  cfm @ _/& in. Hg.
Post-Test Leak Check: Pilot:	Orsat:
                                                                   AH@: /
TravwM
Nurnbe



























Sampling
Time
(mln)
no

3#
^£>
*-lO






















OodcTime
(24-hour
dock)
&9/Q
W93

^^f2 ^f ^^
^^ ** j""^\
f_J "1 , j ^






















Goa Meter
Reading
f 1tt ^^ I ^*
*Q * v ' 9 1 ~^
^^. 7^
011 ,
^03 /QiQ
"71 C . OH *






















Velocity
Head (Ap)
lnH2O
Orif ce Pressure Difterential
(AH) in H2O
Desired
Actual
Stack
Temp.
(Ts)
Temperature
°F
Probe
Fdter
Impinger
Temp.
°F
Dry Gas Meter Temp.
Inlet
(Tm in°F)
y/////////////////////////////////////////////////.


























If $b
/'?














































































?















-































6> °
^/
5=3
57
s *>••





















<^o
?"3
$ ^
^ ^
— ^ 	

















->- . .



Outlet
(Tm out°F)


S*9
$ S"
^^ O'






















Pump
Vacuum
(in. Hg)
y
4
t-f
fy
~jn/"





















-------

PlantL
Date:
 SAMPLE RECOVERY DATA
	  Run No.:
                  ^~^_  Job No.:
                     Sample Box No.:
Sample Location:.
Sample Type:	2
                                            Filter No.:
Sample Recovery Person:
Comments:	
FRONT HALF
Acetone
Container No.;
Filter
Container No.:
                          Liquid
                          Level Marked:.
                           Sealed:
                                             Sealed:
Description of Rlter:
Samples Stored and Locked:
BACK HALF/MOISTURE
Container No.:	
Liquid Level Marked:
                                             Sealed:

IMP. NO.
1
2
3
4
5
6
CONTENTS
IKo
VKo
l«W
*(^o



WEIGHT farams)
INITIAL
6a?
t^^-s
t^-O
7^o


9-^.f
FINAL
c/u
C^^
t^.t
-7JT/.4


>^.t
NET
-,i
0,3
,t
U


Z «7.
Description of Impinger Catch- ,.
                                                                          |vl\
-------
.3 ai
              EPA METHOD 4 MOISTURE CALCULATIONS


     PLANT:  LAACO _ SOURCE/RUN #: IQ-U-l  PATE:


     1 .  Leakage Correction for Volume Metered


         Vmc = V (Lp - La) x 9

         Vmc=Vm-(Lp-0.02)xG


         vmc=<       )•(       -0.02) x(       )


                        ft3
     2.  Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)


                                Pbar-MAH/13.6)N
               = 17.64 xVxYx
                        mc
                                        )x
                          dscf
     3.  Volume Water Vapor Collected, Standard Conditions


         Impingers & Silica Gel = V...  = 0.04707 x (W - W.
                              wstd            f   '

                             Vw  = 0.04707 x( 2  2_
                              wstd            *•'*-

                             V,«  =   O.\o4


     4.  Percent Moisture, by Volume


                     V,
wstd
         R   -         WsW
         °ws	
                  Vw  -K Vm
                    wstd    mstd
         BWS =
-------
                GAS VELOCITY AND VOLUMET-C FLOW RATE
Plant:_LflSCO                            	 Date:  5^33-97
                                                     CIocx Time:  // o o
Samoung Location: ffite
Run *:  IO-\\  -Z
                                           Ooerators:.
Barometric Pressure, in. Hq: 8ft ,<1%        Static Pressure, in. HpQ: -,  g/
Moisture. %:	Molecular wt.. Crv:	      Pilot Tube. Cp:^_~ "
StacK Dimension, m. Diameter or Side i •  JS''     	Side 2'   	
Wet Bulb. °F:  	
    'oint
   Nuowr
  /?'/*
                              Dry Bulb. °F:
              V.toOTV
               n M_Q
                n
                           StAcic
                           "•mo.
                            a_
                        91
  A  ~(    \   .if.     \
Md - <0.44 H %CC,> » '0.32 x %CU - .0.28 X %H,»

Md - 10 4* H    ) - (0.32 x     - (0.28 1    )
                                         • Md id
                                                 iM.O
                                                  too
                     ,H,0
                     100
                                                      100
                                                                 100
                                       P«-Pb - S P"  - i
                                              13.8
                                                             ,3.8
                                       P,.
                                                   -n.H«
                                       V« • 65.40 It

                                       v«.

                                                                 •f
                                                    w.
                                                     2
                                       Q«"
                                       o..
                                                             xflO
                                                            %H.O
                                       °»-d-
                                                  X17J47K"
                             Ml-

                                                                              a'/,
                                                                              O
\*L
                                                                            A ..
-------
                   FIELD DATA SHEET
& lO
Plant:	
Sampling Location
Run Number: ,*/>  Ps:  -', gj
CO2    	     O2:  	
                                         Noule ID:   ---  Thermocouple #:  V/3
                                         Assumed Bws: ~   Filler #:
                      -	Meter Box »:  ]\   Y:
Probe Lenglh/Type:  J7$3    Pilot *: $7^J5   Post Test Leak Rale:
                                                                              cfm
Slack Diameler:
                 "
                       As:
                                          -2$ -ft
Posl Test Leak Check: Pilol
/^in. Hg
rsal:
Trav«rM
Pobt
Numb*



























Sampling
TVm
Mn)
<90
At)
90
no
1O






















Ooc* Tim*
doe*)
IQo\
1^1 1
O5|
I P ^/
/^-*1l






















Gu Meter
Beating
(Vm)ft3
^VP/VSO
^0,55^
^^,30
•?££ /3o
9*73,^70





/I ' 1
9
3
^^
5^
^^

£) " /
^
3
V
Y
333

53 0
23->
Q3V
4^7
>?30
ii3|











Te-^f>





















	



&











Deratui*
°F
| Filter
Impingai
Temp
°F
Dry Gas Maler Temp
Omin0F)
Oudel
(Im outcF)
Pump
Vacuum
(in.Hg)
: '///////////////• '/////////,









v.io
3%^5t
•j&
yi^5
J^^.










60
^ ^
^ t
-***-





-fft>

ftciivi

l*<. 4 rh











fS"
96
^
J&--





















&S
?0
£*£
£g~






















^

Y
_i....





















                                     B
                                                       lm =
                                                                                            .   !
-------
Plant:

Date:
                  SAMPLE RECOVERY DATA

                  	   Run No.:

                  	 Sample Box No.:  W -Co     Job No.:
Sample Location-

Sample Type:
                  \0 Oocj
                                             Filter No.:
Sample Recovery Person:

Comments:
FRONT HALF
Acetone
Container No.:

Filter
Container No.:
                          Liquid
                          Level Marked:.
Sealed:
                                             Sealed:
Description of Rlter:
Samples Stored and Locked:

BACK HALF/MOISTURE
Container No.:	
Liquid Level Marked:
                                             Sealed:

IMP. NO.
1
2
3
4
5
6
CONTENTS
Hn>
VHo
£*fTr
*/c-


TOTAL
INITIAL
VOL (ml)
100
Ue?
^
3^0



WEIGHT faramsl
INITIAL
6(U
G37.^
t^-fe
"?3^3


>-q<^G.3
FINAL
f2>'
GVf
6>>.y
4^3.C
NET
1,4
D.O
o.s
s.-t


-?- 3
Description of Impinger Catch- 	
-------
        EPA METHOD 4 MOISTURE CALCULATIONS


PLANT:   LAS Co _ SOURCE/RUN #' IQ-H-?  DATE:


1 . Leakage Correction for Volume Metered  ,
         W °-02) x 0 .


    Vmc=(       )-(        -0.02) x(
                -
        V_ -^ <^ •"" t-i A  **
     me" '-r 7.^11)  ft
2. Volume Metered, Standard Conditions (68  F, 29.92 in. Hg)


                           Pbar-MAH/13.6)
    V     = 17.64 xVxYx
      m       .     mr
      mstd
    Vmstd= 17.64
       std

 3. Volume Water Vapor Collected, Standard Conditions


     Impingers & Silica Gel = V ...   = 0.04707 x (W. - W. )
                           std             '    '

                              = 0.04707 x(  >>)
 4. Percent Moisture, by Volume
                                        _scf
                           'std
               f    4. W

               wstd    mstd
     Bws =
-------
ana
100
                             METHOD 18 FIELD DATA SHEET
      Plant:.
      Date:_
             >e o
Tested Analyte:.
Orifice Tank #:_
                   /v»fl-4
Location:_
Run #•   A/M-n
Pump/Rotometer #:   v/*
      Pbar:    Zr*/g
                                             Pt:  Pretest (mm Hg):	n.
                                          Post-Test (mmHg):_^
                                      Tt:  Pretest f F):_
      Sample Tube #:	
      Operators:   Si M4
                                          Post-Test fF):	n.
      Leak Check: Pre:   >/    Post:  ,X
                                      Time: Start:04H  Finish:n>H   Total: m
                                      W/B:  -  D/B:—	O2:_^
                          .C02:_
                                             Md = (0.44 K %CO2) 1- (0.32 X. %O2) -r (0.28 x %


                                             Md = (0.44 t.    ) +• (0.32 X    ) •)• (0.28 x


                                             Md =
/5 
-------
          APPENDIX A. 1.13

             Condition 12
(includes flows, moistures, and Method 18)
-------
a at
                              METHOD 18 FIELD DATA SHEET
Plant:.
Date-
       Location-  ^V./i
       Run #;ttE- a-'
       Stack I.D.:
Sample Tube #:.
Operators: iP>
                                     - tfe
Leak Check: Pre:
                              Post-
                                              Tested Analyte:.
                                              Orifice Tank #:_
                                        Pump/Rotometer #:
                                        Pt:  Pretest (mm HQ):
                                            Post-Test (mm Ha):   -
                                        Tt:  Pretest fF):_
                                            Post-Test fF):	n.
Time
733/, JO
X3^/- 3^. /^



Gauge
Vacuum
(Hg)
i
/
/
/



Flow
Setting
i£a ct-
/Soff.
iSC><.C-
/5S
W/B:_££_D/B:^_02:_ZJ_C02:_a_


Md = (0.44 x %CO2) i- (0.32 x %02) -r (0.28 x "/oN^
Travarsa
Point
Number
/
r
3
y
5
L
7
f

i
I,
*
H
f
(,
1
4






	 	
r*p
Velocity
Head
in. H^
.^T>
.ZT
. 3°
,3/
.3-?
.03
.1*
18

. ?(.
"71
77
.2ft
•2-r
.-ZT
21
.21







D.^B
Stack
Temp.
°F
7 9
•79
11
Tf
7f
->^
i?
7^

1 f
"7?
-?1
7?
77
7^5
7^
11







Ti> W
                                        •Md = (0.44 x


                                        Md =  2.^



                                        Ms = Md x11
                                                              (0.32 X
                                                                 •i- (0.28 x
                                                           100
                                                                     100
                                                                100
                                                                          100
                                               Ma
                                                       .b^
                                               r,.  71
                                                       13.6
                                                                       13.6
                                         Vs - 6S.49 x Cp x



                                         Vs - 85.49 x ( ,


                                         v* -
                                                                     Ts(°R)
                                                                    PsxMs
                                                         ) X (
                                                                         )x
                                                AS-  .
                                                Qs - Vs x As x 60 s/m
                                         Qs»

                                         Qs»



                                         Q».td



                                         ^rtd3


                                         Qsatd-
                                                                       x60
                                                              adni
                                                               Ps     %H-0
                                                     Qs x 17.647 x - x (1 - - £-
                                                               ^      100
                                                            X17.847X-
                                                                                   100
-------
i acn
               WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: / /V^-O
Site: /V\4j^, ^rvW^u«J\~ Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. HoO -
Absolute Pressure of Stack - Pbar + -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td • Tw =
Saturation Vapor Pressure of H2O at Tw
Vaoor Pressur@ of HoO — Pva — (Pvwi -

i „ .i« . fi\ r
Location. j'lAiAJ z,x ^MU.^T'
7$ Run #: fle-ii-i Date: 5
Pbar= 2*1 $O
Pg = . Z> -?-
-^ PS= ^13/
I3.b
Tw = U U>
Td= 9 ?
AT= /^
(from Tahlp) - Pvw = ^/. ^H ^'L
(Ps - Pvw) x (AT)
. 2800-(1.3xTw)

-ll'l*
in. Ha
in. HLC
2
in. Hg
°F
°F
°F
in. Hg
in. Hq
          *  >~n L '      2800-(1.3 x ^




      Proportion of Water Vapor by Volume = Bws



      '0....-   (P^)
uvvo
Tamp.
OF
0
10
20
30
40
50
60
70
80
90
100
110
120
130
140
150
160
170
180
100
200
210
220
230
240

0
0.0376
0.0831
0.1025
0.1647
0.2478
0.3626
0.5218
0.7392
1.032
1.422
1.032
2.598
3.446
4.525
5.681
7.569
9.652
1220
1529
10.01
23.47
28.75
35.00
4241
5044-
>S)
1
0.0398
0.0680
0.1080
0.1716
0.2576
0.3764
0.5407
0.7648
1.066
1.467
1.002
2.672
3.543
4.647
6.034
7.750
9.685
12.46
15.63
10.42
2346
2043
35.88
43.11
51.76
( ^.?» )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1603
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.180
7.952
10.12
12.77
15.98
19.84
24.48
29.02
38.37
43.92
52.70
3
0.0441
0.0728
0.1186
0.1876
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.38
13.07
16.34
20.27
24.07
30.52
37.07
44.74
53.65
4
0.0463
0.0768
0.1248
0.1955
0.2S91
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
6.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.57
54.82
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.1 65
6.880
8.557
10.68
13.67
17.07
21.14
26.00
31.75
38.50
46.41
5540
e
0.0517
0.0846
0.1370
0.2118
0.3120
0.4S20
0.6442
0.9046
1.253
1.712
2.310
3.081
4.083
5.302
6.650
8.787
11.12
13.98
17.44
21.59
26.53
32.38
39.24
47.27
56.60
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4688
0.8669
0.9352
i.293
1.765
2.379
3.169
4.174
5.442
7.024
8.981
11.38
14.30
17.82
22.05
27.07
33.02
39.09
46.14
57.61
8
0.0571
0.0932
0.1502
0.2292
0.3304
0.4858
0.6903
0.9666
1.335
1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1821
22.52
27.62
33.67
40.78
4949
5843
9
0.0598
0.0982
0.1567
0.2383
0.3403
0.5035
0.7144
0.9989
1.378
1.675
2.521
3.351
4.406
5.732
7.384
9.424
11.02
14.06
1841
2X09
28.18
3443
41.62
4043
5847
-------
          Plant:.
          Date:_
 METHOD 18 FIELD DATA SHEET

	     Tested Analyte:    ^/^^
	     Orifice
          Location:
          Run #:
          Stack I.P.:   'i. s
                  Pump/Rotometer #:	
                  Pt:   Pretest (mm Hg):.
                                                   Tt-
                      Post-Test (mm Hg):.
          Sample Tube #:.
          Operators:.
          Leak Check: Pre:
    '	     Time: Start:^&££_ Finish :_id££_Total:_&£
 Post: V£>ft?      W/B: 60j
o
H>
lt>
x>
•"*>
so
t*
Time
->->-! °.^1
•012.37





Gauge
Vacuum
(Hg)
/
/





Flow
Setting
\*0c^
-S o f.<-
,*>
\ V
\











Stack
. Temp.
°F

























                   Md = (0.44 x %CO2) -t- (0.32 X %O2) -r (0


                   Md = (0.44 x    ) -i- (0.32 X     ) -t- (0.28


                   Md =

                             % HO      % HO
                   Ms = Mdxd • 	— '• - 18 ( 	i
                               100         'CO
                                                    Ms = (      ) x(1


                                                    Ms-


                                                    T,.       °F =
                                                    Ps - Pb + -§^- = (
                                   	I - 18(	)
                                    100  '       100
                                       ) •*•
                                                                             13.6
                                                    Pa
                                in. Hg
                   Vs " 85.49 X Cp x JEF '




                   Vs - 85.49 x (        ) X (


                   Vs -           It/8



                   As »           "   .


                   Qs » Vs x As x 60 s/m
                                                                             Ms
                                                                               )x
i
                                                     Ga-


                                                     ds-
                                  Acfm
                                                                     Ps
                                                                             x 60
                                                                            %H0
                                                     Q»std=Q« 17.647X — XO   1QO
                                                                  X 17.847 X-
                                                                   dseftn
-------
                             METHOD 18 FIELD DATA SHEET
       Plant:.
       Date:   5-zq-r
                                      Tested Analyte:.
                                      Orifice Tank #:_
       Location:.
       Run #:  A
       Stack I.D.:_iLJL
Sample Tube #:»
Operators:    rW-
                                      Pump/Rotometer #:
                                      Pt:  Pretest (mm Hg):
                                          Post-Test (mm Hg):
                                      Tt:  Pretest fF):_
                                                 Post-Test i°F):      '—
Leak Check: Pre:
Ibif
                                             Time: Start: '6*v Finish:  "_**_ Total:.
                             Post:_^2iD    W/B:lj^D/B: 76.  O2: "^
0
A
u
lo
4»
#
(A
Time
2-333. /-z
2 V3^/, ^o





Gauge
Vacuum
(Hg)
/
j





Flow
Setting
ISO £.<-
ISa <*,
ISO ^
/So e-e.
/SotC
/£0
-------
                             METHOD  18 FIELD DATA SHEET
Date:	2
Location:
Run #:
                                             Tested Analyte:.
                                             Orifice Tank #:_
      Stack I.D.:_jjLJL
      Pbar:   ^."b
       Sample Tube *:ihg5-/z-3/3,
       Operators:   rA-     	
                                               Pump/Rotometer #:
                                               Pt:  Pretest (mm Hg):
                                                   Post-Test (mm Hg):
                                               Tt:  Pretest fF):_
                                            Post-Test ff=)-	
                                        Time: Start: *£LZ_Finish:_
                                                                         Total: ex?
       Leak Check: Pre:
                             Post:
                                                                    CO2: o
//
i\i5
'TOf
           Time
         -nil. fV
                 1Z
        •nf/.  73
                        Gauge
                       Vacuum
                         (Hg)
          Traversa
           Point
          Number
                       Velocity
                        Head
                       in. H^O
                            Flow
                           Setting
                                 ISO C<-
W/B:   — DIB: — Q2:  *.


Md = (0.44x%CO2) +• (0.32 X%O2) i- (0.28 x%Nj)
                                           60
                            Stack
                            Temp.
                                              Md = (0.44 x    ) -i- (0.32 x
                                              Md
                                                  Mdxd - 	—\ • 18 (	=-
                                                          100        100
                                                                         (0.28 X    )
                                              Ms « I
                                                               100
                                                                         100
                                                          "F-
                                              Ps - Pb -t-
        S.P.
        13.6
13.6
                                                           in. Hg
                                                Vs • 65.49 x CD x



                                                Vs - 85.49 X (


                                                Vs-


                                                As-
                                                                    Ts(°R)
                                                                    sxMs
                                                                        )x
                                                            ft/s


                                                            .2
                                               Qs - Vs x As x 60 s/m
                                                                      x60
                                               Qs-
                                                              acfm
                                                              Ps
                                               Qs . .= Qs x 17.047 x — x (1 • - — )
                                                 »W            T,      100
                                                           x 17.847 x-


                                                             dscdn

-------
                              METHOD 18 FIELD DATA SHEET
      Plant:.
      Date:_
                                        Tested Analyte:.
                                        Orifice
      Location:  A/U-.^ g.i
      Run #:_rv\e-_f7-^
      Stack I.P.:  n, 5
      Pbar:   -z^. 3
                                        Pump/Rotometer #\ \JOST Jt'Z-
                                        Pt:   Pretest (mm Hg):       ~~
                                             Post-Test (mm Hg):
                                        Tt:   Pretest fF):	1_
Sample Tube #:.
Operators:  rft
                                   A
Leak Check: Pre:
                              Post:
                        Time: Start:_/i2£.
                        W/B:_6ll_D/B:J
                     Finish:/zojf  Total: Lo
                     g_02:^_C02: 6
•' '5  /o
     74
If 35
           Time
  Z33 7, 73
        1/rs
 Gauge
Vacuum
  (Hg)
   /
                            Flow
                           Setting
                                  . 60 6C
                                               Md = (0.44x%C02) •" (0.32 X%O2) T (0.28x%N2)

65

66
Traverse
Point
Number
i
Z
3
•^
5
(.
1
t

1
^
T,
*/
J
6
7
?








Velocity
Head
in. H^
t3
. 2-J
• Z.~?
.7.")
3,;
35
^^
.3-7

.2.5
. *•<*
.7.^
,-i.l
2-S
. ^^
.?(•
.20








Stack
Temp.
yo
FO
ffl
?'
^/

^ '
yo

to
?6
fO
9°
no
<%0
g0
$°







1i --W
                                               Md = (0.44 x    ) + (0.32 x


                                               Md =  ~L<\
                                                                         (0.28 x
                                                   Mdx(1
                                                   % HO
                                                   - £_ )
                                                     1 00
                                             % HO
                                             -
                                               1 00
                                         Ms -


                                         Ts.



                                               * 13.6

                                         Ps =  Z«. ->    in. Hg
                                                                     °R(°F-460)
                                                                       13.8
                                                            —   J   Ts <°R)
                                                Vs - 85.49 x Co x VAP J
                                                                     ps X MS
                                                Vs - 85.49 x (  ,
                                                                ix< .
                                                                     «
                                                AS-  , , .-x    n'
                                                     J /b T

                                                Qs • Vs x As x 60 s/m
                                                Qs-

                                                Qs-
                                                                       x 60
                                                        acfm
                                                                Ps
                                                Qs . .= Qs x 17.647 x -^- x (1 • 	*— )
                                                  •W            Ts       '00
                                                             X 17.647 X-
                                                                       •*(1'—>
                                                QflAftWeW
                                                *"*WQ
-------
            WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant:
Site:
                           rators:   rft
Location:
Run #: fl
                                                             Date:
                            Pbar +
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack =
Wet-Bulb Temperature, °F  =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of  HpO at Tw (from Table) =   Pvw =

                                    (Ps - Pvw) x (AT)
       Pbar =
        Pg =
        Ps =
        Tw =
        Td =
                                                         ;?
-------
                GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:
                       Date: _s	
                       Clock Time:   i2n
                                           Operators:.
Sampling Location:
Run#:
BaromeirTcTPressure, in. Hq:   213	 Static Pressure, in. HoO:  .«
Moisture, %:  i,*??^       Molecular wt., Drv:  zf      Pitot Tube, Cp:_i
Stack Dimension, in. Diameter or Side 1:     /-?. s	Side 2:   	
Wet Bulb. °F:     6g
Dry Bulb, °F:.
Travtm
Point
Number
v • c
Z
•5
V
5
£
?
f

/
z
3
V
5
(,
7
f









V.locrty
Hud
In. H2O
,t3
. 2-0
"•• .^-}.
.2-1
.•*«
.3 I
.33
.36

,zy
.-2-5
.ZLO
• Zl
.25
.2^
>23
.23








^KP-.5/ftc»
Stack
T«mp.
°F
.9 *
f2-
?«•
S-z_
92_
J^
ff-z-
5T-

9T-
71
SI
11
?z.
?7L
§2.
S-''-








T.- P2.
                                       Md - (0.44 x %CO2) 4- (0.32 x %O2) + (0.28 x %^)


                                       Md«(0.44x  o  )+(0.32x ?/  ) + (0.23x7f

                                       Md -  2- "?
                                         - Mdxd •
                                                % H,0      % HO
                                                   '\j_1A*


         Pa. Pb +J£^=( 2*--
                13.8

         Pa.  ^*».3    in. Hg
                                                              13.0
                          Y-5
                                                             (°R)
                                       V«-»b.4UxCpx AP x
                                       V»-85.48 X( ,?7   )x( ,5/00  )X
                                    ^rt
                                       Q«-VixA«x60a/m
         Qs-

         Qs«

         Q».
                                                     actm
                                                      p.      %K20
                                           .= Q«X 17.647 x	x(1- 	*—
                                           *           !•       100
                                                   X 17.647 X-
                                                            21 •
                                     -x(1
                                                                         100
-------
         WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: L/feo
Site: MAio ^U£4u<*4— Operators: ,A|c£
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of Stack = Pbar + — ^L-
13.6
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H0O at Tw (from T
Location: 1Y\<^^^J
Run #: f^t-ii- 1
Pbar =
Pg =
Ps =
Tw = _
Td =
AT = _
able) = Pvw =
Fx v-VAuST
Date: -^ir-S-Zfi'il
^•3 in. Ha
^ in. H2O
tf. ^ in. Ha
Uti °F
fo °F
H °F
b. ulv£ in. Ha
Vapor Pressure of H2O = Pva = (Pvw) -
                (Ps - Pvw) x (AT)
                2800-(1.3xTw)
Pva=(
)-
                 ( 2.S-3
                     2800-(1.3 x   (

Proportion of Water Vapor by Volume = Bws
(Ps)
Temp.
OF
0
10
20
30
40
50
60
70
80
90
100
110
120
130
140
150
100
170
180
190
200
210
220
230
240

0
0.0370
0.0031
0.1025
0.1047
0.2478
0.3020
0.5218
0.7392
1.032
1.422
1.932
2.596
3.446
4.525
5.881
7.569
9.652
1220
1529
19.01
23.47
26.75
35.00
4241
5044-

1
0.0398
0.0660
0.1080
0.1716
0.2576
0.3764
0.5407
0.7648
1.066
1.487
1.992
2.672
3.543
4.647
6.034
7.759
9.885
12.46
15.63
19.42
23.86
2843
35.68
43.11
51.76
                                               in. Hg
( Z1-3 )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1603
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
15.98
19.84
24.46
2942
36.37
43.82
52.70
3
0.0441
0.0728
0.1186
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.36
13.07
16.34
2027
24.97
30.52
37.07
44.74
53.65
4
0.0463
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2,178
2.911
3.848
5.031
9.513
6.351
10.61
13.37
16.70
20.70
25.46
31.13
37.78
45.57
54.62
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.680
8.557
10.86
13.67
17.07
21.14
26.00
31.75
38.50
46.41
5540
6
0.0517
0.0848
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.850
8.767
11.12
13.98
17.44
21.59
26.53
3248
39.24
4727
56.60
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.981
11.38
14.30
17.82
22.05
27.07
33.02
3949
48.14
57.61
8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1821
22.52
27.62
33.67
40.75
4843
5643
9
0.0598
0.0982
0.1587
0.2383
0.3493
0.5035
0.7144
0.9888
1.378
1.875
2.521
3.351
4.406
5.732
7.384
9.424
11.82
14.86
1641
2248
28.18
3443
4142
4843
5047
-------
              GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:
Date:
Sampling Loc
Run #: K&
ation: ^ ad^s-A- Clock Time: £>
/./, /
V«-85.49x< .99 )*< )x<\| 	
Vt« \f. ^ ft/t
A.- <-\.|/^ R2
Qt • Vi x AM x 60 t/m

Q«- x xOO
Q.. t,\^Vl »«*"
P. "HjO,
Q.ttd-Q.xl7.847x ^ x(1- iflo )

^tW" X17.647X— 	 X(1'~!5~>
-------
r
               WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: LASrr>
Site: {^a^ "^p^y^^ Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack = Pbar + -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td • Tw =
Saturation Vapor Pressure of H^O at Tw
Vapor Pressure of H20 = Pva - (Pvw) -
" '\
Pva=( ^, ,.(«:« - .«
Location: fco^ FxM/v^r
~rHJfZS
Tw = 0? 3
Td = H
AT= II
Pvw = D'^^l-
:AT):<
Tw)
) . D.H
. in. Hg
. in. r-LO
2
. in. Hg
°F
°F
°F
. in. Hg
in. Hg
                          2800-(1.3 x




       Proportion of Water Vapor by Volume = Bws
(Ps)
Tamp.
°F
0
10
20
30
40
50
60
70
60
90
100
110
120
130
140
150
160
170
160
_ 190
-200
210
220
230
240

0
0.0376
0.0631
0.1025
0.1647
0.2478
0.3626
0.5216
0.7392
1.032
1.422
1.932
2.500
3.440
4.525
5.881
7.569
9.652
12.20
15.29
19.01
23.47
26.78
35.00
4241
5044-

1
0.0398
0.0660
0.1060
0.1716
0.2576
0.3764
0.5407
0.7648
1.066
1.467
1.992
2.672
3.543
4.647
6.034
7.759
9.685
12.48
15.63
19.42
23.96
29.33
35.68
43.11
51.76
-------
oacu
                       METHOD 18 FIELD DATASHEET
Plant: / AttO Tested Analyte: Vv^^<.
Date: -5-z*-«-i Orifice Tank #:
Location: &*>«. £**,^s+ Pump/Rotometer #: \/o^:3±'2-
Run #: K£- ii-z, Pt: Pretest (mm Hg):
Stack I.D.: zg"*.iV" Post-Test (mm Hg):
Pbar: Tt: Pretest (°R:
Sample Tube
Operators: -
#-R£'K-2*.ae-r2-Zfl Post-Test PR:
-i4- Time: Start: Finish: Total:
Leak Check: Pre: Post: W/B: D/B: O«: ?/ CO«: o


Gauge
Time Vacuum
(Hg)


/v
//
f /
\ (
v >
Flow
Setting
/ SO ec
/^Wt
t~£a(**-
V Jt--
\


£u,*.'c-
Traverse
Voint
NlJlpber
(\
l \
5 \

$
it
i
i
*
«/
*
• (0.32 x%O2) -r (0.28x%N2)
^**/ MJ _ in M v 1 * (O 12 x i +• (0 28 X )
I •: Md = ^4
\ . j % HO % HO
\ ^j _ |y)(J jj/^ ' < 1 8 ( • 'r
\ "" - :^" ,co -' ,00
x Mr^(2^ )x(i- 1-18( 	 )
\-^ 100 100
Ms -
Ts » °F » °R (°F * 460)
13.6 13.6
Ps = in. Hg
^Jp" =
— I isTR)
vs = oa.ta x «-p x vu-- x ^ ps x Ms
Vs - 85.49 x( )x( ) x \l 	
U
Vs « ft/s

A»- rt2


Qs » Vs x As x 60 s/m

Qi - x x 60

Qft * acfin
p, %H_O
Qs . .= Qs X 17.847 X — — x (1 • )
std T« 100


std 100

QS0f^w QlCnll
-------
3 aca cia
                        GAS VELOCITY AND VOLUMETRIC FLOW RATE
       Plant:	
       Sampling Location:
       Run#:_M-_
-------
3 Ql—'
                  WET-BULB/DRY-BULB MOISTURE CALCULATION
       Plant:
       Site:
Operators:  7
                                       Location: _
                                       Run #:  Q6- \z-
                                                                  Date:
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack =   Pbar
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
                                                     _.
                                                     Pbar =
                                     ~  13.6
                         PS = __2>
                        Tw=
                        AT=
                                                                M
       Saturation Vapor Pressure of H2O at Tw (from Table) =   Pvw =  Q. ^
                                          (Ps - Pvw) x (AT)
       Vapor Pressure of H2O = P.va = (Pvw) -
       Pva=(
                                          2800-(1.3xTw)
                              2800 -(1. 3 x
       Proportion of Water Vapor by Volume = Bws
(Ps)
T«mp.
°F
0
10
20
30
40
50
60
70
60
90
100
110
120
130
140
150
100
170
180
190
200
210
220
230
240

0
0.0378
0.0631
0.1025
0.1847
0.2478
0.3620
0.5218
0.7392
1.032
1.422
1.932
2.598
3.448
4.525
5.881
7.569
9.652
12.20
15.29
19.01
23.47
28.75
35.00
42.31
50.84-

1
0.0398
0.0660
0.1080
0.1710
0.2570
0.3764
0.5407
0.7848
1.088
1.467
1.992
2.872
3.543
4.847
6.034
7.759
9.885
12.48
15.83
19.42
23.98
29.33
35.68
43.11
51.76
in. Hg
in. H20
in. Hg
°F
°F
°F
in. Hg
                                              in. Hg
( Z
-------
^
                         GAS VELOCITY AND VOLUMETRIC FLOW RATE
        Plant:	
        Sampling Location: foe
        Run*
                                                      Date:    5	
                                                      Clock Time:    /^-vz-
Barometric Pressure, in. Hg:_
Moisture, %:_J_2l	Molecular wt., Dry:
Stack Dimension, in. Diameter or Side 1:	
Wet Bulb, °F:     6Y	Dry Bulb,0F:.
Operators:.
Static Pressure, in.
                                                                             -,C 2
                                                              Pitot Tube, Cp:_iH_
                                                              Side 2:
                                                      •75-
TravirM
Point
Number
1
1
•}
t
s
c
/
I
T
V
J
0
»
7
1
4
3
C
/
1
1
9
5
6
•

Vtlocrty
Ha«d
in. H2O
.0*
.00
.0^
oO
.oc,
.0 n
OG
.0^
.05
.0^
.65
.06
.C78
.07
.05
,0V
05
.0<*
. 01
.06,
,«

                                               Md -  1.1

                                                          %H,0      %H,O
                                               M« - Mdx(1 -  	—) * 18 (	— )
                                                           100        100
                                                                ' T  ) + 18(  '"
                                                                100        100
                                        Ma-

                                        Ta« '


                                        Pa-I

                                        Pa-
                                                       13.8
                                                                       13.8
                                                            In.Hg
                                                Vs - 65.48 x Cp x
                                        Vl-85.49x( .
                                                                     Pax Ma
                                                                            «i I
                                                                            V
                                                             ft/I
                                        AI-  *f.e-  \    ft'

                                        Qi-VixAix60i/m

                                        Qa-          x
                                                                       xeo
                                                              ftcffn
                                                               Pi     *H,0
                                                    -Qixl7.847x	x(1	2_)
                                                               Ti      100
                                                            X 17.047 X-
                                                              d«*n
                                                                     2.1.

                                                                                   100
-------
  Plant:
  Site:
           WET-BULB/DRY-BULB MOISTURE CALCULATION
                                   	Location:
                                   */ft' Run #:
Sy WvrQperators:
Barometric Pressure, in. Hg =                       Pbar =	<
Static Pressure, in. H20 =                            Pg =	—
Absolute Pressure of Stack =  Pbar +  ; 9             Ps = —*
                                  1 J.o
Wet-Bulb Temperature, °F =                          Tw = :	
Dry-Bulb Temperature, °F =                           Td =	
Temperature Difference, Td - Tw =                     AT =	
Saturation Vapor Pressure of H2O at Tw (from Table) =   Pvw = _IL

                                    (Ps - Pvw) x (AT)
                                                             Date:  5-21-ft
                                                             ;3	 in. Hg
                                                             iii	 in. HLO
                                                                	 in. Hg
                                                            >S
                                                            n
  Vapor Pressure of H20 = Pva = (Pvw) -
  Pva=(
                                     2800-(1.3xTw)
                         2800-(1.3 x

  Proportion of Water Vapor by Volume = Bws

  Bws=   
 Tamp.
 OF
  0
  10
  20
  30
  40
  50
  60
  70
  80
  90
 100
 110
 120
 130
 140
 150
 160
 170
 180
 190
' 200
~ 210
 220
 230
 240
(Ps)
0
0.0378
0.0831
0.1025
0.1647
0.2478
0.3020
0.5218
0.7392
1.032
1.422
1.932
2.596
3.446
4.525
5.681
7.569
9.652
1220
1529
19.01
23.47
28.75
38.00
4241
5044-
1
0.0398
0.0660
0.1080
0.1718
0.2578
0.3764
0.5407
0.7848
1.066
1.467
1.992
2.672
3.843
4.647
6.034
7.759
9.885
12.48
15.63
19.42
23.96
29.33
38.68
43.11
51.76
                                                         °F
                                                         °F
                                                         in. Hg
                                                                       in. Hg
( -2^.1^ )
VAPOR PRESSURES OF WATER
1
*fc
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.982
10.12
12.77
18.96
19.84
24.46
29.82
38.37
43.92
82.70
3
0.0441
0.0728
0.1186
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.829
3.744
4.900
6.350
8.180
10.38
13.07
16.34
2027
24.97
30.82
37.07
44.74
5345
4
0.0483
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
6.313
8.381
10.61
13.37
16.70
20.70
25.48
31.13
37.78
48.87
54.82
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.660
8.557
10.66
13.67
17.07
21.14
26.00
31.75
38.50
46.41
55.60
6
0.0517
0.0646
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.850
8.767
11.12
13.98
17.44
21.89
26.83
3248
39.24
47.27
56.80
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
6.981
11.38
14.30
17.82
22.05
27.07
3342
3949
48.14
5741
8
0.0571
0.0932
0.1502
0.2292
0.3304
0.4858
0.6903
0.9666
'.338
1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.82
1821
2242
27.62
3347
40.75
4943
5843
9
0.0598
0.0982
0.1587
0.2383
0.3493
0.5035
0.7144
0.9989
1.378
1.878
2.821
3.381
4.408
5.732
7.384
9.424
11.92
14.98
1841
2249
28.18
3443
4142
4943
5947
-------
^F7^
F
C
L
F
v^
F
c
C
L

0 V37 o
*«-> »
09 3 1 20
U 101 SO
mtot--rt
METHOD 18 FIELD DATA SHEET
lant: Lf&tD TesteH Anaiyte: 5/v^-^
late: £-£4-^ Orifice Tank #• ~-
ocation: A;*-. Ih.^/ fc-*K«i^^ Pump/Potometer #: \) «^
Traverse
Point
Number
1
t
^
O
.^1 .28
.-W f ^i
••p > 37
«ft ,"2>8
.-p .'V'/
••Jo b .S9
.-« > .bl
.-§5 .y>

20
^o
. 33
. 38
.38
jj
Stack
Temp.
°F
7 JL
72-
7i
7^
7f.
-j^_
-7-t
Tic

-77_
•7 3
72.
1H
7^
72.
•7Z.
^72.







~i> -"f"t-
Md = (0.44x%C02) f (0.32 x%O2) -r (0.28x%N2>
Ls_-Md -> (0 44 X ^ ) +• (0 32 X 3 f ) +• (0 28 x 7 '.' )
% H20 % H20
^2- Ms - ( 2^ )X(1 . '• T ) . i8( ^' ^ )
1 00 1 00
Ts - -) Z. ^P = <"2o R ( F i- 460)
S P •» ^" • Q^^
- 13.6 13.6
Ps » 'Z') • Vt in. Hg
^5?= .tn-v^
f T- /Op\


Vs - 85.49 x (. W )X( )XAJ 	
1 W
Vs « 2«D c/*\ Ws

x» *^ 2
As - % , / = n

Qs - Vs x As x 60 s/m

Qe - x x 60
_ UflOJ _._
Qs - "T*i acfm
Ps %H,0
Qs . .= Qs x 17.047 x 	 x (1 	 *- )


°*std~ XI7.847X *(l 100 '
Qs«td~ HU^f dsefm
./.I.I
-------
           WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: L/^fecO
Site: Aocili'iLj ,-6*1 Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack = Pbar + -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H20 at Tw
Vapor Pressure of HpO - Pva - (Pvw) -
- w' *'
Pva=( ,-,», ,.<2Vi'-..S8
Location: Aw^il/o^ £/i
TM Run #: 4F-\i.-< Date:
Pbar = L-i • 3
Pa = ^3(0
-He" Ps= Z^
13.C -
Tw= u>3
Td= >X
AT= ^
(from Table) = Pvw = D- "S'BU'Z
(Ps - Pvw) x (AT)
2800-(1.3xTw)
4^ )*(. ^? ) 7>4^S3
I^AU^T
fT-ZI-i'-f
in. Hq
in. HO
2
in. Hg
°F
°F
°F
in. Hg
in. Hq
                       2800-(1.3 x   (j^

 Proportion of Water Vapor by Volume = Bws
Tamp.
 OF
 o
 10
 20
 30
 40
 so
 60
 70
 80
 90
 100
 110
 120
 130
 140
 150
 160
 170
 180
 190
 200
 210
 220
 230
 240
(Ps)
0
0.0376
0.0631
0.1025
0.1647
0.2478
0.3626
0.5218
0.7392
1.032
1.422
1.932
2.596
3.446
4.525
5.881
7.569
9.652
1220
1529
19.01
23.47
28.75
35.00
42.31
5044-
1
0.0398
0.0660
0.1080
0.1716
0.2576
0.3764
0.5407
0.7648
1.066
1.487
1.992
2.672
3.843
4.647
6.034
7.759
9.885
12.48
15.63
19.42
23.96
2943
35.68
43.11
51.76
( Ll.iH )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
15.98
19.84
24.46
29.92
36.37
43.92
52.70
3
0.0441
0.0728
0.1186
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.36
13.07
16.34
20.27
24.97
30.52
37.07
44.74
53.65
4
0.0463
3.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.176
2.911
3.848
5.031
6.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.87
54.62
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.680
8.557
10.66
13.67
17.07
21.14
26.00
31.75
38.50
46.41
5540
6
0.0517
0.0846
0.1370
0.2118
0.3120
0.4S20
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.650
8.767
11.12
13.98
17.44
21.59
26.53
32.38
39.24
47.27
56.60
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.981
11.38
14.30
17.82
22.05
27.07
33.02
39.99
48.14
57.61
8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1821
2242
27.62
33.67
40.75
49.03
5843
9
0.0596
0.0982
0.1567
0.2383
0.3403
0.5035
0.7144
0.9989
1.378
1.87S
2.521
3.351
4.406
5.732
7.384
9.424
11.92
14.96
18.61
22*9
28.18
3443
41.82
4949
5947
-------
                GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:  L
                       Date:
Sampling Location:
Run #:
            	  Clock Time:   uzo
             Operators:. rW /
Barometric Pressure, in. Hg:   2.?, 3	 Static Pressure, in. HUO:  -.9-5
Moisture, %:   /-L        Molecular wt., Dry:   *?      Pitot Tube, Cp: .99
Stack Dimension, in. Diameter or Side 1      t^.-ts     Side 2:	
Wet Bulb, °R.
Dry
Travsrss
Point
Mum bar
'
z
3
y
3
^
7
/

/
2.
3
V
.5
fc
7
r









Vstocrty
Hssd
In. H20
. 2?
•-. 3V
30
*> Q
LJ~)
36
• 2.«/
,28

1^
% 3/
. 3/
•3^
.^9
. 33
. 3*.
. ^^







/,/
$p-D/oH&
Stock
T«mp.
°F
70
10
1O
T*>
13
"75
75"
7^

7^
-73
13
13
13
-73
13
-73








Ts"->j

                                      Md «


                                      Md . (0.44 x

                                      Md -  Z f
                    ) + (0.32 X
+ (0.28 X
                                               %H 0
                                      Ms- Mdx(1 - 	—) +
                                                         % HO
                                      T«.


                                      Pa-Pb
                                             13.8
                                                             13.8
                                                  —      T9(°R)
                                      Vs - 85.48 x (
                        )»(
  )X
)F
         AS- ^.J^     n:

         Qs - VsxAsxeos/m

         Qs-          x
                                                             x80
                                       Qt-w-Q.xl7.e47x
                                                  X 17.847 X-
-------
iOCJ
           WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant:  ^ / .A5io
Site:
                             Operators: rA
Location:
Run #:

                                                          Date:
                                       13.6
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack =  Pbar +
Wet-Bulb Temperature, °F  =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H20 at Tw (from Table) =   Pvw =
                                   (Ps - Pvw) x (AT)
       Pbar =
        Pg =
        Ps =
        Tw =
        Td =
       Vapor Pressure of H20 = Pva = (Pvw)
       Pva=
                                          2800-(1.3xTw)
                                          )*( /O      )
                              2800 -(1. 3 x
       Proportion of Water Vapor by Volume = Bws
(Ps)
Tamp.
°F
0
10
20
30
40
50
60
70
60
90
100
110
120
130
140
150
160
170
180
190
200
210
220
230
240

0
0.0376
0.0631
0.1025
0.1647
0.2476
0.3626
0.5216
0.7392
1.032
1.422
1.832
2.596
3.444
4.525
5.681
7.568
9.652
12.20
15.28
18.01
23.47
28.75
35.00
42.31
50.84-

1
0.0396
0.0660
0.1080
0.1716
0.2576
0.3764
0.5407
0.7648
1.066
1.467
1.882
2.672
3.543
4.647
6.034
7.758
8.885
12.48
15.83
18.42
23.88
29.33
35.88
43.11
51.78
                                                                           in. Hg
                                                                           in. H20
                                                                           in. Hg
                                                                           °F
                                                                           in. Hg
                                                                     in. Hg
' Z' " ' v&
VAPOR PRESSURES OF WATER S^
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.180
7.852
10.12
12.77
15.88
18.84
24.46
2942
3847
4342
52.70
3
0.0441
0.0728
0.1186
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.628
3.744
4.900
6.350
8.150
10.38
13.07
16.34
2027
24.97
30.82
37.07
44.74
5345
4
0.0463
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
0.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.87
54.82
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.680
8.557
10.86
13.67
17.07
21.14
26.00
31.75
38.80
46.41
5540
6
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.083
5.302
6.850
8.767
11.12
13.98
17.44
21.89
26.83
3248
3924
4727
56.60
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.981
11.38
14.30
17.82
2245
27.07
3342
3948
48.14
5741
8
0.0571
0.0932
0.1502
0.2292
0.3364
0.4858
0.6903
0.9666
1.335
•1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1821
22.52
27.62
33.87
40.78
4943
58.83
9
0.0598
0.0982
0.1567
0.2383
0.3493
0.5035
0.7144
0.9989
1.378
1.875
2.521
3451
4.408
5.732
7.384
9.424
11.92
14.98
1841
2249
28.18
3443
4142
4948
5047
-------
                        METHOD 18 FIELD DATA SHEET
Plant:   I
Date: S-z^-vt
L
F
c
F
c
C
L

•m o
2*11 /o
•ZS/ V>
'301 30
i 3 ii Ht>
'»' 60
ocation: AwnllU^y r
-------
a D
F umi^m ^mmm
&9
       Date:	£
       Location:.
       Run #:_?
                            METHOD 18 FIELD DATA SHEET

                           	     Tested Analyte:_
                           	     Orifice Tank #:.
       Stack I.P.:  «?
       Pbar:   7.SV, ./^
Gauge
Vacuum
(Hg)
i
/
I
/
,
\
,
Flow
Setting
/ i* ,c
/S^cc.
/5«^<-'
<*a^
•^o e<_
,io^c
'^oct-
T,
Ti
•\s
-11
Traversa
Point
Number
i
1
^
V
5
(,
7
?

J
1
^
«y
5
^
7
&






	 ^
ift*
Valocity
Htad
in. H^
. zz
, 3 /
,3V
.36
.3?
.31
. 3 \
, 28

, 23
t6
.2?
.3*/
36
. i3
. 30
.21







<3£D
Stack
Tamp.
°F
Ti
13
13
IV
76
76
76*
70

"70
1C
16
16
16
10
16
10







%^ ^?<>
                                              Md = (0.44 x %C02) i- (0.32 x %O2) -r (0.28 x


                                             :Md = (0.44X0  )f(0.32xz/ )*


                                              Md =  Z °l

                                                        •>.', HO       % HO
                                              Ms = Mdxd • 	—} ~ 18 ( 	=—
                                                          i00        100
                                                Ts
                                              Ps
                                                                     R (  F «-460)

                                                                     ' .80
                                                        13.6

                                                        . 2*V  in. Hg


                                                        SSSO
                                                                        13.6
                                                                  "\|-
                                                                      Ts(°R)
Vs " 85.49 x Cp x



Vs - 85.49 x ( . \


Vs- 5 1


Ae - 1, / 3     «t'


Qs » Vs x As x 60 s/m


Qt-           x  Z.'3

     < i «^
               acfm
                                                                    PsxMs
                                                               ft/a



                                                                2
                                                                         x 60
                                                                 P,      %H,0
                                                 Qa .^= Q« x 17.647 x	x (1 • 	£—
                                                   std            T§       100
                                                               dadm
                                                                                  5-3 e.
                                                                                               /(*
-------
f
                 WET-BULB/DRY-BULB MOISTURE CALCUU\TION
Plant: LASCL) Location: /-luYi/'^c, ^
Site: AiAlcdiOu^^ £#•* Operators: TA/ Run #:
Barometric Pressure, in. Hg =
Static Pressure, in. H0O =
d.
Absolute Pressure of Stack = Pbar + 9
13.6
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of HpO at Tw (from Table) =
(Ps - Pvw) x
Vannr Prpeicnre nf H~O — Pun — lP\ntj\ 	
$F-I2-^ Date: ^
Ph3r= Z
-------
                GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:   User,
Samonng Location:
Run #:  ^  j l-> [
              Date:   S~^°)  <* 7
                              CJTL*T
              CIocx Time:
                                          Ooerators:   Cfr/<7
Barometric Pressure, in. Hq:   3 «,. 3 6        Static Pressure, in. HpQ:  -.fel
Moisture. %: _J.L?        Molecular wt.. Crv:  Z^.SH    Pilot Tube. CQ:   «9<;
Stacx Dimension, in. Diameter or Side 1:    /5*	 Side 2:
Wet Bulb. °F
                             Dry Bulb. °F:
                                      Md • 00
                                                     too  ' '     too
p«-*>b *-!£_..<
       13.0
                                                            1 3.8
                                                      . f   -»r-R)
                                                      y   PIXMI



                                                                 *
                                      Q«-

                                      o..
                      xOO
-------
   300.:
U4-4-
uf-fe
*;
                                    METHOD 18 FIELD DATA SHEE1
Plant: L*f>co
Date: *<& -5" -3i.^i
Location- &°\ ct/«?o o^-vu)
Run #: ^ -  *
PumD/Rotometer #:
Pt: Pretest (mm Hq): —
Post-Test (mm Ha): 	
Tt: Pretest (°R: —
Post-Test (°F): 	 	
Time: Start: "«* Finisn: l-2'-^ Total: *8
W/B: — D/B: - O«: >« CQ,:_Q 	
r«/> 2 " 2 —
Time
o HoS
10 ii » <:
>« \( 3-3
V (l b5
*-» I! f-5
^ H5s
<<*> \>ov
Gauge
Vacuum
(HaL
f>"
0 '
0
&
b
0
0
Flow j
Setting |
g^rv-^l
as. 1
*5rt
>-So
0-5o
"V^o
'V*-
                                                       Md - (0.44 K%CO,) * (0.32X%0,1 * (0.28 »%H-,\
                                                  WO
                                                       Md » 10 44 x
                                                                      ^ (0.32 x
                                                                                    (0.28 x
                                                                   "a H,0
                                                                                100
                                                                                     too
                                                                       -2*'5'1
Trav«n«
Point
Number
A 1
Z

9.
/
h













v«ioeny
H««0
'n. H^O
' fa
. ^
^1
. fcl
, (*1
. 
-------
                           FIELD DATA SHEET
Plant: MS °t>
Sampling Location # Ps: -0.fc.fc
«?-;l-3 Date: ^"-^'?-c»7 CO2 rf O2: > v
Pretest Leak Rate: . oo\ cftn @ I/ in
Pretest Leak Check: Pitol: I/ Orsat: "

TlOWM
Point
Nwnta




























Sampling
Tlrm
(mln)
O
|0
"Jo
it>
A.D























OochTirm
doe*)
V\\o<>
ML5
\\7>
V.lb5
\V^3






















. Hg Probe Lenglh/Typ
"•J Slack Diameler:
e: ^-^ Pitol #
\3" As: l.2<;
'&

Gaa MaUr
%Y\ ^\°T
V>i.°\
^i^*^
<2 Vo °\
,gv«\ .<\^






















Velocity
rtoadlAp)
inH2O






















s



Oific* PI*OCUI« Orft>i«nlial
(AH) vi ftZO
D«sii»d | Actjal
•'••'///''///Y////
1 ^3
\^
Vvi






















H
1-3
\ J
v.-l






















Stock
Temp
Pio
'/////, •'/•"


























....


	



-

	 	








Noule ID:
Assumed Bws: _j
Meter Box
                                                                           Thermocouple
                                                                           Filter #:
                                                                           Y: ^_.f/
                                                            Post Test Leak Rate:  ^   cfm@ 3  in. Hg
                                                            Post Test Leak Check. Pitol:  >^Orsal:
oVm=
                                                                                             .   .
-------
no:
      Plant:
      Date: 5~-
 SAMPLE RECOVERY DATA

 	  Run No.:

 	 Sample Box No.:  k/~ ^    Job No.:
      Sample Location:

      Sample Type:
A
                            Filter No.:
      Sample Recovery Person:

      Comments:
      FRONT HALF
      Acetone
      Container No.:
         Liquid
         Level Marked:.
      Filter
      Container No. L
Sealed:
                            Sealed:
      Description of Filter:
      Samples Stored and Locked:

      SACK HALF/MOISTURE
      Container No.:	
      Liquid Level Marked:'
                             Sealed:
Ci?>.a
IMP. NO.
1
2
3
4
5
6
CONTENTS
Hio
HID
£»rT?
Vt


TOTAL
Description of Impinger Catch: .
INITIAL
VOL (ml)
Uo
I Oo
—
^b



WEIGHT farams)
INITIAL
ecf/3<
G3«.-y
f^7. |
7437


U^.7


FINAL
} C^;.^
<**IS
f57,3
"7^0,$-


O-VAJ-
NET
4Z.
3.t
, i-
G.^


if?

-------
        EPA METHOD 4 MOISTURE CALCULATIONS


PLANT:  id^o _ SOURCE/RUN #\JLl2^2- DATE: <-;?? "? ?-


1 . Leakage Correction for Volume Metered
    Vmc=(       )-(        -0.02) x(
2. Volume Metered, Standard Conditions (68  F, 29.92 in. Hg)


                          'Pbar-MAH/13.6)N
    vm^ = 17.64 xVmcxYx
      m
      mstd
 3. Volume Water Vapor Collected, Standard Conditions


     Impingers & Silica Gel = V....   = 0.04707 x (W. - W.)
                          wstd             r    '

                        Vw   = 0.04707 x( Iff. fl
                          wstd


                        Vwstd

 4. Percent Moisture, by Volume

                 V
     R            wstd
     bws      v    + v
               wstd    mstd
     BWS =
                                                               .
                                                             /fl  ft
-------
                GAS VELOCITY AND VOLUMET-iC FLOW RATE
Plant:
Samoung Lccatton:
Run
                                           Ooerators:  G-C-J
                                   Date:     f •Ji>*n
                                   Clacx Time:   /2 9-7
Barometric Pressure, in. Hq:   l^.^p        static Pressure, in. HoQ: — , 71
Moisture. %:_J^_	Molecular wt.. Crv: z*.B^     Pilot Tube. CD:   • 9 7
Stack Dimension, in. Diameter or Side i •   I«S	Side 2~   —»
Wet Bulb. °F:	
  £
              v.tootv
               -••a
               n M.Q
fcC,
            Dry Bulb. °F:
         Stack
         "•mo.
                          113
                          C7J-
                           ici
                           n/
                          I  1 I   i
                                        • i0.44
                    Md • iO ** •
• tO.32 x %Ou) * ,0 28 x *M,>


 (0.32 x    ; - (0.28 X    }

                                                     - i H,O

                                         100


                                         • IB (
                                                                100
                    P«-Pb +-!Z_-<
                           13.8
                                                            13.
                                                           irw
                                                     i»(
                                             IX
             ^
                                                   rt/(
                                      Q«

                                      Q8
                                       •rf-- O« • 17.847 X —• «|
                                        «B          |.g


                                       •^j-       xirj4?>-
                                          xeo



                                         %H,O
                                           *
                                          100
                                                m-
                                                                       108
                                                           fiR
-------
               FIELD DATA SHEET
Plant: L^co ^ ^bO.,--1? Sample Type: W-4- Operator: ££*-»
Sampling Location VV VO b««o oj*<^«^ Pbar:
^.30
Run Number: \0-\1-\ Data: 5-}o,.<\1 CO2 b
Ps: ^- t ^5
02: a \
Pretest Leak Rate: xt>oN cfm@ \J in. Hg Probe Length/Type: S_s Pilot fr^v^
Pretest Leak Check: Phot: (/ Orsal: jv

TiavwM
PoM
NuntM
fc
lo
1-O
->o
(0


;







1
2.
y
4.
r

$

i,
*
5
^
Sampling
TbM
(mlnj
_5'^«
^^
V3^
40(0
4lt»






















OochTirm
(24-hcMjr
dock)




























Gaa Metei
JVm)«3
*)"74 » 3 f^S
-JSJ^b >>
1^0.^
O^f%. L.
^0(o,t^<\






















>(\ Slack Diameter:
Velocity
inK2O
7/7^-"














•>• i^
• i?
, |0
, "2-0
"^
i ~L]
i ^-T-
» *~ i-'
, \ ">
"^>
IS As: t.23£f*'

Oillc« PieMuie OiHeiential
Oasiied | Actual
Stack
Temp
fTs)
nozzle ID: A"» Thernv
Assumed Bws: J_
Meter Box #: (4-
	 Filter *
3couple (f :
F
. j'Lf *^
vc>

s AH@: / X(> L
Post Test Leak Rate: 	 cfm @ 3 in. Hg.
Post Test Leak Check: Pilot. //Orsat: "'-i

lempeiabJie
°F
Prob« ] Filler
Impingei
T»mp
°F
• ''// S/-'/ /r/////// ''/'// //// ' ' //////•''/''/
1 ^
l.V
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l.«i








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1.1
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u








u-
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---






_... . _..







































^0
4^y
51.
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Dry Gas Meter Terry
tilel
Oudat
(Tm out°F)
'///// ''/////,
^0
^0
^ V
<\V






















<\0
lvt)
CVG
^^>























Pump
Vacuum
Jin Hg
3
3
i
^"





















M \
                     1.8
!•
lm=
                                                                -
-------
PlantL
Date:
           ' a
 SAMPLE RECOVERY DATA
	;	  Run No.:
                   k>~-^    Job No.:
                                                               r\
                                                          c. - '
                     Sample Box No.:
Sample Location:
Sample Type:	
                                             Filter No.:
Sample Recovery Person:	^o
Comments:	
FRONT HALF
Acetone
Container No.;
Filter
Container No.:
                          Liquid
                          Level Marked:.
                            Sealed:
                                             Sealed:
Description of Filter:
Samples Stored and Locked:
BACK HALF/MOISTURE
Container No.:	
Liquid Level Marked:
                                              Sealed:

IMP. NO.
1
2
3
4
5
6
CONTENTS
fHo
Hzo
^K
^(r


TOTAL
INITIAL
VOL (ml)
(0.0
\ 00
	
*s.



WEIGHT (aramsl
INITIAL
Co/.^
'^7
tfs )
mi


i^«
FINAL
^cO^o.T
J?C,^
T^^f
7tio


^1.-,
NET
f«
2.;
,.*
"1-7


i,o
Description of Impinqer Catch-
-------
        EPA METHOD 4 MOISTURE CALCULATIONS


PLANT: _Ljfe£ _ : _ SOURCE/RUN *• ro-n-i  DATE: <~


1 . Leakage Correction for Volume Metered


    vmc=VO-p-La)xe

    Vmc=Vm-(Lp-0.02)x9


    vmc=(       )•(       -0.02) x(       )
    w   _ 5, Vfj    ft3
    vmc   •'•'in - n


2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)


                          Pbar+(AH/13.6)
                                                       /13.6)

          = 17.64
3. Volume Water Vapor Collected, Standard Conditions


    Impingers & Silica Gel = V ...   = 0.04707 x (W. - W. )
                         wstd             f    '


                          std
                           std

                        V     = 0.04707 x( $
                        vw
                          wstd
 4. Percent Moisture, by Volume


     B   -       Vw5td
     BWS	v    ^T\T
               wstd   mstd
     B   -
      ws"
           (.I.IIIL  )+(
-------
  go
 ko
tf
                              METHOD 18 FIELD DATA SHEET
        Plant: LASCQ   Peppery
        Date:  r-j<».
o
o

Flow
Setting
05 o%
T-io
Ho
>So
o-ro
>-i 0

- ,^o
Trovcra*
Point
Numbar
A /
L
3
-
J>
9

i %l
• %>
, >5
• » Y
. >i
. w











AS ¥0
Stack
T.mp.
l^^
i-) \
t-\ >
vl>J
TV^
»0

Vix.
» V
%st
0--M
VI *'
>-*-s











>b>
                                          5 J
                                              Md - (0.44x%CO2) •)•


                                              Md - (O.*4x    ) + (0.32X
                                                              + (0.28X    )
                                              Md-
                                                        % H-0      % HO
                                                        - — ) + 18 ( - — )
                                                         ,00       100
                                                              100
                                                                        100
                                                .  ,28.71
                                              T.-

                                              Pt-Pb+-±i^-(     ) +	
                                                      13.6             13.8

                                              P«-  ^9.J
-------
                GAS VELCcrry AND VGLUMET=;C FLOW RATE

Plant:   Usco  p£f.Q..cT »         	      	  Oate:  j-.^o.  77
Sampling Location: jr /o
Run #•  I O  I 1 - }
                                                    CIocx Time:   // / 2 &
Barometric Pressure, in. Hg:   ^ 3 o
                                          Ooerators:.
                       ^Molecular wt.. Cry:.
Moisture. %:

StacK Oimensio'n. in. Di&ieter or Side 1 •     /_$"
Wet Bulb. °F:
                                          Static Pressure, in. HpQ:  '— »
Pilot Tube. Co:   •  


                                     Md •  H.O      x, H,O

                                                '00   *     i00
                                                     100
                                                               loo
                                     p«-?b *JLL.-.<
                                            1 3.8
                                                            1 3.8
                                                 -n.M«



                                                                f
                                     A«. {.  3^.    n2
                                                           x80
                                                                        if
                                     °«-d-
                                                    T«      100


                                                 X17«7K          •
-------
                             METHOD 18 FIELD DATA SHEET
  \(S, 9
 ||C.O
f
Plant:.
Date:
          Pbar:
                LAS
v5"-Pq-l)7 Orific* Tank *• 	 *
tiorv \O' 00*^ QjtL*T Pump/PntnmPter #:
#: \Q-l-L-ii Pt: Pretest ( mm Hq): ""
(I.D.: If ' Post-Test fmmHg): -~_
>1.3r> ^ Tt: Pretest <°FV 	
ole Tube
ators:
e-WFtiii- mr\ Poct.Tp^t^R' —
^•. 7
Check: Pre: (/ Post:_L/ 	

Time: Start: JJJ/ Finish: Ibi Total: Gft^
W/R 	 n/R- — . 0^: P-/ CO~: O

Gauge
Time Vacuum
(Hq)
1 6 0
H r. °
*\ 9o D
1 %t 0
I +o 0
^ *+ 0
/ iti o
• «!•»
rav«r>«
Point
Jumb»r
|
?
}
f
S
4

»
»
i
*
J
i











velocity
H««d
in. H^O
. I«L
' 'T
. id
, 1 ?
. M"
. *C

, 1.4-
. !--?_
. 1 V
• ' ?
. 1^
, -Li.










x V^VW
Flow
Setting
^5b c t »•
9S0
OSc.
7^6
>.STv
K*
5-^6
— i K4-
Stack
T«mp.
°F
73 y
3-3^
'^34
">5^
>i6
ass

^3-«,
1-35
»&
>31
»7
^>1










"1-sa
Md - <0.44x%CO2) * (0.32 x%02) -r (0.28x%^42)
. .i, Md » (0.44 x )-f(0.32x )-t-(0.28x )
»„"••>••»
".HO "4 HO
j^^l, - Mdx(l - -J-.) -18( -j^j- )
^>3 Ma-Cl^ou )x(i • Z'^".. > - '6( Z"^" ) VW5»'
a l ^toj 100 100
'4* Th^C'
jSiyM-- ^B.05
W^Ts - ) !«»- °F ' Cl<- °R <°F * 460)
c p
13.8 13.8
Ps- 1«\.>^ in-Hg
*—
^SP =
F= il 'S(VR)
V9 " 03.<»S* X >-p X VA^ X U p, x Ms

v.. ^yi-tf .t/.

. A«- V» "2

Q« • Vs x Ai x 60 t/m

Q»m x X 00
•2-5\2.
Qa - f\jf ^ c. 1&,- acfm
^^^P, %M,0
°«.td= °* * ' 7-847 x T" x ° ' "T^" '


°%n- fI7-M7x x(1'"^
Q.^^HrJL.n,
                                                                               At
-------
                                                 FIELD DATA SHEET
 Plant:
 Sampling Location   & \fc k>o«o  u.nu'C'
                                          Sample Type: /H - «)-	Operator:
Run Number: \O-\>"
i.^
(,j<
v.*<






















• — •








...














•*>•

—























f

























6 •>
H
J-i-
^3






















y«=
^^
/S'
^c.






















Jt
y.y
J^6
Sr7






















?
JS
3
3






















-------

i
         Plant:
 SAMPLE RECOVERY DATA

	  Run No.:

                   "-^    Job No.:
                                                      /O -
                             Sample Box No.:
Sample Location-

Sample Type:
                           10
                                                     Filter No.:
         Sample Recovery Person:   GC

         Comments:	
         FRONT HALF
         Acetone
         Container NO.L
                         Liquid
                         Level Marked:.
         Rlter
         Container NO.L
                           Sealed:
                                             Sealed:
         Description of Rlter:
         Samples Stored and Locked:

         BACK HALF/MOISTURE
         Container No.:	
         Liquid Level Marked:
                                             Sealed:

IMP. NO.
1
2
3
4
5
6
CONTENTS
frUo
MLO
£*/>?«<
s/t


TOTAL
INITIAL
VOL (ml)
(oo
'00
—
>^0



WEIGHT tarams)
INITIAL
kok.Z-
J?c.y
^1
7^3,0


^ViV*\
FINAL
^/Co
or 7
t^c^
^9-6


'VV^M
NET
ii
« 1
v£
r.fc


U-i
Description erf Impinqer Catch-
                                                                                  war
-------
        EPA METHOD 4 MOISTURE CALCULATIONS


PUNT:  U/fer D _ SOURCE/RUN #:_j£li^ DATE:  6-2<\-ci"}


1 . Leakage Correction for Volume Metered
    vmc=(       )-(       -0.02)x(

                   ft3
2. Volume lyietered, Standard Conditions (68 F, 29.92 in. Hg)


                          P+(AH/13.6)N
         = 17.64
    Vm   = 17.64 x(a.Mifc  )x(  ^U  )x
       st
       sta
                    dscf
3. Volume Water Vapor Collected, Standard Conditions


    Impingers & Silica Gel = V ...   = 0.04707 x (Wr - W. )
                         w               f   '
                           std

                        Vw  = 0.04707 x(
                           std
                        vw
                         wstd
4.  Percent Moisture, by Volume
             V    -4-  V
              wstd    mstd
    B   =
-------
a DC
                               METHOD 18 FIELD DATA SHEET
Plant:.
Date-
               - *«-«»-»
                        Tested Analyte:.
                        Orifice Tank #:_
Location:
Run#:
Stack I.D.:_
Pbar:  it.
                     32-" * lio"
                                                Pump/Rotometer #:_
                                                Pt:  Pretest (mm Hg):	n
       Sample Tube
       Operators:  $•
                            Post-Test (mm Hg):	;_
                        Tt:  Pretest fF):	L.
                            Post-Test
       Leak Check: Pre:
                        Post:
                        Time: Start:o<^ Finish: o^scTotal:
                        W/B:  -  D/B:  -	O9:j2/
            Time
             5. 03
         1*77.1$
 Gauge
Vacuum
  (Hg)
       Vnr
           Trav«rs«
            Point
           Number
                Velocity
                 Head
                in. H20
                             Flow
                           Setting
                            z./
                                    Z-l
                            CO2:_ o
Md = (0.44 x %CO2) -i- (0.32 X %O2) -r (0.28 x %f^)


Md = (0.44 x     ) i- (0.32 x    ) -i- (0.28 x     )
                                   % HO      % HO
                         Ms = Md x(1 • 	_) - 18 ( 	—
                                    100        100
                                     ^
                                                Ms
                                                Ts-
                                                                 100
                                                                            100
            Stack
            Temp.
             °F
7-  SO           S P
JL^—*"   ps-Pb*-i:l-=(
                 13.6
                                                                   ) +
                        13.0
                                                Ps =
                                      in. Hg
                                                             —   .IfTpRT
                                         Vs - 85.49 x Cp :



                                         Va - 85.49 x (


                                         Vs-


                                         Aa-
                                     JSPx ^
                                                                         MS
                                                                 ix(
                                                   )x
                             )f
                                                              ft/8
                                          Qs - Vs x As x 60 s/m


                                          Qa-          x

                                          Qa -           acfm

                                                         Pa
                                          Qa . .= Qaxi7.647x	
                                            atd           T,
                                                                        x 00
                                                                        too
                                                 Qa

                                                       X 17.647 X-


                                                        dacfen
                                                       • x (1 -	)
                                                             ioa-
-------
                             METHOD 18 FIELD DATA SHEET
Date:	£/
Location:_
Run #-.   *!&>-
                                              Tested Analyte:.
                                              Orifice Tank #:_
                       - R
      Stack I.P.:  o-y
      Pbar:_z^i^_
Sample Tube #\
Operators:.  **"
                                        Pump/Rotometer #:_
                                        Pt:  Pretest (mm Hg):	i_
                                            Post-Test (mm Hg):	;
                                        Tt:  Pretest fF):
                                                  Post-Test fF)L
                                              Time: Start:/ ?s/ Finish:  "" Total: **
Leak Check: Pre:
                             Post:
                                          W/B: -   D/B:
                                                                  J2-
                                                                    CO
lo

To
13 i\
           Time
         i4oc> . oc
                 Gauge
                Vacuum
                  (Hg)
          Traverse
           Point
          Number
                Velocity
                 Head
                            Row
                           Setting
                                  Zl
                                          SS
                                          Md = (0.44 x %CO2) -t- (0.32 X %O2) -r (0.28 x '


                                          Md = (0.44 x    ) -i- (0.32 x    ) -t- (0.28 x     )
                                    C.C
                                    30 Ms = Md x 1 1

                                    r1o.
                                                    HO      %H2°
                                                     — ) - 1 8 ( -
                                                    1 00        1 00
                                    °IT_
                            Stack
                            Temp.
                             °F
                                               Ms = i
                                               TS-
                                               Ps = Pb
                                               Ps
                                                   i x (1
                                                               l 00
                                                                          100
                                                  13.6
                                                                  13.6
                                                     in. Hg
                                                                    Ps x Ms



                                               Vs - 85.49 x (       ) x (        ) x


                                               Vs.           ft/s


                                               AS-           ft2


                                               Qs » Vs x As x 60 s/m
                                                                     i
                                         Qs-

                                         Qs«
                                                                      x 60
                                                             acfrn
                                                              Ps
                                               Qs  .= Qs x 17.647 x -— x (1
                                                 8ld            Ts
                                                                100
                                                            x 17.847 x-
                                                             dsefm
                                                                      •x(1-
-------
          APPENDIX A. 1.14

             Condition 13
(includes flows, moistures, and Method 18)
-------
•j ag da
                       GAS VELOCITY AND VOLUMETRIC FLOW RATE
       Plant:  Lt\S(.o
       Sampling Location:
       Run*:,
                                                     Date:  * -ZA-*~I
                                                     Clock Time:  / J-T-*
                                            Operators:.
       Barometric Pressure, in. Hg:  21 zo	 Static Pressure, in. HoO:  .a
       Moisture, %:   id	Molecular wt., Drv: 27
7^
^7
7i
>7
"?7
~77
"M

11
11
•)7
*?T
77
77
T)
T)








p- 11
                                              Md - (0.44 x %CO.j) -I- (0.32 X %O2>


                                              Md - (0.44 x     ) •)• (0.32 x    ) + (0.28 x
                                                   10
                                              Md- ^ 1

                                                        % HO      % HO
                                              Ms- Mdx(1 • 	—) + 18 (	—)
                                                         100        100

                                              M.-(      )X,1.___)^,8(_^5-
                                              TS-
                                                     13.8
                                                                     13-8
                                              P.-
                                                    '"-"a
                                                          =   J   fsW
                                                             X
                                              Vs - 85.48 x (
                                              A«- /.
                                              Q« - Vt x As x 60 a/m
                                               o«-
                                                            Pax Ms


                                                       )M       )x
                                    ^
                                                                     xeo
                                                    X 17.847 X-

                                                   , d«dm
                                                                            :(1
                                                                                100
-------
3CC3
                WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: L A °F
)5 °F
O.-Sw^V m. Ha

                                    2800-(1.3xTw)
Pva=(
                          2800-(1.3 x



      Proportion of Water Vapor by Volume = Bws
(Ps)
Tamp.
OF
0
10
20
30
40
50
60
70
60
90
100
110
120
130
140
150
160
170
180
190
200
210
220
230
240

0
0.0378
0.0631
0.1025
0.1047
0.2478
0.3020
0.5218
0.7392
1.032
1.422
1.932
2.598
3.446
4.52S
5.681
7.569
9.652
1220
1529
19.01
23.47
28.75
35.00
4241
5044-

1
0.0398
0.0660
0.1080
0.1716
0.2578
0.3764
0.5407
0.7648
1.006
1.407
1.992
2.672
3.543
4.647
8.034
7.759
9.885
12.48
15.63
19.42
2346
2943
35.68
43.11
51.76
                                               0.0133^
                                                                 in. Hg
( )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0096
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.740
3.642
4.772
6.100
7.052
10.12
12.77
15.98
19.84
24.46
29.92
3647
43.92
52.70
3
0.0441
0.0728
0.1166
0.1878
0.2782
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.829
3.744
4.000
6.350
6.150
10.36
13.07
16.34
2027
24.97
30.52
37.07
44.74
534S
4
0.0463
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
0.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.87
54.62
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.8222
0.8750
1.213
1.000
2243
2.995
3.954
5.165
6.680
8.557
10.86
13.67
17.07
21.14
26.00
31.75
38.50
46.41
55.60
6
0.0517
0.0846
0.1370
0.2116
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.650
8.767
11.12
13.98
17.44
21.59
26.53
3248
3924
4727
56.60
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4688
0.0609
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
6.981
11.38
14.30
17.82
. 22.05
27.07
3342
3949
48.14
5741
a
0.0571
0.0932
0.1502
0.2292
0.3384
0.4858
0.6903
0.9686
1.335
1.810
2.440
3.259
4.289
5.565
7.202
9.200
11.65
14.62
1821
2242
27.62
3347
40.75
4943
5843
9
0.0598
0.0982
0.1567
0.2383
0.3403
0.5035
0.7144
0.9989
1.378
1.875
2.521
3.351
4.406
5.732
7.364
9.424
11.92
14.98
1841
2249
28.18
3443
4142
4943
5047
-------
       Plant:.
       Date:  *>-7.*-«7
                       METHOD 18 FIELD DATA SHEET

                      	     Tested Analyte:__^t
                      	     Orifice Tank #:	
       Location-  Au.w
       Run #' ME- il-v-
       Stack I.P.:  /7.5
       Pbar:   11.*-
       Sample Tube #• *e-/3~2A)
       Operators:  T"fr	
Leak Check: Pre:
                              Post:
' C-V7
 /!•
i;;;
                                 t-
                                       Pump/Rotometer #:_&£!
                                       Pt:  Pretest (mm Hg):	
                                           Post-Test (mm Hg):_
                                       Tt:  Pretest fF):_
                                           Post-Test fF):_
/o
je
&
Jb
Time
7f C>«. /5
-)<30I ^7
1 ^02, :-1
'T & A iJ 7"1
1705. Tl
") yo-j, ci
") sol, zy
Gauge
Vacuum
(Hg)
I
1
I
1
1
1
I
Flow
Setting
,*^t
/rf»*c
/50«
/ 5»«-
/S<> ^c.
/fete
/^»cc
r^
1C
10
12
•n
                                               Time: Start:/*??  Finish:-7>7. Total:
                                               W/B: (,(. D/B: ?/   O2: -z./  C02: <

                                               Md = (0.44 x %C02) * (0.32 x %O2) T (0.28 x "/oN^
                                              -Md = (0.44xc  ) + (0.32X *(  ) •>• (0.28 x 7 <5  )
                                               Ms "I '2-7
                                               Ms-
                                               Ts-  ?/
                                                  :i H20

                                                   100

                                                  ) x(1 •
                                                                   % HO
                                                                   - —
                                                                    100
                                                              '
                                                                          ^j
                                                                   ) - 18 (
                                                               100         100
                                                             °R(°F*460)
Traverse
Point
Number
1
t.
>
Y
5
&
r
7

f
j.
9
4f
5
fr
7
1








Velocity
Head
in. H;jO
.zs
. 20
.z 5
•2-f
. 31
. 3 1
. JV
.3T

• U
.25
.20
.•2.0
2."!
• «fc.
.J.T
.25








Stack
Temp.
°F
^/
tl
Si
ft
tl
s\
fl
90

yo
tl
?,
f/
ti
10
//
tl








                                               Ps - Pb f ^^- = (t9. L  ) + __Jl	
                                                      13.6             13.6
                                        Ps- Z
-------

Plant:
Site:
           WET-BULB/DRY-BULB MOISTURE CALCULATION
                                        Location:  h/f&tti
                       Operators:
                              -  13.6
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack =  Pbar
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw (from Table) =   Pvw =
                                   (Ps - Pvw) x (AT)
Vapor Pressure of H2O = Pva = (Pvw) •
                                   2800-(1.3xTw)
Pva =(
)-
                   (
                       2800-(1.3 x
Proportion of Water Vapor by Volume = Bws
Ql__    (Pva)    _       (           ;
(Ps)
T«mp.
OF
0
10
20
30
40
50
60
70
80
90
100
110
120
130
140
150
160
170
180
190
200
210
220
230
240

0 .
0.0376
0.0631
0.1025
0.1647
0.2478
0.3026
0.5218
0.7392
1.032
1.422
1.932
2.596
3.446
4.525
5.881
7.569
9.652
1250
1559
19.01
23.47
28.75
3540
4241
5044-

1
0.0398
0.0660
0.1080
0.1716
0.2576
0.3764
0.5407
0.7648
1.066
1.467
1.992
2.672
3.543
4.647
6.034
7.759
9.885
12.48
15.63
19.42
23.96
2943
35.68
43.11
51.76
                                           =    Q.t>i^ ^
                                                                      in. Hg
( )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1803
0.2077
0.3900
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
15.98
19.84
24.46
2942
3647
4942
52.70
3
0.0441
0.0728
0.1186
0.1878
0.27B2
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.629
3.744
4.900
6.350
8.150
10.36
13.07
16.34
2057
24.97
30.52
37.07
44.74
5345
4
0.0463
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
1031
9.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.57
54.62
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.680
8.557
10.66
13.87
17.07
21.14
26.00
31.75
38.50
48.41
55.60
6
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
44442
0.9040
1.253
1.712
2.310
3.081
4.063
5.302
6.850
8.767
11.12
13.98
17.44
21.59
2643
3248
3944
47.27
5640
7
0.0541
0.0692
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.785
2.379
3.169
4.174
5.442
7.024
8.981
11.38
14.30
17.82
22.05
27.07
33.02
3949
48.14
5741
8
0.0571
0.0932
0.1502
0.2292
0.3304
0.4858
0.6903
0.9666
1.335
1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1851
22.52
27.62
33.67
40.75
4943
5843
9
0.0596
0.0982
0.1567
0.2383
0.3403
0.5035
0.7144
0.9989
1.378
1.675
2.521
3.351
4.408
5.732
7.384
9.424
11.92
14.06
1841
2240
28.18
3483
4142
4043
5047
-------
GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:	
Sampling Location: /-')*;,, /3y^..--r
Run #:   <*)£-'.V3	
                                                      Date:
                                               - ^-c< 7
                                      Clock Time:
                            Operators :
Barometric Pressure, in. Hg:   7-^- *-
Moisture, %:  '-^           Molecular wt., Dry:  3?
                            Static Pressure, in. HoQ:   .
Stack Dimension, in. Diameter or Side 1:    »7. r •
Wet Bulb. °F:     6#	Dry Bulb, ° F: __
                                      Pitot Tube, Cp:
                                      Side 2:
TravcrM
Point
Number
I
2
->,
1
?
ir
7
r

/
7
•v
T
5
U
^7
t









Velocity
H««d
in. H20
LZ-
,2C
. Z.1
i-7
.30
- ^2.
.W
. 3>1

2.V
.Z5
. 2_«S
16
15
^:
-2-1
.2.6








^SF -.5220
Stack
Tamp.
°F
S"2
cz
S Z-
£-2-
?z-
fz.
1r^-
f «-

y*.
STi_
sz_
S'Z--
^^
^z.
9 a.
S^^








S- ^
                       Md - (0.44 x %CO2) + (0.32 x %O2> + (0.28 x ntty

                       Md - (0.44 x ^  ) ••• (0.32 x £/  ) + (0.28 x 7 ?  )

                       Md -   2. V
                                                  %HO
                       M« - ( -? ?   ) x (1
                                           %H°
                                       100
                               13.0
                                               13.8
                                    In. Hg
                                    —       Ts
                       Vt - 85.40 x Cp x
                        Vs<
                        A.-
                                            Pax Ms
                                     «/•

                                     .2
                                         Q« - V«xA8XOO«/m

                                         C3»-          x
                                               X80
                                       p.
                                      —
                                                     X 17.647 X-

                                                      d«dm
                                                      7.2. A
                                                           100
-------
   Plant:
   -:.
   Site:
             WET-BULB/DRY-BULB MOISTURE CALCULATION
                                              Loc^ion:   /^Ar   £*A
                           Operators:  T&h<    Run #:  ^, ^     Date;
                                                        Pbar =
                                                          Pg =
                                                          Ps =
                                                          Tw =
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of Stack =   Pbar
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw (from Table) =    Pw =

                                        (Ps - Pvw) x (AT)
                                                                 0 .
   Vapor Pressure of H2O = Pva = (Pvw) -
                                           2800 -(1.3xTw)
Pva = (             j . (_	;	}_
                           2800 -(1.3 x

Proportion of Water Vapor by Volume = Bws

Bws =
 T«m0.
  OF
   o
   10
  20
  30
  40
  50
  60
  70
  80
  90
 100
 110
 120
 130
 140
 190
 160
 170
 160
_190
 200
 210
 229
 290
 240
      0
     0.0376
     0.0631
     0.1025
     0.1647
     0.2476
     0.3626
     0.5218
     0.7392
     1.032
     1.422
     1.032
     2.596
     3.446
     4.525
     5.881
     7.569
     9.852
     12.20
     15.28
     19.01
     23.47
     28.75
     35.00
     42.31
     5084-
               1
             0.0398
             0.0660
             0.1060
             0.1718
             0.2576
             0.3764
             0.5407
             0.7648
             1.066
             1.487
             1.992
             2.072
             3.543
             4.647
             6.034
             7.7S9
             9.885
             12.48
             15.63
             19.42
             23.86
             29.33
             35.68
             43,11
             51.76
in. Hg
in. H20
in. Hg
                                                                                  °F
                                                                                  in. Hg
                                                                                  in. Hg
	 : 	 	 : 	 = _v_« — J_L- •• . i--
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3906
0.5601
071* i ~
.75', .•:
1.1C2
1.513
2.052
2.740
3.S4?
4.772
0.1 60
7.982
10.12
12.77
15.98
1944
24.46
2942
3647
AM O4
4342
52.70
3
0.0441
0.0728
0.1186
0.1878
0.2762
0.4052
0.5802
0.8183
1.136
1.561
2.114
2.829
3.744
4.900
0.350
8.150
10.36
13.07
16.34
2027
24.97
30.82
37.07
44.74
5348
4
0.0463
0.0768
0.1248
0.1955
0.2891
0.4203
0.6009
0.8462
1.175
1.010
2.1.78
2.911
3.848
5.031
0.513
8.381
10.61
13.37
16.70
20.70
25.48
31.13
37.78
48.87
5442
5
0.0489
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2243
2.995
3.954
5.165
6.680
6.557
10.66
13.67
17.07
21.14
26.00
31.78
'38.50
4641
8840
8
0.0517
0.0646
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.083
5.302
6.650
8.767
11.12
13.98
17.44
21.59
26.53
3248
3924
4727
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4688
0.6669
0.9352
1.293
1.765
2.379
3.189
4.174
5.442
7.024
8.981
11.38
14.30
17.82
2245
27.07
33.02
3949
46.14
5741
g
0.0571
3.0932
0.1502
0.2292
0.3384
0.4858
0.6903
0.9666
1.335
1.819
2.440
3.259
4.289
5.585
7.202
9200
11.68
14.62
1821
2242
27.62
3347
40.78
4943
5843
g
0.0598
0.0982
0.1587
0.2383
0.3493
0.5038
0.7144
0.9989
1.378
1.878
2.821
3.381
4408
5.732
7.384
9424
1142
1446
1841
2240
28.18
3443
4142
404*
8047
-------
GBGJ
                         METHOD 18 FIELD DATA SHEET
Plant: t-Aito TesteH AnaiytP- *A^_.
Date: 5-n-«i Orificn Tank #• —
ocation: *«*« *»*•.*+ Pump/Rntnmeter #• t/os-f **J-
Run #: te - i»— » R: Prefect (mm Hg); —
Stack I.D.: 2 *'*«.
^
Vslocity
H«ad
in. HjO
. «£
.»<•
. .•<•
00
. 6"!
-0*T
,*T
.00
.**
.0*
.**
,01
.10
.+»
.OS]
.t>3
.OS
./o
.60
• A3
75
7f
75
rr
?r
-7^
7*
•»3
if
73
7*
•7*
7V
If
•}£
7f
if
7t
7T
IS
71
-^—^— e. f-
Md - (0.44 x %CO2> + (0.32 X "fcOj) + (0.28 x %Nj)
m utft _ in AA. » i j. (n a? x ) + <0 28 x )
Md - (f
$1
% HO % HO
j6 Mt.Mdx(1.-^r) + l8(-jS-)
^ Ma-< )x(1- '"^ )-H6(— — ) (7 ;.
^^ 100 100 J5^5'
n0 Ma- ^B.b^
7^> Ts- T-S' °F= 5!)^ °R(°F*460)
SP "~.0,^-
D- _ nh I °'r' i / 1 i.
13.8 13.8
Ps- - 1\.l* In. Hg
JSp- -Mlb
^= J Ts <°R)
vs - 09.4W x up x 
-------
           WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant:
Site:  fcyry  £ykitcsrt—Operators:
Location:
Run #:
                                                           Date:
                          Pbar +
                                 1 3.6
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of Stack =
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw (from Table) =   Pvw = —H
                                   (Ps - Pvw) x (AT)
       Pbar =
        Pg =
        Ps =
        Tw =
        Td =
                                                        /D
                                                            ZZz
Vapor Pressure of H2O = Pva = (Pvw) -
                                   2800-(1.3xTw)
        \rn-
                       2800.-(1.3 x
Proportion of Water Vapor by Volume = Bws
Q,.,*_   (pva)     _       (  .^»
(PS)
Temp.
OF
0
10
20
30
40
50
60
70
60
90
100
110
120
130
140
1.50
160
170
180
190
200
210
220
230
240

0
0.0376
0.0631
0.1025
0.1647
0.2478
0.3626
0.5218
0.7392
1.032
1.422
1.932
2.596
3.440
4.525
5.881
7.569
9.652
12.20
15.29
19.01
23.47
28.75
35.00
42.31
50.04-

1
0.039S
0.0660
0.1060
0.1716
0.2578
0.3764
0.5407
0.7648
1.066
1.467
1.992
2.672
3.543
4.647
6.034
7.759
9.805
12.40
15.63
19.42
2346
29.33
35.08
43.11
51.76
in. Hg
in. H20
:in. Hg
                              °F
                              in. Hg
                                                                     in. Hg
( ~l*.&' )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
6.190
7.952
10.12
12.77
15.96
19.04
24.40
29.02
30.37
43.02
52.70
3
0.0441
0.0728
0.1186
0.1878
0.2782
0.4052
0.5802
0.6183
1.138
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.30
13.07
16.34
2047
24.97
30.52
37.07
44.74
53.65
4
0.0463
0.0768
0.1248
0.1955
0.2891
.£.4203
0.6009
0.8462
1.175
1.610
2.178
2.911
3.848
5.031
9.513
6.351
10.01
13.37
16.70
20.70
25.48
31.13
37.78
4547
54.62
5
0.0469
0.0810
0.1302
0.2035
0.3004
0^80
(Q&M.
STSTSO
1.213
1.660
2.243
2.995
3.954
5.165
6.600
8.557
10.86
13.07
17.07
21.14
20.00
31.75
30.50
46.41
5540
6
0.0517
0.0646
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
6.850
8.707
11.12
13.98
17.44
21.50,
26.53*
3248
3944
4747
5640
7
0.0541
0,0892
0.1429
0.2203
0.3240
0.4686
0.6669
0.9352
1.293
1.705
2.379
3.169
4,174
£.442
••".024
3.981
11.30
14.30
17.02
22.05
27.07
3342
3949
48.14
5741
8
0.0571
0.0932
0.1502
0.2292
0.3384
0.4858
0.6903
0.9660
1.335
•1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.02
1041
22.52
27.02
3347
40.75
4943
58.63
9
0.0598
0.0982
0.1507
0.2303
0.3493
0.5035
0.7144
0.9900
1.370
1.075
2.521
3.351
4.400
5.732
7.384
9.424
11.92
14.06
1841
2240
28.16
3443
4142
4043
5047
-------
3BC3 (
                   GAS VELOCITY AND VOLUMETRIC FLOW RATE
     Plant:
LfiM.o Date: 5-e.<»-c»n
ling Location: A**, fix**,^ Clock Time: t^ *
f. RB-/3-2. Operators: r«-/^X
netric Pressure, in. h
ure. %: 1.®
q: j -T. ^ Static Pressure, in. HoO: — -. ^ 1
Molerularxwt Hrv- 29 Pilot Tube. CD: .99
Dimension, in. Diameter or Side 1 : 2 % " Side 2: 2v -
5ulb.°F: 6^ DrvBulb.Op. 7 <:

v«rM
olnt
mb«r
(
?
>
V
r
0
/
X.
I
V
f
V
(
X
>
f
T
V
c
i
i
V
r
c.


Velocity
H«ad
in. H20
^5
/ o S
o5
OS
oO
.& Is
.01
0~7
,0?
.o5
o5
-oS
, 08
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, oO
.c>^
u£
• 0?
.0*
,ol
.0^
,^5
,*<•
.^f
IT— --»/i.
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T«mp.
°F
TT
^
; + 1fl ( ... . 1
Ms- ( C-Y )X(1 ..^ I * io( IQO i
Mi-
TS. ~>7 °F- S3S" °R (0F + 460)
Po - Pb t S-P- , i 29. •» ) t- "' U
13.8 ' 13.8
Pa - 21./C- In. Hg
JSP- .^G3
— / Ts (^R)
. V«-(t».4UxUpx^P x \l P8XM8
Vn-nido-rr 991 )x( i^O-^txAl -^-JS
V «. '6 «
V« - / (, . 6r 8 ft/«
A.. ^.6i n2


o«- x y.C~( xeo
Q,. ^/&7/ *cfm
p, %K,0
Q.ftd-Q.xl7.e47x — x(1--j^-)
•2^./Q
                                                                  100
                                      ONW-
-------
WET-BULB/DRY-BULB MOISTURE CALCUU\TION
Plant: L#3_o
Site: &*VM ^c^omj^r- Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack = Pbar + -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td • Tw =
Saturation Vapor Pressure of H^O at Tw
Vapor Pressure of H^O ~ Pva — (Pvw) •
Pva={ }.( 	 1 	
Location: fof*\ £vhaa
TAfa Run #: 6E-&-2, Date: ;
Phar= 2^-2,
Pq= -a.u-i
pg Pe= 2«-u<
13.b ,-
T«/= l*t»
TH = ^S
AT= 10
(fr«m Tahl°) = Pvw = ^ZZT-
(Ps - Pvw) x (AT)
2800-(1.3xTw)
.•5
) x ( ) _a*rfT
-------
              GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:
Date:  5 -z9-/>*„> r- Clock Time: / *-??
/:U7, nnoratnrs- 74/5.5
Barometric Pressure, in. H
Moisture, %: \-*-»
Stack Dimens
Wet Bulb, °F:
TrsvtrM
Point
Number
i
^
V
fj
$
(j
(
2
}
H
5
G
I
2.
"i
H
£•
6
i
T-
5
^
5
6


q: Z^.Z. static Pressure, in. hUO: -.63
Molecular wt.. Drv: 2 V Pitot Tube, Cp: , If —
•ion, in. Diameter or Side
tii Dry E

Vttooty
H««d
in. H20
- t>7
6'7
oG
. 01
• 0T
,07
• 06.
. 05
• oO
.05
.05
,c~>
,Cfe
,07
0^
G5
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.0?
,ofe
.05"
.C75
. OS
.oS
.Q0

^F-,ZH6I
Stack
Tamp.
°F
7L
~7U
70
7^
"> 0
"1C
7(,
7c
7lx
?C
l_ 1C
•76
-70
1C,
~?0
"7(/
16
7C.
7^
7c
7k
?(.
76
7i/

T:- 76
1- 2.8" Side 2: if "
nlh,0p 7L
Md - (0.44x%CO2) + (0.32X%02> -i- (0.28 X%^)
Md-(0.44x<7 ) -t-(0.32x-I/ (+(0.28x7^ )
Md - Zf
% H_O % HO
M.-MUX(1 ' 10Q » ' 101 100 '
M.-e=L
-------
           WET-BULB/DRY-BULB MOISTURE CALCULATION
 Plant:     I^A&t)                      Location:
Site: &^  Date: 5--^
Pbar = 2A •*
Pa = -• US
-^2_ ps _ i*. 15
1 T r ro— ' -^
1 J.b
Tw= UH
Td= >^
AT= ^2.
(from Table) = Pvw = O.^OOf
(Ps - Pvw) x (AT)
'-.*?-
in. Hg
_ in. H.O
2
_ in. Hg
°F
°F
°F
in. Hg

 Pva=(
                  (
                       2800-(1.3 x

 Proportion of Water Vapor by Volume = Bws

 Bws =
Tamp.
 "F
 0
 10
 20
 30
 40
 50
 60
 70
 60
 90
 100
 110
 120
 130
 140
 150
 160
 170
 180
 190
 200
 210
 220
 230
 240
(Ps)
0
0.0378
0.0631
0.1025
0.1647
0.2478
0.3826
0.5218
0.7392
1.032
1.422
1.932
2.598
3.446
4.525
5.881
7.569
9.652
1250
1559
19.01
23.47
28.75
35.00
4241
5044-
1
0.0398
0.0660
0.1080
0.1716
0.2576
0.3764
0.5407
0.7648
1.066
1.467
1.992
2.872
3.543
4.647
6.034
7.759
9.685
12.48
15.63
19.42
2346
2943
35.68
43.11
51.76
in. Hg
( )
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0696
0.1127
0.1803
0.2877
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
8.190
7.952
10.12
12.77
15.98
19.64
24.46
29.92
36.37
43.02
52.70
3
0.0441
0.0728
0.1188
0.1878
0.2762
0.4052
0.5802
0.8183
1.138
1.561
2.114
2.829
3.744
4.900
6.350
8.150
10.36
13.07
16.34
20.27
24.97
30.52
37.07
44.74
5345
4
0.0463
0.0768
0.1248
0.1955
02891
0.4203
0.6009
0.8482
1.175
1.610
2.178
2.911
3.848
5.031
6.513
8.351
10.61
13.37
16.70
20.70
25.48
31.13
37.78
45.87
54.62
5
0.0469
0.0810
0.1302
0.2035
0.3004
0.4359
0.6222
0.8750
1.213
1.660
2.243
2.995
3.954
5.165
6.680
8.557
10.86
13.67
17.07
21.14
26.00
31 .75
38.50
46.41
55.60
6
0.0517
0.0846
0.1370
0.2118
0.3120
0.4520
0.6442
0.9046
1.253
1.712
2.310
3.081
4.063
5.302
8.850
8.767
11.12
13.98
17.44
21.59
26.93
32.38
39.24
4757
56.60
7
0.0541
0.0892
0.1429
0.2203
0.3240
0.4680
0.8669
0.9352
1.293
1.765
2.379
3.169
4.174
5.442
7.024
8.981
11.36
14.30
17.82
22.05
27.07
33-02,
3949
48.14
5741
a
0.0571
0.0932
0.1502
0.2292
0.3384
0.4856
0.6903
0.9666
1.335
1.819
2.449
3.259
4.289
5.585
7.202
9.200
11.65
14.62
1851
2242
27.62
3347
40.75
4943
5643
9
0.0598
0.0962
0.1567
0.2383
0.3493
0.5035
0.7144
0.9989
1.378
1.875
2.521
3.351
4.406
5.732
7.364
9.424
11.92
14.96
1841
2249
28.18
3449
4142
4849
5947
-------
METHOD 18 FIELD DATA SHEET
Plant: Lftsco
C
L
F
c
F
c
C
L

&t£> o
/*»» ye
iW *>
f&o id
/»•• LJO
A'° *7
•**
Date: S-**-
.ocation: fa
Run #• rtF-
Tested Analyte: *vv ,*.*«.
?T Orificp Tank *: —
• //A-* /TS*I Pump/Rntometer #: ^»1* * "i-
n-l' Pt: Pretp^T rmm Ha^: —
Jtackl.D.: /17S Post-Test ( mm Ha^: —
3bar: 2* 20
Sample Tube
Operators: 7
Tt: Pretest I°R: -
-A
.eak Check: Pre
Time
2,5. OT>
i^Cff, y$
2362, /fl

^
/
«
1
f








Velocity
Head
in. H2O
.23
Jf
. J5
.3C.
i 39
. 3*7
.35
,t.1

.*/
.1 3
21
. 31
. 3 Y
.31
.JO
. 2^/
•







Stack
Temp.
°F
7t
7Z
73
73
76
76
•76.
7C.

76
•76
76
7C
76
7C
79
76








Vs • 85.49 x Cp x






Vs - 85.49 x (  .77  ) X




Vs-   j*7,^  tt/s




As-  2. /3      ft2




Qs - Vs x As x 60 s/m




Qa •          x




Qs»  ^7^ 7   acfn1




Qa . ,= Qa x 17.647 x	
  std             T8
                                            x 60
                                            100
                    •atd-
                                x 17.847 x-
                               • x < 1	)
                                     100
-------
         WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: | J^ffc Location: /Uvi'
Site: /cvXfAW P^AJ Operators:-^ Run #: ArP-ftrt
Barometric Pressure, in. Hg = Pbar =
Static Pressure, in. H20 = Pg = -
Absolute Pressure of StacK = Pbar + 3 Ps =
Wet-Bulb Temperature, °F - Tw = '
Dry-Bulb Temperature, °F = Td =
Temperature Difference Td - Tw = AT =
Saturation Vapor Pressure of H~O at Tw (from Table) = Pvw = __D
(Ps - Fvw) x (AT)
2 ' ' jy. 2800- (1.3 xTw)
Pva=< ,-' .„...' "< } = ^
/AAx £«1U
Date: 5"'Z1-^
ZA- 2- in. Hq
"*.QO in. HO
^•tq m. Ha
J4 °F
% °F
1 2. °F
,UO
-------
3 oca c=a
                        GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:	
Sampling Location:
Run#
                                                              Date:
                                                              Clock Time:  /7/f
                                                    Operators:
       Barometric Pressure, in. Hg: ^f. 20	  Static Pressure, in. h^O:
       Moisture, %: !•>          Molecular wt., Dry:    7*      Pilot Tube,
       Stack Dimension, in. Diameter or Side 1:      / ?. 7-5     Side 2:	
       Wet Bulb, °F:___0_5_
          TravarM
            Point
          Number
            2''
                               DryBulb,°F:	T{.
               Velocity
                H««d
               in. H2O
                           .51
                            35
                        .3,1
Stack
T«mp.
 °F
                          •76
                                  Ic
                                  17
                                  76
                                  •76,
                            •7C
Md - (0.44 x %CQ2) + (0.32 X

Md-(0.44xO  )*(0.32X
+ (0.28 X %Wj)

 •t-(0.28x7>'
                                                         % H-O      % HO


                                                P..
                                                13.8             13-8

                                             2i
                                                                             *i."f
                                                              ft/t
                                                A.-   ,
                                                Qt - v« x A» x ao «/m

                                                0.-          x 2. /3    xeo
                                            .rf
                                           •to
                                               Qi xl 7.847 X
                                                                      %K,0
                                                                      •• ^
                                                                        100
                                                      X 17.847 X-

                                                       dtcfm
                                                                                   100
-------
            WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: LtS^^
Slte: AgXLLtoy.EAri Operators:
Barometric Pressure, in. Hg =
Static Pressure, in. H2O =
Absolute Pressure of Stack = Pbar +
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H20 at Tw
Vapor Pressure of H~O = pva = (Pvw) -
Pva=( \ (
2800 -1 1.3
Location: Aw/ft I//AL* Pi
TAlys Run*:.AP-tflu> Date::
Pbar= ^-2_
Pa= -O.fel
HO
-73-5- . Ps= 2-MH
Tw = (D *S
Td = V^-
AT= \~L-
(from Table) = Pvw = *£>• ^oi^Z.
(Ps - Pvw) x (AT)
2SOO-(1.3xTw)
)x( ) 0.44(02,
x \
5y*»
5"-23-
-------
J am da
                        GAS VELOCITY AND VOLUMETRIC FLOW RATE
                                                              Date:
                                                              Clock Time:
Plant:	
Sampling Location: A,A.\
Run #:   PtP -  'V*.	  Operators:^	
Barometric Pressure, in. Hq:   '.vi..i  	  Static Pressure, in. H^O:^
Moisture, %:_±3-	Molecular wt., Dry:^	Pitot Tube, Cp:.
Stack Dimension, in. Diameter or Side 1:    /•?• 7-5	Side 2:
Wet Bulb. °F:     C5"
                                      Dry Bulb, °F:.
Trav«rM
Point
Number
I
1
3
•Y
5
6
•7
7

/
t.
^
f
5
6
"7
5









Velocity
H«md
In. H2O
-IV
,3>j
, 55
, 16
.3?
,S5
. 3^
, ^

«Z7
.2L5-
,25
-«,3
,35"
. 33
. iO
i^l








«P-.^%
Stack
T«mp.
°F
7V
-It
16
75
76
1-1
•?-?
n

-?6
75"
7C
"76
nc
76,
16
~>6








IS- 16
                                               Md - (0.44 x %CO2) i- (0.32 X %O2) + (0.28 X %^)

                                               Md-(0.44xc   )+(0.32xe/ )+ (0.28x77
                                              'Md-  2.
                                                  - Mdx(1
                                                   % HO
                                                   - i-)
                                                    100
                                                                 18
                                                                100
             %H,0

            '-^-

            .) + 18 (
                                                                           100
                                         Ma-

                                         Tl-

                                         Ps - Pb •»•

                                         Pa-
                                                          "F-
S.P.
13.0
                                                                   ) -t-
                                                                       13.0
                                                            =  .I   fs(°R)
                                         Va - 85.40 x Cp x


                                         Vs - 85.40 x (  .77  ) x (

                                         Va-
                                                                     PsxMa
                                                                          )x
                                                Q« - Vs x Aa x 00 a/m
                                         Qa-
                                                             x 2. / 3    xeo
                                                     'Qaxl7.647x-^-x(1- 	*_ )
                                                                Ta       100
                                         °Vtd-
                                                OHM-
                                                             X 17.047 X-
                                                                                   100
-------
              WET-BULB/DRY-BULB MOISTURE CALCULATION
Plant: LA^D
Site: A(A~*{ fa, £^, OoerarorR-
Barometric Pres/ure, in. Hg =
Static Pressure, in. H20 =
Absolute Pressure of Stack = Pbar + -
Wet-Bulb Temperature, °F =
Dry-Bulb Temperature, °F =
Temperature Difference, Td - Tw =
Saturation Vapor Pressure of H2O at Tw
Vapor Pressure of H~O = pva = /PWV, .
Pva = t \ ( "
Location: Au^llar^ (~i
rate Run #: Af~ 15- b uate: j
Pbar= 2.4.^
Pa= -D.^2.
-±2_ PS- Z4 H
136 KS ~ l'
Tw = ^
Td= >^
AT= U
(from Table) = Pvw = O.UZ/i-l'
(Ps - Fvw) x (AT)
2800-(1.3xTw)
)*< ) 0/5Qi,q-
     =         (             )
           (Ps)
 Tamp.
  OF
   o
   10
  20
  30
  40
  50
  60
  70
  00
  90
 100
 110
 120
 130
 140
 150
 160
 170
 180
_190
 200
 210
 229
 230
 240
  0
0.0376
0.0631
0.1025
0.1847
0.2478
0.3626
0.5216
0.7392
 1.032
 1.422
 1.932
2.596
3.446
4.525
5.881
7.569
9.652
1240
1549
19.01
2X47
28.75
3540
4241
5044-
              0.0398
              0.0660
              0.1080
              0.1718
              0.2576
              0.3764
              0.5407
              0.7648
              1.066
              1.467
              1.092
              2.672
              3.543
              4.647
              6.034
              7.759
              9.865
              12.48
              15.63
              19.42
              23.96
              29.33
              35.68
              49.11
              51.76
	 • 	 . 	 : 	 = ^ » — v i ro
VAPOR PRESSURES OF WATER
In Inches of Mercury
2
0.0417
0.0696
0.1127
0. 1 803
0.2677
0.3906
0.5601
0.7912
1.102
1.513
2.052
2.749
3.642
4.772
040V*
• 190
7.952
10.12
12.77
15.98
19.84
24.46
2942
-------
              GAS VELOCITY AND VOLL'METr.iC FLOW RATE
Plant:   L
Samoung LC
Run #: 1 -
cation: # *\ ^utu C^T«.*T COCK Time: ^P^
-* ~ 1 	 nnRrarors- Cr C* r
Barometric Pressure, in. H
Moisture. %: |
StacK Oimen
Wet Bulb. °F
T'«v*iM
3olm
Numoac
1 1
3
3
*
_T
t,
I
*
>
*
s
V.







•^^— ^— -^^— .


^^•"•^•^••^B™
lg: 1 «r. *Zp Static Pressure, in. HoO: — • 7Z.
Molecular wt.. Drv: 'Z-^.MH Pilot Tube. Co: . 7 1
sion. in. Diameter or Side 1 : /£" Side 2: — •

QrvHulhOc. —

v«toeBv [
- — .
-i ,H,Q 1
3tACk
1
"•mo.
" • i
I 6€ 1 /t.«J :
. fci i no !
, c-7 1 H>- 1
, fy 1 Ur
I7.T
I?A







— •— — «^«


—— — — —
s-n-o-
Md - (0.44 I %CO,) » .0.32 X %O,) -r (0.28 X %hi,»
Md • iO.4Ai ; » (0.32 X > - (0.20 « )
•«-?». 8 f
^ M,O S H,O
Ml • Md 1 ( 1 . ^— — _ . - 1 fl ( _^_ ^ .
100 100
M««. ix(l. — ___..iai 	 __-^
10O 1OO
M.. 3»'1l
71 - I-?T- °F- U3; °««°p-«a
SD
13.8 iTi
?«- ">^,^ -"-HO
VS? -
_^ f "i f*Rl
>..«a.4»Mua«<6P> .] p,^.

V
v«- 5<^.
-------
                      METHOD 18 FIELD DATA SHEET
Plant:.
Date-
           c c
Tested Anatyte:.
Orifice TanK #:_
Location:_
Run #:__3_-
                        c x n. « 7
Pump/Rotometer #:	
Pt:  Pretest (mm Hg):.
Stack I.D.:
Pbar:	
                                      TV
                                          Post-Test (mm Hg):_
Sample Tube #:jfe2±J
Operators:   Cc*-
Leak Check: Pre:
                      Post:
Time: Start: /£-v Finish: H3? Total:
W/B: ^  D/B: ~   O2:  *» COC:1
GAS /««T<«-
m, *(o

1. HI


















—






Time
/bn
Kf -7
'CJ~7 >
116? "s
fill f
nai nk
nvl ^
^~
Tr«v«r««
Point
Numbvr
A 1
> •
•}
4.
^-
fe
A 1
>
3
4.
j-
4>













Gauge
Vacuum
(Hg)
o 0
0
o 0
* 0
D <9
o
) 0

Velocity
H«M
m. H$,> !
>-*o
•^.^

- .no-
Slack
T«mp.
°F
M \l
1 £ C!
\T J>
114-
l 1J
i T f
1 & ^
k'j
' It*
»T <
VI V
\ T n












\T \
Vld • 10 44 x ) - (0 3

/ % H O

Kti Mt., )x<1- —
^^ ^
ilf%* M< " 7*^*^
•I^T,-!-)! °F-t>
T '-$* S P
^r] p, — p)., ^ J'r- - (
13.8

Vjp" =

Vs • 6S 49 x Co x JAP x


V« • 85.48 x (

V« • fSL^-^r f P nit
fa flf
->!• V '
As » \ > V ft2


Qs » v« x As x 60 «/m

Qs « x

Qs » iJr'f^" ac*
^ p
Qs ..-Osx 17.847 X —


Q«.j- X17^
„... 	 ^,-n... , _J,_ . .--*!. .• ' '

                                                    - (0.32x%0.,) -. (0.28
                                                               (0.28 X

                                                              13.8
                                                            -s i^-R)

                                                       )x(

                                                                  i
                                                              xOO
                                                      p,     %H-0
                                                      -^— x(l •    ^
                                                                          100:
-------
     FIELD DAT/WHEET
Plant   UK^CQ	
Sampling Location ^ °V
Run Number: <\-\V>  Date: S- ^=\-S1
Pretest Leak Rate: _.6«>l  elm @ \5  in. Hg.
Pretest Leak Check: Pitot:  U  Orsat:  WN
Sample Type: yn ~ \-
Pbar:_
C02:
                    Operator:
                O2:   > I
Probe Length/Type:
Slack Diameter:   \
Nozzle ID:  K><^    Thermocouple #:	
Assumed Bws: _J	Filter #:   A<^	
Meter Box #: ) <.    Y:.%x  AH@: I. %(>*,
Post-Test Leak Rate:  Q   cfm @ ^ in. Hg.
                       As:
Post-Test Leak Check: Pilot:
Orsat:
TNWWM
Wnl
Numtoi



























Samplm
Thw
(min)
0
IO
70
30
vo






















CkxdcFim*
(244iour
doc*)
lfci-7
It VI
itn
Hoi
\1\T






















Goa Meter
Readmg
(Vm)tt3
<\Vl.^o
^^oA
^>lo
°(^i
^4-3, CGt






















Velocity
Head (Apl
tnH2O
Oifica Piesoute Oittorenttol
(AH) in H2O
Desired
Actual
Stack
Temp.
as)
Temperature
°F
Probe
Fitter
Impinger
Temp.
°F
Dry Gas Meter Temp
Inlet
(Tmin°F)
Outlet
(Tm out°F)
Pump
Vacuum
(in. Hg)
y////////y//////////////////////^^^^



















-






14
v.*
i.tf
u






















\.s
\.H)
/.^
I.*






















^
"
/—
-^






















—
—
-
—






















-
—
"™ ""
—






















<-Tr
SI
J~J.
S3






















Sf
»f
Xt
%
-------
Plant:  l/laco
Date: -T
                  SAMPLE RECOVERY DATA
                  	;	  Run No.:
                  	 Sample Box No.: >°--5      Job No.:
          3  fo-$"-«o3
Sample Location:.
Sample Type:	
                                             Filter No.:
Sample Recovery Person:
Comments:	H6«97
FRONT HALF
Acetone
Container No.:
                          Liquid
                               Marked:.
Filter/     '
Container No.:
Sealed:

Sealed:
Description of Rlter:
Samples Stored and Locked:
BACK HALF/MOISTURE
Container No.:	
Liquid Level Marked:
                                             Sealed:

IMP. NO.
1
2
3
4
5
6
CONTENTS
Mlo
Hu>
6«,T-r
^/(r


TOTAL
INITIAL
VOL (ml)
«*
\to
—
>.*0



WEIGHT (arams)
INITIAL
GrC-o
07.7
4^t>
11?. <•


WH.T
FINAL
tffil
07^
f9C£
7^"f>-r


\**M«
NET
3,7
, I
,-u
j-.^


^•\
Description of Impinqar Catch- • 	
-------
J3OE3
              EPA METHOD 4 MOISTURE CALCULATIONS


     PLANT:  /.XfoO _ SOURCE/RUN #' °\-HJL  DATE:_£lHlll


     1 .  Leakage Correction for Volume Metered
          vmc=sV(Lp-0.02)x0.


          Vmc=(        )-(        -0.02) x(
      2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)


                                Pbar-MAH/13.6)N
               = 17.64 xVmcxYx
                                                               13.6V
          Vm
           mstd
      3.  Volume Water Vapor Collected, Standard Conditions


          Impingers & Silica Gel = V ...   = 0.04707 x (W. - W. )
                                wstd             T    '

                              Vw   = 0.04707 x(  
-------
GAS VELOCITY AND VOLUMETriC FLOW RATE
Plant: L/>5e^ Harp- T- ^P- » .0 20 X%N-,>
Md - 10.44 • i - (0.32 X : - (0.2B X )
•*»- )b^4-
S M^O S H,O
M« • Md > 1 1 • ' . - ' fl ( — — .
IOO 100
M« - » ) K(I . . « IB ( ,
lOO 100
M.. >1--1^
^. (I !> °F- S.i3 °a(°P.«OI
e p
1 3.8 1 3-8
"•••'M.vv in-M9
^.
V..«5.4W«CO«^P « >J p,KM.

V
V. . S *• ^> IM
A.. V§OP> n2
Qt« vciAaieOMn
Q«- x xeo
Oa M • * * ^k Aj^nt*
01 " o<*(\d- •"•"
__ %M_Q
M W *?>**
o« _-as«ir.64Tx— — «
-------
                               METHOD 18 FIELD DATA SHEET
         Plant:.
         Date:
          Sc o
        Location- =» to  OC.CA/
        Run at:  / 0- I b-l
        Stack I.D.:	L
        Pbar:
        Sample Tube
        Operators:
Leak Check: Pre:
                               Post:
n.oil
 i.1*
   0

                         Gauge
  \/>0
                    Jii.
                  0
         /G» 0
                   j-o
                H
                            FIow
Tested Analyte:   ST? e'-lf Total: S_S
W/B:   -   D/B: -	O0: 2r
                                  vrrm^
                                  pTv  o^
Trev«ri«
Point
Number
1
)
^
4-
J-
fe
I
J>
"i
4-
J"
L













Velocity
H««d
•n.H^O
. 1^
. 1 (,
. fv
, Isf
. 1T^
, 7.3
. 1^
, T-O
. ^-"L.
, zo
. i*
, 'L'T-












. ^riVU
Slack
T.mp.
°P
^^^
->-30
>5»
5--^ /
T-3J"
>e> 4
>3Z-
•^^c
>i£.
3 % 7
-"Sj7
T-T-O












^>>o
Md - «0.44 x %CO=) - (0.32 X %02) - (0.28 X VoN;;)

Md - 10.44 x     j - (0.32 X    . * (0.2B x     )


    7$lu
          'S H,0      "' H0
                                                P8
                                                             in.Ha
                                                Vs - 65.49 x Co x
                                                Vs - 85.48 x (
                                                                     =, x Ms
                                                                )x(
                                                                 )x
                            i
                                                A.- \.>>    n


                                                Qi • V» x As x 60 t/m


                                                Q« .          x

                                                Os-
                                                                       1fl0

-------
     FIELD DATA SHEET
Plant: Lt\* c O Sa

Samf
Run^
Prete
rfingLoc
4umber:
si Leak P
ation fl It) Ou*u OuT4*"^ Pb.
io-13-1 Dale: 5" •>«* 9 "7 CO
ate: , d0 / cfm @ l-S\n
Pretest Leak Check: Pilot: / Oral: h

:_
^ !
i
;!
>. 4".
Tiav«rM
Pofcil
Numb*







J



















Sampling
Tbra
0
(0
«.o
3> 0
to






















OockTim.
(24-houi
dock)
\^>0
IJT30
(S'fO
U-fo
\fet)0






















Hg Prc
.1 Sla

GajMoUf
Ftoadng
JT^O ,7 O 9
5>58>5^>
Q0C «A-
cj^v , y>
Q | ^ 0"1 C






















V.kjcrty
'///.'/•


























Sample Type: yv\-d	Operator: Q C
               Ps:    ^  ,  VS
                                       Noule ID:
                                       Assumed Bws:
               02
                Thermocouple
                Filler*:   AM
Probe Length/Type:
Stack Diameter:   |
Meier Box*: J4-  Y: .''
Post Test Leak Rate:   °  cftn @ ^ in. Hg
Post Test Leak Check: Pilot:  X'Orsal:  t/«l
OiiSc* Pl«»sur« Orttoicnbal
(&H)inH2O
Dasii*d | Actual
Stack
T«mp
a»i
lempeiatLirt
°F
Piob« | Filur
Impingai
T»mp
°F
Dry Gas Metof Tamp
kilat
amin°F)
Outlet
(Tm out°F)
Pump
Vacuum
(in.Hg)
''-'''//''////////////////•''/ : '///////////////. '////A •'///,
i ^
l-T)
!•»























VI
1-^
_L-Z_

















































*—



_;-- 	 	


















	

























5-5
s*
J- »-























•i^
«t
Pf























i^_
-------
Plant;    <-/>s c o

Date:  Z-W- t
G.Q


li-7
Description of Impinqer Catch! —
-------
og
             EPA METHOD 4 MOISTURE .CALCULATIONS


     PLANT:   l^Co _ SOURCE/RUN #:_ili£li_ DATE:


     1 . Leakage Correction for Volume Metered


         vmc =
         Vmc=(       )-{        -0.02) x(

                        ft3
     2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)

                               Pbar+(AH/13.6)\
         Vmst(j= 17.64 xVmcxYx
         Vm   =         risrf
          mstd
     3. Volume Water Vapor Collected, Standard Conditions


         Impingers & Silica Gel = VW  = 0.04707 x (W.-W. )
                              wstd            T   '

                             V    = 0.04707 x(
                                std


                               fstd
     4. Percent Moisture, by Volume

                     V,..
         R
         °ws     w      /
          B
           WS"
                    wstd    mstd


                    ( -
-------
                GAS VELOCITY AND VQLUMETF.iC FLOW RATE
Plant:  L * s c
            ^_
Samonng Location:  a  IQ ntitf,
                                                    Date:   j"-0       static Pressure, in. HpQ:  —.  70

Moisture. %: /^2.-j*2,    Molecular wt.. Dry; ze.en    Ptteat Tube. Co:   .97

StacK Dimension, in. Diameter or Side i:       Lf	Side 2:   —   	
Wet Bulb. °F:
                             Dry Bulb. °F:    —
                                     M4-I0.44M    '),-<0.32X
                                                             >0.2B I %N,»
                                                             -(0.20K
                                        - 78-^4-
                                                100
                                                     too
                                                         S H,O

                                                           100


                                                          • is r
                                                               too
                                      P"Pb*Tn-
-------
                 GAS VELOCITY AND VOLUMETRIC FLOW RATE
Plant:    LA.S c
Samoiing Location:  j /n Ouet,  „.,-, .T
     *r   io-tY. •».
                                                       Date:
    	 CIocK Time:   / * .'/CT
     Ooerators:    Cfc >.?	
     static Pressure, in.
Barometric Pressi^e. in. Hq:
Moisture. %:   /^, i.g Molecular wt.. Crv: 1Z.W      Pilot Tube CD:   .97
Stack Dimension, in. Diameter or Side 1 •      / f _ Side 2'  — _
Wet Bulb. °F:
                               Dry Bulb. Qc.
                                       Md • io.44 • %CO.) * <0.32 X %O-l » i0.28 X %H,>


                                       Md • <0.44 •     ; «• (0.32 X    .  . 40.28 X     )
M« • Md K 1 1
                                                   M.O      S H,O
                                                    " i . I a (   '
                                                   100        100
                                                        too
                                                                  100
                                               13.8
                                                               t3.8
                                         • 05.481 Co *
                                         • 05.48 • I
                 . I   ~*rm
                 y   PIKM«
                                                       ) a I
                                            v • v >
                                                              xflO



                                                             %H;O

                                                              too
                                                     .
                                                    K17JM7X'
                                                    TRiu
                                   103
-------
 Plant	
 Sampling Location H lo
 Run Number:  lb-13^
'Pretest Leak Rate: .cot
                      Date
                       elm
Pretest Leak Check: Phot:
   15  in. Hg.
Orsat:  r*j>
                     FIELD DATASHEET
Sample Type: rn 
CO2:       O   O2:    1 I
Probe Length/Type:	Pilot
Stack Diameter:    If    As:  <. 2,j
Nozzle ID: N»
Assumed Bws:
Meter Box #:  >4-
Post Test Leak Rate:
Post-Test Leak Check: Pilot: // Orsat:
Thermocouple
Filter #:
Y:
                                                                                          A/I
                                                                                 .AH@:
O cfm
               in.
TrawwM
Point
Numbw

























Sampling
TbTM
(mln)
0
10
7A
ao
1*





















1
OocfcTiriM
(24-hour
dock)
Uo?-
l«|7-
m>-
V91>V
\v^v






















Gas Mel«f
Reading
(Vm)«3
cf^s.i^
^vu
^?.J
o^.-b
c\n^,\>s






















V.locrty
HMd (Ap)
inH2O
Orifice Pr«Mur« Orfterantial
(AH) in H20
Desired
Actual
Stack
Temp.
(Ts)
Temperature
°F
Probe
Filter
Impinger
Temp.
°F
Dry Gas Meter Temp.
Wei
(Tmin°F)
Outlet
(Tm out°F)
Pump
Vacuum
(in. Hg)
'//////// //////////////////y///////^/////////////// y//// •'///,-.


























u
\ X
l-?s
\X






















l«
(4
1.*
l.W






















—

























brA

























lot

























C^
S-4-
3-^
S4-






















q.i
M
*\0
^0






















9J
-------
PlantL

Date:
 SAMPLE RECOVERY DATA

	.	  Run No.:

                     	  Job No.:
                                                                -  3
                     Sample Box No.:.
Sample Location-   "^  >o.

Sample Type:	!ZL
                                              Filter No.:
Sample Recovery Person:

Comments:
FRONT HALF
Acetone
Container No.;
                          Liquid
                          Level Marked:.
Filter
Container
                            Sealed:
                                              Sealed:
Description of Filter:
Samples Stored and Locked:

BACK HALF/MOISTURE
Container No.:	
Liquid Level Marked:.
                                              Sealed:
IMP. NO.
1
2
3
4
5
6
CONTENTS
to a
Ho
£*lpTMf
*


TOTAL
INITIAL
VOL (ml)
(d<»
I'o
— .
*S&



WEIGHT (arams)
INITIAL
e?* 7
Gf34
f -T7. C,
"&& .-r


*>A«s.>
FINAL
6i3. t
C4ij
fJ"?7
7G3.^


>4-^l-t
NET
*>
'1
•\
")>


li-4-
 Description of Impinger Catch:
-------
        EPA METHOD 4 MOISTURE CALCULATIONS


PLANT:  MftO _ SOURCE/RUN #: JL±J_ DATE:  5-tf-


1 . Leakage Correction for Volume Metered
    Vmc=(       )-(        -0.02) x(
2. Volume Metered, Standard Conditions (68 F, 29.92 in. Hg)

                           Pbar+(AH/13.6)N
            17.64 xVmcxYx
                                        2/4.2
     Vm   =    -      risrf
      mstd

 3. Volume Water Vapor Collected, Standard Conditions
     Impingers & Silica Gel = V ...   = 0.04707 x (W, - W. )
                          wstd             T    '

                        Vw   = 0.04707 x(
                           rstd


                           rstd
 4.  Percent Moisture, by Volume




     R   -
     UtAIC — '
              Vwstd+ Vmstd
     o   _
     °WS"
-------
Plant:  LAS<-Q
Date:	£:
- fl
           METHOD 18 FIELD DATA SHEET
Tested Analyte:   SViv
Orifice Tank #:	
Location:.
Run #:  MDA- 13-1
Stack I.D.:
Pbar:	
   " i«
Pump/Rotometer #:  VQST
Pt:   Pretest (mm Hg):	:
     Post-Test (mm Hg):	;
Tt:   Pretest (°F):_
Sample Tube #:.
Operators:
           - i A B
    Post-Test fF):_
Leak Check: Pre:   V   Post:	\/_
Time: StartifcB  Finish:
W/B:  w  D/B:  -   O2:
                                                        CO
Time
1 laoa.^
|(oO-M ^ J
/<,6 7. z$
1too°! "S^
Uo/i ,S£
u/ s - n
iudS-iM
Gauge
Vacuum
(Hg)
\
i
{
\
,
1
1
Flow
Setting
2.1
TL\
"2 i
•2-1
"2_!
2-1
-2.1
AO&,
Traverse
Point
Number





















-



Velocity
Head
in. HjO

























Stack
Tamp.
°F

























"JJ"
^
Jf
^^














                            Md = (0.44 x %C02) -t- (0.32 X %02) ^ (0.28 x
                            Md - 10.44 x
                                                        (0.32 X
                           (0.28 :
                                       :'oH,0      %HO
                            Ms = Md x ( 1 •  - ^— ) - 1 8 ( - '.
                                        1 00         1 00
                            Ms = (
                            Ms
                                                   i x(1 • 	) - 18 ( 	
                                                          100         100-
                                         Ts -         F »

                                        y       SP
                                        1 p, = Pb + -±:i-=(
                                                 13.6
                             Ps =           in. Hg
                                                        .460)
                                                ) +
                                                     13.6
                                         Vs- e



                                         Vs - 85.49 x I


                                         Vs-


                                         As-
                                                  Ts(°R)
                                              ix(
                           )x
            ^f
                                           ft/8



                                            2
                             Qs - Vs x As x 60 s/m
                                          Qs-

                                          Qs-
                                                     x 60
                                           acfrn
                             Qs
                               std
                                               Qsx 17.647 x
Ps

Ts
                    x(1
                                                     100
                                          X 17.847 X-
                                           dsedn
-------
 APPENDIX A. 1.15




NDO Summary Data
-------
     PACIFIC ENVIRONMENTAL SERVICES, INC.
      Prepared By
       3
3_



f
Date
Checked By
                                    ProiectN°
                                                 Page
                                                     of
                                     Client
                                     Location
Date
Sheet Title
                                500-7*0
                                                    400-500
                                                                  £00
                                       -lit)
                                                                   .£&?-
                                                                                 -',?; :
-------
    O
     PACIFIC ENVIRONMENTAL SERVICES, INC.
                                        Project No.
                                        Client
                    Location
                                                        Page
    of

/      /
     Prepared By
Date   Checked By  Date  Sheet Title
                                            M&o-B
     ' 1130
                                        - 3 x>
                                                                         -3*0
1733-
-------
   VCIFIC ENVIRONMENTAL SERVICES, INC.
                                    Project No.
                                                       Page
                                                             of
                                    Client
                                                    '   LA sco
                    Location
                        /%.
  Drepared By
  2 K. tJt
Date
Checked By
Date
Sheet Title
                               V
              0-2-
Wi
                                            3*0
              j
              /
              //-/"".
              f-i.
                                                       f 7
 ^w
 P
-------
E7
 PACIFIC ENVIRONMENTAL SERVICES, INC.
                             Project No.
                                                             Page       of

                                                                    i      i
                             Client
                             Location
Prepared By
              Date
                 Checked By
Date
Sheet Title
                                  A/Do  /%
                                             „/
?**
           L*

            7-1
                            7
                     VJb-A    A/Do- B     A/fio-c
          7-3       2*0-130
-------
TECHNICAL REPORT DATA
Please read instructions on the reverse before completing
1. REPORT NO.
EPA-454/R-99-024a
4. TITLE AND SUBTITLE
Air Emissions From Reinforced Plastics M
Products: Volume I /i
Volume I of III
2.
anufacturing Process, LASCO Panel
posJ-Vc
7. AUTHOR(S)
Franklin Meadows
Daniel F. Scheffel
9. PERFORMING ORGANIZATION NAME AND ADDRESS
Pacific Environmental Services, Inc.
Post Office Box 12077
Research Triangle Park, North Carolina 27709-2077
12. SPONSORING AGENCY NAME AND ADDRESS
U.S. Environmental Protection Agency
Office of Air Quality Planning and Standards
Emissions, Monitoring and Analysis Division
Research Triangle Park, North Carolina 277 1 1
3. RECIPIENT'S ACCESSION NO.
5. REPORT DATE
August 1999
6. PERFORMING ORGANIZATION CODE
8. PERFORMING ORGANIZATION REPORT NO.
10. PROGRAM ELEMENT NO.
11. CONTRACT/GRANT NO.
68-D-70069
13. TYPE OF REPORT AND PERIOD COVERED
Final
14. SPONSORING AGENCY CODE
15. SUPPLEMENTARY NOTES
16. ABSTRACT
The United States Environmental Protection Agency (EPA) Emission Standards Division (BSD) requested that the EPA's Emissions Monitoring
and Analysis Division (EMAD), Emission Measurement Center (EMC) provide testing support in the investigation of the reinforced plastics composite
manufacturing source category to properly set the Maximum Achievable Control Technology (MACT) standards as required by the Clean Air Act
Amendments of 1990. The reinforced plastics composite manufacturing process located at LASCO Panel Products in Florence, Kentucky was selected
by the BSD as the host facility for this emissions testing program.
The sampling program was designed to support the following ESD objectives: 1) Identify and quantify the hazardous air pollutants (HAPs) emitted
by reinforced plastic manufacturing, 2) Identify the sources of HAPs and the total HAPs mass emission rates from the wet application area and the oven
area, 3) Evaluate three ventilation scenarios, 4) Depending on the effectiveness of the industry proposed "closed" system, develope a performance-based
emission limitation achieved by the use of a wet area enclosed table system, 5) Assess the existing emission factors for volatile organic compound
emissions from a continuous lamination process for the purposes of updating the information in AP-42 and determining cost effectiveness for MACT
options involving emissions abatement, and 6) Determine the effect of various process paramenters such as line speed, laminate thickness, HAP content
of raw material and the addition of a gel coat layer on the emission factor.
Sampling was performed during 13 process operating conditions. Measurements were made of the total hydrocarbons (THC), styrene, cumene,
and methyl methacrylate (MMA), and the air flow rate at all enclosure exhausts. A secondary objective of the sampling program was to obtain the
emissions of HAPs from the oven stacks.
This volume (Volume I) is comprised of 464 pages and consists of the report text and Appendix A.I (Manual Methods Raw Field Data).
1 7. KEY WORDS AND DOCUMENT ANALYSIS
a. DESCRIPTIONS
Cumene
Emission Measurements
Hazardous Air Pollutants
Lamination Process
Methyl Methacrylate
Reinforced Plastics Manufacturing
Styrene
Total Hydrocarbons
Volatile Organic Compounds
18. DISTRIBUTION STATEMENT
Unlimited
b. IDENTIFIERS/OPEN ENDED TERMS

19. SECURITY CLASS (This Report)
Unclassified
20. SECURITY CLASS (This page)
Unclassified
c. COASTI Field/Group

21. NO. OF PAGES
-l^W-l/loH
22. PRICE
EPA Form 2220-1 (Rev. 4-77)  PREVIOUS EDITION IS OBSOLETE
F:\U\FMeadows\TRD.Frm\WP 6.1
-------