74-KPM-12 (REPORT NUMBER) AIR POLLUTION EMISSION TEST BRUNSWICK PULP AND PAPER (PLANT NAME) COMPANY BRUNSWICK, GEORGIA (PLANT ADDRESS) U. S. ENVIRONMENTAL PROTECTION AGENCY Office of Air and Water Programs Office of Air Quality Planning and Standards Emission Standards and Engineering Division Emission Measurement Branch Research Triangle Park, N. C. 27711 ------- EPA REPORT NUMBER 74-KPM-12 BRUNSWICK PULP AND PAPER COMPANY BRUNSWICK, GEORGIA FINAL REPORT Submitted to Environmental Protection Agency Office of Air Programs Contract No. 68-02-0225 Task No. 24 Submitted by Engineering-Science, Inc. 7903 Westpark Drive McLean, Virginia 22101 December 1974 ------- TABLE OF CONTENTS Section Title Page I INTRODUCTION l II SUMMARY AND DISCUSSION OF RESULTS 2 III PROCESS DESCRIPTION AND OPERATION 9 A. Process Description * B. Process Operation 10 IV SAMPLING AND ANALYTICAL PROCEDURES 16 A. Location of Sampling Points 16 B. Sampling Procedures *7 C. Analytical Procedures 17 (Appendices omitted from this copy.) ------- LIST OF TABLES Table Title Page II-l Particulate Emission Summary 3 II-2 Particulate Emission Summary (Metric System) 4 II-3 System Performance 6 H-4 System Performance (Metric System) 7 III-l Summary of Calculations of Equivalent Pulp Production Rate 15 LIST OF FIGURES Number Title Page III-l The Kraft Pulping Process 10 III-2 No. 5 Recovery Furnace and Electrostatic Precipitator 12 IV-1 General Layout, Brunswick Unit #5 Precipitators 17 IV-2 Stack Dimensions, Brunswick Pulp & Paper Company 18 IV-3 Cross Section Outlet Stack (One of Two) 19 ii ------- I INTRODUCTION Under Section 111 of the Clean Air Act of 1970, as amended, the Environ- mental Protection Agency (EPA) is charged with the establishment of perfor- mance standards for new stationary sources which may contribute significantly to air pollution. A performance standard is based on the best emission systems which have been shown to be technically and economically feasible. In order to set realistic performance standards, accurate data on pollutant emissions are normally gathered from the stationary source category under consideration. The No. 5 black liquor recovery furnace at the Brunswick Pulp and Paper Company in Brunswick, Georgia, was designated as a well-controlled stationary source in the Kraft pulp industry and was thereby selected by the Office of Air Quality Planning and Standards for an emission testing program. Tests were conducted by Engineering-Science, Inc. personnel during January 22-25, 1974. This facility processes about 1,500 tons of bleached Kraft pulp per day. The No. 5 recovery furnace burns approximately 136,750 pounds/hour of black liquor solids. Air pollution abatement equipment for this furnace consists of an electrostatic precipitator with two parallel chambers. A total of six particulate samples from each of the two chambers of the electrostatic precipitator were collected. These samples were taken down- stream of the respective chamber to determine filterable and total particu- / late emissions. As this process operated continuously with no known periods of peak emissions, testing was conducted during normal operating conditions. Opacity observations of the two outlet ducts were conducted during the particulate testing by personnel from Environmental Science and Engineering, Inc., Gainsville, Florida. This work was performed under a different contract and was reported separately. The test team and the EPA are greatly indebted to Mr. Andy Ryfun of Bruns- wick Pulp and Paper Company for his cooperation in this sampling program. ------- II SUMMARY AND DISCUSSION OF RESULTS The purpose of this test was to establish emission levels from a well-con- trolled black liquor recovery furnace. The twelve particulate runs conducted provide a strong and consistent data base for the determination of emissions from this unit. Exhaust gases from the No. 5 recovery furnace are controlled by an electro- static precipitator with two parallel chambers. The outlet of the north chamber is designated the "A" stack while the "B" stack is the outlet of the south chamber. Individual tests are specified by a letter and number corres- ponding to the stack and test run number. A summary of the individual test results is given in Tables II-l and II-2. Each stack individually shows little variation but the south chamber (B stack) emissions are about 3 times heavier than those of the north chamber (A stack). An average of the particulate concentrations established by the sample train 3 front-half catches for the A stack is 0.013 gr/scf (29.0 mg/Nm ) while for 3 the B stack is 0.054 gr/scf (124.1 mg/Nm ). An average of concentrations 3 determined by total train catches yields values of 0.023 gr/scf (53.2 mg/Nm ) 3 for A and 0.064 gr/scf (146.4 mg/Nm ) for B. Using these averages shows that the front-half catch accounts for approximately 56% of A stack and 84% of B stack total emissions. The data also reveals that the sample train back-half catches are about the same for all the test runs in both the A and B stacks. The average exhaust flow rates for the stacks were 94,930 scfm for A and 108,370 scfm for B. The maintenance histories for the two chambers are not the same and could account for some of the differences. Approximately one month prior to the testing, the north chamber was down for its periodic maintenance and repair. The south chamber maintenance shutdown was about 3 months before the testing. ------- TABLE II-l PARTI CULATE EMISSION SUMMARY Run code Test A-l Test R-l Test A-2 Test B-2 w Test A-3 Test B-3 Tost A-t* Test B-l* Test A-5 Test B-5 Test A-6 Test B-6 stop sru's:2.7 i Dry gas vol ume (scf) 17.05 111.10 85.77 97.31 ?<5.06 100.50 01. OR loi.oi 88.99 98.81 91.95 102.07 Mo! sture (%> 27.17 27.87 30.71* 27.75 28.1*8 29.1*6 29.67 29. nit 29.61* 29.67 28.76 29.09 Orsat C02 12.6 11*. 9 11*. 7 11*. 7 lit. 1 ll.i* 13.U 13.2 1U. 0 11*. 0 13.1 13.2 analysis (S) 02 CO 6.8 .1 I*. 7 0. 1*.7 .1 «* . 7 .1 5.«* 0. 8.5 0. 6.n 0. 6.1 0. 5.2 .2 5.2 .2 6.6 .2 6.2 0. Exhaust flow rate (scfm) 99113. 112163. 02668. 106305. 91296. 107637. 95835. 107018. 93029. 108315. 07637. 108768. Stack temp. (F) i*0i*. 9 it i»8. 5 1*1*5.0 «*02.5 1*32.5 1*01.1 1*31*. 0 1*0?. 0 1*30.1* 3"9.9 1*33.8 393.0 IsokJn- etlc (%> 105.6 106.9 101*. 5 18.7 101.7 10.0.7 102.5 101.8 103.2 98.1* 101.6 101.2 Part. cone. Ur/scf) front total .011 .058 .018 .055 .013 .052 .010 .057 .010 .051 .Oil* .052 .017 .067 .030 .063 .027 .062 .020 .061* .021 .061 .025 .065 Emission rate (Ib/hr) front total 9.1*1 56.03 11*. 36 50.1*6 9.91 1*8.38 8.22 51.90 8.1«* U7.03 11.80 1*8.59 11*. 02 6U.70 23.51 57.51 20.95 57.53 16.1*0 59.02 17.07 56.81* 21.01 61.00 ------- TABLE II-2 PARTICULATE EMISSION (Metric System) SUMMARY Run code Test A-l Test R-\ Test A-2 Test B-2 Test A-3 Test 3-3 Test A-!* Tost B-i* Test A-5 Test B-5 Test A-5 Test B-6 Dry gas vol ume (Nm3) 2.75 3.15 2.51* 2.76 2.i»l* 2.85 2.58 2. 86 2.52 2.80 2.60 2.89 Mo! sture U) 27.17 27.87 50.71* 27.75 28.1*8 29.1*6 29.67 29.01* 29.6it 29.67 28.76 29.09 Orsat C02 12.6 11*. 9 1U. 7 U. 7 It*. 1 11. I* 13.1* 13.2 11*. 0 11*. 0 13.1 13.2 analysis Exhaust (%) flow rate 02 CO (Nm3/m) 6.8 .1 i*.7 0. i*.7 .1 it. 7 .1 5.1* 0. 8.5 0. 6.0 0. 6.1 0. 5.2 .2 5.2 .2 6.6 .2 6.2 0. 2806. 3176. 2621*. 3010. 2585. 301*8. 2711*. 3030. 2631*. 3067. 2765. 3080. Stack temp. (C) 207.2 231.'* 229.5 205.3 222.5 205.1 223.3 208.9 221.3 201*. I* 223.2 200.6 Isokin- Part. cone. etlc (mg/N'm3) (%) front total 105.6 106.9 101*. 5 98.7 101.7 100.7 102.5 101.8 103.2 98.1* 101.6 101.2 25.31*5 133.376 U1.375 126.751* 28.993 120.030 22.906 129.502 23.365 115.91*3 32.272 119.289 37.763 151*. 025 68.029 11*1*. 1(63 61.261 11*2.718 1*5. G97 11*7.260 1*8.987 l'*0.123 57.1*53 11*9.71*2 Emission rate (kg/hr) front total i*.27 25.1*1 6.51 22.89 i*.50 21.95 3.73 23.51* 3.59 21.33 5.35 22.01* 5.36 29.35 10.71 26.09 5.50 26.10 7.1*1* 26.77 7.7U 25. 7S 9.53 27.67 ------- Tables II-3 and II-4 provide a tabulation of system performance for the No. 5 recovery furnace. The total furnace emission rates were obtained by adding the emission rates from the individual chambers. Based on the front- half catch, the average total furnace emission rate was 60.7 Ibs/hr (27.5 Kg/hr). The corresponding average total furnace emission rate, based on total catch, was 78.3 Ibs/hr (35.5 Kg/hr). A weighted average concentration was selected as an appropriate characterization of the particulate loading of the effluent gas stream of the total system. The weighted average concen- tration is defined by the following equation: (gr/scf x SCFM) + (gr/scf x SCFM)_ Weighted Avg. Cone, (gr/scf) (SCFM) + (SCFM) ' ^ (II A B The mean value of the weighted average concentration for the six experimental 3 runs was 0.035 gr/scf (79.7 mg/Nm ), based on the front-half catch, and 0.045 o gr/scf (103 mg/Nm ), based on the total catch. Process emission rates (i.e., particulate emission rate/production rate) were computed for each of the individual chambers and for the total system. Based on the furnace production rates expressed in equivalent tons of unbleached air dried pulp per hour, and on the particulate emission rates for the total system, the following average process emission rates were determined for the No. 5 recovery furnace: 3 Front-half catch =1.33 Ib/ton = 0.667 Kg/10 Kg 3 Total catch =1.72 Ib/ton = 0.860 Kg/10 Kg Some minor equipment problems were encountered during the test program that resulted in short time delays but had no adverse effect on test results. During test run A-l, the heater element in the filter holding section of the sample box malfunctioned and,resulted in the formation of condensate in the cyclone prior to the filter. A total of 43 ml of condensate was collected ------- TABLE II-3 PARTICULATE EMISSIONS SUMMARY (English Units) Production Rate, (tons/hr, unbleached air-dried pulp basis) Front-Half Particulate : Weighted Average Concen- tration, (gr/dscf) Total Furnace Emission Rate, (Ib/hr) Process Emission Rates: Chamber A, (Ib/ton) Chamber B, (Ib/ton) Total System, (Ib/ton) Total Particulate: Weighted Average Concen- tration, (gr/dscf) Total Furnace Emission Rate, (Ib/hr) Process Emission Rates: Chamber A, (Ib/ton) Chamber B, (Ib/ton) Total System, (Ib/ton) 1 45.8 0.036 65.4 0.21 1.22 1.43 0.044 78.7 0.31 1.41 1.72 2 45.7 0.038 64.8 0.31 1.10 1.41 0.048 81.1 0.52 1.26 1.78 Run Number 3 4 44.9 0.034 58.3 0.22 1.08 1.30 0.046 78.5 0.47 1.28 1.75 45.8 0.035 60.1 0.18 1.13 1.31 0.043 75.4 0.36 1.29 1.65 5 45.4 0.032 55.2 0.18 1.04 1.22 0.042 73.9 0.38 1.25 1.63 6 45.3 0.034 60.4 0.26 1.07 1.33 0.046 82.0 0.46 1.35 1.81 Avg. 45.5 0.035 60.7 0.23 1.11 1.33 0.045 78.3 0.42 1.31 1.72 ------- TABLE II-4 PARTICULATE EMISSIONS SUMMARY (Metric Units) 3 Production Rate, (10 Kg/hr, unbleached air-dried pulp basis) Front-Half Particulate: Weighted Average Concen- tration, (mg/Nm3) Total Furnace Emission Rate, (Kg/hr) Process Emission Rates: Chamber A, (Kg/103Kg) Chamber B, (Kg/103Kgl Total System, (Kg/103Kg) Total Particulate: Weighted Average Concen- tration, (mg/Nm3) Total Furnace Emission Rate, (Kg/hr) Process Emission Rates: Chamber A, (Kg/10^Kg) Chamber B, (Kg/103Kg) Total System, (Kg/103Kg) 1 41.6 82.7 29.7 0.103 0.612 0.715 99.5 35.7 0.153 0.706 0.859 2 41.5 87.0 29.4 0.157 0.552 0.709 109 36.8 0.258 0.629 0.887 3 40.7 78.3 26.4 0.110 0.539 0.649 105 35.6 0.233 0.641 0.874 4 41.5 79.1 27.3 0.090 0.567 0.657 99.3 34.2 0.179 0.644 0.823 5 41.2 73.2 25.0 0.090 0.518 0.608 98.0 33.5 0.188 0.626 0.814 6 41.1 78.1 27.4 0.130 0.536 0.666 106 37.2 0.232 0.673 0.905 Avg. 41.3 79.7 27.5 0.113 0.554 0.667 103 35.5 0.207 0.653 0.860 ------- in the cyclone and this measured volume was included in the moisture deter- mination. This liquid catch was added to the front-half wash for particulate analysis. During this same test, it was noticed that arcing had occurred between the stack port and the probe nozzle, resulting in a small section of the knife edge being burned away. The nozzle was replaced for subsequent tests and both probes were grounded to the stacks to prevent reoccurrence. Temperatures on stack B were mostly taken with a long stem thermometer generally positioned in one place. An inoperable pyrometer prevented obtaining the temperature readings at the traverse points as is normally done. An integrated bag sample of exhaust gas was taken during each test at both stacks for Orsat analysis. During the twelve test runs, two of the sample results were not obtainable. A pump malfunctioned during test run B-2 and no gas sample was obtained. The pump was repaired before the next test proceeded. The bag sample obtained during test run B-5 was voided because analysis showed that the sample was contaminated with ambient air. Exhaust gases in both stacks originated in the same boiler thus constituent concentrations should be the same for each test run. Because of this, the data obtained from A-2 and A-5 were used for calculations purposes for the missing B-2 and B-5. ------- Ill PROCESS DESCRIPTION AND OPERATION The Brunswick Pulp and Paper mill at Brunswick, Georgia, produces 1500 tons of bleached kraft pulp per day. The pulp is made into various paper and board products. The EPA test program at this mill consisted of six particulate tests on both stacks of the No. 5 recovery furnace precipitator. A. Process Description 1. General Kraft pulp is produced from wood as shown in Figure III-l. In the process, wood is chipped into small pieces, then cooked in 18 batch digesters at ele- vated temperature and pressure. The cooking chemicals, called white liquor, are sodium hydroxide and sodium sulfide in water solution. The white liquor chemically dissolves lignin from the wood; the remaining cellulose (pulp) is filtered from the spent liquor and washed. The pulp is then made into the various paper products. The balance of the process is designed to recover the cooking chemicals. Spent cooking liquor and the pulp wash water are combined for treatment. The combined stream, called weak black liquor, is concentrated in evaporators to about 65 percent solids, and then fired in a recovery furnace. Combustion of the organics in the black liquor provides most of the heat \ needed to generate process steam. Inorganic chemicals from the black liquor are recovered as a molten smelt at the bottom of the furnace. The smelt, con- sisting of sodium carbonate and sodium sulfide, is dissolved in water and transferred to a causticizing tank. Lime added to this tank converts sodium carbonate to sodium hydroxide, completing the regeneration of white liquor, which is then recycled to the digesters. The calcium carbonate mud, that pre- cipitates from the causticizing tank, is recycled to a kiln to regenerate lime. ------- FIGURE III-1 THE KRAFT PULPING PROCESS Wood - White Liquor (NaOH + Na2S) DIGESTER SYSTEM Pulp * u PULP WASHERS eak Black Lioun Pulp Water RECOVERY FURNACE SYSTEM Heavy Black Liquor (Na2C03 •Water o CJ Of. Smelt 3 t Air I Na2S) MULTIPLE EFFECT EVAPORATOR SYSTEM SMELT DISSOLVING TANK I Green Liquor t White Liquor (recycle to digester) CAUSTICIZING TANK .Lime Calcium Carbonate Mud 10 ENGINEERING-SCIENCE, INC ------- 2. Recovery Furnace The No. 5 recovery furnace was designed by the Babcock and Wilcox Company to burn 338 gallons of black liquor per minute at a solids content of 64 per- cent; this corresponds to a pulp production rate of 1100 air dried tons per day. This direct fired (no direct contact evaporator) recovery furnace was installed in 1972. Soot is continuously blown from the boiler tubes with steam. Each soot blowing cycle takes about two hours and ten minutes. 3. Electrostatic Precipitator Exhaust gases from the No. 5 recovery furnace are cleaned in an electro- static precipitator. The precipitator was designed for a collection efficiency of 99.8 percent and installed in 1972 by the Koppers Company. The unit was designed to treat 415°F combustion gases at a rate of 393,000 ACFM. As shown in Figure III-2, the precipitator has two separate chambers in parallel; each chamber has five electrical fields. The precipitator is situated on the roof of the recovery building. The gases from each chamber exhaust through a separate stack. Dust collecting on the precipitator electrodes is shaken loose by a sys- tem of rappers. The rappers operate in a continuous cycle, with each cycle lasting about 1 1/2 minutes. The dust falls to the bottom of the precipitator where it is removed by drag conveyors to a mix tank. In the tank, the dust is dissolved in the black liquor and recycled to the process. B. Process Operation 1. Recovery Furnace and Electrostatic Precipitator The purpose of the tests was to measure particulate emission levels during normal furnace operation. The information was to help demonstrate actual con- trol levels for recovery furnace operations. 11 ------- NO, 5 RECOVERY FURNACE AND ELECTROSTATIC PRECIPITATOR 10 AIR tn ESP N Chamber A ESP S Chamber B t — SAMPLE LOCATION 1 —SAMPLE LOCATION ŁT> 73 \ ro ------- During the particulate tests, significant furnace and precipitator para- meters were monitored. Readings were made every half hour and recorded on the process data sheets contained in Appendix C. As far as known from the process data and conversations with the operators, the equipment operated normally during the tests. The black liquor charge rate was 345 gallons per minute during each test. The percentage of solids in the black liquor ranged between 59.8 and 61.8 percent. No auxiliary fuel was fired during the tests. 2. Equivalent Pulp Production Rate The operation of the recovery furnace is quantitatively related to the pulp production rate in the digesters. As a result, pollutant emission rate can be expressed on the basis of equivalent pulp production, as shown below: (Emission Rate\ _ /Emission Rate\ / /Equivalent Pulp\ (lb/ton pulp)] ( (Ib/hr) I / (Production Rate) . Eq. (III-l) / \ // V (tons/hr) / To use Equation III-l, the equivalent pulp production was calculated from the black liquor charged during the tests, as shown below: /Equivalent Pulp\ /Black Liquor\/ \ //Solids to Pulp\ I Production 1= I Charge )(% Solids)/1 Ratio ). Eq. (III-2) \ (tons) / \ (Ibs) /\ 100 // \ (Ibs/ton) / The solids-to-pulp ratio used in Equation III-2 was 3000 pounds of black liquor per ton of unbleached air-dried pulp. This is based on the assumption (used by the recovery furnace's manufacturer) that 3000 pounds of solids re- sult for each ton of unbleached pulp produced. Equation III-2 was used to calculate the equivalent pulp production during each test on the recovery furnace. Dividing by the time elapsed while charging the black liquor, gave the equivalent unbleached pulp production rate. 13 ------- The calculations are summarized in Table III-l. As shown, the average rate was found to be 45.5 tons per hour. Substituting into Equation III-l gives the following equation, which was used to calculate mass emission rates: /Emission Rate \ (Ib/ton) >\ = /Emission Rate\ / / 45.5 \ > . / I (Ib/hr) j / (fcon/hr)) ' Eq.(III-3) 14 ------- TABLE III-l SUMMARY OF CALCULATIONS OF EQUIVALENT PULP PRODUCTION RATE Black Hours (1) Date T Jan. Jan, Jan. Jan. Jan. Jan. 1974 22 23 23 24 24 25 Start 1401 0935 1551 0909 1526 0804 Finish 1932 1337 1920 1311 1913 1134 Liquor Readings Integrator (2) Start 515,387,000 519,327,000 520,739,000 524,337,000 525,753,000 529,167,000 Finish 516,632,000 520,237,000 521,521,000 525,248,000 526,602,000 529,959,000 Avg. % Solids 60.7 60.3 60.3 60.5 60.9 60.0 Black Liquor Charged (Ibs) 1,245,000 910,000 782,000 911,000 849,000 792,000 Equivalent Pulp Elapsed Production (3) Time (tons) (hrs) 251.9 182.9 157.2 183.1 172.4 158.4 5.5 4.0 3.5 4.0 3.8 3.5 Equivalent Pulp Production Rate (4) (tons/hr) 45. 45. 44. 45. 45. 45. 45. 8 7 9 8 4 3 5 (Avg.) (1) Item 12 on the process data sheets. (2) Item 11 on the process data sheets. (3) Calculated from Equation 2. (4) Calculated by dividing Equivalent Pulp Production by Elapsed Time. ------- IV SAMPLING AND ANALYTICAL PROCEDURES A. Location of Sampling Points The two pricipltator outlet stacks are identical as far as dimensions and port locations are concerned. They are rectangular and protrude from the building roof about 10 feet with a cross section of 270" x 72". Each has six 4" pipe ports evenly spaced along the long dimension. From the centerline of the sampling ports it is 7'-0" down stream to the stack outlet and an estimated minimum distance of 7'-0" up stream to a flow disturbance in the precipitators. The stacks have an equivalent diameter of about 113" thus flow disturbances are less than one diameter from the sample points in both directions. Because of the sampling location it was decided that nine sampling points would be utilized along each traverse. This resulted in an elemental sampling area of 8" x 45" which is not ideal but the best that could be done with the given conditions. The north chamber stack is called the A stack and the south chamber stack the B stack. Looking at the test side of the stacks, the ports are labled 1 thru 6 reading from left to right on both units. The sampling points for each port are numbered 1 through 9 with point 1 located closest to the port and point 9 located nearest the far wall. t Thus, a specific point could be called A-2-3, which would be the #3 point in the #2 port in the A stack. No sample point was closer than 4" to the stack wall. Each stack had six traverses with nine test points for a total of 54 sampling points. Figures IV-1, IV-2, and IV-3 fully describe the stacks, port arrangements, and sample point locations. 16 ------- FIGURE IV-1 GENERAL LAYOUT BRUNSWICK UNIT #5 PRECIPITATORS Stack Test Ports ~"*-o o o Gas i jDistributing I i Plates—*l Electrostatic jPrecipitator Elevator Stops Here To N. To S. Chamber Chamber From Recovery Boiler 17 ENGINEERING-SCIENCE, INC ------- STACK DIMENSIONS BRUNSWICK PULP & PAPER COMPANY oo Z O m m o V - 1 rh 270" V///////. Some vertical electrical conduits and pneumatic lines, 2-3' from stack A Stack- r*. i I B Stack "3/16" Steel \o co 9, North Chamber / /////ft'///////////^7, t- Roof Line LFlange South Chamber 11" Z 9 CO o m Z O m CD C 73 Z O ------- FIGURE IV-3 CROSS SECTION OUTLET'STACK (ONE OF TWO) CM CM CM X- tn Port #(1 E D E D E D E Traverse Points 234 56789 I I I I I I I I I I I I I I I I I o r» CM 72" 19 ENGINEERING-SCIENCE, INC. ------- B. Sampling Procedures The sample train box and eight-foot probe assembly, used for the testing, was suspended from a monorail fixture which stands on four 7' long plastic pipe legs. The trolley, which supports the weight of the test equipment, rolls along the rail and allows for a simple means of traversing the stack. This portable set-up was convenient for accommodating the six ports on each stack because it was not necessary to disassemble the test equipment when moving the support rig to the next port. Two monorail assemblies were utilized so that the two stack could be tested simultaneously. Some difficulty was encountered when moving the supports because some vertical electrical conduits were located in the area. The varying port heights, due to the sloping roof, were handled by changing the hanger length to the sample box. A standard EPA sampling train with a cyclone separator was used during all the testing. The cyclone was installed up stream of the filter holder inside the heated box. A manometer with an expanded lower scale was used instead of the standard unit in the RAC meter box. The 0-0.25 in WG manometer was necessary because of the low gas velocities encountered in the stacks. The sampling was conducted as specified by EPA Methods 1 through 5 with the additional requirement that the impinger contents were collected and analyzed for particulate content. These methods were published in the Federal Register. Volume 36, No. 247, Part II, Thursday, December 23, 1971. The procedure for recovery and analysis of the impinger contents are published in the Federal Register, Volume 36, No. 159, Part II, Tuesday, August 17, 1971. C. Analytical Procedures^ The clean-up area was located in an unused control room on the third floor of the recovery boiler building. All sample train preparation and clean-up 20 ------- was performed in this clean, well-lighted area. The trains were capped and sealed during all movement to and from the test site on the roof. The probes were capped before and after testing and cleaned in a small well-lighted enclosed area on the eleventh floor level. This eliminated the time and handling necessary to move them in the small elevator to the third floor area. All the integrated gas samples taken during the particulate sampling were run through the Orsat analysis the same day they were collected, soon after the test run was completed. All samples obtained during testing at the Brunswick Pulp and Paper Company were sealed in lead-free Wheaton glass bottles. The bottles, which were not previously used, were acid washed in preparation for the testing. All the sample containers were sent back to the laboratory for final analysis. An outline of the analytical procedures followed by the laboratory is included in Appendix E. 21 ------- |