United States
Environmental Protection
Agency
industrial Environmental Research
Laboratory
Research Triangle Park NC 27711
EPA-6OO/7-80-115
May 1980
EPA Alkali Scrubbing
Test Facility: Advanced
Program — Final Report
(October 1974-June 1978)
Interagency
Energy/Environment
R&D Program Report
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RESEARCH REPORTING SERIES
Research reports of the Office of Research and Development, U.S. Environmental
Protection Agency, have been grouped into nine series. These nine broad cate-
gories were established to facilitate further development and application of en-
vironmental technology. Elimination of traditional grouping was consciously
planned to foster technology transfer and a maximum interface in related fields.
The nine series are:
1. Environmental Health Effects Research
2. Environmental Protection Technology
3. Ecological Research
4'. Environmental Monitoring
5. Socioeconomic Environmental Studies
6. Scientific and Technical Assessment Reports (STAR)
7, Interagency Energy-Environment Research and Development
8. "Special" Reports
9. Miscellaneous Reports
This report has been assigned to the INTERAGENCY ENERGY-ENVIRONMENT
RESEARCH AND DEVELOPMENT series. Reports in this series result from the
effort funded under the 17-agency Federal Energy/Environment Research and
Development Program. These studies relate to EPA's mission to protect the public
health and welfare from adverse effects of pollutants associated with energy sys-
tems. The goal of the Program is to assure the rapid development of domestic/
energy supplies in an environmentally-compatible manner by providing the nec-
essary environmental data and control technology. Investigations include analy-
ses of the transport of energy-related pollutants and their health and ecological
effects; assessments of, and development of, control technologies for energy
systems; and integrated assessments of a wide'range of energy-related environ-
mental issues.
EPA REVIEW NOTICE
This report has been reviewed by the participating Federal Agencies, and approved
for publication. Approval does not signify that the contents necessarily reflect
the views and policies of the Government, nor does mention of trade names or
commercial products constitute endorsement or recommendation for use.
This document is available to the public through the National Technical Informa-
tion Service, Springfield, Virginia 22161.
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EPA-600/7-80-115
May 1980
EPA Alkali Scrubbing Test
Facility: Advanced Program — Final
Report (October 1974-June 1978)
by
D.A. Burbank and S.C. Wang
Bechtel National, Inc.
50 Beale Street
San Francisco, California 94105
Contract No. 68-02-1814
Program Element No. EHE624
EPA Project Officer: John E. Williams
Industrial Environmental Research Laboratory
Office of Environmental Engineering and Technology
Research Triangle Park, NC 27711
Prepared for
U.S. ENVIRONMENTAL PROTECTION AGENCY
Office of Research and Development
Washington, DC 20460
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NOTICE
This report was prepared by Bechtel National, Inc. as an account of work
sponsored by the Environmental Protection Agency (EPA). Neither the EPA
nor Bechtel, nor any person acting on behalf of either:
a. Makes any warranty or representation, expressed or implied, with
respect to the accuracy, completeness, or usefulness of the informa-
tion contained in this report, or that the use of any information,
apparatus, method, or process disclosed in this report may not
infringe privately owned rights; or
b. Assumes any liabilities with respect to the use of, or for damages
resulting from the use of, any information, apparatus, method or
process disclosed in this report.
n
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ABSTRACT
This final report presents the summary of test results from October 1974
through June 1978 of an Advanced Test Program on a prototype lime/limestone
wet-scrubbing test facility for removing SC^ and particulates from coal-fired
boiler flue gases. The test facility is located at TVA's Shawnee Power Station,
Paducah, Kentucky. Tests were conducted on two parallel scrubber systems, a
venturi/spray tower (35,000 acfm @ 300°F) and a Turbulent Contact Absorber or
TCA (30,000 acfm C 300°F).
The initial phase of the test program was devoted to achieving reliable oper-
ation of the scrubber and, especially, the mist eliminator. In late 1975, when
limestone utilization tests were being conducted, a significant breakthrough
occurred when it was demonstrated repeatedly that the mist eliminator is much
easier to keep clean when the scrubber is operated under conditions giving high
alkali utilization.
High alkali utilization is inherent with a lime system. However, operation of
a limestone system at high alkali utilization requires a reduction in limestone
feed which causes a lowering of the pH and reduced S02 removal efficiency. This
led to the investigation of chemical additives, such as magnesium oxide, to
recover the lost SO? removal efficiency. Short-term (6 to 8 hours) factorial
tests were then conducted to characterize the scrubber performance at different
operating conditions, both with and without magnesium oxide addition. Mathe-
matical models were fitted to the factorial test data, as well as longer-term
(one week) test data, for predicting S02 removal as a function of operating
parameters.
Beginning in January 1977, procedures for forced oxidation of the largely
calcium sulfite slurries were investigated. Oxidized slurry solids, having
much higher calcium sulfate (gypsum) content, have improved dewatering and
handling characteristics.
Forced oxidation with two scrubber loops was developed on the venturi/spray
tower system. This system was successfully demonstrated with limestone, lime,
and limestone/MgO slurries. An open pipe air sparger discharging into an
agitated tank was successfully used to oxidize the slurry. Attempts to oxidize
the venturi/ spray tower bleed stream were successful only when magnesium ion
was present to buffer the slurry pH and to increase the liquor sulfite concen-
tration for oxidation. Forced oxidation with limestone slurry in a single
scrubber loop was demonstrated on the TCA system. In this system, more effi-
cient oxidation was achieved with an air sparger than with an eductor.
Other testing on the TCA included limestone type and grind testing, automatic
limestone feed control testing, and limestone testing with Ceilcote egg-crate
type packing. , Flue gas characterization testing on both scrubber systems was
conducted to determine inlet and outlet particulate mass loadings, particulate
size distribution, and S03 concentration.
Auxiliary studies included laboratory reactivity studies of various limestone
types and grinds, development of pressure drop correlations for both scrubbers,
trace element analyses in the slurry liquor, and waste solids dewatering and
characterization studies.
111
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ACKNOWLEDGMENTS
This report was prepared as a team effort by the following Bechtel personnel
Mr. Dewey A. Burbank, Project Manager (after May 1979)
Dr. Marian N. Head, Project Manager (March 1976 through May 1979)
Dr. Michael Epstein, Project Manager (before March 1976)
Dr. Shin-Chung Wang, Technical Manager
A.M. Abdulsattar R.R. McKinsey
G.A. Dallabetta D.T. Rabb
C.L. DaMassa L.S. Reider
J.K. Donnelly C.H. Rowland
T.M. Martin M.A. Smith
J.L. Hing K.E. Wong
D.Y. Kawahara
Dr. Gary Rochelle of the University of Texas has acted as technical consultant
on this project.
Acknowledgment and appreciation are extended to the TVA staff at the Shawnee
Test Facility and to TVA's Emission Control Development Projects group at Muscle
Shoals, Alabama, who are responsible for operation, maintenance, and engineering
modification of the facility.
Special appreciation is expressed to John E. Williams, EPA project officer, who
has guided this portion of the program.
IV
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TABLE OF CONTENTS
Notice
Abstract
Acknowledgments
Illustrations
Tables
Section
1
2
SUMMARY
INTRODUCTION
2.1 Test Facility
2.2 EPA Pilot Plant
2.3 Advanced Test Program
2.4 Reports
2.5 Definition of Terminology
LIME SCRUBBING
3.1 Chemistry of Lime Scrubbing
3.2 Factors Affecting Lime Scrubbing
3.3 Control of Lime Systems
LIMESTONE SCRUBBING
4.1 Chemistry of Limestone Scrubbing
4.2 Factors Affecting Limestone Scrubbing
4.3 Limestone Utilization as a Function of
Scrubber Inlet pH
4.4 Limestone Type and Grind Test Results
4.5 Laboratory Limestone Reactivity Tests Results
v
n
iii
iv
ix
xi i
1-1
2-1
2-2
2-4
2-5
2-6
2-10
3-1
3-2
3-7
3-13
4-1
4-2
4-5
4-9
4-19
4-22
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Section Page
4.6 Automatic Limestone Feed Control 4-24
4.7 Control of Limestone Systems 4-25
5 LIME/LIMESTONE SCRUBBING WITH MAGNESIUM ENHANCEMENT 5-1
5.1 Effect of Magnesium Additive on Dissolved 5-2
Sulfite Species
5.2 Importance of Calcium Solids Equilibria 5-3
5.3 Effectiveness of Magnesium in the Presense 5-4
of Chloride
5.4 pH Independence of Dissolved Sulfite 5-5
Concentrations
5.5 Lime/Limestone Tests with Magnesium 5-9
Enhancement
6 FORCED OXIDATION 6-1
6.1 Forced Oxidation with Two Scrubber Loops 6-3
on the Venturi/Spray Tower System
6.2 Forced Oxidation with One Scrubber Loop 6-18
on the TCA System
6.3 Venturi/Spray Tower Bleed Stream Oxidation 6-34
7 MATHEMATICAL MODEL FOR S02 REMOVAL WITH CORRELATIONS 7-1
OF SHAWNEE DATA
7.1 Development of the Model 7-3
7.2 Correlations of Shawnee Data for S02 Removal 7-7
7.3 Parametric Plots Derived from the Correlations 7-11
8 CALCULATIONS OF GYPSUM SATURATION 8-1
9 SCRUBBER CHARACTERISTICS 9-1
9.1 Turbulent Contact Absorber (TCA) 9-1
VI
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Section Page
9.2 Venturi 9-22
9.3 Spray Tower 9-29
10 WATER BALANCES AROUND SCRUBBER SYSTEMS 10-1
10.1 Factors Affecting Water Balances 10-1
10.2 Limestone Systems with High Fly Ash Loading 10-6
10.3 Lime Systems with High Fly Ash Loading 10-8
10.4 Limestone and Lime Systems with Low Fly 10-9
Ash Loading
10.5 Summary 10-11
11 MIST ELIMINATOR SYSTEMS 11-1
11.1 Description of Shawnee Mist Eliminators 11-3
11.2 Other Mist Eliminator Configurations Tested 11-4
at Shawnee
11.3 Factors Influencing Clean Mist Eliminator 11-6
Operation
11.4 Operating Charateristics of Shawnee M1st Eliminator 11-13
12 OPERATING CONSIDERATIONS 12-1
12.1 Hot Gas Cooling Interface 12-1
12.2 Field Laboratory pH Measurement 12-2
12.3 Reheat 12-4
13 EQUIPMENT OPERATING EXPERIENCE DURING LIME/LIMESTONE 13-1
TESTING
13.1 Scrubber Internals 13-1
13.2 Oxidizers 13-7
13.3 Reheaters 13-9
13.4 Induced-Draft Fans 13-10
vii
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Section Page
13.5 Pumps 13-10
13.6 Alkali Addition Systems 13-12
13.7 Instrument Operating Experience 13-14
13.8 Other Materials and Equipment Evaluation 13-19
14 FLUE GAS CHARACTERIZATION FOR PARTICULATE AND 14-1
SULFUR TRIOXIDE EMISSIONS
14.1 Particulate Mass Removal Efficiency 14-1
14.2 Particulate Size Distribution 14-3
14.3 Slurry Entrainment 14-5
14.4 Sulfuric Acid Vapor (S03) 14-6
15 WASTE SOLIDS DEWATERING AND HANDLING 15-1
CHARACTERISTICS
15.1 Clarifiers 15-1
15.2 Filters 15-2
15.3 Centrifuge 15-3
15.4 Effects of Operating Conditions on Dewatering 15-4
16 ANALYTICAL REQUIREMENTS 16-1
16.1 General Test Schedule 16-1
16.2 Laboratory Staffing 16-3
16.3 Quality Assurance 16-3
17 REFERENCES 17-1
APPENDICES
A CONVERTING UNITS OF MEASURE A-l
B DATABASE SUMMARY B-l
vi i i
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ILLUSTRATIONS
Figure Page
2-1 Schedule for Advanced Test Program 2-7
4-1 Stoichiometric Ratio Versus Scrubber Inlet Liquor pH in the 4-10
Venturi/Spray Tower System With a Single Hold Tank at 20
Minutes Residence Time
4-2 Stoichiometric Ratio Versus Scrubber Inlet Slurry pH in the 4-11
Venturi/Spray Tower System With a Single Hold Tank at 12
Minutes Residence Time
4-3 Stoichiometric Ratio Versus Scrubber Inlet Liquor pH in the 4-12
Venturi/Spray Tower System With a Single Hold Tank at 6
Minutes Residence Time
4-4 The Effect of Effluent Hold Tank Residence Time and Scrubber 4-14
Inlet Liquor pH on Stoichiometric Ratio in the Venturi/Spray
Tower System
4-5 Stoichiometric Ratio Versus Scrubber Inlet Liquor pH in the 4-15
TCA System With a Single Hold Tank at 12 Minutes Residence
Time
4-6 Stoichiometric Ratio Versus Scrubber Inlet Liquor pH in the 4-16
TCA System With Three Hold Tanks in Series at 14.4 Minutes
Residence Time
4-7 Stoichiometric Ratio Versus Scrubber Inlet Liquor pH in the 4-17
TCA System With Three Hold Tanks in Series at 10.8 Minutes
Residence Time
4-8 The Effect of Scrubber Inlet Liquor pH and Hold Tank 4-18
Configuration on Stoichiometric Ratio in the TCA System
5-1 Concentration of Dissolved Sulfite Species (S03=, Mg3°, and 5-6
CaS03°) as a Function of Effective Magnesium Concentration
(Mg - Cl/2)
5-2 Independence of Dissolved Sulfite Concentration (S0o=, Mg3°, 5-7
and Ca3°) and Liquor pH at Various Concentrations of Effective
Magnesium (Mg-Cl/2)
6-1 Flow Diagram for Two-Scrubber-Loop Forced-Oxidation Tests 6-4
in the Venturi/Spray Tower System
6-2 Arrangement of the Venturi/Spray Tower Oxidation Tank 6-5
With Sparger
ix
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Figure Page
6-3 Flow Diagram for One-Scrubber-Loop Forced Oxidation 6-21
With Air Eductor in the TCA System Using One Tank
6-4 Flow Diagram for One-Scrubber-Loop Forced Oxidation 6-22
With Air Eductor in the TCA System Using Two Tanks
6-5 Arrangement of the TCA Oxidation Tank With Eductor in 6-24
Vertical Position
6-6 Flow Diagram for One-Scrubber-Loop Forced Oxidation 6-28
With Air Sparger in the TCA System Using One Tank
6-7 Flow Diagram for One-Scrubber-Loop Oxidation With Air 6-30
Sparger in the TCA System Using Two Tanks
6-8 Arrangement of the TCA Oxidation Tank With Air Sparger 6-31
6-9 Flow Diagram for Bleed Stream Oxidation in the Venturi/ 6-35
Spray Tower System
7-1 Predicted (Equation 7-7) Versus Measured S0? Removal - 7-9
TCA With Limestone
7-2 Predicted (Equation 7-7) S02 Removal as a Function of 7-12
Slurry Flow Rate and Total Height of Spheres - TCA With
Limestone
7-3 Predicted (Equation 7-7) S02 Removal as a Function of 7-13
Scrubber Inlet Liquor pH and Slurry Flow Rate - TCA With
Limestone
7-4 Predicted (Equation 7-7) SOo Removal as a Function of 7-14
Effective Liquor Magnesium Concentration and Slurry Flow
Rate - TCA With Limestone
7-5 Predicted (Equation 7-7) S02 Removal as a Function of 7-15
Liquid-to-Gas Ratio and Scrubber Inlet Liquor pH - Spray
Tower Wfth Limestone
7-6 Predicted (Equation 7-7) SOo Removal as a Function of 7-16
Effective Liquor Magnesium concentration and Liquid-to-Gas
Ratio - Spray Tower With Limestone
7-7 Predicted (Equation 7-7) SOo Removal as a Function of 7-17
Scrubber Inlet Liquor pH and Slurry Flow Rate - TCA With
Lime
7-8 Predicted S02 Removal as a Function of Slurry Flow Rate 7-18
and Effective Liquor Magnesium Concentration - TCA With Lime
-------
Figure page
7-9 Predicted (Equation 7-7) S02 Removal as a Function of 7-19
Scrubber Inlet Liquor pH and Liquid-to-Gas Ratio -
Spray Tower With Lime
9-1 Schematic of Three-Bed TCA 9-2
9-2 Test Facility Mist Eliminator Configuration 9-3
9-3 TCA Bed Pressure Drop (3 Beds, 4 Grids) - 0 Inches 9-5
Total Bed Height of Nitrile Foam Spheres
9-4 TCA Bed Pressure Drop (3 Beds, 4 Grids) - 15 Inches 9-6
Total Bed Height of Nitrile Foam Spheres
9-5 TCA Bed Pressure Drop (3 Beds, 4 Grids) - 22.5 Inches 9-7
Total Bed Height of Nitrile Foam Spheres
9-6 TCA Bed Pressure Drop (3 Beds, 4 Grids) - 30 Inches 9-8
Total Bed Height of Nitrile Foam Spheres
9-7 Comparison of Experimental Data and Predicted Values of 9-11
Bed Pressure Drop - Three-Stage TCA With 1-5/8 Inch
Dia., 6.5 gram Solid Nitrile Foam Spheres
9-8 Comparison of Experimental Data and Predicted Values of 9-12
Bed Pressure Drop - Three-Stage TCA Without Spheres
9-9 Failure Rate of 6-Gram TPR Spheres in Limestone/Fly Ash 9-15
Slurry Service
9-10 Erosion/Shrinkage Rate of Nitrile Foam Spheres 9-17
9-11 Pressure Drop Across 4 Bar Grids and 23 Layers of Ceil cote 9-19
Support Plate Packing
9-12 Schematic of Venturi Scrubber and Spray Tower 9-24
9-13 Comparison of Experimental Data and Predicted Values of 9-26
Pressure Drop in the Chemico Venturi from Equation 9-3
9-14 Comparison of Experimental Data and Predicted Values of 9-27
Pressure Drop in the Chemico Venturi from Equation 9-4
9-15 The Effect of Gas Velocity and Slurry Flow Rate on the 9-31
Flue Gas Pressure Drop Across the Four Slurry Headers
in the Spray Tower
9-16 The Effect of Header Position and Number of Headers on the 9-32
Flue Gas Pressure Drop at 14 gpm/ft^ Total Slurry Flow Rate
xi
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TABLES
Table Page
1-1 Test Blocks on the Venturi/Spray Tower System During 1-5
the Advanced Test Program
1-2 Test Blocks on the TCA System During the Advanced Test 1-6
Program
3-1 Major Chemical Reactions in Lime Scrubbing of S02 3-3
4-1 Major Chemical Reactions Involved in Limestone Scrubbing 4-3
of S02
4-2 Analyses of Limestones Used in the Test Series 4-20
4-3 Summary of TCA Limestone Type and Grind Tests (With high 4-21
fly ash loading, no MgO addition)
4-4 Limestones Used in Reactivity Tests 4-23
5-1 Summary of Limestone Tests With MgO Addition on the 5-11
TCA System
5-2 Summary of Lime Tests With MgO Addition on the TCA System 5-13
6-1 Results of Forced-Oxidation Tests With Two Scrubber Loops 6-7
on the Venturi/Spray Tower System Using Limestone Slurry
6-2 Results of Forced-Oxidation Tests With Two Scrubber Loops 6-12
on the Venturi/Spray Tower System Using Limestone Slurry
With Added Magnesium Oxide
6-3 Results of Two-Scrubber-Loop Forced-Oxidation Lime Tests 6-15
on the Venturi/Spray Tower System
6-4 Summary of One-Scrubber-Loop Forced-Oxidation Limestone 6-25
Tests With Air Eductor on the TCA System
6-5 Summary of One-Scrubber-Loop Forced-Oxidation Limestone 6-33
Tests With Air Sparger on the TCA System
6-6 Results of Forced-Oxidation Tests on the Venturi/Spray 6-37
Tower Bleed Stream Using Limestone Slurry With Added
Magnesium Oxide
7-1 Correlation for Predictions of S02 Removal by Limestone/ 7-10
Lime Wet Scrubbing With a Spray Tower or a TCA
Xll
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Table Page
10-1 Summary of Water Balances for Limestone Runs 10-3
10-2 Summary of Water Balances for Lime Runs 10-4
10-3 Water Balances for Runs With High and Low Fly Ash Loading 10-5
With Forced Oxidation and Two-Stage Dewatering
11-1 Mist Eliminator Wash Systems 11-10
15-1 Summary of Centrifuge Operation, Wear, and Repair 15-5
15-2 Summary of Dewatering Characteristics on Shawnee System 15-7
Bleed
16-1 Type and Frequency of Sample Analysis 16-2
xm
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Section 1
SUMMARY
This is the final report on an Advanced Test Program under the sponsorship
of the Environmental Protection Agency (EPA) to test prototype lime and
limestone wet-scrubbing systems for removing sulfur dioxide (Sty ancl parti -
culate matter from coal-fired boiler flue gases. This report covers the
period from October 1974 through June 1978. The test facility is located
at the Tennessee Valley Authority (TVA) Shawnee Steam Plant, Paducah,
Kentucky. Bechtel National, Inc.* of San Francisco is the major contractor
and test director, and TVA is the constructor and facility operator.
The original program at the Shawnee Test Facility began in March 1972, and
lasted until October 1974. Results from this test period are presented in
Reference 1. During the original program, in which Bechtel also served as
the major contractor and test director and TVA as the constructor and facil-
ity operator, emphasis was placed on solving scaling and plugging problems
of the scrubber and mist eliminator and on demonstrating reliable operation.
Detailed results of the Advanced Test Program from October 1974 through
June 1978 have been documented in four progress reports (References 2,
* Bechtel Corporation before January 1978.
1-1
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3, 4, and 5). This final report summarizes only the major conclusions
and recommendations based on the findings In this period. As such, the
context of the report Is more qualitative In nature. Readers who are
Interested In more 1n-depth quantitative discussions are referred to the
above references.
There are two parallel scrubber systems operated during the Advanced Test
Program:
• A venturl followed by a spray tower
• A Turbulent Contact Absorber (TCA)
Each system has a capacity of approximately 10 MW equivalent in flue gas
from Boiler No. 10 (35,000 acfm* § 300°F for the venturi/spray tower and
30,000 acfm § 300°F for the TCA). The flue gas contains 1500 to 4500 ppm
of S02» and is withdrawn from the ductwork either upstream (high fly ash
loading of 3 to 6 grains/dry scf) or downstream (low fly ash loading of
0.04 to 0.20 grain/dry scf) of the Boiler Nc. 10 paniculate removal
equipment.
In the early part of the Advanced Test Program (Reference 2), efforts on
demonstrating reliable scrubber operation continued. The primary objective
during that period was to achieve reliable operation of the mist eliminators.
A significant breakthrough occurred while the interrelationships among the
operating pH, limestone utilization, hold tank design and residence time,
* Although it is the policy of the EPA to use the metric system for
quantitative descriptions, the British system is used in this report.
Readers who are more accustomed to metric units are referred to the
conversion table in Appendix A.
1-2
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and S02 removal were being investigated (Reference 3). It was demonstrated
that reliable operation of the mist eliminator is a strong function of
alkali utilization (i.e., clean mist eliminator operation is more easily
maintained when the system is operated under conditions leading to high
alkali utilization).
Fewer problems with mist eliminator fouling have been experienced with a
lime system because of its inherent high alkali utilization, about 90 percent.
However, operation of a limestone system at high utilization (above about 80
percent), to obtain reliable mist eliminator operation, results in a reduction
of S02 removal efficiency due to the lower pH operating regime. This has
been one of the major factors in redirecting the Shawnee program toward the
investigation of chemical additives to overcome the loss of SC^ removal.
In the latter part of the Advanced Test Program more emphasis was placed
on the chemistry of lime and limestone scrubbing.
From February 1976 through November 1976 (Reference 4) extensive investi-
gation was conducted on the magnesium-enhanced lime and limestone scrubbing
systems. Addition of magnesium oxide (tested up to about 10,000 ppm effective
Mg"1"1" ion in liquor) increases the dissolved alkaline sulfite species (S03=,
MgS03°, and CaS03°) in liquor for S02 removal. Both short factorial tests
(6 to 8 hours each) and longer term tests (1 week each) were conducted.
The major effort of testing in the period from November 1976 through June
1978 (Reference 5) was directed toward developing forced-oxidation procedures.
Forced oxidation converts predominantly calcium sulfite sludge to calcium
sulfate (gypsum). The latter has improved dewatering and handling characteris-
tics. Calcium sulfite slurry settles slowly; the dewatered sludge has high
1-3
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water content (40 to 50 percent) and is thixotropic. Oxidized gypsum
slurry settles much faster and dewaters easily to a moist soil-like mass
(15 percent water) which is easy to handle.
Tables 1-1 and 1-2 list the test blocks conducted at Shawnee on the venturi/
spray tower and TCA, respectively. The test blocks are classified according
to the type of alkali, fly ash loading in flue gas, MgO addition, and oxida-
tion scheme (no forced oxidation, bleed stream oxidation, one or two-loop
oxidation*). Other combinations of these variables are possible, but they
are either of lesser interest or not practical. For example, a lime system
with one-loop forced oxidation (high or low fly ash loading, and with or
without MgO addition) is not expected to yield good S02 removal because of
the oxidation of scrubbing sulfite species to non-scrubbing sulfate. Time
limitations prevented investigation of other combinations. The specific
objectives of the Advanced Test Program are delineated in Section 2.3.
A brief description of the chemistry of lime and limestone scrubbing is
presented in Sections 3 and 4, along with a qualitative discussion of the
effects of operating variables on reliable, scale-free scrubber operation.
Major operating variables include pH, alkali utilization, slurry solids
concentration, hold tank residence time and configuration, liquid-to-gas
ratio, fly ash loading, chloride concentration, oxidation, and sulfite and
sulfate saturations. System controls with respect to S02 removal perform-
ance and reliability are also discussed. The relationship between pH and
limestone utilization, and the limestone reactivity of different limestone
types and grinds are given in Section 4.
*See Section 2.5.10 for the definitions of one-loop and two-loop forced
oxidation.
1-4
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Table 1-1
TEST BLOCKS CONDUCTED ON THE VENTURI/SPRAY TOWER
SYSTEM DURING THE ADVANCED TEST PROGRAM
Test
Block
1
2
3
4
5(2)
6
7
8
g(2)
10<2)
11
12
13
Alkali
Limestone
Limestone
Limestone
Limestone
Limestone
Limestone
Limestone
Lime
Lime
Lime
Lime
Lime
Lime
Fly Ash
Loading
High
High
High
High
High
Low
Low
High
High
High
Low
Low
Low
MgO
Addition
Yes
Yes
Yes
No
No
No
No
Yes
No
No
Yes
No
No
Oxidation.
Scheme ^ l'
No
Bleed Steam
2-loop
No
2-loop
No
2-loop
No
No
2-loop
No
No
2-loop
(1) All oxidation tests used either an air sparger ring or a 3-inch
air pipe.
(2) Includes long-term (greater than one month) reliability tests.
1-5
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Table 1-2
TEST BLOCKS CONDUCTED ON THE TCA
SYSTEM DURING THE ADVANCED TEST PROGRAM
Test
Block
1
2(D
3(2)
4
5
6
7
8
Alkali
Limestone
Limestone
Limestone
Limestone
Limestone
Limestone
Lime
Lime
Fly Ash
Loading
High
High
High
High
High
Low
High
High
MgO
Addition
Yes
Yes
No
No
No
No
Yes
No
Oxidation
Scheme
No
1-1 oop, Air
No
1-1 oop, Air
1-loop, Air
No
No
No
Sparger
Eductor
Sparger
(1) One run only.
(2) Includes long-term (greater than one month) tests.
1-6
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The effect of magnesium addition on S02 removal is presented in Section 5.
Forced-oxidation procedures and test results are presented in Section 6.
Mathematical models correlating Shawnee S02 removal data, with and without
magnesium enhancement, are given in Section 7. Parametric plots of S02
removal as a function of operating variables are also shown.
Simplified equations for calculating gypsum saturation from the measured
concentrations of calcium, magnesium, and sulfate ions are given in Section
8. The equations were fitted to the predicted values of gypsum saturation
from the Bechtel-Modified Radian Equilibrium Computer Program (Reference 1).
The equations are useful for those not having access to the modified Radian
program.
Section 9 presents the mechanical operating characteristics of the TCA,
venturi, and spray tower scrubbers. The pressure drop, turndown character-
istics, and ranges of operating conditions are discussed.
Water balances around scrubber systems for closed-liquor-loop operation are
given in Section 10. Makeup water requirements under a wide range of
operating conditions are calculated based on the 10 MW size Shawnee high-
sulfur scrubbers. The results should allow extrapolation to larger scale
units operating under similar conditions.
Section 11 presents the mist eliminator operating experience at Shawnee.
Alkali utilization was identified as the most important factor affecting
the mist eliminator operability. It is much easier to keep the mist
eliminator clean at high alkali utilization than at low utilization.
In Section 12 experiences with operating difficulties, and the appropriate
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steps taken to solve problems, are presented. These involved preventing
solids and scale buildup at the hot-gas/cooling slurry interface in the
TCA inlet duct, maintaining accurate pH measurements, and flue gas reheating.
Operating experience with equipment and materials during the Advanced Test
Program are summarized in Section 13. Conclusions are given wherever
possible.
A brief summary is given in Section 14 of the results of the stack gas
emission characterization tests on both venturi/spray tower and TCA systems.
Particulate mass removal efficiency, typical outlet mass loading, particu-
late size distribution, slurry entrainment, and sulfuric acid vapor (SOj)
emission are discussed.
Section 15 presents the operating experience with the dewatering equipment
(clarifiers, filter, and centrifuge). Laboratory results on cylinder
settling tests and vacuum funnel filtration tests, which are routinely
conducted to monitor the slurry settling and dewatering characteristics,
are also presented. Major factors affecting these properties are gypsum
content in the sludge (oxidized or unoxidized), magnesium concentration
in the liquor, and initial slurry solids concentration. The laboratory
results correlated well with the results from the filter and centrifuge.
Finally, Section 16 presents the analytical requirements as practiced at
Shawnee. The sample locations, type and frequency of analyses, and the
criteria used to judge the acceptability of the analytical results are
given. It should be noted that the Shawnee laboratory is fully equipped
and staffed to perform all necessary chemical analyses, not only for process
controls but also for characterizing the scrubber performances. Therefore,
1-8
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the Shawnee laboratory operation is elaborate by necessity for a research
facility, and is not typical of a full scale flue gas desulfurization
plant.
1-9
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Section 2
INTRODUCTION
In June 1968 a program was initiated under the direction of the Environ-
mental Protection Agency (EPA)* to test prototype lime and limestone wet-
scrubbing systems for removing S02 and particulates from flue gases. A
test facility was built which operates with flue gas from coal-fired Boiler
No. 10 at the Tennessee Valley Authority (TVA) Shawnee Steam Plant, Paducah,
Kentucky. Bechtel Corporation of San Francisco was the major contractor
and test director, and TVA was the constructor and facility operator.
The original testing program at the facility lasted from March 1972 to
October 1974. Results are presented in Reference 1. During the original
program emphasis was placed on solving scaling and mist eliminator problems
for demonstrating reliable operation.
In June 1974 the EPA, through its Office of Research and Development and
Control Systems Laboratory, initiated an Advanced Test Program at the Shaw-
nee Test Facility. Bechtel continued as the major contractor and test
director, and TVA as the constructor and facility operator. During the
Advanced Test Program more emphasis was placed on the chemistry of lime
* The National Air Pollution Control Administration prior to 1970.
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and limestone scrubbing. Four progress reports have been published (Refer-
ences 2, 3, 4, 5) which document the results of the Advanced Test Program
from October 1974 through June 1978. This final report presents conclusions
and recommendations based on the results of the Advanced Test Program.
2.1 TEST FACILITY
Initially the Shawnee Test Facility included three parallel lime/limestone
wet scrubbing systems, all operating on flue gas from Boiler No. 10 at the
Shawnee Steam Plant. However, one system (Marble-Bed absorber) was discon-
tinued early in the program because of operational difficulties. The two
scrubbers in operation during the Advanced Test Program were:
t A venturi followed by a spray tower
• A Turbulent Contact Absorber (TCA)
These scrubbers were chosen for their ability to remove both S02 and particu-
lates from the burning of medium- to high-sulfur coal. Each system has a
capacity of approximately 10 MW equivalent in flue gas (35,000 acfm @ 300°F
for the venturi/spray tower and 30,000 acfm
-------
discharging into a separate hold tank. In the former case, forced oxida-
tion of sulfite to sulfate was effected by sparging air into a bleed stream
hold tank. In the latter case with two-scrubber-loop operation, air was
introduced into the venturi hold tank which was normally followed by a small
desupersaturation tank to provide additional time for gypsum crystallization
and air-free pump suction.
The TCA system can operate with a single effluent hold tank or up to three
tanks in series. Air for forced oxidation can be introduced into a hold
tank within the scrubber loop.
Alkali is fed to the scrubber system as a slurry. Lime is slaked onsite to
a 20 weight percent slurry with makeup water. Limestone is dry-ground onsite
and slurried to a 60 weight percent slurry with makeup water or clarified
liquor from the dewatering system. Scrubber additives such as magnesium
oxide are metered as dry powder directly to the hold tanks.
Each scrubbing system has its own independent dewatering system. A tightly
closed liquor loop is maintained with all liquor from the dewatering systems
returned to the scrubbing loops. Water leaves the scrubbing system via
the discharge solids and the humidified flue gas. A small amount of water
also leaves the system with the flue gas as entrained liquid droplets. The
venturi/ spray tower system normally operates with a thickener followed by
a rotary drum vacuum filter. The TCA dewatering system normally consists of
a thickener followed by a solid bowl centrifuge. Discharge solids concentra-
tions normally range from about 50 weight percent for unoxidized solids to
above 80 weight percent for oxidized solids.
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The scrubbing systems are highly instrumented with continuous recording of
important process variables, including flue gas flow rate, inlet and outlet
S02 concentration, major slurry and liquor stream flow rates and densities,
inlet and outlet slurry liquor pH, tank levels, oxidation air rates, and
pressure drops across major pieces of equipment.
The onsite analytical laboratory, staffed around the clock, provides complete
slurry analyses at least once a shift and runs supplemental analyses as needed.
The test facility has its own TVA operations, maintenance, laboratory, and
technical staff, which are independent of the power plant operation. Bechtel
maintains a small onsite staff to direct the program. In addition, Bechtel
personnel in the San Francisco Home Office provide the technical support and
direction; TVA's Emission Control Development Projects group at Muscle Shoals,
Alabama, provides engineering support.
2.2 EPA PILOT PLANT
There are two smaller scrubbing systems (300 acfm or 0.1 MW equivalent each)
at the EPA Industrial Environmental Research Laboratory (IERL) in Research
Triangle Park, North Carolina. These small pilot-scale scrubber systems are
capable of simulating the Shawnee scrubber systems with excellent agreement
in the lime/limestone wet-scrubbing chemistry. Preliminary data are generated
on the pilot-scale system to determine the validity of new process concepts
and to guide the selection of those promising concepts that should logically
be investigated on the larger scale Shawnee units. Examples of studies ori-
ginating at the EPA pilot plant and then later investigated at the Shawnee
test facility include gypsum unsaturated operation, increasing limestone
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utilization, forced oxidation of sulfite to sulfate, and magnesium-enhanced
lime and limestone scrubbing.
2.3 ADVANCED TEST PROGRAM
This section contains a description of the Shawnee Advanced Test Program,
which began in October 1974 and was completed in June 1978. The objectives
of the Advanced Test Program were:
t To demonstrate process reliability, with an emphasis on mist elimi-
nation systems
• To investigate advanced process and equipment design variations for
improving system reliability and economics
t To evaluate process variations for a substantial increase in alkali
utilization for limestone systems
t To evaluate the effect of increased magnesium ion concentration on
improving control, reducing gypsum saturation, and increasing S02
removal
• To evaluate the efficiency and reliability of lime and limestone
scrubbers under conditions of widely varying flue gas flow rate and
inlet S0£ concentration
t To evaluate system performance and reliability without fly ash in
the flue gas
• To determine the effectiveness of forced oxidation in producing an
improved throwaway sludge product
• To determine the practical upper limits of S02 removal efficiency
for both limestone and lime scrubbing systems
• To perform reliability demonstration runs on advanced process and
equipment design variations
• To characterize stack gas emissions, including inlet and outlet
particulate mass loading and size distribution, slurry entrainment
and total sulfate emissions
• To evaluate methods of automatic control
• To provide material for the field evaluation of sludge disposal
processes. (The field evaluation is being conducted under a
separate EPA program.)
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• To evaluate corrosion and wear of alternative plant equipment
components and materials
• To develop a computer program for the design and cost comparison
of full-scale lime and limestone systems
A bar chart of the Advanced Test Program, showing the time spent on each of
the defined objectives, is presented in Figure 2-1.
2.4 REPORTS
This final report summarizes the recommendations and conclusions resulting
from the Advanced Test Program. The tests conducted during the Advanced
Test Program are documented in four earlier progress reports. This section
lists these reports and briefly describes the content of each.
2.4.1 First Progress Report
The First Progress Report (Reference 2) presents the results of testing from
October 1974 through mid-April 1975. During this period the primary objective
was to achieve reliable operation of the mist eliminators. Reliable opera-
tion was demonstrated with lime slurry on the venturi spray tower system in an
823-hour run at 8 ft/sec superficial flue gas velocity. With limestone slurry,
reliable operation was achieved through the use of a wash tray to isolate the
mist eliminator from the scrubbing slurry. The TCA system was was operated
successfully with such a wash tray in limestone service in an 1835-hour run*
*The test, Run 535-2A, was made at an average limestone utilization of only
65 percent before it was discovered that high alkali utilization (greater
than about 85 percent) promotes reliable mist eliminator operation (see
Reference 3 and Section 11). Reliable mist eliminator operation has been
achieved routinely in the later tests at high alkali utilization and 12.5
ft/sec scrubber superficial gas velocity using a 3-pass open-vane chevron
mist eliminator without a wash tray (References 4 and 5).
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Figure 2-1
Schedule For Advanced Test Program
-------
at 8.6 ft/sec superficial gas velocity in the scrubber section (5.6 ft/sec
in the mist eliminator section).
2.4.2 Second Progress Report
The Second Progress Report (Reference 3) covers the operating period from
June 1975 through mid-February 1976. (The scrubbers were down for six weeks
in April-May 1975 because of a scheduled Boiler No. 10 maintenance outage.)
The interrelationships of operating pH, limestone utilization, hold tank
design and residence time, and S02 removal were explored during this period.
A breakthrough occurred when it was demonstrated that reliable operation
of the mist eliminator is strongly dependent on alkali utilization. (High
utilization is accompanied by more reliable operation.) An 1143-hour
variable-load test with lime slurry in the venturi/spray tower system demon-
strated that the system can be operated with good control when following a
typical daily boiler load cycle.
2.4.3 Third Progress Report
Testing from mid-February 1976 through November 1976 is covered in the
Third Progress Report (Reference 4). Short factorial tests (6 to 8 hours
each) were conducted on both scrubber systems to determine SC^ removal as
a function of operating parameters. These tests were conducted with lime,
limestone, and limestone with added magnesium oxide. Mathematical models
fitted to these data are presented in the report. Additional longer term
tests (1 week each) were conducted on both systems to evaluate magnesium
enhanced scrubbing with both lime and limestone slurries. The effects on
scrubber performance of high and low fly ash loadings in the incoming flue
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gas were also explored. In flue gas characterization studies, scrubber
inlet and outlet particulate mass loading, particulate size distribution,
and sulfuric acid mist (SOj) concentration were measured as a function of
operating conditions.
2.4.4 Fourth Progress Report
The Fourth Progress Report (Reference 5) documents testing from late-
November 1976 through June 1978. The major emphasis during this period
was on developing forced oxidation procedures to convert the predominantly
calcium sulfite sludge to calcium sulfate (gypsum). Such oxidized slurry
solids have improved dewatering and handling properties.
Further tests were conducted with low fly ash loadings and with added mag-
nesium oxide. Additional testing included limestone type and grind testing,
automatic limestone feed control testing, and limestone testing with Ceil cote
egg-crate type packing. Monitoring of flue gas mass loading, particulate
size distribution, and sulfuric acid mist continued.
Two additional limestone reliability tests were conducted: a 747-hour test
on the TCA without forced oxidation and a 840-hour test on the venturi/spray
tower in a two-scrubber-loop configuration with forced oxidation. A 779-
hour lime reliability test was also conducted on the venturi/spray tower
in a two-scrubber-loop configuration with forced oxidation.
Auxiliary studies during this test period included laboratory reactivity
studies of various limestone types and grinds, development of pressure drop
correlations for both scrubbers, trace element analyses in the slurry liquor,
and waste solids dewatering and characterization studies.
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2.4.5 Database
All major1analytical data for the entire Advanced Test Program has been re-
corded in an active database along with test conditions for each run. A
database report including test conditions and analytical summaries for each
run is given in Appendix B.
2.4.6 Laboratory Procedures Manual
All analytical procedures used in the Shawnee onsite laboratory have been
documented in a Laboratory Procedures Manual (Reference 6). A copy of this
manual is available on request from the project manager, Bechtel National, Inc.
2.5 DEFINITION OF TERMINOLOGY
This subsection defines the terminology of lime/limestone wet scrubbing,
as used in this report.
2.5.1 Air Stoichiometry
For a lime/limestone system using forced oxidation, the air Stoichiometry
is the number of gram-atoms of oxygen fed to the air sparger per gram-mole
of S02 absorbed. One mole of sulfite or bisulfite ions (S03S, HS03~)
requires one atom of oxygen to be oxidized to sulfate or bisulfate (S04=,
HS04"). The calculated values for air Stoichiometry would be higher if the
moles of S02 oxidized naturally in the scrubber and hold tank are excluded
from the moles of S02 absorbed.
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2.5.2 Closed Liquor Loop
A scrubber system is said to operate with closed liquor loop when no excess
liquor stream is discharged other than that associated with the waste sludge.
Closed loop operation requires either a solids dewatering device (clarifier,
filter, centrifuge) or a pond, with recycle of all supernatant liquor to the
scrubber system.
For Shawnee closed liquor loop operation, discharge of excess liquor, such as
clarifier overflow or filtrate, is not allowed. When a clarifier alone is
used, the system waste discharge (clarifier underflow) solids concentration
is normally maintained at about 40 percent. With a filter or centrifuge in
series with the clarifier, the waste discharge (filter or centrifuge cake)
solids concentrations range from 50 to over 80 percent, increasing with
increased gypsum content. Thus a very "tight" liquor loop is achieved with
forced oxidation (high gypsum content in solids) and with filter or centri-
fuge as a final dewatering device.
Makeup water (mist eliminator wash, water in fresh alkali addition stream,
and recirculated slurry pump seal water) is limited to the quantity which
leaves the scrubber system with flue gas (as evaporated water and entrainment)
and discharge sludge.
2.5.3 Effective Magnesium
Effective magnesium-is total dissolved magnesium minus one-half the total
dissolved chloride, in gram-moles/liter. Magnesium is added to a lime/
limestone wet scrubbing system to enhance the S02 removal. Although
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dissolved magnesium sulfite/sulfate affects S02 removal, magnesium chloride
(MgCl2) has little effect.
2.5.4 Gas Velocity
Gas velocity is the velocity of humidified flue gas (125°F) through the
scrubber, based upon empty scrubber cross-sectional area (no allowance
made for piping, spray nozzles, or other scrubber internals).
2.5.5 Lime/Limestone Stoichlometry and Utilization
Lime/limestone stoichiometry is the ratio of the calcium added as lime
or limestone to the S02 absorbed in the scrubber, mole/mole. Lime/limestone
utilization, expressed 1n percent, is the inverse of stoichlometry, multiplied
by 100 percent.
2.5.6 Llquld-to-Gas Ratio
The liquid-to-gas ratio, or L/6, is the gallons per minute of slurry
recirculated to the scrubber divided by the thousands of cubic feet per
minute of humidified gas (125°F) flowing through the scrubber.
2.5.7 Particulate Mass Loading
The particulate mass loading of the scrubber inlet or outlet gas is usually
expressed as the total weight of solid particles (fly ash and solid reaction
products) in grains per dry standard cubic foot of gas (60°F). Particulate
emissions standards are usually specified in pounds of particulates in the
stack gas per million Btu of boiler heat input. For a typical Shawnee coal
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and 30 percent total excess air (boiler excess air plus air in-leakage to
system), an emission of 0.10 Ib particulates/MM Btu is equivalent to a
stack gas particulate mass loading of 0.052 gr/dry scf.
2.5.8 S02 Make-per-Pass
The S02 make-per-pass is defined as the number of milligram-moles of S0£
absorbed in the scrubber per liter of liquor as the recirculated slurry
makes one pass through the scrubber.
2.5.9 Statistical Parameters Used with Correlations
The accuracy of correlations of Shawnee data is usually expressed in terms
of two statistical parameters: the standard error of estimate and the
percent of variation in the data explained (sometimes called the index of
determination).
i)
The fraction of variation explained by a correlation is equal to R , where
p
R is the correlation coefficient. The equation defining Rc is:
Fraction of Variation 2 s(y-y')2
Explained K l £(y-y)2
where:
y = value of the independent variable for a particular
data point
y1 = predicted (correlation) value of the independent
variable for the same data point
y = arithmetic average of all values of the independent
variable in the correlated set of data
ty
The percent of variation is equal to 100 x R .
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The standard error of estimate is defined by the following equation:
Standard Error
of Estimate
where:
n = number of data points in the correlated set of data
k * number of dependent variables fitted with coefficients
For a normal distribution of errors, or deviations between the measured and
predicted values of the independent variable, about two-thirds of the
predicted values should be within plus/minus one standard error of the
measured values, and about 95 percent within plus/minus two standard errors.
2.5.10 One-Loop/Two-Loop Forced Oxidation
Forced oxidation is achieved by air sparging of the slurry in an oxidation
tank, to convert calcium sulfite solids (CaS03*l/2H20) to gypsum (CaS04*2H20),
For a one-loop forced oxidation system, the slurry effluents from all
scrubbers in the system (e.g., venturi scrubber and spray tower at Shawnee
constitute a two-scrubber system, and TCA a one-scrubber system) are sent
to one tank, which is the oxidation tank. A one-loop system may or may
not include a second hold tank for further alkali dissolution and gypsum
crystallization prior to recycle to the scrubbers.
For a two-loop forced oxidation system, there are two scrubbers (e.g.,
venturi scrubber and spray tower at Shawnee) with each scrubber effluent
going to a separate tank. The effluent hold tank for the upstream scrubber
(in terms of gas flow) is the oxidation tank.
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2.5.11 Gypsum Saturation in Liquor
The fraction gypsum saturation of a limestone/lime wet scrubbing liquor is
defined as:
Fraction Gypsum = (Ca'H')(SO/|=)
Saturation K$
where:
(Ca++), (S04=) = activities of dissolved Ca++ and S04= ions,
respectively, g-mole/1.
KSD = solubility product for gypsum
= 2.2 x 10'5 (g-mole/1)2 at 50°C
Percent gypsum saturation is 100 percent times the fraction gypsum satura-
tion. The fraction gypsum saturation of Shawnee scrubbing liquors are
calculated by inputting the laboratory liquor analytical data into either
the Bechtel-Modified Radian Equilibrium Computer Program (Reference 1) or
the simplified equations presented in Section 8.
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Section 3
LIME SCRUBBING
Quicklime (CaO) is produced from limestone (CaC03) by calcining to drive
off C02« It is normally delivered to the site as pebbles and stored in
silos. Lime is fed to the scrubbers in a 20 weight percent slurry after
having been slaked (combined with water) to form hydrated lime [CafOH^].
As a scrubbing medium, lime has several advantages over limestone. Lime
is more reactive than limestone and therefore a lime slurry scrubbing
system is more responsive. Alkali utilization (moles S0£ removed per mole
of alkali) is usually better with lime. Furthermore, transportation costs
are less per unit of alkalinity. The major drawback of lime is its higher
cost at the point of origin.
In this section a simplified description of the chemistry of lime scrubbing
is presented, followed by a discussion of operating conditions and control
procedures.
The chemistry described was compiled from several sources and is not wholly
based on results at the Shawnee Test Facility. Documentation of sources is
given where possible. Details of the chemistry presented are based on inter-
pretation of observations to date and are subject to modification as more
information becomes available.
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3.1 CHEMISTRY OF LIME SCRUBBING
The overall reaction of lime with S02 may be represented by:
CaO + S02 —»• CaS03 (3-1)
One mole of lime reacts with one mole of sulfur dioxide to produce one mole
of calcium sulfite. The product is actually a mixture of calcium sulfite
hemihydrate (CaS03*l/2 H20) and the oxidation product, calcium sulfate
dihydrate (CaSO^'Z H20), commonly called gypsum.
The detailed reaction mechanism of this process is complex, involving mass
transfer between the gas, liquid, and solid phases, with several reactants
in each phase (Reference 7). For this reason equations that describe
the chemistry can be written in many ways, depending on which aspect of
mass transfer is being emphasized. Moreover, scrubber operating conditions
such as pH, liquid-to-gas ratio, and hold tank residence time can determine
which reactions predominate, and whether they occur in the scrubber or in
the hold tank (Reference 8).
A representative set of chemical equations that describe wet scrubbing of
S02 by lime is shown in Table 3-1. They describe the main reactions in an
S02 wet-scrubbing system using lime under the following normal operating
conditions:
Recirculated slurry liquor pH = between 7 and 9 at the scrubber inlet
and between 4.5 and 5.5 at the scrub-
ber outlet
Stoichiometric ratio
(moles of lime added per = 1.0 to 1.2
mole of S02 absorbed)
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Table 3-1
MAJOR CHEMICAL REACTIONS IN LIME SCRUBBING OF S02
Reactions in the Scrubber
Absorption
S02 (gas) *-S02 (aqueous) (1)
Neutralization
S03= + S02 (aqueous) + H20—*-2 HS03" (2)
Dissolution
CaS03 (solid) *-Ca++ + S03= (3)
Oxidation
HS03" + 1/2 02 *-S04= + H4 (4)
Reactions in the Hold Tank
Dissolution
Ca(OH)2 (solid) »~ Ca++ + 2 OH" (5)
NeutralIzation
OH" + HS03" *"S03= + H20 (6)
Oxidation
S03= + 1/2 02 *-S04= (7)
Precipitation
Ca++ + aS03= + bS04= + 1/2 H20 *- Ca(S03)fl(S04)b • 1/2 H20 (solid) (8)
Ca++ + S04= + 2 H20 »-CaS04 • 2 H20 (solid) (9)
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3.1.1 Reactions in the Scrubber
The major chemical reactions that occur in the scrubber include:
t Absorption of S02 from the flue gas into the slurry liquor
• Neutralization of the absorbed S02 by alkaline components in
the liquor
0 Dissolution of alkaline components from the slurry solids into
the liquor
• Oxidation of sulfite species in the liquor to sulfate
Absorption of S02 from the flue gas into the slurry liquor is represented
by Equation 1 of Table 3-1. In addition, some C02 is absorbed in the liquor.
Without additional reactions the liquor would rapidly become saturated with
S02 and C02, effectively terminating absorption.
Neutralization of the absorbed S02 is represented by Equation 2 of Table 3-1.
The reaction in lime system is primarily that of the alkaline sulfite ion (SOj)
with S02 to form bisulfite (HSO^) ions. This neutralization reaction is
essentially instantaneous (Reference 9), thus allowing additional S02 to be
absorbed. Absorbed C02 is neutralized by sulfite (SOp 1n a similar manner
to form bicarbonate (HCO^) and bisulfite (HSO^).
Dissolution of alkali components is the limiting step in S02 removal. Alka-
linity is maintained in the slurry liquor primarily by dissolving solid cal-
cium sulfite (CaSf^) to replenish the sulfite ion (SOp (Equation 3, Table
3-1). In addition, the slurry solids contain a small amount of calcium car-
bonate (CaCC^) plus some residual calcium hydroxide [Ca(OH)2] which dissolve
and react with aqueous S02. The solids dissolution rate is a function of
the solids concentration, the particle size distribution of the solids, and
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scrubber operating conditions, including liquid-to-gas ratio, holdup time
in the scrubber, and slurry liquor pH (References 3 and 8).
Oxidation of the bisulfite ion (HSO^) in the liquor phase to sulfate
(SO^) is represented by Equation 4 of Table 3-1. Oxygen for this reaction
is supplied from the excess air in the flue gas. At Shawnee about 10 to 30
percent of the sulfite is oxidized. Although no reliable means of predicting
the degree of oxidation have been developed at Shawnee, some general obser-
vations can be made (Reference 10):
0 Increasing excess air tends to increase the rate of sulfite oxidation.
0 Percent oxidation tends to increase with a decreasing SO? removal
load.
0 In general, operation at lower slurry pH gives higher sulfite
oxidation.
0 Most sulfite oxidation at Shawnee occurs in the scrubber and pos-
sibly the downcomer.
0 Slurry liquor composition can affect oxidation at Shawnee. An in-
crease in total dissolved solids lowers oxygen solubility, which
decreases oxidation. However, increased dissolved solids may
increase oxidation by increasing the sulfite concentration or by
decreasing the average droplet size inside the scrubber, or both.
0 Catalysts may affect sulfite oxidation. Potential oxidation cata-
lysts are introduced from the flue gas (NO, NOo), fly ash (metal
oxides), lime (metal oxides), makeup water (metal ions), and from
equipment erosion or corrosion products (Fe, Cr, Mn, and Cu com-
pounds). There are no independent Shawnee data at this time to
support the hypothesis of oxidation catalysis.
3.1.2 Reactions in the Hold Tank
The primary chemical reactions that occur in the hold tank are:
0 Dissolution of lime
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• Neutralization of the bisulfite species
t Oxidation of sulfite species
• Precipitation of reaction products
Dissolution of lime (Equation 5, Table 3-1) under normal operating conditions
goes to nearly 100 percent completion in the hold tank. The dissolved lime
raises the liquor pH, increases the Ca++ concentration, and converts the
bisulfite (HSO^) to sulfite (S0§) (Equation 6, Table 3-1). A certain
amount of sulfite (SOg) is oxidized to sulfate ($04) (Equation 7, Table
3-1), owing to dissolved air from the scrubber and air entrained in the hold
tank.
Because calcium sulfite (CaS03) is sparingly soluble, it precipitates
(Equation 8, Table 3-1). A small amount of calcium sulfate (CaS04) is
included as a solid solution with the sulfite precipitate. Up to about 12
to 15 mole percent sulfate can be included in the sulfite solid solution.
Thus, if sulfite oxidation in the scrubber system is limited to less than
12 to 15 percent (Reference 11), the scrubber liquor will be unsaturated
in sulfate and the system will operate free of gypsum (CaSO^'ZHgO) preci-
pitation and scaling. This mode of operation has been frequently observed
at Shawnee and at the EPA-IERL pilot plant (References 3 and 12).
If sulfite oxidation is greater than 12 to 15 percent, the excess sulfate
will precipitate as gypsum (CaS04*2H20) (Equation 9, Table 3-1). Calcium
sulfate has a tendency to supersaturate in the scrubber liquor and to
precipitate as hard scale on scrubber surfaces. As a practical matter, if
gypsum saturation is limited throughout the scrubber system to less than
about 135 percent, gypsum crystals will not form on scrubber surfaces, and
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hence, there will be no gypsum scaling (References 1 and 12). Furthermore,
at least about 3 percent gypsum solids by weight in the slurry will provide
sufficient gypsum crystallization sites to prevent supersaturation and
scaling.
Calcium carbonate (CaCC^) also precipitates in the hold tank as a result of
bicarbonate ion (HCO^) reacting with hydroxide (OH~). Although some of the
CaCC>3 redissolves in the scrubber, it is the main solid waste product that
limits lime utilization in the system. In addition, there is a small amount
of "dead burned" lime in the system that has limited reactivity and becomes
part of the waste product solids. "Dead burned" lime results primarily from
overheating due to temperature control limitations inherent in the calcining
process by which quick lime is made.
3.2 FACTORS AFFECTING LIME SCRUBBING
The quantitative effects of operating conditions on S02 removal are presented
in Section 7. This section will focus on the qualitative factors affecting
reliable, scale-free scrubber operation.
3.2.1 Operating pH
At Shawnee the scrubber inlet pH is normally set between 7 and 8 when operating
with lime. The critical factor is to maintain scrubber inlet pH below
about 9 to prevent carbonate scaling and scrubber outlet pH below about
5.5 to prevent sulfite scaling (Reference 5, Section 7.2).
3-7
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If the scrubber inlet pH is allowed to exceed 9, sufficient C02 from the
flue gas will dissolve to react with Ca(OH)2 in the slurry and precipitate
carbonate scale.
Normally in lime scrubbing, calcium sulfite dissolves in the scrubber to re-
plenish the sulfite ion that reacts with S02 to form soluble bisulfite
(Equation 2, Table 3-1). However, it has been found at Shawnee that at a
scrubber outlet pH above about 5.5, the calcium sulfite will precipitate in
the bottom of the scrubber and form scale. Presumably, under scaling condi-
tions, excess lime [Ca(OH)2] dissolves faster than sulfite is reacted causing
the calcium ion concentration to increase and calcium sulfite to precipitate.
Thus, if sulfite scaling is observed in a lime scrubber, it can be reduced or
eliminated entirely by reducing the scrubber inlet pH. For a given scrubber
in lime service, an operating pH should be chosen that is sufficiently high
for good removal but sufficiently low to prevent sulfite and carbonate scaling.
At Shawnee this pH has been in the range of 7 to 8 at the scrubber inlet.
3.2.2 Alkali Utilization
Lime systems inherently operate at high alkali utilization (moles S02 absorbed
per mole of Ca added). Typically at Shawnee, alkali utilization ranges about
90 to 95 percent. Any attempt to improve S02 removal by increasing lime rate
(thus decreasing utilization) would result in higher pH and scaling as
described above.
3.2.3 Recirculated Slurry Solids Concentration
The recirculated slurry must have sufficient solids to provide adequate surface
3-8
-------
area for alkali dissolution and to provide crystal sites for product preci-
pitation. Additionally, a smaller filter or centrifuge is required when
operating at higher solids concentration. On the other hand, high solids
concentrations contribute to equipment erosion and to system fouling
(especially of the mist eliminator).
The normal mode of operation with lime slurry at Shawnee is at 15 weight
percent slurry solids when operating with high fly ash loading and at 8
weight percent solids with low fly ash loading. As the fly ash constituted
about 40 weight percent of the slurry solids, the concentration of calcium
based solids was about the same in both cases. These concentrations repre-
sented a compromise among the factors listed above.
In a few runs the slurry solids concentration was dropped to only 4 percent
with low fly ash loading (Reference 4, Section 7.2). Test results were
essentially the same. However, slight scaling of the scrubber internals
resulted with the 4 percent slurry. Other tests (Reference 5, Section 7.2)
indicated that slurry solids below about 7 percent (low fly ash loading)
caused scaling and a drop in S0£ removal. Thus, a minimum of about 7 percent
slurry solids concentration, exclusive of fly ash, is recommended.
3.2.4 Effluent Hold Tank Residence Time
A majority of the lime scrubbing runs at Shawnee were made at 12 to 17 minute
effluent hold tank residence times. However, satisfactory runs (Reference 4,
Section 7.2) were made at a residence time as low as 3 minutes. Only one
combination, 3 minutes residence time and 4 percent slurry solids concen-
tration (low fly ash loading), resulted in some scaling. At 8 percent slurry
solids no scaling was observed.
3-9
-------
As noted earlier, lime reacts with the effluent slurry in the hold tank to
precipitate a sulfite/sulfate product. Residence time is considered satis-
factory as long as precipitation is essentially complete in the hold tank.
In the Shawnee configuration with 8 percent slurry solids concentration,
3 minutes was found to be adequate.
3.2.5 Liquid-to-Gas Ratio
the relationship of liquid-to-gas ratio to scaling tendencies is manifested
by its effect on effluent pH. At very low liquid-to-gas ratio a low
effluent pH could encourage sulfite oxidation and thereby promote gypsum
scaling. Low pH, however, should not affect sulfite scaling.
The quantitative relationships between liquid-to-gas ratio and S02 removal
efficiency for the two types of scrubbers operated at Shawnee are summarized
in Section 7.
3.2.6 Effect of Chloride on pH and SQ2 Removal
Chloride exists in coal and is introduced as HC1 with flue gas into the
scrubber where it is absorbed by the scrubber liquor. Chloride concentration
in the liquor is dependent on its content in coal and the scrubber liquor
loop closure.
At a constant stoichiometric ratio (i.e., constant moles of lime added per
mole of S02 absorbed), increasing the chloride concentration reduces the
equilibrium pH and the liquor alkalinity. As the Cl" concentration increases,
the Ca++ concentration increases to maintain ion balance. The Ca"1"1" concen-
tration is also related to the C0| concentration by the solubility product
3-10
-------
equation:
(Ca++) (COj) = KCaC03 = constant (3-2)
The COg concentration, in turn, is related to the H* concentration (at
constant C02 and S02 partial pressures) as follows:
(H+)2(COo) = K x p = constant (3-3)
H2C03 C02
Thus, as Ca++ concentration increases, C03 concentration decreases (to keep
their product constant). The H+ concentration must then increase (or alter-
nately, the pH must decrease) in accordance with Equation 3-3.
To raise the pH again to a point at which it would be without the chloride,
more lime is required. Thus, at a constant scrubber inlet liquor pH, S02 re-
moval should increase with increasing chloride concentration. This increased
S02 removal is not a direct result of the presence of Cl~, but rather is a
result of the higher lime stoichiometry required in the presence of chloride
to maintain a constant pH.
3.2.7 Saturations and Scaling in Lime Wet Scrubbing Systems
As previously mentioned, if the saturation level of gypsum in the scrubber
slurry liquor exceeds about 135 percent, calcium sulfate will precipitate in
the scrubber as hard scale. Results from the lime tests indicated that the
gypsum saturation level can be reduced by:
• Increasing percent solids recirculated
t Increasing effluent residence time
3-11
-------
t Increasing liquid-to-gas ratio and
• Decreasing flue gas inlet SC^ concentration (S02 absorption rate)
It was also noted that lime addition to the scrubber downcomer, instead of
the effluent hold tank, substantially reduces the gypsum saturation. This
effect is due to the high calcium sulfite precipitation rate in the downcomer
where lime is added, which tends to pre-emt sulfite oxidation. This latter
innovation allows for operation at reduced percent solids recirculated and/or
residence time.
3.2.8 Effect of Fly Ash
Tests were made at Shawnee with both high fly ash loading (3-6 gr/dry scf
in the flue gas) and low fly ash loading (0.04 - 0.20 gr/dry scf). The
presence of fly ash in scrubber slurry has both process and mechanical
implications. Observed process effects due to fly ash were:
• At a controlled scrubber inlet pH of 8, lime utilization
for the tests with low fly ash loading averaged about
93 percent, compared with about 88 percent for runs made
with high fly ash loading under similar test conditions.*
• The filter cake solids contents from the low fly ash loading
runs were 5 to 10 weight percentage points lower than those
from the corresponding runs with high fly ash loading.
t The total dissolved solids concentrations, particularly
chloride species, were higher for the low fly ash loading
runs than for the runs with high fly ash loading because of
the tighter water balance resulting from the reduced waste
solids discharge.
*This difference was believed to be caused by the acidic fly ash (verified by
the laboratory pH measurement of fly ash/water slurry) which releases its
acidity from absorbed $03 under scrubber conditions, even though the fly ash
pond liquor at Shawnee is alkaline after a prolonged period of leaching.
3-12
-------
• Reduced waste solids discharge Implies reduced makeup water
requirements. This effect could be detrimental if the
quantity of makeup water is limited to that below the
minimum required for mist eliminator flush (see Sections
10 and 11).
Mechanical effects relate to the detrimental abrasion and/or erosion effects
of fly ash. An illustration of this effect is provided by a comparison of the
spray tower nozzle wear rate in high and low fly ash loading operation. Eight
Bete stainless steel nozzles (No. TF48FCN) were tested for 1565 hours on lime
slurry with low fly ash loading. During the testing period, the average flow
rate per nozzle was 45 gpm at a 10 psi pressure drop. Most of the operation,
approximately 1200 hours, was with 8 percent solids slurry. The remainder
was with 4 percent solids slurry. During the testing individual nozzles lost
from 0.93 to 2.43 percent of their initial weight because of erosion (about
1 percent per 1000 hours).
Earlier testing of these nozzles, before the Advanced Test Program, with lime
and limestone slurries containing high fly ash loadings had resulted in an
average weight loss of approximately 28 percent in 4320 hours (about 6 per-
cent per 1000 hours). This was a considerably higher erosion rate than
observed in operation with slurry having low fly ash loading. The average
flow rate per nozzle was also 45 gpm at a 10 psi pressure drop during the
tests with high fly ash loading.
3.3 CONTROL OF LIME SYSTEMS
Two of the major parameters affecting the S0£ removal efficiency and the
reliable, scale-free operation of lime scrubbing systems are the pH and the
weight percent solids concentration of the recirculating slurry.
3-13
-------
Control of the scrubber inlet pH is easily achieved by regulating the quan-
tity of lime added to the effluent hold tank or scrubber downcomer. In
practice, this operation is readily automated by coupling the pH signal to
the lime addition pump drive. The pH level is chosen to maximize SC^ removal
while minimizing lime usage, carbonate scaling at the scrubber inlet, and
sulfite scaling at the scrubber outlet.
Control of the recirculated solids concentration is achieved by regulating
the bleed flow rate from the effluent hold tank to the dewatering area. The
magnitude of the bleed flow rate is adjusted periodically following compar-
ison of the desired solids concentration with the actual value. At Shawnee,
slurry solids concentration is monitored continuously via Ohmart radiation
density meters and Dynatrol U-tube density meters, and periodically via slurry
filtration and drying techniques. A constant liquid level in the effluent
hold tank is achieved by balancing the bleed flow rate with the feed forward
flow rate of clarified liquor from the dewatering area.
Overall system levels are maintained by matching the water outputs through
flue gas humidification, entrainment and wet waste solids with water inputs
through alkali makeup, mist eliminator flush water, pump seal water and any
other additional makeup water.
Operating experience with lime wet scrubbing systems has identified sequences
of operation that permit reliable system startup and shutdown. A primary
consideration during initial startup is the quantity of fresh lime in the
system. The amount of lime should be adequate to avoid a precipitous drop
in slurry pH when initial contact with S02 bearing flue gas is made. At
the same time, an excess of lime at startup is undesirable because of the
3-14
-------
possibility of scaling at high dissolved calcium concentrations. Consid-
erations relating to shutdown are primarily mechanical and are more critical
during the winter months. Pertinent precautions include: draining and
flushing the valves, pumps, sensing elements and piping to avoid freeze
damage; removing in-line pH sensing elements; continuing agitation in slurry
hold tanks to prevent settling; and putting the clarifier/thickener under-
flow on recycle to prevent line pluggage, preferably using a pump that does
not require seal water (such as a Moyno pump).
A thorough study of the response of lime wet scrubbing systems to abrupt
changes in gas flow rate (liquid-to-gas ratio) and inlet S02 concentration
level was made during two separate testing blocks. The first block was
operated with natural oxidation and the second with forced oxidation. During
the 1143 hour natural oxidation test block (Reference 3, Section 6), the
gas flow rate was varied between 17,000 and 35,000 acfm (at 300°F) while the
inlet S02 concentration ranged from 1500 to 4400 ppm. No problems due to
the cycling gas rate and gas composition* were encountered. The condition
of the mist eliminator remained almost unchanged, with a 2 percent restriction
of the total cross-sectional area by dust-like solids at the conclusion of
test block.
During the 779 hour two-loop forced-oxidation test block (Reference 5, Section
7.2.11), the gas flow rate was varied between 18,000 and 35,000 acfm (at SOOT)
while the inlet S02 concentration ranged from 2300 to 3600 ppm. Again, no
equipment problems due to cycling gas rate and gas composition were encountered.
*It should be noted that with the boiler operating philosophy at Shawnee,
significant increase in flue gas oxygen concentration accompanies operation
at low boiler load.
3-15
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Average S02 removal for the entire block was 88 percent at 2950 ppm average
inlet S02 concentration. This corresponds to an average emission 0.9 Ib
S02/MM Btu.
3-16
-------
Section 4
LIMESTONE SCRUBBING
Limestone is a naturally occuring mineral consisting primarily of calcium
carbonate. It is normally delivered to Shawnee from the Fredonia Quarries
in Kentucky in the form of crushed stones averaging about 1-1/2 inches in
size. The crushed stones are dried and ground to about 95 percent less than
325 mesh in a dry ball mill remaining from an earlier EPA-sponsored dry-
limestone injection program. The stones normally contain 97 weight percent
CaC03» 1 weight percent MgCC^, and 2 weight percent inerts.
In this section a simplified description of limestone scrubbing chemistry
is presented, followed by a discussion of operating conditions and control
procedures.
The chemistry described was compiled from several sources and is not wholly
based on results at the Shawnee Test Facility. Documentation of sources is
given where possible. Details of the chemistry presented are based on inter-
pretation of observations to date and are subject to modification as more
information becomes available.
4-1
-------
4.1
CHEMISTRY OF LIMESTONE SCRUBBING
The overall reaction of limestone with S02 may be represented by:
CaC03 + S02
CaS03 + C02
(4-1)
One mole of limestone reacts with one mole of S02 to produce one mole
of calcium sulfite and one mole of carbon dioxide. Like lime scrubbing,
the chemistry of limestone scrubbing is also complex.
Table 4-1 contains equations that represent the major chemical reactions
that occur during wet scrubbing of S02 with limestone slurries under
normal operating conditions. These conditions are:
Absorbent slurry liquor pH
Stoichiometric ratio
(moles of limestone
added per mole
of S02 absorbed)
= between 5.0 and 6.0 at the
scrubber inlet and between
4.5 and 5.5 at the scrubber
outlet
= 1.1 to 1.6
These equations are not meant to be all inclusive, for the same reasons
discussed in Section 3.1.
4.1.1 Reactions in the Scrubber
S02 reacts with limestone in the scrubber to produce Ca"1"1" and HSO^ in the
liquor, and to precipitate calcium sulfite. As in lime scrubbing, most sulfite
oxidation probably occurs in the scrubber. Unlike lime scrubbing, in limestone
scrubbing there is considerable carbon dioxide desorption in the scrubber (as
well as in the hold tank).
4-2
-------
Table 4-1
MAJOR CHEMICAL REACTIONS INVOLVED IN LIMESTONE
SCRUBBING OF SO.,
Reactions in the Absorber
Absorption
SO2 (gas) »* SO2 (aqueous) (1)
CO2 (gas) ** CO2 (aqueous) ** H2CO3 (2)
Desorption
HCO3 -I- SO2 (aqueous) + H2O *=s H2CO 3 -r HSOj (3)
H2CO3s± CO2 (gas) + H2O (4)
N eu trail zation
+ SO2 (aqueous) + H2O 5* H2CO3+ HSG>3 ( 5)
SO3 + SO2 (aqueous) + H2O 5* ZHSO^ ( 6)
(solid) + 2SO2 (aqueous) + 2H2O ;* Ca++ + 2HSO5 + H2CO3 (7)
Oxidation
HS03+ 1/2025* S04+ H+ (8)
Precipitation
Ca++ + (l-x)SOl + xS04+ 1/ZHaO s± Ca(SO3) l _X(SO4)X- 1 /2 H2D(solid) (9)
Reactions in the Hold Tank
Dissolution and Deeorption
CaCO3 (solid) + HSO§ 5^ Ca + SO3 + HCO§ (10)
HCO5 + HSO3 5* H2CO3 + 803 (11)
H2CO3 *t CO2 (aqueous) 5* CO 2 (gas) (12)
Oxidation
Precipitation
HSOj + 1/2O2 »* S04 -I-H+ (13)
++ =
Ca 4- SO4 + 2H2O *i CaSO4. 2HzO (solid) (14)
+ (l-x)SO3 + (x)SO4 + 1/2H2O 5* Ca(SO3) l-x (SO4)X-1 /2H2O (solid) (15)
4-3
-------
4.1.2 Reactions in the Hold Tank
Limestone also dissolves in the hold tank, causing calcium sulfite to
precipitate. Gypsum precipitates in the hold tank as calcium sulfite/
sulfate solid solution and also as a separate phase if the gypsum satura-
tion is greater than 100 percent (Reference 13). Note that both calcium
sulfite and gypsum have a strong tendency to become supersaturated in
liquor without precipitation.
4.1.3 Reactions at High Stoichiometry
Stoichiometry is an important controllable variable in limestone scrubbing
of S02. At high Stoichiometry, where the moles of CaC03 added per mole of
S02 absorbed is greater than about 1.3, CaC03 dissolution occurs primarily
in the scrubber (Equation 7, Table 4-1 and Reference 8). For every mole
of S02 absorbed, 1/2 mole of Ca++ can precipitate in the hold tank or in
the scrubber as CaS03 (as a solid solution with calcium sulfate) or CaSO^
4.1.4 Reactions at Low Stoichiometry
At low Stoichiometry, (where the moles of CaC03 added per mole of S02
absorbed are less than or equal to 1.1), CaS03 dissolution in the scrubber
may occur, as in the lime system, and contribute to S02 removal. The
equation is (Reference 8):
CaS03 + S02 + H20 «=± Ca++ + 2HS03 (4-2)
According to Equation 4-2, twice as much Ca*"1" is released per mole of S02
absorbed by the reaction of S02 with CaS03 than by the comparable bisulfite
4-4
-------
producing reaction of S02 with CaC03 (Equation 7, Table 4-1). Therefore,
slurry leaving the scrubber will have more dissolved Ca++ in it at low
stoichiometry than at high stoichiometry, as long as Ca++ precipitation
in the absorber as gypsum does not occur fast*enough to reduce the Ca++
concentration to its equilibrium value.
4.2 FACTORS AFFECTING LIMESTONE SCRUBBING
The quantitative effects of operating conditions on S02 removal are
presented in Section 7. This section discusses the qualitative factors
influencing reliable, scale-free scrubber operation.
4.2.1 Operating pH
At Shawnee the scrubber inlet pH is normally set between 4.5 and 6.0
when operating with limestone. The critical factor is to control scrubber
inlet pH below about 6 to prevent carbonate deposition at the inlet. Also,
the scrubber outlet pH was controlled above about 4.0 to prevent sulfite
blinding of limestone and to mitigate downcomer corrosion.
In limestone scrubbing, if the scrubber inlet pH is allowed to exceed 6,
the excess limestone deposits as soft scale at the scrubber inlet. Addi-
tionally, a scrubber outlet pH above 5.5 may cause sulfite scaling at the
scrubber outlet, depending on the S02 make-per-pass. Presumably, for an
outlet pH above 5.5, excess limestone dissolves faster than calcium sulfite
is reacted (Equations 6 and 7, Table 4-1), causing the calcium ion concen-
tration to increase and calcium sulfite to precipitate.
4-5
-------
Normally in limestone scrubbing, calcium carbonate dissolves in the scrub-
ber to produce the bicarbonate ion that reacts with SC^ to form soluble
bisulfite and evolve C02 (Equations 3 and 4, Table 4-1). However, it has
been observed at Shawnee that at a scrubber outlet pH below about 4.0, the
bisulfite ions may coat (blind) the fresh limestone particles and thereby
reduce their utilization.
Thus, reliable operation of a limestone scrubber can be obtained by main-
taining the scrubber outlet pH between 4.0 and 5.5. For a given scrubber
in limestone service, an inlet pH should be chosen that is sufficiently
high for good S0£ removal but adequately balanced at the outlet to prevent
sulfite scaling and limestone blinding. At Shawnee this inlet pH has been
in the range of 4.5 to 6.0.
4.2.2 Alkali Utilization
Extensive testing indicated an increase in limestone utilization with
increasing hold tank residence time, greater number of hold tanks, and
decreasing scrubber inlet pH. At Shawnee limestone utilization normally
varied from about 60 percent at a scrubber inlet liquor pH of 6.0 to about
95 percent at a scrubber inlet liquor pH of 5.2. Operation at reduced
scrubber inlet liquor pH, however, caused a reduction in SOo removal effi-
ciency when other test conditions were held constant.
4.2.3 Recirculated Slurry Solids Concentration
The recirculated slurry must have sufficient solids to provide adequate
surface area for alkali dissolution and to provide crystal sites for product
4-6
-------
precipitation. Also, a smaller filter or centrifuge is required when opera-
ting at higher solids concentration. On the other hand, high solids con-
centrations contribute to equipment erosion and to fouling of the system
(especially of the mist eliminator).
The normal mode of operation with limestone slurry at Shawnee was at 15
weight percent slurry solids when operating with high fly ash loading and
at 8 weight percent solids with low fly ash loading. Because the fly ash
constituted about 40 weight percent of the slurry solids, the concentration
of calcium based solids was about the same in both cases. These concen-
trations represented a compromise among the factors listed above.
As with lime scrubbing, scaling in the limestone scrubber occurred at slurry
solids concentrations below about 7 percent, exclusive of fly ash. Further-
more, a significant drop in S02 removal was experienced at slurry solids
concentrations below this level. This latter effect was much stronger for
limestone scrubbing than for lime scrubbing.
4.2.4 Effect of Forced Oxidation*
Because CaS03 dissolution can be an important scrubbing mechanism at low
stoichiometry in the limestone system (and at normal stoichiometry in the
lime system), forced oxidation in the hold tank of CaS03 to CaS04, which
eliminates this scrubbing mechanism, could result in low S02 removal effi-
ciencies. Forced oxidation has been investigated at the EPA-IERL pilot
plant. Preliminary results indicate that C0 stripping caused by the air
* Forced oxidation represents any means external to the scrubber by
which essentially all of the CaS03 is oxidized to gypsum.
4-7
-------
sparging enhances limestone dissolution, and hence nullifies any possible
adverse effects on S02 removal caused by forced oxidation.
4.2.5 Effect of Fly Ash
At the same limestone utilization, the scrubber inlet pH for runs with
low fly ash loading tended to be 0.3 to 0.4 pH unit higher than for runs
with high fly ash loading. This is similar to the observations made during
lime tests with a controlled scrubber inlet pH of 8, in which lime utili-
zation averaged about 93 percent for runs with low fly ash loading, compared
with abouut 88 percent for runs with high fly ash loading (Section 3.2.8).
Effects on total dissolved solids concentration, water balance, along with
the mechanically induced results of abrasion and/or erosion are similar to
those for lime systems (see Section 3.2.8).
4.2.6 Effect of Hold Tank Residence Time and Configuration
Unlike lime scrubbing systems where approximately 3 minutes of residence
time was found adequate with a single tank configuration, limestone scrub-
bing systems require about 5 minutes residence time. Greater residence
time is required because of the lower limestone equilibrium solubility and
slow dissolution rate. However, the total residence time can be reduced
by use of a plug flow hold tank reactor. Kinetic theory shows that for a
continuous system where the reaction order is greater than zero, raw mate-
rials are more completely converted in plug flow than in a backmix reactor
with the same residence time. This concept for improving limestone utili-
zation was successfully tested at the EPA-IERL pilot plant and the Shawnee
4-8
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Test Facility (References 3 and 8). Hold tank configurations tested and
the results obtained are described in Section 4.3.
4.3 LIMESTONE UTILIZATION AS A FUNCTION OF SCRUBBER INLET pH
Tests were conducted primarily to correlate stoichiometric ratio (the
reciprocal of alkali utilization) with scrubber inlet liquor pH, effluent
hold tank residence time, and hold tank design (Reference 3). Hold tank
configurations tested included a single backmix hold tank and three backmix
hold tanks in series (to simulate a plug flow reactor). No attempt was made
to account for secondary variables such as chloride concentration in the
slurry liquor, which ranged from 1500 to 6500 ppm during testing. Models
that take such secondary variables into consideration are described in
Section 7.
For each combination of hold tank residence time and hold tank design,
tests were conducted to cover a range of values of scrubber slurry liquor
pH. Normally the systems were run for about 4 to 5 days at a specified
level of pH. During testing, the stoichiometric ratios were determined
every 4 hours from solids analyses of the scrubber recirculation slurry.
Data showing the relationship between stoichiometric ratio and scrubber in-
let liquor pH for the venturi/spray tower system are plotted in Figures 4-1,
4-2, and 4-3 for residence times of 20, 12, and 6 minutes, respectively.
The stoichiometric ratio/pH relationship was best defined for the 12 minutes
residence time tests. As expected, scatter in the data was greatest at 6
minutes residence time, where pH recovery time was limited and small varia-
4-9
-------
1.8
—r~
a
1.7 • •
1.6 • •
CN
03
1.5 • •
1.4 • •
<3
«
ac
u
£
1.2 +
a
I
1.1 • •
VENTURI/SPRAY TOWER SYSTEM
SINGLE HOLD TANK
20 MINUTES RESIDENCE TIME
O RUN 701 - 1A
D RUN 702 - 1A
A RUN 703 - 1A
7 RUN 704 - 1A
O RUN 705 - 1A
A. AY
1.0 •
4.8
5.0
5.2 5.4 5.6
SCRUBBER INLET LIQUOR pH
5.8
6.0
6.2
Figure 4-1. Stoichiometric Ratio versus Scrubber Inlet Liquor
pH in the Venturi/Spray Tower System with a Single
Hold Tank at 20 minutes Residence Time
4-10
-------
1.8
1.7- •
1.6 • •
N
8
3
1
2 1.34
cc
o
c
Ul
i 1.2
I
1.1 • •
VENTURI/SPRAY TOWER SYSTEM
SINGLE HOLD TANK
12 MINUTES RESIDENCE TIME
O RUN 706 -1A
RUN 707 - 1A
RUN 708-1A
RUN 709 -1A
RUN 710-1A
D
A
1.0"
+
4.8
5.0
5.2 5.4 5.6
SCRUBBER INLET LIQUOR pH
5.8
6.0
6.2
Figure 4-2. Stoichiometric Ratio versus Scrubber Inlet Slurry
pH in the Venturi/Spray Tower System with a Single
Hold Tank at 12 minutes Residence Time
-------
1.8
1.7- -
1.6
1
«N
8
1.5- •
1.4- •
<3
O
K 1.3 +
<
ec
o
E
..2 +
O
I
1.1-
1.0-•
VENTURI/SPRAY TOWER SYSTEM
SINGLE HOLD TANK
6 MINUTES RESIDENCE TIME
O RUN 711 - 1A
D RUN 711-1B
A RUN 712-1A
V RUN 713-1A
A
A
,° 2
O
4.8
5.0
5.2 5.4 5.6
SCRUBBER INLET LIQUOR pH
5.8
6.0
Figure 4-3.
Stoichiometric Ratio versus Scrubber Inlet Liquor
pH in the Venturi/Spray Tower System with a Single
Hold Tank at 6 minutes Residence Time
6.2
4-12
-------
tlons in tank level resulted in significant changes in residence time. At
20 minutes residence time only a limited number of data were obtained at
higher pH values.
Sight-average curves drawn through the data in Figures 4-1 through 4-3 are
compared in Figure 4-4. In Figure 4-4 a tendency for lower stoichiometric
ratio at a given pH can be seen as residence time increases. However,
above a pH of 5.8 the sight-average curve for 20 minutes residence time
fell between 6 and 12 minutes. This inconsistency is indicative of the
broad scatter of the data.
In the TCA system, hold tank configurations tested included: (i) single
hold tank at 12 minutes residence time; (ii) three hold tanks in series
at 14.4 minutes total residence time (5.2, 2.6 and 6.6 minutes, respectively);
and (iii) three hold tanks in series at 10.8 minutes total residence time
(4.6, 2.3, and 3.9 minutes, respectively).
Results of the utilization testing for these three configurations are
plotted as stoichiometric ratio versus inlet liquor pH in Figures 4-5,
4-6, and 4-7, respectively. Sight-drawn averages from Figures 4-5 through
4-7 are compared in Figure 4-8. For the runs with three tanks in series,
there was no significant difference between 10.8 minutes and 14.4 minutes
residence time. However, there was a distinct difference between operation
with a single tank and that with three tanks in series at pH values greater
than about 5.0. For example, at a scrubber inlet liquor pH of 5.6, the
stoichiometric ratio averaged 1.19 with a single hold tank as compared
with 1.11 with three tanks in series. The latter is a 7 percent improve-
ment in limestone utilization. At higher pH the improvement was greater;
e.g., at pH 5.8, the improvement in utilization was 14 percent.
4-13
-------
1.8
1.7 •
1.6 ••
1.5 • •
-------
1.8
1.7 • •
1.6 ••
1.5
CM
8
3
tr
o
E
UJ
I 1.2
O
1.1 • •
TCA SYSTEM
SINGLE HOLD TANK
12 MINUTES RESIDENCE TIME
O RUN 562-2A
RUN 562 -2B
RUN 563-2A
RUN 564-2A
RUN 581 - 2A
D
A
V
O
1.0 ••
+
+
4.8
5.0
5.2 5.4 5.6
SCRUBBER INLET LIQUOR pH
5.8
6.0
6.2
Figure 4-5. Stoichiometric Ratio versus Scrubber Inlet Liquor pH
in the TCA System with a Single Hold Tank at 12 minutes
Residence Time
4-15
-------
1.8 T
1.7 • •
1.6 ••
1
-------
1.8
1.7 -
1.6-
N
1.5 •
<3
E
g 1.3
cc
o
E
UJ
1.2
u
5
1.1 • •
1.0
4.8
TCA SYSTEM
THREE HOLD TANKS IN SERIES
10.8 MINUTES RESIDENCE TIME
O RUN 569-2A
D RUN 569-2B
A RUN 570-2A
V RUN 571-2A
O RUN 572-2A
O RUN 579-2A
5.0
5.2 5.4 5.6
SCRUBBER INLET LIQUOR pH
5.8
6.0
6.2
Figure 4-7. Stoichiometric Ratio versus Scrubber Inlet Liquor pH
in the TCA System with Three Hold Tanks in Series
at 10.8 minutes Residence Time
4-17
-------
1.8
1.7 ••
1.6 -•
1" 1.5 - -
CM
8
£
1.4 -.
1.3 --
u
E 1.2 +
UJ
u
I t.4
TCA SYSTEM
1 TANK, 12 minutes
3 TANKS, 10.8 minutes
3 TANKS, 14.4 minutes
1.0 - •
4.8
5.0
5.2 5.4 5.6
SCRUBBER INLET LIQUOR pH
5.8
6.0
Figure 4-8. The Effect of Scrubber Inlet Liquor pH and Hold
Tank Configuration on Stoichiometric Ratio in the
TCA System
6.2
4-18
-------
4.4 LIMESTONE TYPE AND GRIND TEST RESULTS
Six tests were conducted at Shawnee to investigate the effect of limestone
type and grind on system performance (Reference 5, Section 10). System
performance was evaluated in terms of S®2 removal and scrubber inlet
slurry pH at a controlled stoichiometric ratio of 1.2 moles Ca/mole S02
removed. Limestone type, limestone grind, effluent hold tank (EHT)
residence time, and effluent hold tank configuration were varied.
The levels of independent variables evaluated were:
• Limestone grind (Table 4-2) - fine (96 percent less than
325 mesh) versus coarse (65 to 69 percent less than 325
mesh)
• Limestone type - Fredonia White versus Longview, Alabama
• Effluent hold tank residence time - 4.1 minutes versus
12 minutes
• Effluent hold tank configuration - single tank versus
3 tanks in series
A summary of the pertinent results and the major test conditions is presented
in Table 4-3. For the variables evaluated in this test series, the fineness
of grind had the greatest effect on S02 removal efficiency. Effluent hold
tank residence time, limestone type, and effluent held tank configuration
all had lesser effects.
A more extensive limestone type and grind testing program is currently
scheduled in the Shawnee Advanced Program.
4-19
-------
Table 4-2
ANALYSES OF LIMESTONES USED IN THE TEST SERIES
Bahco Analysis Fredom'a Fine Fredonia Coarse Longview Coarse
Micron Size % Less Than % Less Than % Less Than
3 39.5 21.1 16.1
6 57.9 33.4 26.8
9 67.8 38.4 34.4
12 73.8 43.6 40.0
16.5 80.0 49.4 47.0
22 84.7 54.8 48.0
27 87.6 58.6 57.4
30 88.9 60.4 59.2
Screen Analysis
Mesh Size % Less Than % Less Than % Less Than
400 93.1 64.6 61.7
325 95.9 69.1 64.8
200 99.3 80.8 74.6
100 99.4 81.0 74.8
50 100.0 99.9 99.3
30 100.0 100.0 100.0
Number of Samples 262
Chemical Analysis
CaO
MgO
C02
Acid insolubles
Number of Samples
54.14%
0.48
39.56
2.18
6
53.18%
0.74
39.54
2.27
11
54.23%
0.66
39.99
1.27
4
4-20
-------
Table 4-3
SUMMARY OF TCA LIMESTONE TYPE AND GRIND TESTS
(With high fly ash loading, no MgO addition)
Major Test Condi tions'1^
Limestone type
Average grind, wtZ <325 mesh
Gas rate, acfm @ 300°F
Liquor rate, gpm
Percent solids recirculated
Effluent residence time, min.
Limestone stoichiometric ratio (controlled)
Selected Results
Scrubber inlet pH
Stoichioraetric ratio
Percent SO- removal
Inlet SOy concentration, ppm
SOo make-per-pass, m-mol/liter
Inlet liquor % gypsum saturation @ 50°C
Percent sulfite oxidation
Onstream hours
707-2A
Fredonia
96
30,000
1200
15
4.1
1.2
5.6
1.23
72
3100
11.5
100
17
113
708- 2A
Fredonia
69
30,000
1200
15
4.1
1.2
5.2
1.15
49
3100
8.0
115
14
128
709-2A
Longview
65
30,000
1200
15
4.1
1.2
5.3
1.18
55
3350
9.5
110
20
56<2)
710-2A
Fredonia
69
30,000
1200
15
12
1.2
5.4
1.21
54
3400
9.5
110
16
162
711-2A
Fredonia
96
30,000
1200
15
12
1.2
5.65
1.25
64
3250
11.0
80
15
93
712-2A
Fredonia
96
30,000
1200
15
12 (3 tanks)
1.2
5.85
1.21
69
3050
11.5
60
18
117
•F*
I
PO
Notes:
(1) Clarifier only used for solids dewatering in all runs.
(2) Run 709-2A was terminated prematurely due to severe limestone feed line plugging problems.
-------
4.5 LABORATORY LIMESTONE REACTIVITY TEST RESULTS
Laboratory tests of limestone reactivity were conducted at Shawnee to study
the effect of limestone source and grind on reactivity. Detailed results
of these tests have been reported earlier in Section 19 of Reference 5.
During this test series, limestones from eleven different quarries were
evaluated. Table 4-4 lists their chemical compositions and the degree of
grinding.
Two methods were used to determine reactivity:
(1) HC1 method - 5 grams of dried limestone powder were added
to an agitated 300 ml solution of HC1 at pH 3 and 25°C
and the rise of pH with time was recorded.
(2) S02 method - First 0.2 mole of limestone was dissolved
in two liters of distilled water at 50°C until a constant
pH was reached. Then a constant stream (0.273 g-mole/hr)
of pure SOp gas was bubbled through the slurry and the pH
drop with time was monitored.
As expected, for a given limestone the reactivity improved with increased
grinding. However, the relative benefits of grinding varied among the
limestones. In general, the denser (low porosity and/or small pore size)
the limestone, the stronger the dependence of reactivity on particle size
(grinding). Similar behavior was also observed during the limestone type
and grind tests at Shawnee (see Section 4.4).
Some conflicting results were obtained when comparing react ivies obtained
by the two methods. The S02 method, although somewhat more involved than
the HC1 method, was judged to be more appropriate for evaluating reactivity
because it more closely simulated the environment existing in S02 wet-
scrubbing processes.
4-22
-------
Table 4-4
LIMESTONES USED IN REACTIVITY TESTS
I
ro
CO
Limestone Source
Citadel Stone Company
Commonwealth Edison
Cowan Stone Company
Fredonia Quarries
Georgia Marble
Hoover Incorporated
Long view Lime Company
Luttrell Mining Company
Rigsby & Barnard Quarry
The Stone Man
Vulcan Material Company
Location
Selma, Alabama
Joliet, Illinois
Cowan, Tennessee
Fredonia, Kentucky
Sylacauga, Alabama
Nashville, Tennessee
Longview, Alabama
Knoxville, Tennessee
Cave In Rock, Illinois
Chattanooga, Tennessee
Knoxville, Tennessee
Chemical Composition, wt percent
Calcium
(Ca)
32.5
37.9
36. 0
35.8
38.8
36.6
38.2
38.8
38.4
36.4
38. 1
Magnesium
(Mg)
0.2
1.4
1. 5
2. 5
0.5
1.2
0. 7
0. 2
0. 2
1. 0
1. 1
Carbonate
(COj)
47.4
56.6
55.9
60.5
59.2
54. 1
59.9
58.4
57.8
57.2
60.2
Acid
Insolubles
14.8
3.5
4. 0
2.2
2.0
3.8
1.0
1.4
0.4
4. 1
0.5
Grind, percent less than
-200
Mesh
94
65
80
75
71
92
72
77
69
72
97
-325
Mesh
93
78
91
90
78
84
77
82
90
78
95
-------
Additional tests have been planned for both the EPA-IERL pilot plant and the
Shawnee Test Facility to study the relationships among the S02 removal, pH,
and stoichiometry for different limestone types and grinds.
4.6 AUTOMATIC LIMESTONE FEED CONTROL
The feasibility of automatic alkali -feed control in a limestone wet-scrubbing
system was investigated at Shawnee (Reference 5, Section 11). The incen-
tives for automatic limestone feed control were:
t Minimizing limestone required to meet an S02 emission
target of 1.2 Ibs/MM Btu
• Reducing manual operation and operator errors
• Improving scrubber reliability
The control scheme tested at Shawnee was based on the material balance
concept. In this scheme, a desired stoichiometric limestone feed was
maintained in relation to the amount of S02 entering or absorbed in the
scrubber according to the following equation:
Limestone (60 percent slurry) addition rate, gpm
= G x (S02I - Kout) x KSR
where: G = flue gas rate, acfm @ 300°F
S02I = inlet S02 concentration measured by Du Pont
analyzer, ppm
Kout = a manually adjustable constant related to desired
outlet S02 concentration, ppm
K$R = a manually adjustable constant proportional to
the stoichiometric ratio
= (unit conversion factor) x (stoichiometric ratio)
= 2.34 x 10"8 x (stoichiometric ratio)
4-24
-------
In practice, the gas rate, G, and inlet SC^ concentration, $02!, vary
within a wide range depending on the boiler load and the coal sulfur content.
Therefore, the control scheme included the following overrides:
• If the outlet S02 concentration exceeded a set maximum, the
limestone feed rate was stepped up to a preset maximum
• If the outlet SC^ concentration dropped below a set minumum,
the limestone feed rate was stepped down to a preset minum
The former provision minimized excursions beyond the S02 emission target,
while the latter effected limestone savings by limiting unnecessary SC^
removal.
The limited experience with this first-generation control design at Shawnee,
although favorable, revealed several areas for improvement. One specific
area that could be readily improved relates to the override control methods.
These resulted in either under-feeding or over-feeding of limestone with
resultant loss in scrubber performance and sometimes system scaling, respec-
tively. A proposed modification would add a proportioning device to regulate
the limestone feed rate, at the overriding conditions, in proportion to the
difference between the outlet S02 setpoint and the prevailing SO^ outlet
concentration.
4.7 CONTROL OF LIMESTONE SYSTEMS
As in the case of lime scrubbing systems, two of the major parameters in lime-
stone scrubbing are the concentrations of alkaline species in the scrubbing
liquor (indicated by the pH in lime systems) and the weight percent concentra-
tion of solids in the recirculated slurry.
4-25
-------
Unlike the lime systems, the pH of the recirculating slurry in limestone
systems is a poor indicator of the alkalinity level because, in the oper-
ating pH range of 5.5 to 6.0, the limestone slurry is highly buffered. A
more appropriate but harder to measure indicator is the stoichiometric ratio
of calcium to sulfur in the mixed reactant and product solids. In practice,
the stoichiometric ratio is controlled within narrow limits (see Section
4.6) with the pH used as the override because it is readily measured.
Unlike lime systems, the suspended limestone solids concentration in the
slurry has a significant effect on the pH and S02 removal because limestone
dissolves less readily than lime. This is especially true at slurry solids
concentrations below about 7 percent, excluding fly ash (see Section 4.2.3).
At a constant limestone addition rate lower slurry solids concentration
yields low pH because less limestone dissolution occurs per unit time.
Unlike the lime system, the limestone system is buffered, and thus its re-
sponse to abrupt changes in inlet S02 concentrations is sluggish. For example,
it is possible that, if the inlet SC^ concentration drops abruptly and signi-
ficantly, high stoichiometric ratios can result owing to the large inventory
of unused limestone in the system. This can result in severe scaling. Alter-
nately, a sudden and significant rise in inlet S02 concentration may result
in the degradation of S02 removal performance because of the lack of adequate
limestone capacity. Under these conditions, a significant drop in pH may
lead to bisulfite blinding (loss of reactivity) of the limestone particles,
if the operator response is slow in raising the limestone feed rate.
The control of recirculated solids concentration, tank levels and the startup
and shutdown considerations are similar to those for lime wet scrubbing
systems (see Section 3.3).
4-26
-------
A thorough study of the response of limestone wet scrubbing systems to
abrupt changes in gas flow rate (liquid-to-gas ratio) and inlet S0£ concen-
tration level was made during two separate testing blocks. The first block
was operated with natural oxidation and the second was conducted with two-
loop forced oxidation. During the 747-hour natural oxidation test block
(Reference 5, Section 13.3), the gas flow rate was varied between 20,000
and 30,000 acfm (at 300°F) and inlet S02 concentration ranged from 2200 to
3400 ppm. No problems due to the cycling gas rate and gas composition*
were encountered since these changes were mostly within the operator and
system response capabilities. The condition of the mist eliminator remained
unchanged, with a 1 percent restriction of the total cross-sectional area
by dust-like solids at the conclusion of test block. Some minor fall-out
solids from the outlet duct and reheater above were found on the mist
eliminator.
During the 840-hour two-loop forced-oxidation test block (Reference 5, Sec-
tion 5.2.13), the gas flow rate was varied between 18,000 and 35,000 acfm
(at 300°F) and inlet SOg concentration ranged from 2500 to 3400 ppm. Again,
no problems due to cycling gas rate and gas composition were encountered.
The actual average S02 emissions were about 1.1 and 1.0 Ib/MM Btu for the
forced and natural oxidation test blocks, respectively. Thus the average
S02 emissions for both were below the 30-day average of 1.2 Ib/MM Btu.
S02 emissions varied overall from 0.4 to 1.8 Ib/MM Btu. There were 10
periods greater than 24 hours during which the S02 emission exceeded 1.2
* It should be noted that with the boiler operating philosophy at Shawnee,
significant increase in flue gas oxygen concentration accompanies operation
at low boiler load.
4-27
-------
Ib/MM Btu: six during the forced oxidation run and four during the natural
oxidation run. There were about 25 other "spikes" lasting three hours or
longer and divided almost equally between the two testing blocks.
4-28
-------
Section 5
LIME/LIMESTONE SCRUBBING WITH MAGNESIUM ENHANCEMENT
In both lime and limestone wet scrubbing of S02, the concentration of dis-
solved species in the scrubber inlet liquor that can react with S02 in the flue
gas is very low, about 1-2 m-mole/1. This is well below the S02 make-per-pass,*
typically about 10 m-mole/1 for Shawnee. Therefore, the S02 absorption rate is
largely dependent upon the slow rate of limestone and CaS03 dissolution into
the liquor passing through the scrubber.
Addition of an appropriate soluble magnesium compound, such as reactive MgO
or MgSO^, to the scrubbing liquor increases the concentration of dissolved
o _
sulfite species, MgS03 and $03", thus making the S02 absorption rate more
dependent on the fast liquid-phase base-acid reactions of these sulfite
species with S02 (aq):
base + dibasic acid *- monobasic acid (5-1)
MgS03° + S02 (aq) + H20 *• 2HS03~ + Mg++ (5-2)
S03= + S02 (aq) + H20 • 2HS03" (5-3)
* Defined as milligram-moles of S02 absorbed from the flue gas per liter of
liquor as the recirculated slurry makes one pass through the scrubber.
5-1
-------
Conversion of S02 (aq) to HS03~ by the above reactions in the scrubber encourages
the absorption of more S02 (g) into the liquor as S02 (aq), thus increasing
S02 removal.
About 200-400 m-mole/1 (5000-10,000 ppm) of dissolved magnesium associated with
sulfite and sulfate (magnesium chloride, MgCl2» has little effect on S02 removal)
are required to provide a concentration of dissolved sulfite species equal to
the S02 make-per-pass. High S02 removal was generally achieved under this con-
dition for the Shawnee spray tower and TCA. The quantitative effect of magnesium
addition on 3^2 removal for these scrubbers with lime and limestone is discussed
in Section 7.
5.1 EFFECT OF MAGNESIUM ADDITIVE ON DISSOLVED SULFITE SPECIES
The concentration of dissolved sulfite species increases with magnesium
addition. Dissolution of MgO into a lime/limestone wet scrubbing liquor
provides Mg*4 ion, thus greatly increasing the total cation concentration
(dissolved calcium species are only about 20 m-mole/1 for calcium sulfite/
sulfate liquors). To maintain electroneutrality additional anions must go
into solution. Therefore the concentrations of dissolved S02 and sulfate
as ionic sulfite, bisulfite and sulfate (S03=, HS03", and S04=) increase
with increasing magnesium. The concentration of the ion pair of magnesium
and sulfite, MgS03°, which is the major dissolved sulfite species with
magnesium additive, also increases with both tig*4 and S03=. This increase
in dissolved sulfite species, S03= and MgS03°, which are basic to S02(aq),
increases S02 removal.*
* The concentration of CaS03°, which is also basic to (S02)aq, is
essentially constant for liquors saturated with calcium sulfite.
5-2
-------
5.2 IMPORTANCE OF CALCIUM SOLIDS EQUILIBRIA
The Importance of dissolved calcium is that the solubility products and
relative saturations of calcium sulfite (CaS03*l/2H20) and gypsum (CaS04*2H20)
determine the concentration ratio of sulfite ion to sulfate ion, [S03=]/[S04=],
in the scrubbing liquor. The ionic species in the liquor are related to the
solubility products and relative saturations by:
(Ca++)(S03=) = KjRSj (5-4)
(Ca++)(S04=) = K2RS2 (5-5)
where:
(Ca++), (S03=), (S04=) = activities of dissolved Ca++, S03=,
and S04= ions, respectively, g-mole/1.
Ki = solubility-product for calcium sulfite, about 3.5 x 10"7
(g-mole/1)2 at 50°C.*
Ko = solubility product for gypsum = 2.2 x 10"5 (g-mole/1)2
at 50°C.
RS], R$2 = relative saturations of liquor with calcium sulfite
and gypsum, respectively.
= 1 if liquor is in equilibrium with the corresponding
solid.
Scrubber inlet liquors are assumed to be saturated with calcium sulfite
(RSj = 1). Also, the activity coefficients of S03= and S04= are assumed
equal as a first approximation. Under these conditions Equations 5-4 and
5-5 can be combined to give:
CS03-MS04-] - (5-6)
This value is a calculated average for Shawnee scrubber inlet liquors, and
may include kinetic, as well as thermodynamic, effects in lime/limestone
wet scrubbing.
5-3
-------
At 50°C, the ratio [S03=]/[S04=] is about 1/(60 RS2).
From Equation 5-6 it is apparent that:
Magnesium can be added as solid MgO, as MgS04 solid or
solution, or even as Mg(HS03)2 solution. For any of
these cases, the calcium_solids equilibria will establish
the concentration of S0o= in accordance with Equation 5-6,
and the concentration of MgS03° in accordance with the
equilibrium among Mg , S03=, and MgS03°.
For operation with gypsum-unsaturated liquor (RS2 < 1, low
sulfite oxidation with co-precipitation of calcium sulfate
as an Impurity in calcium sulfite), the concentration of
dissolved sulfite species is higher than for gypsum-
saturated operation. Thus, S02 removal should increase
as the degree of gypsum saturation in the liquor decreases.
5.3 EFFECTIVENESS OF MAGNESIUM IN THE PRESENCE OF CHLORIDE
As noted previously, the primary objective of magnesium addition is to
dissolve more anions that are basic to S02 (aq), thus increasing S02
removal. However, when chloride is introduced into the scrubber liquor,
by absorption of HC1, the effectiveness of magnesium is reduced because HC1
1s a stronger acid than S02 (aq).*
Because chloride does not react with S02, it Is convenient to describe the
reactivity of a magnesia enhanced scrubbing liquor (containing calcium-based
slurry solids) in terms of the dissolved magnesium sulfite/sulfate concen-
tration, referred to as the effective magnesium concentration
* This detrimental effect of the anion of a strong acid is mitigated for
sulfate, because of the low solubility of calcium sulfate.
5-4
-------
[Mg++]E = [Mg++]total - (1/2)[CT] (5-7)
where:
[Mg++]E = effective magnesium concentration, g-mole/1
[Mg++]tota-j = total concentration of dissolved magnesium species,
g-mole/1
[Cl~] = concentration of dissolved chloride species, g-mole/1
The usefulness of effective magnesium as a control variable for magnesium
enhanced lime/limestone systems is apparent from the linear relationship
between dissolved sulfite and effective magnesium, and the near independence
of this relationship on chloride concentration. Figure 5-1 indicates that,
for scrubbing liquors saturated with gypsum and calcium sulfite, effective
magnesium should correlate with SC^ removal about as well as dissolved
sulfite does. This was indeed the case for Shawnee data. Effective magne-
sium as a dependent variable successfully expressed the beneficial effect of
magnesium additive on S02 removal (see Section 7).
5.4 pH INDEPENDENCE OF DISSOLVED SULFITE CONCENTRATIONS
As shown in Figure 5-2, the concentration of dissolved sulfite species (S03=;
CaS030, and MgS03°) in liquors saturated with calcium sulfite and gypsum is
nearly independent of liquor pH. This implies that the dissolved sulfite
concentrations for saturated scrubber inlet liquors, at the same effective
magnesium concentration, will virtually be the same for lime (high pH)
and limestone (low pH) liquors.
This lack of dependence of dissolved sulfite on pH can be explained by
5-5
-------
FIGURE 5-1.
CONCENTRATION OF DISSOLVED SULFITE SPECIES
-------
FIGURE 5-2.
INDEPENDENCE OF DISSOLVED SULF3TE CONCENTRATION (SO3=, Mg3°, AND Ca3°)
AND LIQUOR pH AT VARIOUS CONCENTRATIONS OF EFFECTIVE MAGNESIUM (Mg-CI/2)
20
16
£
o
i
12
O
o
UJ
I-
_
O 8
UJ
DISSOLVED CHLORIDE = 200 m-mole/l
CaS03 SATURATION = 1.0
GYPSUM SATURATION = 1.0
400 m-mole/l
300 m-mole/l
200 m-mole/l
EFFECTIVE MAGNESIUM CONC. = 100 m-mole/l
6
8
LIQUOR pH
5-7
-------
consideration of the equilibria involved. For a liquor saturated with calcium
sulfite (RSj = 1), Equation 5-4 can be rearranged and the activity of sulfite
ion, (S03=), can be calculated as follows:
(S03=) - ICj/CCa**) (5-8)
Similarly, Equation 5-5 can be rewritten to obtain the activity of calcium
ion, (Ca'f+), for a liquor saturated with gypsum (RS2 = 1);
OCa**) = K2/(S04=) (5-9)
In addition, the activity of the magnesium sulfite ion pair, (MgS03°), can
be expressed as:
(MgS03°) * (Mg^MSO/J/kj (5-10)
where: k-i is the formation constant for MgS03° (about 1 x 10"^
g-mole/1 at 50°C).
Combination of Equations 5-8 through 5-10 yields the following expressions
for the activities of S03= and MgS03°:
(S03m) » (S04=) (Kj/Kg) (5-11)
(MgS03°) = (Mg++)(S04=)(K1/K2k1) (5-12)
Also, as noted earlier, the activity of the calcium sulfite ion pair,
(CaS03°), is constant for a saturated liquor:
++
(CaS03°) = (Ca)(S03*)/k2 = ^2 = constant (5-13)
where: k? is the formation constant for CaS03° (about 3 x 10~4
g-mole/1 at 50°C).
5-8
-------
Equations 5-11 through 5-13 demonstrate that the concentrations of the
dissolved sulfite species are dependent only upon the concentrations of Mg++
and SO^" ions and the activity coefficients of the various dissolved species,
not upon the pH. Furthermore, the concentrations of Mg++ and SO^ ions are
determined by the total dissolved magnesium concentration (in the absence
of chloride), and are independent of pH, because sulfuric acid is too strong
an acid to allow significant formation of bisulfate ion, HS04~.* The activity
coefficients are dependent only upon the ionic strength which is primarily
determined by the Mg++ and SO^ concentration for these systems.
Therefore, the ionic equilibria demonstrate that pH independence of dissolved
sulfite concentration is a good approximation for saturated liquors. This
is also true for liquors having the same relative calcium sulfite and gypsum
saturations, even when the individual relative saturation values are not equal
to one.
5.5 LIME/LIMESTONE TESTS WITH MAGNESIUM ENHANCEMENT
This subsection discusses only test results for the most recent lime and
limestone tests with magnesium additive and no forced oxidation (Sections
16 and 17, Reference 5). Test results for forced oxidation and factorial
runs with magnesium are summarized in Sections 6 and 7, respectively.
* Concentrations of calcium, sulfite, and bisulfite species are relatively
low, so that the concentrations of Mg++ and S04~ ions are nearly equal.
5-9
-------
5.5.1 Limestone Test Runs
Six limestone runs were made, including two base case runs without magnesium
oxide and four runs with magnesium oxide addition. Flue gas with high fly
ash loading was used in all runs. Table 5-1 presents the major test condi-
tions and important test results.
Because of coal shortage caused by the coal miners' strike in the first
quarter of 1978, coals from different sources were burned in Boiler No. 10.
As a result, inlet S02 concentration fluctuated as much as tenfold (320 to
3400 ppm) andvthe run-average concentrations were considerably lower than
normal in most of the runs. These wide variations in inlet S02 concentration
not only created process control problems, but also caused some difficulties
in the interpretation of run data and in the run-to-run comparision of test
results.
Comparison of data from runs with and without magnesium oxide addition
indicated that at a 5000 ppm effective Mg"1"1" concentration, S02 removal
increased to 92 percent from 77 percent without magnesium oxide addition,
at an inlet S02 concentration of about 2400 ppm. At 9000 ppm effective Mg++
concentration, average S02 removal was 93 to 95 percent at a higher inlet
S02 concentration of 2850 ppm.
In summary, magnesium-enhanced limestone testing indicated:
t Even though limestone and lime scrubbing liquors have
similar dissolved sulfite concentrations, higher
effective Mg concentration is required in a lime-
stone system than in a lime system to obtain similar
improvement in S02 removal (see Section 7). This
may be due to the lower pH in the limestone system,
where the shift towards bisulfite reduces S02 removal
efficiency.
5-10
-------
Table 5-1
SUMMARY OF LIMESTONE TESTS WITH MgO ADDITION
ON THE TCA SYSTEM
on
i
Major Test Conditions^
MgO addition
Fly ash loading
Gas rate, acfra 0 300°F
Slurry flow rate to TCA, gpm
Percent solids recirculated
EHT residence time, m1n'2'
EHT level, ft^
Downcomer to EHT(2'
Limestone stoichiometric ratio (controlled)
Limestone addition point^3'
Effective Mg concentration, ppm
Selected Results
Percent S02 removal
Inlet SO- concentration, ppn
SO, make-per-pass , m-moles/ liter
f41
TCA inlet liquor sulfite concentration, ppnr '
TCA inlet liquor gypsum saturation, X
Percent sulfite oxidation
Percent limestone utilization
TCA Inlet pH
Effective Mg** concentration, ppm
On stream hours
590-2A
No
High
30,000
1200
15
4.1
17
Ext.
1.2
DC
0
64
2100
7.3
770
110
45^)
88
5.0
0
45
590-28
No
High
30,000
1200
15
4.1
17
Int.
1.2
DC
0
77
2450
9.9
270
120
31
85
5.3
0
92
591-2A
Yes
High
30.000
1200
15
4.1
17
Ext.
1.2
EHT
5000
92
2300
11.3
2000
105
43
80
5.5
4930
207
592-2A
Yes
High
30,000
1200
15
4.1
17
Ext.
1.2
EHT
9000
95
2850
13.8
4360
105
25
74
5.4
8870
293
593-2A
Yes
High
30,000
900
15
4.1
12.8
Ext.
1.2
EHT
9000
93
2850
18.8
4855
85
24
63
5.45
9000
260
594-2A
Yes
High
30,000
1200
15
4.1
17
Int.
1.2
EHT
9000
93
2850
13.8
5370
90
18
81
5.35
8950
99
Notes:
(1)
(2)
3
4
(5
All runs were made with 3 beds (4 grids) and with nominally 5 Inches/bed of 1 5/8 inch diameter nitrile foam spheres.
Clarifier and centrifuge were used for solids dewatering in all runs.
The effluent hold tank (D-204) was 7 ft in diameter and 21 ft high. Tests were made with either an Internal or external
downcomer.
EHT or downcomer (DC).
Total sulfite includes S03= and HS03".
Steady-state sulfite oxidation was not reached during Run 590-2A.
-------
• Under typical operating conditions, SOp removal improved
by about 15 percentage points with 9000 ppm effective Mg++
concentration.
0 At the magnesium levels tested the scrubber inlet liquors
were approximately saturated with gypsum.
• Gypsum saturation tended to be higher at lower S02 make-
per-pass and higher sulfite oxidation.
• Generally, a higher oxygen/sulfur dioxide ratio in the
scrubber inlet gas resulted in higher sulfite oxidation.
5.5.2 Lime Test Runs
Nine lime runs were made, including two base case runs without magnesium oxide
addition and seven runs with 2000 ppm effective Mg*4" concentration. Flue gas
with high fly ash loadings was used. Major test conditions and important
test results are summarized in Table 5-2.
As noted earlier, coals from several different sources were burned in the
first quarter of 1978. Inlet S02 concentration fluctuated as much as tenfold
(320 to 3400 ppm) and the run-average concentrations were significantly lower
than normal during most of the runs. The wide variations 1n Inlet S$2 concen-
tration created process control problems and caused difficulties in the data
Interpretation and 1n the run-to-run comparison of test results.
In summary, magnesium-enhanced lime testing Indicated:
t At the high S02 removals (90-96 percent) and low inlet S02
concentrations (1600-2100 ppm) for these tests, no improve-
ment in removal was observed with 2000 ppm effective Mg
concentration. Overall reaction rate may be controlled by
the gas phase mass transfer at these conditions.
• Lower inlet S02 concentrations resulted in sulfite oxidations
10 to 15 percentage points higher than normal, probably because
of the higher 02/S02 ratio in the inlet flue gas.
5-12
-------
Table 5-2
SUMMARY OF LIME TESTS WITH MgO ADDITION
ON THE TCA SYSTEM
Major Test Conditions'1'
HgO addition
Fly ash loading
Gas rate, acfm @ 300°F
Slurry flow rate to TCA, gpm
Percent solids recirculated
EHT residence time, min
EHT level, ft'2'
Downcomer to EHT * '
TCA inlet pH (controlled)
Lime addition point'3'
Effective Mg++ concentration, ppm
Selected Results
Percent S02 removal
Inlet S02 concentration, ppm
SO, make-per-pass , m-moles/liter
(4)
TCA inlet liquor sulfite concentration, ppmv '
TCA inlet liquor gypsum saturation, X
Percent sulfite oxidation
Percent lime utilization
Effective Mg** concentration, ppm
Onstream hours
618-2A
No
High
30,000
1200
8
4.1
17
Int.
7.0
DC
0
90
2100
10.2
85
120
28
93
0
162
618-26
No
High
30,000
1200
8
4.1
17
Ext.
7.0
DC
0
96
1900
8.9
80
120
30
94
0
88
619-2A
Yes
High
30,000
1200
8
4.1
17
Ext.
7.0
DC
2000
94
1850
9.2
355
90
23
98
2360
306
620-2A
Yes
High
30,000
900
8
4.1
12.8
Ext.
7.0
DC
2000
91
1600
10.3
330
95
27
97
2090
106
621-2A
Yes
High
30,000
1200
8
3.0
12.5
Ext.
7.0
DC
2000
96
1950
10.3
310
105
29
98
2135
239
622- 2A
Yes
High
30.000
900
8
4.1
12.8
Ext.
7.0
EHT
2000
92
2600
16.4
t C \
94015'
95
22
99
4510(5)
91
622-2B
Yes
High
30.000
900
8
4.1
12.8
Ext.
7.0
DC
2000
85
2600
15.0
465
95
14
96
2150
125
623- 2A
Yes
High
30,000
1200
8
3.0
12.5
Ext.
7.0
DC
2000
91
2550
12.3
410
70
14
94
2190
271
624-2A
Yes
High
30.000
900
8
3.0
9.4
Ext.
7.0
DC
2000
82
2900
16.4
480
65
15
99
1950
269
en
i
Notes:
(1) All runs were made with 3 beds (4 grids) and with nominally 5 Inches/bed of 1-5/8 inch diameter nitrlle foam spheres.
(2)
(3)
(4)
(5)
... Clarifier and centrifuge
were used"for solids dewatering in all runs except Run 624-2A in which clarifier only was used.
The effluent hold tank (D-204) was 7 ft in diameter and 21 ft high. Tests were made with either an internal or external downcoroer,
EHT or downcomer(DC).
Total sulfite includes $03" and HS03-.
Steady-state concentrations were not reached for Run 622-2A from a previous high magnesium limestone run.
-------
• Within the range of low hold tank residence times tested
(3.0 to 4.1 minutes), lower residence time resulted in
lower saturation at similar sulfite oxidation level
(Run 622-2B vs. 624-2A).
• Generally, magnesium addition reduced gypsum saturation
(from about 120 to 95 percent), perhaps because of somewhat
higher S02 make-per-pass and slightly lower sulfite oxidation.
5-14
-------
Section 6
FORCED OXIDATION
This section presents the results of testing at the Shawnee Test Facility to
develop commercially feasible forced-oxidation procedures for reducing the
volume and improving the disposal characteristics of the waste solids product
(Reference 5).
The waste solids consist primarily of calcium sulfite, calcium sulfate
(gypsum), and fly ash. The relative amounts of sulfite and sulfate depend
on the degree of oxidation in the scrubbing system. In most medium-to-high
sulfur coal applications, natural oxidation of sulfite to sulfate in the
scrubber system amounts to only 10 to 30 percent and calcium sulfite is the
predominant material in the waste sludge.
Calcium sulfite wastes present a serious disposal problem because of the
difficulty of dewatering. The slurry can be dewatered only to about 50 to
60 percent solids, producing an unstable, thixotropic material unsuitable
for landfill. Where space is available, ponding of the untreated sulfite
sludge has been practiced. However, the pond area may be impossible to
reclaim, and in many locations sufficient space is not available.
6-1
-------
Preliminary economic evaluations by TVA (Reference 14) have shown that
forced oxidation is a more economical method of producing landfill materials
than other methods such as commercial fixation of sulfite sludge with additives
and blending sulfite sludge with fly ash.
Beginning in 1976, studies conducted by EPA with the 0.1-MW pilot plant
(Reference 15), showed that calcium sulfite could be readily oxidized to
gypsum by simple air/slurry contact in the hold tank of the scrubber recircu-
lation loop. Although the rate of oxidation reached a maximum at a pH of 4.5
and then declined at higher pH, it was found that oxidation could be accom-
plished at a practical rate up to a pH of about 6.0.
Based on the findings at the pilot plant, a program was set up at the Shawnee
Test Facility to develop procedures for forced oxidation. Forced oxidation
testing was Initiated in January 1977 and continued throughout the Shawnee
Advanced Test Program.
Systems successfully demonstrated were:
• Forced oxidation in the first of two scrubber loops using Hme slurry,
limestone slurry, and limestone slurry with added magnesium oxide
• Forced oxidation within a single scrubber loop using limestone slurry
• Forced oxidation of a scrubber bleed stream using limestone slurry
with added magnesium oxide
6-2
-------
6.1 FORCED OXIDATION WITH TWO SCRUBBER LOOPS ON THE VENTURI/SPRAY TOWER SYSTEM
6.1.1 System Description
Forced oxidation with two scrubber loops in series was successfully demon-
strated in the venturi/spray tower system with three alkali types: limestone,
lime, and limestone with added magnesium oxide. In this arrangement (Figure
6-1), the flue gas passed through two scrubbers in series, each with its own
hold tank and slurry recirculation loop. The first loop was operated at a
relatively low pH to provide favorable conditions for forced oxidation while
the second loop was operated at a higher pH for good S02 removal.
The hold tank in the first scrubber (venturi) recirculation loop was used
as the oxidation tank. The arrangement of this tank is shown in Figure 6-2.
The tank was 8 ft in diameter and could be operated at 10, 14, or 18-ft slurry
levels. In early tests the tank contained an air sparger ring made of
straight 3-inch 316L SS pipe pieces welded into an octagon approximately
4 ft in diameter. It was located 6 inches from the bottom of the tank.
Sparger rings had either 130 1/8-inch diameter holes or 40 1/4-inch diameter
holes, pointing downward. The sparger ring was fed with compressed air to
which sufficient water was added to assure humidification. In later tests
the sparger ring was replaced by a 3-inch diameter pipe with an open elbow
discharging air downward at the center of the tank about 3 inches from the
tank bottom.
The oxidation tank had an agitator with two axial flow turbines, both pumping
downward. Each turbine was 52 inches in diameter and contained 4 blades. The
bottom turbine was 10 inches above the air sparger. The agitator rotated at
6-3
-------
FLUE GAS
i
-p.
MAKEUP WATER
COMPRESSED
VENT AIR
iARIFIED LIQUOR FROM SOLIDS DEWATERING SYSTEM
BLEED TO
SOLIDS
DEWATERING
SYSTEM
DESU PER SATURATION
Figure 6-1. FLOW DIAGRAM FOR TWO-SCRUBBER-LQOP FORCED-OXIDATION
TESTS IN THE VENTURI/SPRAY TOWER SYSTEM
-------
BAFFLE
OUTLET
SPARGER
COMPRESSED AIR
AGITATOR
OXIDATION TANK
PLAN VIEW
VENT
COVER
OUTLET ' —
r~~
RAFFI F •
SPARGER WITH
130 1/8-inch HOLES OR
40 1/4- inch HOLES
(DOWNWARD DISCHARGE)
X,
;_
" '
-
|
/
V
,
1 1
1
1 — 1
k
)
/
^
!,
„
B-
,t
1
— ' INLET
— 1
OXIDATION TANK
AGITATOR
COMPRESSED AIR
ELEVATION VIEW
01 2345
SCALE, FEET
Figure 6-2.
Arrangement of the Venturi /Spray Tower
Oxidation Tank with Sparger
6-5
-------
56 rpm and was rated at 17 brake Hp.
A 10-ft diameter desupersaturation tank, operating at a 5-ft slurry level,
followed the oxidation tank to provide time for gypsum precipitation and to
provide air-free pump suction.
Provision was made to add alkali to either scrubber loop. Clarified liquor
from the dewatering system could be returned to either scrubber loop or to
the mist eliminator wash circuit.
6.1.2 Tests with Limestone
In this subsection the results of two-scrubber-loop forced-oxidation limestone
tests on the venturi/spray tower system are reported. A total of 15 runs
were made with high fly ash loading in the flue gas, including a one-month
reliability run. In addition, 8 runs were conducted using flue gas with low
fly ash loading. Except for the one-month reliability run, each test normally
lasted 5 to 6 days, a time judged sufficient to reach kinetic equilibrium and
to allow collection of adequate run data.
Major test conditions and important test results for these runs are summarized
in Table 6-1. Detailed information for these tests can be found in Section 5,
Reference 5.
The following conclusions were made based on the Shawnee limestone test
results from the venturi/spray tower system operating on a two-scrubber-loop
configuration:
• Forced oxidation in the first of two independent scrubbing loops
was successfully demonstrated in the two-scrubber-loop venturi/
spray tower system with limestone slurry. Successful demon-
stration was culminated with a one-month reliability limestone
6-6
-------
Table 6-1
RESULTS OF FORCED-OXIDATION TESTS WITH TWO SCRUBBER LOOPS
ON THE VENTURI/SPRAY TOWER SYSTEM USING LIMESTONE SLURRY
Major Test Conditions
Fly ash loading
Gas rate, acfin 0 3QO°F
Venturi liquor rate, gpm
Spray tower liquor rate, gpm
Venturi percent solids recirculated (controlled)
Residence times, min: Oxidation tank^2'
Desupersaturatlon tank
Spray tower EHT
Venturi inlet (oxidation tank) pH (controlled)
Venturi pressure drop, in. H,0
Air rate to oxidation tank, scfm
Clarified liquor returned to^7'
Selected Results
Percent S0? removal
Inlet S02 concentration, ppm
Spray tower percent solids recirculated
Spray tower inlet pH
Spray tower limestone stoichlometric ratio
Spray tower inlet liquor gypsum saturation, %
Spray tower sulfite oxidation, t
Overall sulfite oxidation, %
Overall limestone utilization, J
Venturi inlet liquor gypsum saturation, X
Venturi inlet liquor sulfite concentration, ppm
Air stoichiometry, atoms 0/mole SO, absorbed
/ i f\ \ <-
Filter cake solids, wt*uu)
Onstream hours
801-1A
High
25,000
400
1300
15
17
7
19.4
4.5
9
400<4>
S.T
62
3400
5.8
5.7
1.20
75
13
93
91
100
29
4.7
81
263
802-1A
High
25,000
400
1400
15
17
7
18
5.0
9
400<4>
S.T
60
3500
6.1
5.5
1.37
no
16
95
83
110
24
4.7
86
256
803-1A
High
25,000
600
1400
15
11.3
4.7
18
5.0<3>
9
400<4>
S.T
67
3150
5.4
5.65
1.47
120
16
96
87
105
21
4.7
81
138
804-1 A
High
25,000
600
1400
15
11.3
4.7
18
5.0
9
400<4>
V. i S.T.
71
3150
7.4^
5.8
1.45
105
15
97
88
105
22
4.4
85
151
805-1A
High
25,000
600
1400
15
11.3
4.7
18
5.0
9
400<4>
V.
78
3450
15.6
6.15
1.53
25
11
98
87
95
16
3.7
81
112
806-1 A
High
25,000
600
1400
15
11.3
4.7
18
4.5
9
250<4>
V.
73
3400
15.1
6.15
1.30
20
10
99
95
95
16
2.5
84
45
806- IB
High
25,000
600
1400
15
11.3
4.7
18
4.5
9
150«>
V.
74
2850
14.5
6.1
1.25
55
15
98
95
95
15
1.7
82
45
806-1C
High
25,000
600
1400
15
11.3
4.7
18
4,5
9
100<4>
V.
73
3250
14.2
6.0
1.25
50
17
97
96
100
15
1.0
79
54
806-1D
*jyu 1 1^
High
25,000
600
1400
15
11.3
4.7
18
4.5
g
50<4>
V.
80
3100
15.9
6.15
1.35
15
15
67
91
105
130
0.50
„(!!)
41
01
I
Note: Footnotes for this table are listed at the end of Table 6-1 (continued)
-------
Table 6-1 (continued)
RESULTS OF FORCED-OXIDATION TESTS WITH TWO SCRUBBER LOOPS
ON THE VENTURI/SPRAY TOWER SYSTEM USING LIMESTONE SLURRY
Major Test Conditions
Fly ash loading
Gas rate, acfm £ 300°F
Venturl liquor rate, gpm
Spray tower liquor rate, gpm
Venturl percent solids redrculated (controlled)
Residence times, mln: Oxidation tank*2'
Desupersaturatlon tank
Spray tower EHT
VentuH Inlet (oxidation tank) pH (controlled)
Venturl pressure drop, In. HgO
Air rate to oxidation tank, scfm
Clarified liquor returned to1
Selected Results
Percent S02 removal
Inlet SO, concentration, ppm
Spray tower percent solids redrculated
Spray tower Inlet pH
Spray tower limestone stolchlometHc ratio
Spray tower Inlet liquor gypsum saturation, X
Spray tower sulfite oxidation, X
Overall sulfite oxidation, %
Overall limestone utilization, X
Venturl Inlet liquor gypsum saturation, X
Venturl Inlet liquor sulfite concentration, ppm
Air stolchlometry, atoms 0/mole SQy absorbed
(10)
Filter cake solids, wtX*
Ons t ream hours
807- 1A
High
25,0-0
600
1400
15
11.3
4.7
18
4.5
9
0
V.
79
3350
16.6
6.25
1.34
8
7
18
91
135
555
0
74<»>
66
808-1 A
High
25,000
600
1400
15
11.3
4.7
18
4.5
150(4>
V.
76
2850
15.5
6.25
1.20
23
16
97
98
100
19
1.7
65
809- 1A
Low
2,5,000
600
1400
15
11.3
4.7
13.4
4.5
150<5>
S.T
82
2450
7.9
5.7
1.30
105
21
98
98
95
35
1.85
80<12>
137
810- 1A
Low
25,000
600
1400
15
11.3
4.7
13.4
5.0
150<5>
S.T
83
2700
8.1
5.8
1.35
105
22
98
96
95
25
1.65
.(13)
162
811-1A
Low
25,000
600
1400
15
11.3
4.7
13.4
5.5
L)<5>
S.T
85
2600
8.0
5.9
1.40
105
25
97
96
105
45
1.65
.(13)
184
812-1A
Low
25,000
600
1400
15
11.3
0
13.4
5.5
150<5>
S.T
93
2350
7.0
5.95
1.93
100
25
98
81
105
60
1.70
86
141
813 1A
Low
25,000
600
1400
15
11.3
0
13.4
5.5
ISO'5'
S.T
-
7
en
00
-------
Table 6-1 (continued)
ID
RESULTS OF FORCED-OXIDATION
ON THE VENTURI/SPRAY TOWER
TESTS WITH TWO SCRUBBER LOOPS
SYSTEM USING LIMESTONE SLURRY
Major Test Conditions
Fly ash loading
Gas rate, acfm 0 300°F
Venturi liquor rate, gpm
Spray tower liquor rate, gpm
Venturi percent solids recirculated (controlled)
Residence times, min: Oxidation tank'2'
Desupersaturation tank
Spray tower EHT
Venturi inlet (oxidation tank) pH (controlled)
Venturi pressure drop, in. H_0
Air rate to oxidation tank, scfm
Clarified liquor returned to^
Selected Results
Percent S02 removal
Inlet SO. concentration, ppm
Spray tower percent solids recirculated
Spray tower inlet pH
Spray tower limestone stoichiometric ratio
Spray tower inlet liquor gypsum saturation, J
Spray tower sulfite oxidation, %
Overall sulfite oxidation, %
Overall limestone utilization, X
Venturi inlet liquor gypsum saturation, X
Venturi Inlet liquor sulfite concentration, ppm
Air stoichiometry, atoms 0/mole SO. absorbed
( 1 (\\
Filter cake solids, wtKuu'
Onstream hours
814-1A
Low
25,000
600
1400
15
8.8
4.7
13.4
5.5
9
150<5>
S.T
91
2450
8.4
5.95
1.78
100
27
98
83
105
25
1.65
88
136
815-1A
Low
35,000
600
1400
15
8.8
4.7
13.4
5.5
9
210^
S.T
86
2500
8.4
5.85
1.98
105
26
96
67
105
40
1.70
87
306
816-1A
Low
35,000
600
1400
15
11.3
4.7
13.4
5.5
9
210<5)
ST.
86
2350
7.7
5.75
1.68
105
27
98
83
100
25
1.80
86
142
817-1A
High
35,000
600
1400
15
11.3
4.7
16.8
5.5
9
210<6>
V.
83
2500
8.9
5.9
1.60
100
21
97
82
105
25
1.75
86
188
818-1A
High
35,000
600
1600
15
11.3
4.7
14.7
5.5
7.5-9
210(6)
V.
86
2550
9.6
5.9
1.64
100
19
98
81
105
25
1.70
86
141
819-1A
High
.(1)
600
1600
15
11.3
4.7
14.7
5.5
S9
210<6)
V.
86
2950
10
5.85
1.65
100
21
98
81
100
25
1.45-2.80
87
840
819-1B
High
.
V.
85
3000
9.6
5.9
1.65
110
19
98
83
105
25
1.45-2.80
86
126
Notes:
(1)
(2)
(3)
4
5
6)
7)
8)
9)
(10)
(11)
(12)
(13)
(14)
Gas rate was varied from 18,000 to 35,000 acfm to follow the boiler load
™ "^ "* ^
Used a
Air
*"
The Sparger r1"9 had 13° 1/8-1nch ho1es on the b°tta"
The Spai"9er H"9 had 40 ^^"^ ""'es on the bottom side
at center of oxidation *•* about
6returned to venturi an
Clarifier and filter in series were used for solids dewatering in all runs except as noted
Values may not be representative due to changes in oxidation in short runs.
Excludes last half of run when filter was out of service
Clarifier only was used.
Test with oxidation tank agitator turned off. Terminated after 7 hours because the air sparging alone did not keep the solids suspended.
-------
test using flue gas with high fly ash loading.
• Under the one-month reliability test conditions of 18,000 to
35,000 acfm gas rate, 600 gpm venturi slurry rate, 1600 gpm
spray tower slurry rate, 15 percent venturi slurry solids
concentration, 18 ft oxidation tank level, and 5.5 oxidation
tank pH, 98 percent average sulfite oxidation was achieved at
air stoichiometric ratios ranging from 1.4 to 2.8 atoms oxygen/
mole SO2 absorbed. The filter cake solids concentration averaged
87 percent.
0 Ranges of conditions under which nearly complete sulfite oxidation
(greater than 95 percent) was demonstrated were an oxidation tank
pH of 4.5 to 5.5, oxidation tank level of at least 14 ft, and an
air stoichiometric ratio of at least 1.5 atoms oxygen/mole SO?
absorbed. Filter cake solids contents greater than 80 percent
were consistently achieved under these conditions.
• Forced oxidation of the slurry within the scrubber loop dramat-
ically improved the dewatering characteristics of the waste
solids. Sulfite oxidation of 90 percent or higher was required
for maximum improvement.
• Forced oxidation was achieved by simple air/slurry contact in
the oxidation tank. Air/slurry contact efficiency did not appear
to be affected, within the ranges of test conditions, whether an
air sparger with 130 1/8-inch diameter holes, an air sparger with
40 1/4-inch diameter holes, or a 3-inch diameter open pipe was
used. Air/slurry contact was primarily achieved by the two-
turbine agitator operated at 56 rpm and rated at 17 brake Hp.
• Slurries with high or low fly ash loadings oxidized equally well.
• With forced oxidation, the venturi inlet slurry constantly exhi-
bited a gypsum saturation of about 100 percent, which was below
the incipient scaling level of 135 percent. This was undoubtedly
caused by the abundance of gypsum crystal seeds produced by
forced oxidation.
t Limestone utilization was improved with the two-scrubber-loop
operation to at least 80 percent and as high as 98 percent,
depending on the venturi inlet pH which averaged from 4.5 to
5.5. The venturi inlet pH was controlled by limestone addition
to the spray tower hold tank.
t In limestone scrubbing, a low slurry solids concentracion in
the spray tower reduced the percent S0£ removal. Furthermore,
a solids concentration of 7 percent or higher was required to
prevent calcium sulfite and sulfate scaling.
• Operation without the desupersaturation tank in the venturi slurry
loop did not have an adverse effect on either sulfite oxidation or
gypsum saturation in the venturi loop.
6-10
-------
• Operation with the agitator turned off in the oxidation tank was
not successful. Air sparging alone in the oxidation tank could
not keep the solids from settling.
6.1.3 Tests with Limestone/MgO
Six runs were made during which magnesium oxide was added to the spray tower
hold tank along with the limestone slurry. The primary purpose of the magne-
sium oxide addition was to enhance SC^ removal efficiency in the spray tower
loop by increasing the dissolved sulfite ion concentration for S02 scrubbing.
In a two-scrubber-loop configuration, the magnesium ion concentration in the
venturi loop was higher than that in the spray tower loop because of the water
loss in humidifying the flue gas in the venturi loop. However, because the
sulfite ion was converted into nonscrubbing sulfate ion by forced oxidation,
the higher magnesium ion concentration in the venturi loop did not enhance
862 removal in the venturi loop. The secondary purpose of the magnesium oxide
addition was to determine whether the presence of magnesium ion had an effect
on oxidation efficiency.
Table 6-2 presents the major test conditions and important test results for
the six limestone runs with magnesium oxide addition. More detailed infor-
mation for these runs is given in Section 6 of Reference 5.
An additional observation in this series of runs was that overall limestone
utilization increased from 82 to 92 percent as the air rate to the oxidation
tank was increased from 0 to 210 scfm. Presumably, the higher air rate im-
proved agitation of the slurry and C0£ stripping and promoted the limestone
dissolution.
6-11
-------
Table 6-2
RESULTS OF FORCED-OXIDATION TESTS WITH TWO SCRUBBER LOOPS
ON THE VENTURI/SPRAY TOWER SYSTEM USING LIMESTONE SLURRY WITH ADDED MAGNESIUM OXIDE
Major Test Conditions
Fly ash loading
Flue gas rate, acfm • 300°F
Slurry rate to venturl. gpn
Slurry rate to spray tower. op»
Venturl percent solids reclrculated (controlled)
Residence times, mln: Oxidation tank
Desupersaturatlon tank
Spray tower EHT
Venturl Inlet (oxidation tank) pH (controlled)
Spray tower limestone stolchlometrlc ratio (based on solids)
Effective Mg** concentration (S.T. loop), ppm
Venturl pressure drop, In. H20
Oxidation tank level, ft
Air rate to oxidation tank, scflr '
Clarified liquor returned to*2'
Selected Results
Percent SO? removal
Inlet SOj concentration, ppn
Spray tower percent sol Ids reclrculated
Spray tower Inlet pH
Spray tower limestone stolchlonetrlc ratio (based on total slurry)
Spray tower Inlet liquor gypsum saturation. X
Spray tower sulflte oxidation, X
Effective Mg0 concentration (S.T. loop), ppn
Overall sulflte oxidation. 1
Overall limestone utilization, X
Venturl Inlet liquor gypsum saturation, X
Venturl Inlet liquor sulflte concentration, ppm
A1r stolchlometry. atoms 0/mole SOj absorbed
Filter cake solids, wtX(3'
Onstream hours
820- 1A
High
35,000
600
1600
15
11.3
4.7
14.7
5.5
-
5000
9
18
210
V.
96
2250
6.0
6.05
1.16
100
30
5150
98
92
130
50
1.70
85
462
B20-1B
High
35,000
600
1600
15
11.3
4.7
14.7
-
i.e'5)
5000
9
18
150
V.
94
2500
8.3
5.9
1.28
105
17
4985
92
90
130
950
1.10
82
137
820-1C
High
35,000
600
1600
15
11.3
4.7
14.7
-
1.6*5)
5000
9
18
0
V.
91
2750
10.5
5.9
1.52
90
20
4700
36
82
145
5585
0
63
134
821- 1A
High
35,000
600
0
15
11.3
4.7
-
5.5
-
5000
9
18
210
V.
-
-
.(6)
-
-
-
-
-
-
-
-
-
-
-
-
822-1A
High
35.000
600
1600
15
11.3
4.7
14.7
-
1.6^5)
5000
9
18
210
V.
91
2750
8.0
5.75
1.55
100
21
4895
97
79
125
735
1.45
85
232
822-1B
High
35,000
600
1 Jt\
160014)
15
11.3
4.7
14.7
-
1.6*5'
5000
9
18
210
V.
90
2400
5.6
• 5.55
1.21
110
23
4845
98
93
130
410
1.70
35
85
Notes:
Air discharged downward through 3-Inch diameter pipe with an open elbow at center of oxidation tank about 3 Inches from tank bottom.
Venturl loop (oxidation tank).
Clarlfler and filter used for solids dew*Urinp In all runs.
Spray tower turned off for 30 Minutes every a hour* to obtain SO. removal with venturl alone. Venturl S02 removal averaged 291.
In runs with control by spray tower itolchlowetrlc ratio, the venturl Inlet-pH averaged S.O.
Run faded due to low HgO dfs«o!utfon rate In spray tower effluent hold tank.
-------
The following conclusions were drawn from the evaluation of the test results:
• The anticipated S0£ removal enhancement was achieved. Under
typical operating conditions, average overall S02 removal was
96 percent at 2250 ppm average inlet SO? concentration with
5150 ppm effective magnesium ion concentration in the spray
tower (Run 820-1A). Under the same operating conditions but
without magnesium oxide addition, overall S0£ removal averaged
86 percent at 2550 ppm inlet SOo concentration (Run 818-1A,
Table 6-1).
• Magnesium ion does not enhance S02 removal in a scrubber loop
in which oxidation is forced, because sulfite ion is oxidized
into nonscru^bing sulfate ion. S02 removal in the venturi
loop (oxidation loop) was 29 percent (Run 822-1B with inter-
mittent spray tower operation), which is typical of removal
efficiency with limestone slurry in the absence of magnesium
ion.
• The oxidation efficiency appeared to be unaffected, if not
improved, by the presence of magnesium ion. Under typical
conditions, sulfite oxidation was 98, 92, and 36 percent at
1.7, 1.1 and 0 air stoichiometry, respectively (Runs 820-1A,
820-1B, and 820-1C, respectively). Nearly complete oxidation
appeared to be possible at an air stoichiometric ratio as low
as 1.3.
0 Filter cake solids concentration at 98 percent oxidation averaged
85 percent, demonstrating that magnesium oxide addition does not
adversely affect the dewatering characteristics of oxidized sludge.
6.1.4 Tests with Lime
In this subsection, the results of forced-oxidation lime tests with a two-
scrubber-loop configuration on the venturi/spray tower system are presented.
A total of 20 lime runs were made. These included 10 runs each with high and
low fly ash loadings in the flue gas. Tests with high fly ash loading included
a one-month lime reliability run. Except for the one-month reliability run,
each test normally lasted 5 to 6 days, a time period which was judged suffi-
cient to reach kinetic equilibrium and to allow collection of adequate run
data.
6-13
-------
Table 6-3 summarizes the major test conditions and important test results
for the two-scrubber-loop forced-oxidation lime runs. Additional detailed
information for these runs can be found in Section 7 of Reference 5.
The operating characteristics and test results of the two-scrubber-loop
forced-oxidation lime tests were similar to those of limestone tests in many
aspects (see Section 6.1.2). The following conclusions were made based on
the results of lime testing from the venturi/spray tower system:
*
• Forced oxidation of sulflte to sulfate in the first of two Independent
scrubbing loops was successfully demonstrated in the two-scrubber-loop
venturi/spray tower system with Hme slurry. Successful demonstration
of the forced oxidation was culminated with a one-month reliability
lime test using flue gas with high fly ash loading.
• Under the one-month reliability test conditions of 18,000 to 35,000
acfm gas rate, 600 gpm venturi slurry rate, 1600 gpm spray tower
slurry rate, 15 percent venturi slurry solids concentration, 18-ft
oxidation tank level, and 5.5 oxidation tank pH, an average sulfite
oxidation of 97 percent was achieved with air stoichiometric ratios
ranging from 1.40 to 2.75 atoms oxygen/mole S02 absorbed. The filter
cake sol Ids concentration averaged 85 percent.
• As with limestone tests, ranges of conditions under which nearly
complete sulfite oxidation (greater than 95 percent) was demonstrated
were an oxidation tank pH of 4.5 to 5."5, oxidation tank level of at
least 14 ft, and an air stoichiometry of at least 1.5 atoms oxygen/
mole S02 absorbed. Filter cake solids contents of about 80 percent
or higher were achieved under these conditions.
t The degree of sulfite oxidation was not affected when the venturi
slurry solIds concentration was dropped from the normal 15 percent
to 8 percent by weight.
t Oxidation efficiency appeared to drop off at pH's greater than
about 6.
• Sulfite oxidation of 90 percent or higher was required to obtain
maximum improvement in waste solids dewatering characteristics.
• As with limestone tests, forced oxidation was achieved by simple
air/slurry contact in the oxidation tank. Within the ranges of
test conditions, air/slurry contact efficiency did not appear to
be affected whether an air sparger with 130 1/8-inch holes, an air
sparger with 40 1/4-inch holes, or a 3-inch diameter open pipe was
used. Air/slurry contact was primarily achieved by the two-turbine
agitator operated at 56 rpm and rated at 17 brake Hp.
6-14
-------
Table 6-3
RESULTS OF TWO-SCRUBBER-LOOP FORCED-OXIDATION LIME TESTS
ON THE VENTURI/SPRAY TOWER SYSTEM
Major Test Conditions
Fly ash loading
Gas rate, acfm 1? 300°F
Venturi liquor rate, gpm
Spray tower liquor rate, gpm
Venturi percent solids recirculated (controlled)
Residence times, min: Oxidation tank
Desupersaturation tank
Spray tower EHT
Venturi inlet (oxidation tank) pH (controlled)
Spray tower inlet pH (controlled)
Venturi pressure drop, in. H,,0
Oxidation tank level, ft
Air rate to oxidation tank, scfm
Clarified liquor returned to'8'
Selected Results
Percent S02 removal
Inlet SO- concentration, ppm
Spray tower percent solids recirculated
Spray tower lime stoichiometric ratio
Spray tower inlet liquor gypsum saturation, %
Spray tower sulfite oxidation, %
Overall sulfite oxidation, %
Overall lime utilization, %
Venturi inlet liquor gypsum saturation, %
Venturi inlet liquor sulfite concentration, ppm
Air stoichiometry, atoms 0/mole S0£ absorbed
Filter cake solids, wt%* '
Onstream hours
851-1A
High
25,000
600
1400
15
11.3
4.7
18
4.5
8.0
9
18
ISO'5'
V. & S.T.
78
3300
6.0
1.13
80
15
97
98
95
39
1.45
81
110
852-1A
High
25,000
160
1400
15
42
17.7
18
.>4.5<2>
8.0
(min)
18
150<5>
V. & S.T.
70
3400
8.3
1.13
50
13
83
96
105
22
1.55
73
74
853-1 A
High
25,000
600
1400
15
11.3
4.7
18
i4.5<3>
8.0
(min)
18
150<5>
S.T.
77
3450
6.4
1.14
80
14
97
95
100
35
1.40
78
161
854- 1A
High
25,000
600
1400
15
11.3
4.7
18
5.2
8.0
9
18
S.T.
82
3150
6.1
1.15
55
11
96
97
100
35
1.40
79
166
855-1A
Low
25,000
600
1400
15
11.3
4.7
18
4.5<4>
8.0
9
18
ISO'6'
S.T.
83
2350
7.3
1.14
95
18
98
98
105
24
1.90
75(11)
158
856-1 A
Low
25,000
600
1400
15
11.3
4.7
18
5.0
8.0
9
18
150<6>
S.T.
88
2500
7.9
1.16
90
12
97(9)
98
95
36*9)
1.65
83'11)
209
857-1A
Low
25,000
600
1400
15
11.3
4.7
18
5.5
8.0
9
18
ISO*6'
S.T.
84
2650
7.9
1.14
90
11
97
99
100
64
1.65
78
128
858-1 A
Low
25,000
600
1400
8
11.3
4.7
18
5.5
8.0
9
18
ISO'6'
V.
83
2750
15.2
1.13
85
14
97
98
110
20
1.60
81
162
Note: Footnotes for this table are listed at the end of Table 6-3 (continued)
-------
Table 6-3 (continued)
RESULTS OF TWO-SCRUBBER-LOOP FORCED-OXIDATION LIME TESTS
ON THE VENTURI/SPRAY TOWER SYSTEM
Major Test Condtions
Fly ash loading
Gas rate, acfm S 300°F
Venturl liquor rate, gpn
Spray tower liquor rate, gpm
Venturl percent solids reclrculated (controlled)
Residence times, m1n: Oxidation tank
Desupersaturatlon tank
Spray tower EHT
Venturl Inlet (oxidation tank) pH (controlled)
Spray tower Inlet pH (controlled)
Venturl pressure drop, 1n. H_0
Oxidation tank level, ft
Air rate to oxidation tank, scfm
Clarified liquor returned to*8'
Selected Results
Percent SO, removal
Inlet S02 concentration, ppm
Spray tower percent solids reclrculated
Spray tower lime stoichlometric ratio
Spray tower inlet liquor gypsum saturation, I
Spray tower sulflte oxidation, %
Overall sulflte oxidation, X
Overall lime utilization, %
Venturi inlet liquor gypsum saturation, %
Venturi inlet liquor sulfite concentration, ppm
Air stoichiometry, atoms 0/mole SO- absorbed
Filter cake solids, wtt^10'
Onstream hours
859-1A
Low
25,000
600
1400
15
11.3
4.7
18
5.5
8.0
9
18
135(6)
S.T.
92
2950
7.2
1.16
60
10
76
97
95
99
1.20
74
115
859-1B
Low
25.000
600
1400
15
11.3
4.7
18
5.5
8.0
9
13
150<6>
S.T.
92
2700
7.6
1.16
90
12
99
99
105
33
1.50
78
70
859-1C
Low
25,000
600
1400
15
11.3
4.7
18
5.5
8.0
9
18
100(6)
S.T.
92
2700
7.3
1.15
90
20
69
96
105
82
1.0
71
120
859-10
Low
25,000
600
1400
15
11.3
4.7
18
5.5
8.0
9
18
0
S.T.
93
2600
7.1
1.17
50
10
30
90
115
85
0
55
72
860-1 A
Low
25,000
600
1400
15
11.3
4.7
12.6
5.5
8.0
9
18
150<6>
S.T.
95
2200
7.0
1.18
70
10
99
99
100
20
1.75
82
133
861-1A
Low
25,000
600
1400
15
11.3
4.7
18
5.5
8.0
9
18
150<7>
S.T.
92
2700
7,3
1.16
90
19
98
99
95
35
1.50
86
117
ert
-------
Table 6-3 (continued)
RESULTS OF TWO-SCRUBBER-LOOP FORCED-OXIDATION LIME TESTS
ON THE VENTURI/SPRAY TOWER SYSTEM
en
-vl
Major Test Conditions
Fly ash lading
Gas rate, acfm Q 300°F
Venturi liquor rate, gpm
Spray tower liquor rate, gpm
Venturi percent solids recirculated (controlled)
Residence times, min: Oxidation tank
Desupersaturation tank
Spray tower EHT
Venturi inlet (oxidation tank) pH (controlled)
Spray tower inlet pH (controlled)
Venturi pressure drop, in. HJ3
Oxidation tank level, ft
Air rate to oxidation tank, scfm
Clarified liquor returned to'8'
Selected Results
Percent S02 removal
Inlet S02 concentration, ppn
Spray tower percent solids recirculated
Spray tower lime stoichiometric ratio
Spray tower inlet liquor gypsum saturation, %
Spray tower sulfite oxidation, %
Overall sulfite oxidation, %
Overall lime utilization, S
Venturi inlet liquor gypsum saturation, %
Venturi inlet liquor sulfite concentration, pptn
Air stoichiometry, atoms 0/mole SO- absorbed
Filter cake solids, w«'10'
Onstream hours
862- 1A
High
35,000
600
1400
15
11.3
4.7
18
5.5
8.0
9
18
210<7>
V.
85
2650
17.3
1.11
85
18
97
98
105
30
1.65
86
162
863-1A
High
m
600
1600
15
11.3
4.7
14.7
5.5
7.8
M
18
210<7>
V. & S.T.
88
2950
10.4
1.11
100
21
97
98
105
35
1.40-2.75
85
779
864-1A
High
35,000
600
1600
15
11.3
4.7
14.7
5.5
7.8
9
18
210<7>
V. & S.T.
94
2250
9.5
1.13
100
24
98
99
100
25
1.75
85
115
865-1A
High
35,000
600
1600
15
6.3
4.7
14.7
5.5
7.8
9
10
290/210(7'
V. S S.T.
89
2300
10.1
1.10
95
26
89
98
100
65
2.10
80
254
866-1 A
High
35,000
600
1600
15
6.3
4.7
14.7
5.5
7.8
9
10
350<7>
V. a S.T.
94
1700/2400
9.9
1.15
90
26
98/81
98
95
40
3.85/2.70
81
159
867-1A
High
35,000
600
1600
15
8,3
4.7
14.7
5.5
7.8
9
14
210<7>
V. & S.T.
89
2300
11.8
1.12
85
20
98
99
90
40
1.80
86
137
Notes:
(1)
(2
(3.
(4)
(5)
(6)
(7)
(8
(9.
(10)
(11)
Gas rate was varied from 18,000 to 35,000 acfm to follow the boiler load.
Actual pH range was 4.6-6.2 (avg. 5.6).
Actual pH range was 4.3-5.2 (avg. 4.8).
Actual average pH was 4.7.
Used a sparger ring located 6 Inches from tank bottom. The sparger ring had 130 1/8-inch holes on the bottom side.
Used a sparger ring located 6 inches from tank bottom. The sparger ring had 40 1/4-inch holes on the bottom side.
Air discharged downward through a 3-inch diameter pipe with an open elbow at center of oxidation tank about 3 inches from tank bottom.
Spray tower loop (effluent hold tank) or venturi loop (oxidation tank).
Excluded a period 7/2/77-7/5/77 in which oxidation dropped to as low as 62% for unknown reason.
Clarifier and filter in series used for solids dewatering in all runs.
Intermittent filter operation.
-------
0 Slurries with high and low fly ash loadings oxidized equally well.
t Independent lime addition to both scrubber loops was necessary to
have smooth ventui and spray tower inlet pH control.
t As in the limestone tests, the venturi inlet slurry liquor constantly
exhibited a gypsum saturation level of about 100 percent when
oxidation was forced within the venturi loop. This was probably
the result of the abundance of gypsum crystal seeds produced by
forced oxidation. The 100 percent saturation level is well below
the incipient scaling level of 135 percent.
• Lime utilization in the spray tower averaged about 88 percent.
Overall lime utilization averaged 98 percent, demonstrating the
advantage of a two-scrubber loop system.
• Spray tower scaling (mostly by calcium sulfite) may occur when the
reclrculated slurry solids concentration in the spray tower drops
below about 7 percent (low fly ash loading). This is especially
true when the spray tower outlet pH stays above about 5.5.
• Oxidation efficiency did not appear to be affected when the oxidation
tank level was dropped from 18 ft to 14 ft at 1.8 air stoichiometry
and 5.5 pH. At a 10-ft tank level, an air stoichiometry approaching
4 was required to obtain nearly complete oxidation.
6.2 FORCED OXIDATION WITH ONE SCRUBBER LOOP ON THE TCA SYSTEM
Forced oxidation with good S02 removal in a single scrubber loop was demonstrated
in the TCA system using limestone slurry. In this arrangement, sulfite oxidation
was achieved by contacting the slurry with air in the scrubber hold tank. A
compromise was made in the scrubber liquor pH between a higher pH desired for
good S02 removal and a lower pH desired for good oxidation. Although the
optimum oxidation rate occurs at about 4.5 pH, it was found that the oxidation
rate was adequately fast up to a pH of about 6. Thus the oxidation pH range
is compatible with the limestone scrubbing pH range of 5 to 6.
6-18
-------
Forced oxidation in a single scrubber loop is detrimental to lime slurry
scrubbing because sulfite ion, a major scrubbing species in a lime based
scrubbing system, is removed in the oxidation process. Thus, forced oxidation
substantially reduces S0£ removal efficiency in a single loop lime system.
The single loop configuration was of prime interest commercially because the
majority of commercial installations, both operating and planned, are of this
type. Modification of these installations for forced oxidation would require
as a minimum a compressor (or blower) plus an air sparger in the scrubber
hold tank.
Two devices for air/slurry contact were tested on the TCA system. During the
initial phase an air eductor was tested. Because of erosion problems and
high energy consumption, the eductor was replaced with an air sparger similar
to the one used in the venturi oxidation tank. All tests were conducted with
flue gas containing high fly ash loadings.
6.2.1 Air Eductor System Description
An air eductor (Penberthy-Houdaille Model ELL-10 Special) was used to provide
air/slurry contact. The high velocity of the slurry pumped through the eductor
nozzle aspirated air into the liquid stream. The high shear developed in the
throat of the eductor broke air into minute bubbles which were ejected into
the oxidation tank, aerating the slurry in the tank.
The main feature of the eductor was its ability to create smaller air bubbles
than could be obtained with an air sparger. This resulted in a higher mass
transfer coefficient. However, the air eductor consumes more energy than
an air sparger and is more prone to severe erosion in high-velocity slurry
6-19
-------
service.
The eductor used was capable of educting 600 scfm of air from the atmosphere
at zero back pressure with a slurry flow rate of 1600 gpm. The eductor nozzle
and a whirler within the nozzle were made of Stellite and the body was made
of neoprene-lined carbon steel.
Two flow configurations were used on the one-scrubber-loop forced oxidation
tests. In the one-tank configuration (Figure 6-3) slurry was recirculated
from the TCA effluent hold tank (oxidation tank) through the eductor and
back into the hold tank. The hold tank was 20 ft in diameter and operated
at slurry levels from 6 to 12 feet. Limestone makeup was added either to
the hold tank or to the pump suction of the scrubber recirculation line. In
the two-tank configuration (Figure 6-4) a small downcomer tank (7-ft diameter)
was used to receive the slurry from the scrubber. Slurry was then pumped
from the downcomer tank through the eductor to the large hold tank (oxidation
tank) where limestone was added. A slurry tie line connecting the two tanks
equalized the slurry level in both tanks. The slurry flow through the eductor
was maintained at a higher rate than the slurry flow to the scrubber. Thus
there was always a slurry back-flow through the tie line from the hold tank
to the downcomer tank. The two-tank configuration had the advantage that the
pH of the slurry passing through the eductor was lower and thus the chemical
reaction rate was higher.
In both one-tank and two-tank configurations, tests were made with the eductor
mounted in both vertical and horizontal positions. In the vertical position
as shown in Figures 6-3 and 6-4, the eductor was mounted above the effluent
hold tank (oxidation tank) in an off-centered position and the air/slurry
6-20
-------
FLUE GAS
MAKEUP WATER
FLUE GAS
LIMESTONE
CLARIFIED LIQUOR
FROM SOLIDS DEWATERING
SYSTEM
AIR (ATM. PRESS.)
EDUCTOR
(PENBERTHY
ELL-10 SPECIAL)
BLEED TO SOLIDS
DEWATERING SYSTEM
OXIDATION
TANK
Figure 6-3. FLOW DIAGRAM FOR ONE-SCRUBBER-LOOP FORCED OXIDATION
WITH AIR EDUCTOR IN THE TCA SYSTEM USING ONE TANK
6-21
-------
FLUE GAS
MAKEUP WATER
FLUEQAS
LIMESTONE
CLARIFIED LIQUOR.
FROM SOLIDS OEWATERING
SYSTEM
ALT
ooo
ooooo
ooo
oooool
ooo
oooo_g
TCA
BLEED TO SOLIDS
DEWATERINQ SYSTEM
AIR (ATM. PRESS.)
EDUCTOR
(PENBERTHY L"
ELL-10 SPECIAL)
TANK
DOWNCOMER
HOLD TANK
Figure 6-4. FLOW DIAGRAM FOR ONE-SCRUBBER-LOOP FORCED OXIDATION
WITH AIR EDUCTOR IN THE TCA SYSTEM USING TWO TANKS
6-22
-------
mixture was discharged vertically downward. Figure 6-5 shows the detailed
arrangement of the oxidation tank with the eductor in vertical position. With
the eductor in horizontal position (not shown in figures), air/slurry mixture
was discharged into the oxidation tank through the tank wall in a horizontal,
radial direction (at about 4 o'clock position on the plan view of Figure 6-5)
and at an elevation 10 inches above the tank bottom.
6.2.2 Air Eductor Tests with Limestone
A total of 15 runs were made using limestone slurry with high fly ash loadings.
These included 11 runs made with the air eductor mounted in a vertical position
over the oxidation tank, and 4 runs with the eductor in a horizontal position
beside the oxidation tank. Each test run normally lasted 5 to 6 days.
Table 6-4 summarizes the major test conditions and important test results for
the 15 runs. Additional detailed information can be found in Section 12 of
Reference 5.
The following conclusions were made from the results of these tests:
• Under the base case conditions of 30,000 acfm gas rate, 1200 gpm
TCA slurry rate, 1600 gpm (with high fly ash loading), eductor
slurry rate, 15 percent recirculated slurry solids (with fly ash),
and 8 to 12 ft slurry level in the effluent hold tank (oxidation
tank), sulfite oxidation of better than 90 percent was achieved at
an eductor inlet pH range of 4.95 to 5.45 and air stoichiometric
ratios as low as 2.0 atoms oxygen/mole S02 absorbed.
• The dewatering and handling characteristics of slurry solids
oxidized to 90 percent or higher in a one-scrubber-loop system
were as good as those in a two-scrubber-loop system.
• Operation in a two-tank configuration allowed for a higher pH to
the TCA for good S02 removal and a lower pH to the eductor for good
sulfite oxidation. Sulfite oxidations up to 98 percent were achieved
with satisfactory SOo removal (80-89 percent).
6-23
-------
AGITATOR
DOWNCOMER
BAFFLE
DOWNCOMER
BAFFLE
AIR (ATM. PRESS.)
-TO EDUCTOR
PLAN VIEW
INLET
AIR (ATM. PRESS.)
SLURRY
TO EDUCTOR
ELEVATION VIEW
01234 5
SCALE. FEET
Figure 6-5. ARRANGEMENT OF THE TCA OXIDATION TANK
WITH EDUCTOR IN VERTICAL POSITION
6-24
-------
Table 6-4
SUMMARY OF ONE-SCRUBBER-LOOP FORCED-OXIDATI ON LIMESTONE TESTS
WITH AIR EDUCTOR ON THE TCA SYSTEM
Major Test Conditions
Fly ash loading
Gas rate, acfm @ 300°F
Slurry flow rate to TCA, gpm
Slurry flow rate to eductor, gpm
Percent solids recirculated
EHT (oxidation tank) residence time, min. '
Downcomer (low pH) tank residence time, min.^ '
EHT level, ft
Eductor mounting position in EHT
Eductor discharge point, ft from EHT bottom
Limestone stoichiometric ratio controlled at
TCA inlet pH controlled at
EHT (oxidation tank) agitator speed, rpm
( 21
Limestone addition point* '
Air flow rate to eductor, scfm
Selected Results
Percent SO^ removal
Inlet SCL concentration, ppm
Percent sulfite oxidation
Air stoichiometry, atoms 0/mole S02 absorbed
TCA inlet pH
Eductor inlet pH
Percent limestone utilization
Gypsum saturation in TCA inlet liquor, %
Onstream hours
801 -2A
High
30,000
1200
1600
15
12
-
6.1
Ver.
6<4>
1.2
-
45
EHT
~600
70
2750
53
6.4
5.8
5.8
80
105
102
801-2B
High
30,000
1200
1600
15
15.7
-
8.0
Ver.
6<4>
1.2
45
EHT
530
70
2750
63
5.6
5.8
5.8
80
105
47
802-2A
High
30,000
1200
1600
15
23.5
-
12
Ver.
10
1.2
-
45
EHT
485
76
2900
56
4.5
5.75
5.75
82
100
142
803-2A
High
30,000
1200
1600
15
23.5
_
12
Ver.
10
_
5.0
45
EHT
465
62
2950
91
5.2
5.05
5.05
90
105
165
804-2A
High
30,000
1200
1600
15
23.5
_
12
Ver.
10
_
5.0
68
EHT
410
62
3000
93
4.5
5.0
5.0
93
105
166
805- 2A
High
30,000
1200
1600
15
23.5
«.
12
Ver.
10
.
5.3
68
TCA
470
72
3050
93
4.4
5.35
5.25
84
105
140
806-2A
High
30,000
1200
1200
15
23.5
12
Ver.
10
_
5.3
68
TCA
290
70
3000
58
2.8
5.35
5.3
91
110
115
ro
en
Note: Footnotes for this table are listed in Table 6-4 (continued).
-------
Table 6-4 (continued)
SUMHARY OF ONE-SCRUBBER-LOOP FORCED-OXIDATION LIMESTONE TESTS
WITH AIR EDUCTOR ON THE TCA SYSTEM
Mijor Test Conditions
Fly Hh loading
Gas fate, acfm » JOO°F
Slurry flow rate to TCA. gpi
Slurry flow rate to eductor. gpai
Percent solids reclrculated
EHT (oxidation tank) residence tlM, mln/1'
Oowncoavr (low pH) tank residence time. «1n.(1)
EHT level, ft
Eductor mounting position In EHT
Eductor discharge point, ft from EHT botton
Limestone stolchlometrlc ratio controlled at
TCA Inlet pH controlled at
EHT (oxidation tank) agitator speed, rpm
Limestone addition point'2'
Air flow rate to eductor, scfm
Selected Results
Percent SOj removal
Inlet SO; concentration, ppm
Percent sulflte oxidation
Air stolchlometry, atom 0/mle S02 absorbed
TCA Inlet pH
Eductor Inlet pH
Percent limestone utilization
Gypsum saturation In TCA Inlet liquor, X
Onstream hours
807-2A
High
30.000
1200
1600
15
23.5
2.9
12
Ver.
10
-
5.4
68
EHT
475
83
2700
96
4.3
S.4S
5.1
82
100
IBS
eoa-2A
High
30.000
1200
1600
15
23.5
2.9
12
Ver.
10
1.3
-
68
EHT
200
71-
2900
93
2.0
5.1
4,95
63
125
162
809-2^)
High
30.000
1200
1600
15
15.7
1.9
8
Ver.
6<4>
1.3
-
66
EHT
300<5)
77
3200
96
2.S
5.2
5.0
63
115
149
810-2A(3)
High
30.000
1200
1600
15
15.7
1.9
8
Ver.
6<4>
-
5.4
68
EHT
300<5>
84
2900
98
2.5
5.5
5.15
77
110
130
811-2A
High
30,000
1200
1600
15
23.5
2.9
12
Hor.
0.8
1.3
-
68
EHT
270
87
2800
96
2.3
5.85
5.45
60
100
164
812-2A
High
30.000
1200
1600
15
15.7
1.9
8
Hor.
0.8
1.3
-
68
EHT
350
81
3000
93
2.9
5.5
5.3
56
100
141
813-2A
High
30.000
1200
1600
15
23.5
-
12
Hor.
0.8
-
5.3
68
TCA
310
80
2850
95
2.8
5.35
5.15
90
90
130
814-2A
High
30,000
1200
1200
15
15.7
-
8
Hor.
0.8
-
5.3
68
TCA
145
74
2550
61
1.6
5.35
5.3
85
115
119
Ch
INJ
Notes:
Residence tines are based on slurry flow rate to TCA.
EHT (effluent hold tank) or TCA (pump suction on the TCA Inlet slurry line).
Filter 1n series with clarlfler wasused during Runs 809-2A and 810-2A. Filter cake solids contents were 85 and 88*. respectively.
At discharge of 4 ft long by 10-Inch diameter pipe attached beneath the eductor.
Air flow controlled by a sliding plate In the air intake line to eductor.
-------
• With a single-tank configuration and limestone addition to the effluent
hold tank, low hold tank pH (hence, low SC^ removal) was necessary
to achieve good sulfite oxidation. The SO? removal could be improved,
however, by limestone addition to the TCA inlet slurry stream instead
of the hold tank.
• S0£ removal tended to be a few percentage points higher than the
predicted SOp removal under similar operating conditions without
forced oxidation. The reason for this removal enhancement is believed
to be air stripping of C02 from the liquor, which increases the
limestone dissolution rate.
• No significant difference in sulfite oxidation efficiency was
observed between operations with the air eductor in the vertical,
top-entry position or in the horizontal, bottom-entry position.
• Sulfite oxidation was unsatisfactory (about 60 percent) when the
eductor slurry flow rate was reduced from 1600 to 1200 gpm. Decreased
agitation in the oxidation tank at the lower flow rate is believed to
be the main reason for poor oxidation, rather than the reduced air
stoichiometric ratio.
• Air eduction by the eductor was as predicted by the manufacturer.
Air flow rate was sensitive to the depth of the eductor1s submer-
gence in the slurry, ranging from 600 scfm at zero submergence to
200 scfm at 12 ft submergence, at a 1600 gpm slurry rate. 200 scfm
of air was sufficient to achieve good sulfite oxidation at 1600 gpm
slurry flow.
• Air/slurry contact was hampered by the configuration of the eductor
discharge hold tank (20 ft diameter tank with only 8 to 12 ft normal
liquid depth). A smaller diameter but deeper tank would probably
have given better oxidation efficiency.
• Erosion of the air eductor (in limestone/fly ash service) was a
problem. The eductor body was constructed of neoprene-lined
carbon steel. The rubber near the nozzle had eroded in a circular
pattern after 1500 operating hours, and the carbon steel body was
eroded through after additional 550 hours. The Stellite nozzle and
whirler showed only minor evidence of erosion.
6.2.3 Air Sparger System Description
Two operating configurations were used in the one-scrubber-loop forced-oxidation
tests. With one tank as shown in Figure 6-6, effluent slurry from the TCA was
discharged to the oxidation tank where limestone was added and the slurry was
6-27
-------
MAKE UP WATER
FLUE GAS
LIMESTONE
CLARIFIED LIQUOR
FROM SOLIDS DEWATERING
SYSTEM
BLEED TO SOLIDS
DEWATERING SYSTEM
FLUE GAS
ooo
ooooc
ooo
ooooo
QOO
ooooc
TCA
"JO-
WATER
COMPRESSED
_AIR
Figure 6-6. FLOW DIAGRAM FOR ONE-SCRUBBER-LOOP FORCED OXIDATION
WITH AIR SPARGER IN THE TCA SYSTEM USING ONE TANK
6-28
-------
recycled back to the TCA. With two tanks in series as shown in Figure 6-7,
effluent slurry was discharged to the oxidation tank and the slurry then
overflowed to a second tank (effluent hold tank) where limestone was added.
Slurry was recycled from the second tank back to the TCA.
Although the one-tank configuration is simpler, and modification of the
existing full-scale installations to this forced oxidation scheme can be made
readily (with the addition of an air sparger and a compressor or blower), a
balance must be made in the single tank between the higher pH desired for good
S02 removal and the lower pH desired for good sulfite oxidation. The two-tank
configuration has the advantage of oxidizing the lower pH scrubber effluent
slurry before limestone is added. The two-tank mode also provides better
limestone utilization.
The oxidation tank arrangement is shown in Figure 6-8. The tank was 7 ft in
diameter and was operated at a 17 to 18-ft level. All tests were conducted
with an air sparger ring made of straight 3-inch 316L SS pipe pieces welded
into an octagon of approximately 4-ft diameter. It was located 8 inches from
the bottom of the tank and had 40 1/4-inch diameter holes pointed downward.
The sparger ring was fed with compressed air to which sufficient water was
added to assure humidification.
6.2.4 Air Sparger Tests with Limestone
The results of TCA one-scrubber-loop forced-oxidation limestone tests using
an air eductor for air/slurry contact have been reported in Section 6.2.2.
Erosion of the air eductor used in those tests was a major problem. Testing
was terminated after about 2050 hours when the neoprene-lined carbon steel
eductor body was eroded through.
6-29
-------
FLUE GAS
MAKEUP WATER
FLUEQAS
CLARIFIED LIQUOR.
FROM SOLIDS DCWATERING
SYSTHI
BLEED TO SOLIDS
DEMATERmG SYSTEM
0000.
\_J
TCA
COMPRESSED
AIR
WATE]
O^ERFLOM
A A
EFFLUENT HOLD
TANK
OXIDATION
TANK
Figure 6-7. FLOW DIAGRAM FOR ONE-SCRUBBER-LOOP FORCED OXIDATION
WITH AIR SPARGER IN THE TCA SYSTEM USING TWO TANKS
6-30
-------
INLET
AGITATOR
BAFFLE
SPARGER
COMPRESSED AIR
OXIDATION TANK
PLAN VIEW
J
OUTLET .
BAFFLE v.
SPARGER WITH
40 1/4-inch HOLES
(DOWNWARD DISCHARGE) x
\
01 2345
^,
V
H^M —
1
c
If-""
K-
— i
— *
>
/
Y-
. -
s
/
t
AGITATOR
^X^(37 rpm, 3 Hp)
-* OXDATION TANK
/ COMPRESSED AIR
"—• _ INLET
r
SCALE, FEET
ELEVATION VIEW
Figure 6-8. Arrangement of the TCA Oxidation Tank with Air Sparger
6-31
-------
As in the testing with the air eductor, only limestone slurry with high fly
ash loading was used in tests with air sparger. Forced oxidation within the
scrubber loop using lime slurry was not expected to yield good S02 removal.
Seven runs were made using limestone slurry with high fly ash loading. In
addition, one run was made with limestone slurry and added magnesium oxide.
Each test lasted about 6 days.
A major shortcoming of this oxidation system was that the agitator was rated
at only 3 Hp and rotated at 37 rpm (compared with 17 brake Hp and 56 rpm for
the venturi oxidation tank). This agitator was similar in configuration to
the agitator in the venturi oxidation tank with two axial flow turbines (49
inches 1n diameter) pumping downward. Because of the weaker agitation, runs
with similar oxidation tank environment (pH, air stoichiometry, tank level,
percent slurry solids, and limestone utilization) had lower oxidation effi-
ciency in the TCA oxidation tank than in the venturi oxidation tank.
A 20-Hp variable speed agitator is on order and will be used to develop the
relationship between oxidation tank agitation and air requirements.
A second shortcoming was that the existing Shawnee air compressor did not
have sufficient capacity to serve the venturi and the TCA oxidation tanks
simultaneously at full flue gas load. To circumvent this problem, several
of the TCA runs were made at reduced flue gas flow rates. An additional air
compressor has been ordered to correct this limitation.
Table 6-5 summarizes the major test conditions and the important test results.
Detailed information concerning these runs can be found in Section 15 of
Reference 5.
6-32
-------
Table 6-5
SUMMARY OF ONE-SCRUBBER-LOOP FORCED-OXIDATION LIMESTONE TESTS
WITH AIR SPARGER ON THE TCA SYSTEM
Major Test Conditions*2^
cn
1
co
co
Fly ash loading
Flue gas rate, acfm 0 300°F
Slurry flow rate to TCA, gpm
Percent solids recirculated
Residence times, min: Oxidation tank
EHT
Oxidation tank level, ft
Air flow rate to oxidation tank
Limestone stoichiometric ratio (controlled)
TCA inlet pH (controlled)
Effective Mg** concentration, ppm
Limestone addition point
Total static height of spheres, inches
Selected Results
Percent S02 removal
Inlet SOg concentration, ppm
Percent sulfite oxidation
Air stoichiometry, atoms 0/mole S02 absorbed
TCA inlet pH
Oxidation tank pH
Limestone utilization, %
Gypsum saturation in TCA inlet liquor, %
Effective Mg'1"*' concentration, ppm
Onstream hours
815-2A
High
30,000
1000
15
5.2
14.4
18
130
1.3
EHT
20
89
3000
40
1.0
6.25
-
80
no
75
816-2A
High
30,000
1000
15
5.2
14.4
18
180
1.3
EHT
22.5
91
2850
54
1.40
6.25
5.7
76
100
48
817-2A
High
20,000
1000
15
5.2
14.4
18
130
1.3
EHT
22.5
79
3000
94
1.70
5.8
5.45
81
100
161
818-2A
High
25,000
1000
15
5.2
14.4
18
130
1.3
EHT
22.5
85
3000
67
1.25
6.2
5.65
77
95
131
818- 2B
High
25,000
1000
15
5.2
14.4
18
0
1.3
EHT
22.5 •
82
3300
24
0
6.2
.
81
110
140
819-2A
High
20,000
1000
15
4.9
17
130
1.3
"
Oxid. Tk
22.5
75
2800
94
1.90
5.55
5.55
77
110
164
820-2A
High
20,000
1000
15
4.9
17
130
5.9
Oxid. Tk
22.5
79
2500
92
2.0
5.65
5.65
62
115
259
fl?l-Pfl
ocl CM
High
30,000
1200
1 C
1 D
4.1
17
l /
170
1 J
1 . £.
-
5000
Oxid. Tk
15
fia
O*T
2500
QC
;?3
1 fi^
1 • U3
5 **R
J . J3
R 15
•J • O J
79
/ 7
110
4960
182
Notes:
-------
Despite oxidation tank agitator and air compressor limitations, forced oxidation
with an air sparger in a one-scrubber-loop TCA system was demonstrated. The
following conclusions were made from the test results:
0 With two tanks in series, 94 percent sulfite oxidation was achieved
at an air stoichiometry of 1.7, oxidation tank pH of 5.45, and an
oxidation tank level of 18 ft. Under similar oxidation tank envi-
ronment, higher oxidation efficiency (95-99 percent) was achieved
in the venturi oxidation tank. The poorer performance in the TCA
system was attributed to the weaker agitation in the TCA oxidation
tank.
• Higher air stoichiometry (about 1.9) was required to achieve a
similar degree of oxidation (94 percent) in a one-tank configuration
because of higher pH.
• Operation in the two-tank mode gave better limestone utilization
and S02 removal than the one-tank mode.
• As expected, magnesium oxide addition did not enhance the SO?
removal when oxidation was forced within the scrubber loop.
6.3 VENTURI/SPRAY TOWER BLEED STREAM OXIDATION
Bleed stream forced oxidation with limestone slurry and added magnesium oxide
was successfully demonstrated in a month-long .series of tests on the venturi/
spray tower system. Oxidized slurry from these tests had good dewatering
properties with filter cake solids concentration averaging about 84 percent.
Thus, It Is quite practical to improve the quality and reduce the volume of
waste solids In Installations Incorporating magnesium ion in the slurry
liquor by simple air/slurry contact of the bleed stream.
6.3.1 System Description
The venturi/spray tower system was arranged as shown In Figure 6-9 for the
bleed stream oxidation tests. Both the venturi and the spray tower slurries
6-34
-------
FLUE GAS
CO
en
COMPRESSED
VENT AIR
EFFLUENT
HOLD TANK
CLARIFIED LIQUOR
FROM SOLIDS
DEWATERING SYSTEM
BLEED TO
SOLIDS
DEWATER ING
SYSTEM
Figure 6-9. FLOW DIAGRAM FOR BLEED STREAM OXIDATION IN THE VENTURI/SPRAY TOWER SYSTEM
-------
discharged into a single hold tank to which limestone and magnesium oxide were
fed. A bleed stream was taken from the spray tower downcomer to take advantage
of the low pH at that point. The bleed stream was discharged to the oxidation
tank. All tests were conducted at an 18-ft oxidation tank level. Bleed from
the oxidation tank was dewatered by a clarifier and a filter in series.
6.3.2 Tests with Limestone/MgO
Four bleed stream oxidation runs were made on the venturi/spray tower system
using limestone with added magnesium oxide. All tests were conducted with
approximately 5000 ppm effective magnesium ion concentration in the slurry
liquor. Major test results are reported in Table 6-6. More detailed infor-
mation for these tests can be found in Section 8 of Reference 5.
The following conclusions were made from the bleed stream oxidation tests:
• Bleed stream oxidation is not expected to work with lime or lime-
stone slurries (without magnesium oxide addition). Slurry pH rise,
caused by the dissolution of residual alkali, prevents solid calcium
sulfite from dissolving and oxidizing in the liquid phase.
t Bleed stream oxidation of limestone slurry is feasible in the presence
of magnesium ion. Magnesium ion tends to buffer the pH rise from
dissolving residual alkali in the waste slurry solids, and it tends
to promote dissolved sulfite availability, allowing oxidation to take
place at a higher pH.
t Average sulfite oxidation of 96 percent or higher was achieved with
1.6 air stolcMometry, 5.4 to 6.3 oxidation tank pH, 18-ft oxidation
tank level, and 5000 ppm effective magnesium ion concentration. Oxi-
dation was consistently high even though oxidation tank pH rose to as
high as 6.7.
t Oxidized slurry in all runs had good dewatering properties, averaging
about 84 percent filter cake solids concentration.
• Oxidation of the bleed stream did not interfere with the enhancement
of SOp removal by the magnesium ion as was experienced when oxidation
was accomplished within the scrubber loop.
6-36
-------
Table 6-6
RESULTS OF FORCED-OXIDATION TESTS ON THE VENTURI/SPRAY TOWER BLEED STREAM
USING LIMESTONE SLURRY WITH ADDED MAGNESIUM OXIDE
Major Test Conditions
Fly ash loading
Flue gas rate, acfm G 300DF
Slurry rate to venturl .gpm
Slurry rate to spray tower, gpm
Percent solids recirculated (controlled)
EHT residence time, min.
Spray tower inlet pH (controlled)
Scrubber limestone stoichiometric ratio {control led)(based on solids)
Effective Mg concentration, ppm
Venturi pressure drop, in. H,0
Oxidation tank level, ft
A1r rate to oxidation tank, scfnr '
Recycle flow from oxidation tank to EHT, gpw
Selected Results
Percent S02 removal
Inlet SO, concentration, ppffl
Scrubber percent solids recirculated
Scrubber inlet liquor pH
Oxidation pH
Limestone utilization, % (based on total slurry)
Sulfite oxidation m oxidation tank, %
Sulfite oxidation in scrubber inlet slurry, 1
Gypsum saturation 1n scrubber Inlet liquor, X
Gypsum saturation In oxidation tank, %
Effective Mg** concentration in scrubber inlet liquor, ppm
Oxidation tank liquor sulflte concentration, ppm
Air stoichiometry, atoms 0/roole S02 absorbed
Filter cake solids, wt«(2>
Onstream hours
823-1A
High
18,000
600
1600
15
11.2
5.3
-
5000
9
18
110
30
94
2600
13.3
5.25
6.30
36
98
86
120
115
4990
66
1.55
83
205
824-1 A
High
35,000
600
1600
15
11.2
-
1.9
5000
9
18
210
30
88
2600
14.1
5.25
5.90
38
97
49
85
90
5215
105
1.60
85
159
825-1 A
High
18,000
600
1600
IS
11.2
-
1.4
5000
9
18
110
0
95
2500
14.7
5.45
5.65
64
97
39
105
115
5380
220
1.60
85
229
826- 1A
High
26,500(3)
600
1600
15
11.2
-
1.4
5000
9
18
210
0
89
2750
15.2
5.35
5.45
61
96
29
105
115
4970
230
2.0
84
246
Notes:
1) Air discharged downward through 3-1nch diameter pipe with an open elbow at center of oxidation tank about 3 inches from tank bottom.
2) Clarifier and filter in se>1es used for solids dewatering in all runs.
3) Desired flow rate was 35,000 acfm but problems with the venturl plug lifting mechanism limited the rate to 26,500 acfm.
-------
In two runs (Run 823-1A and 824-1A), 30 gpm of oxidized slurry was
recycled from the oxidation tank back to the scrubber effluent hold
tank in an attempt to reduce the pH difference between the two tanks.
However, the opposite occurred. The hold tank pH was depressed, re-
quiring excess limestone feed to maintain a pH of 5.3, resulting in a
very poor limestone utilization (less than 40 percent). This pheno-
menon was attributed to the limestone blinding by CaS03 precipitated
in the scrubber slurry loop. Sufficient CaS03 crystal seeds were
not available because the slurry had high gypsum content caused by
the recycle stream. The 30 gpm recycle flow proved to be unecessary
in the succeeding two runs (Run 825-1A and 826-1A). Without the re-
cycle flow, the pH difference betweeen the two tanks averaged only 0.1
and 0.2 pH units with the oxidation tank pH averaging 5.65 or less.
6-38
-------
Section 7
MATHEMATICAL MODEL FOR S0? REMOVAL
WITH CORRELATIONS OF SHAWNEE DATA
Correlations of data are presented here for sulfur dioxide (S02) removal
achieved by the Shawnee spray tower and TCA scrubbers between October 1973 and
November 1977. The data are for limestone and lime alkali with and without
magnesia (MgO) additive, and without forced oxidation.
The Shawnee spray tower has four spray banks on a 4-ft spacing, each with
seven nozzles with about 12 psi of pressure drop. The TCA contains three
beds of mobile packing spheres and four retaining grids. The sphere diameter
was 1.5 inches during the period in which the correlated data were obtained.
Fractional S0£ removal was measured both for short-term factorial tests (February
through April, 1976) with about 8 hours of steady-state operation, and for long-
term tests lasting four days or more (usually about one to four weeks), often
at widely fluctuating inlet S02 concentrations (1500 to 4500 ppm) and S02
removals. For most of the spray tower long-term tests the venturi scrubber
was operated at 9 in. 1^0 pressure drop and 600 gpm slurry flow rate in series
with and upstream of the spray tower. The factorial tests were specifically
designed for statistical analysis of S0£ removal data; the long-term tests
were primarily designed to demonstrate reliability of system operation. Run-
averaged data for the long-term tests sufficiently agree with the factorial
7-1
-------
data to justify overall correlation of both.
The correlations of Shawnee data for S02 removal follow the form of a semi-
theoretical mathematical model that is compatible with boundary constraints
on S02 removal and the operating variables (e.g., S02 removal between zero
and 100 percent, and zero removal at zero liquor rate). The correlations
permit reasonable extrapolations beyond the range of the fitted data. For
the TCA, the possibility of flooding (excessive pressure drop) should be
considered when extrapolating beyond the ranges of gas and slurry flow rates
investigated.
The variables strongly affecting S02 removal in the correlated tests were
slurry flow rate in the TCA (Section 9.1.3), liquid-to-gas ratio in the spray
tower, inlet liquor pH for both scrubbers, effective magnesium ion concentra-
tion for both scrubbers, and total height of mobile packing spheres in the
TCA. Limitations in the range of data did not permit a thorough understand-
ing of the effects of inlet gas S02 concentration and scrubber slurry nozzle
pressure drop on fraction 502 removal. The available data indicated that
fraction S02 removal decreases strongly with increasing inlet S02 concentra-
tion. In some cases minor effects of gas velocity and chloride ion concentra-
tion (Section 3.2.6) were present.
Shawnee correlations for S02 removal have been inserted into the Joint TVA/
Bechtel Economics Study Computer Program (Reference 16). The correlations
are used by TVA, Bechtel National Inc.'s Air Quality Group, and others for
preliminary design of new S02 wet scrubbing installations and for preliminary
estimation of S02 removal for planned tests at Shawnee.
7-2
-------
7.1 DEVELOPMENT OF THE MODEL
For absorption of S02 from the gas phase into the liquid phase, the following
differential equation applies (Reference 17):
[S02 - (S0p)e] dz
-v d(S02) = KGa [S02 - (S02)e] dz = ______ (7-1)
where:
KQ = overall gas mass transfer coefficient, based on both
liquid-side and gas-side resistances to mass transfer,
ft/sec
kG = gas-side mass transfer coefficient, ft/sec
k£ = liquid-side mass transfer coefficient for physical
absorption, ft/sec
a = gas-liquid interfacial area per scrubber volume, ft2/ft3
$ = average chemical reaction enhancement factor for mass
transfer in the liquid film, dimensionless
v = scrubber gas velocity, ft/sec
z = vertical distance in the scrubber, ft
S02 = mole fraction of SOo in the gas phase at a given value
of z
(S02)e = mole fraction of S02 in the gas phase that would be
in equilibrium with the liquid phase
H = Henry's Law constant for S02, mole fraction in gas/mole
fraction in liquor
Analysis of typical Shawnee limestone/lime wet scrubbing liquors, by use of
an equilibrium computer program developed by Radian Corporation and modified
by Bechtel (References 1 and 18), has shown that the equilibrium S02 is
much less than the actual S02. Also, a comparison of Shawnee limestone/lime
scrubbing data with earlier Shawnee data (June-August 1972) for gas-side
7-3
-------
controlled soda-ash scrubbing has shown that liquid-side resistance is
o
dominant, i.e., k|_ /H « kG, for 1 imestone/1 ime scrubbing (Reference 19).
Under these conditions of negligible (S02)e and (l/kGa), Equation 7-1 can
be simplified to:
-v d(S02) « (k£a$/H) S02 dz (7-2)
Integration of Equation 7-2 across the entire vertical height of the scrubber
and under the assumption that the ratio (k^a/H) 1s constant yields:
S°2 " 1 ' exP C-^L«/"v3 (7-3)
7.1.1 Physical Absorption
Equation 7-4 below represents the physical absorption group, k^a z/Hv,
In a form that fits boundary constraints on S0£ removal, slurry flow rate,
gas flow rate, and total height of spheres (TCfl only).
k£az/Hv « «! La2 (l/v)a3 exp («4 \ot ) (7-4)
where:
L • slurry flow rate per cross-sectional area, gpm/ft2
htot « total height of spheres In the TCA, Inches (zero for
the spray tower)
«'s » positive constant coefficients to be fitted to limestone/
lime wet-scrubbing data
Equation 7-4 conforms to the expectation that (k£a) increases with slurry
o
flow rate (Reference 17) and that (k|_az) in the TCA increases with height
of spheres.
7-4
-------
7.1.2 Chemical Reaction
The parameter $ in Equation 7-3 represents the chemical reactivity of the
scrubber liquor with absorbed S02 gas. This chemical reactivity should
increase with increasing scrubber liquor pH, increasing effective magnesium
ion concentration, and decreasing inlet gas $02 concentration. An empirical
relationship for $, expressed in terms of these chemical operating variables
and compatible with boundary constraints on S02 removal, is:
£ = exp [a5 pH1 +a6 (Mg)fi -ay (S02)i ] (7-5)
where:
= scrubber inlet liquor pH
(Mg)e = effective magnesium ion concentration, ppm
= [ppm Mg++ - (ppm Cr/2.92)] for Mg++ > CT/2.92
= 0 for Mg** <. CT/2.92
where 2.92 = ratio by weight of Cl~ to Mg++ in MgCl2
-j = scrubber inlet gas S02 concentration, ppm
= positive constant coefficients fitted to the data
The increase in chemical reactivity with an increase in pH is due to the
additional alkali stoichiometry needed to maintain the higher pH.
Chemical reactivity can also be increased by addition of magnesia (MgO).
Dissolution of MgO into the liquor provides Mg++ ion, thus increasing the
total cation concentration. To maintain electroneutrality additional anions
must be dissolved. Therefore, the concentrations of sulfite and sulfate as
ionic sulfite, bisulfite, and sulfate (S03=, HS03", and S04=) increase with
7-5
-------
increasing magnesium. The sulfite ion, S03~, and its ion pair with magne-
sium, MgS03 (which also increases as both Mg++ and S03= increase), can react
with incoming S02 gas to form bisulfite ion, HS03~.
S02 (aq) + S03= + H20 «=* 2 HS03~ (7-6a)
S02 (aq) + MgS03 + H20 +± 2 HS03~ + Mg++ (7-6b)
This removal of aqueous S02 by chemical reaction increases the ability of the
liquor to absorb more S02.
Any chloride present in the liquor reacts with magnesium to form MgCl2,
which does not react with S02. Magnesium stoichiometrically equivalent
to measured chloride is subtracted from the total dissolved magnesium to
obtain the effective magnesium ion concentration.
Equation 7-5 predicts that S02 removal efficiency decreases with increasing
(S02)1-. For the mass transfer conditions in limestone/lime scrubbing, i.e.,
negligible (S02)e and negligible gas phase resistance, S02 (aq) at the gas-
liquid interface increases in direct proportion to the S02 gas concentration.
This increase in S02 (aq) lowers the pH at the interface, reducing liquor
reactivity and the fraction of acidic S02 gas absorbed. This decrease in S02
removal with increasing S02 gas concentration has also been observed at other
limestone/lime wet scrubbing installations (References 20, 21, and 22).
7.1.3 Final Form of the Model
The semi-theoretical form of the model for fraction S02 removal is obtained by
combining Equations 7-3 through 7-5:
7-6
-------
Fraction S02 = i _ exp
Removal
exp [0.4 htot + a
- «
7
(7-7)
For the spray tower with lime an additional term, <*g Cl (Cl = Dissolved
chloride ion concentration, ppm) was required in Equations 7-5 and 7-7
to adequately correlate the data. This is discussed further below.
7.2 CORRELATIONS OF SHAWNEE DATA FOR S02 REMOVAL
Equation 7-7 has been correlated to Shawnee spray tower and TCA limestone/lime
wet scrubbing data. The resulting correlations are summarized in Table 7-1.
The correlations explain about 88 percent of the variation in the data, i.e.,
the square of the correlation coefficient is 0.88. The standard errors of
estimate are about four percent S02 removal.
The operating variables having the greatest statistical significance in fit-
ting the data were slurry flow rate in the TCA, liquid-to-gas ratio (propor-
tional to L/v) in the spray tower, scrubber inlet liquor pH, effective
magnesium, and total height of spheres in the TCA.
The correlated data cover the following ranges of the operating variables:
L = 14-32 gpm/ft2 for the spray tower and 18-38 gpm/ft2 for
the TCA
v = 5.3-9.3 ft/sec for the spray tower and 8.3-12.5 ft/sec
for the TCA
htot = 0-22.5 inches
pH.j = 5.1-5.9 for limestone and 6.0-9.0 for lime
(Mg)e = 0-10,000 ppm for limestone, 0-2500 ppm for the spray
tower with lime, and 0-4000 ppm for the TCA with lime
(S02)i = 1500-4500 ppm for the TCA with limestone, and 2300-
3500 ppm otherwise
Cl = 1000-20,000 ppm
7-7
-------
For the TCA scrubber with limestone alkali Figure 7-1 shows measured percent
S02 removals and those predicted by Equation 7-7 with the coefficients
indicated in Table 7-1. Figure 7-1 shows that the fit is good for both the
100 factorial tests and the 82 long-term tests.
The effect of (S02)-j for the TCA with limestone was determined as a-j = 1.5 x 10~
This is in good agreement with a separate analysis of 213 individual data points
from Shawnee TCA limestone long-term Runs 535-2A and 535-2B and with an analysis
of four limestone data points at varying (S02)-j from a 300-acfm TCA at the EPA-
IERL pilot plant (Reference 4 and 20). The two Shawnee runs operated for 2325
hours from September through December, 1974, with an inlet S02 range of 1500 to
4900 ppm. The pilot plant data covered an inlet S02 range of 400 to 4600 ppm.
The coefficient a-j in Table 7-1 for cases other than TCA with limestone should
be regarded as less accurate simply because of the narrow range of the run-
average values of inlet S02 concentration available for these cases. Therefore,
for these other cases, caution should be exercised when extrapolating the
inlet S02 concentration beyond the narrow range of 2300 to 3500 ppm indicated
abcve.
The chloride term, UQ Cl, for the spray tower with lime (see Table 7-1) was
required to explain higher percent S02 removal in factorial testing (at 5000 to
13,000 ppm chloride) than in long-term testing (at 1000 to 7000 ppm chloride).
The chloride term increases the percent of the variation explained for the
overall spray tower lime data from 65 percent to 82 percent. However, such
effect was not noted in the other three cases. Further work is needed in this
area to substantiate the effect of chloride on pH and S02 removal postulated
in Section 3.2.6.
7-8
-------
100
90
O 80
ui
C
CM
S 70
oc
UJ
a.
O
ui
g 60
QC
a.
50 -
40
FIGURE 7-1.
PREDICTED (EQUATION 7-7) VERSUS
MEASURED SO2 REMOVAL - TCA WITH LIMESTONE
O FACTORIAL TESTS
O LONG-TERM TESTS
50 60 70 80
MEASURED PERCENT SO2 REMOVAL
90
100
7-9
-------
Table 7-1
CORRELATION FOR PREDICTIONS OF SO? REMOVAL
BY LIMESTONE/LIME WET SCRUBBING WITH A SPRAY TOWER OR A TCA
Fraction S02 - 1 - expj- ajLa-2 ( J)a3 exp [
Removal f \ / L
exp a4 htot
+ o
+o6 (Mg)e -ay (S02)i
C1 !
J '
Definition of Variables
i
o
L
V
ntot
PH1
(Mg)e
Cl
slurry flow rate in scrubber, gpm/ft
gas velocity 1n scrubber, ft/sec
total height of TCA spheres, in
scrubber Inlet liquor pH
effective magnesium 1on concentration, ppm
inlet gas S02 concentration, ppm
total chloride ion concentration, ppm
°2
°3
°4
a5
°6
°8
Number of
data points
Percent of
variation
explained
Standard
error of
estimate
Spray Tower
Limestone
1.37 x 10"3
1
1
0
1
1.25 x lO'4
0
0
77
90
4.2
Lime
0.082
1
1.36
0
0.29
3.2 x 10~4
9.5 x 10-5
5.2 x 10-5
64
82
4.5
TCA
Limestone
2.0 x 10"3
0.71
0
0.030
0.72
8.4 x TO'5
1.5 x 10'4
0
182
88
4.3
Lime
0.0187
1
0
0.026
0.16
1.6 x ID'4
2.9 x 10'4
0
54
93
3.6
-------
For design purposes pH values used in the correlations should not exceed
5.6 for the spray tower with limestone, 5.8 for the TCA with limestone, and
8.0 for lime. For correlated Shawnee tests at higher pH values, alkali
stoichiometries (uncontrolled) were often high enough to result in scaling
problems for long-term operation.
7.3 PARAMETRIC PLOTS DERIVED FROM THE CORRELATIONS
Figures 7-2 through 7-9 show predictions of S02 removal by the correlations
in Table 7-1 (constants for Equation 7-7 fitted to Shawnee data) for an inlet
S02 concentration of 2500 ppm, and for other operating conditions as indicated
on the figures.
Figure 7-2 shows the effects of slurry flow rate and total height of spheres
on S02 removal for the TCA with limestone operating at a high inlet liquor
pH of 5.8 without additives. For a total sphere height of 15 inches, an
increase in slurry flow rate from 20 to 40 gpm/ft2 increases S02 removal from
about 70 to about 85 percent, thus reducing S02 emission by a factor of two.
At a slurry flow rate of 30 gpm/ft2, increasing the total height of spheres
from zero to 22.5 inches increases S02 removal from about 65 to about 85
percent, reducing S02 emission by more than a factor of two.
Figure 7-3 presents the effects of scrubber inlet liquor pH on S02 removal
for the TCA with limestone, 15 inches of spheres, and no additive. Slurry
P
flow rate is shown as a parameter. For a slurry flow rate of 30 gpm/ft£, an
increase in scrubber inlet pH from 5.2 to 5.8 increases S02 removal from
about 65 percent to about 80 percent.
7-11
-------
FIGURE 7-2.
PREDICTED (EQUATION 7-7) SO2 REMOVAL AS A FUNCTION OF
SLURRY FLOW RATE AND TOTAL HEIGHT OF SPHERES - TCA WITH LIMESTONE
100
90
80
O
ui
oc
CM
70
UI
u
c
in
a.
60
SO
40
SCRUBBER INLET LIQUOR pH - 5.8
EFFECTIVE LIQUOR MAGNESIUM CONCENTRATION
zero
15
20
25 30 35
SLURRY FLOW RATE, gpm/ft2
40
45
7-12
-------
FIGURE 7-3.
PREDICTED (EQUATION 7-7) SO2 REMOVAL AS A FUNCTION OF
SCRUBBER INLET LIQUOR pH AND SLURRY FLOW RATE • TCA WITH LIMESTONE
100
90
80
UJ
8 70
UJ
U
cc
UJ
Ou
60
50
40
T
T
T
T
TOTAL HEIGHT OF SPHERES = 15 inches
EFFECTIVE LIQUOR MAGNESIUM CONCENTRATION = zero
4.8
5.0
J.
JL
_L
JL
_L
5.2 5.4 5.6
SCRUBBER INLET LIQUOR pH
5.8
6.0
7-13
-------
FIGURE 7-4.
PREDICTED (EQUATION 7-7) SO2 REMOVAL AS A FUNCTION OF EFFECTIVE
LIQUOR MAGNESIUM CONCENTRATION AND SLURRY FLOW RATE -TCA WITH LIMESTONE
100
90
80
oc
CM
8
70
u
oc
iu
a.
60
50
40
SCRUBBER INLET LIQUOR pH = 5.5
TOTAL HEIGHT OF SPHERES = 15 inches
I
I
2,000 4,000 6,000 8,000 10,000
EFFECTIVE LIQUOR MAGNESIUM CONCENTRATION, ppm
12,000
7-14
-------
FIGURE 7-5.
PREDICTED (EQUATION 7-7) SO2 REMOVAL AS A FUNCTION OF
LIQUID-TO-GAS RATIO AND SCRUBBER INLET LIQUOR pH -SPRAY TOWER WITH LIMESTONE
100
90
80
O
ui
oc
CM
8
H
UJ
O
OC
UJ
Q.
70
60
50
40
20
EFFECTIVE LIQUOR MAGNESIUM CONCENTRATION = zero
30 40 50 60
LIQUID-TO-GAS RATIO, gal/mcf (saturated)
70
80
7-15
-------
FIGURE 7-6.
PREDICTED (EQUATION 7-7) SO2 REMOVAL AS A FUNCTION OF EFFECTIVE
LIQUOR MAGNESIUM CONCENTRATION AND
LIQUID-TO-GAS RATIO - SPRAY TOWER WITH LIMESTONE
100
90
80
UJ
K
CM
70
u
oc
ui
60
50
40
_L
J.
SCRUBBER INLET LIQUOR pH - 5.5
J 1 1 1 I
2,000 4,000 6,000 8,000 10,000
EFFECTIVE LIQUOR MAGNESIUM CONCENTRATION, ppm
12.000
7-16
-------
FIGURE 7-7.
PREDICTED (EQUATION 7-7) SO2 REMOVAL AS A FUNCTION OF
SCRUBBER INLET LIQUOR pH AND SLURRY FLOW RATE - TCA WITH LIME
100
90
TOTAL HEIGHT OF SPHERES = 15 inches
EFFECTIVE LIQUOR MAGNESIUM CONCENTRATION
zero
80
5
§
UJ
a.
CM
H
UJ
u
cc
UJ
0.
70
60
4Q
50
40
6
SCRUBBER INLET LIQUOR pH
7-17
-------
FIGURE 7-8.
PREDICTED SO2 REMOVAL AS A FUNCTION OF SLURRY FLOW RATE
AND EFFECTIVE LIQUOR MAGNESIUM CONCENTRATION - TCA WITH LIME
100
90
80
UJ
oc
M
8
UJ
O
cc
UJ
60
50
40
15
T
T
T
T
_L
TOTAL HEIGHT OF SPHERES - 15 inches
SCRUBBER INLET LIQUOR pH - 8.0
1 1 '
20
25 30 35
SLURRY FLOW RATE, gpm/ft2
40
45
7-18
-------
FIGURE 7-9.
PREDICTED (EQUATION 7-7) SO2 REMOVAL AS A FUNCTION OF SCRUBBER INLET
LIQUOR pH AND LIQUID-TO-GAS RATIO - SPRAY TOWER WITH LIME
100
90
80
ui
oc
CM
8 70
UJ
O
OC
60
50
40
i • I •
GAS VELOCITY- 7.5 ft/sec
LIQUOR CHLORIDE CONCENTRATION = 10.000 ppm
EFFECTIVE MAGNESIUM CONCENTRATION = zero
6
8
SCRUBBER INLET LIQUOR pH
7-19
-------
Figure 7-4 shows the effect of magnesium additive on S02 removal for the TCA
with limestone, scrubber inlet pH of 5.5, and a total sphere height of 15
inches. Slurry flow rate is the parameter. For a slurry flow rate of 30
gpm/ft2, the addition of 5000 ppm effective magnesium to the scrubber liquor
increases S02 removal from about 70 to about 85 percent, cutting SOp emission
by a factor of two. Addition of 10,000 ppm effective magnesium increases S0?
removal to 95 percent. Such high S02 removal is unattainable without additive
for the Shawnee TCA with limestone at reliable operating conditions.
Figure 7-5 shows the effects of spray tower liquid-to-gas ratio (L/G) and
spray tower inlet pH on S02 removal for limestone without additive. For a pH
of 5.4 an increase in L/G from 30 to 70 gal/mcf increases spray tower SOo
removal from 42 to 72 percent, corresponding to emission decrease by a factor
of two. For an L/G of 50 gal/mcf an increase in spray tower inlet pH from
5.2 to 5.6 increases S02 removal from 52 to 67 percent. Note that for the
spray tower alone with limestone and an inlet S02 concentration of 2500 ppm,
S02 removal is limited to about 83 percent for reliable operation (pH » 5.6,
stoichiometry about 1.3-1.4) at an L/G of 80 gal/mcf.
Figure 7-6 shows the effect of magnesium additive on S02 removal for the spray
tower with limestone at an inlet pH of 5.5. Spray tower L/G is the parameter.
For an L/G of 50 gal/mcf addition of 5000 ppm of effective magnesium to the
liquor increases S02 removal from about 65 to about 85 percent, reducing S0?
emission by more than a factor of two. Addition of 10,000 ppm magnesium
increases S02 removal to 97 percent, far better than the spray tower can
achieve without additive even at very high L/G and stoichiometry.
7-20
-------
Figure 7-7 shows the effect of TCA inlet liquor pH on S02 removal with lime
at a total sphere height of 15 inches. The parameter is slurry flow rate.
For a slurry flow rate of 30 gpm/ft2 an increase in pH from 6.0 to 8.0
increases S02 removal from 65 to 77 percent.
Figure 7-8 shows the effects of slurry flow rate and effective magnesium
concentration on S02 removal for the TCA with lime, an inlet pH of 8.0, and
a total sphere height of 15 inches. With no magnesium additive an increase
in slurry flow rate from 20 to 40 gpm/ft2 increases S02 removal from about
60 to 85 percent, cutting S02 emission by a factor of two and a half. This
is slightly stronger than the corresponding effect with limestone (see Figure
7-2).
For a slurry flow rate 30 gpm/ft2 addition of 2000 ppm effective magnesium
increases S02 removal from 76 to 86 percent; addition of 4000 ppm effective
magnesium increases the removal to 94 percent. Thus for the TCA, magnesium
additive is even more effective with lime than with limestone (compare Figure
7-8 with Figure 7-4).
Figure 7-9 shows the effects of spray tower inlet pH and L/G on S02 removal
for lime alkali. The curves correspond to those predicted from Table 7-1
with a chloride concentration of 10,000 ppm and a gas velocity of 7.5 ft/sec,
average values for the spray tower lime factorial runs.* For an L/G of 50
* It is recommended that these values of gas velocity =7.5 ft/sec and
chloride = 10,000 ppm be used by anyone using Equation 7-7 as correlated
in Table 7-1 for design of a spray tower lime scrubbing system. The effects
of gas velocity and chloride on SOo removal are unverified, and are statis-
tically far less significant than the effects of pH, liquid-to-gas ratio,
and magnesium concentration.
7-21
-------
gal/mcf an Increase in spray tower inlet pH from 6.0 to 8.0 increases S0£
removal from about 60 percent to 80 percent, cutting emission by a factor of
two. The lime pH effect for the spray tower is stronger than that for the
TCA (see Figure 7-7).
Figure 7-9 also indicates that, for an inlet pH of 8.0, increasing the L/G
from 30 to 70 gal/mcf increases S02 removal from 62 percent to nearly 90
percent, reducing S02 emission by almost a factor of four.
7-22
-------
Section 8
CALCULATION OF GYPSUM SATURATION
Monitoring of gypsum (calcium sulfate dihydrate) saturation is important because
Shawnee testing has demonstrated that scaling usually occurs whenever the satura-
tion exceeds about 135 percent. This section presents simplified equations for
the calculation of gypsum saturation from the measured concentrations of calcium,
magnesium, and sulfate ions. These equations were fitted to the predictions of
gypsum saturation made by the Bechtel-Modified Radian Equilibrium Computer
Program (Reference 1) for liquors sampled from the Shawnee lime and limestone
long-term reliability tests. These equations are used to calculate the gypsum
saturation in the Shawnee database.
Equations 8-1 and 8-2 predict the degree of gypsum saturation in lime/limestone
wet-scrubbing liquors, at 25 and 50°C, respectively. The equations have been
fitted to results from the Bechtel-Modified Radian Equilibrium Computer Program.
At 25°C:
Fraction Gypsum Saturation = (Ca) (S04) 1*300 + 76~j (8-1)
8-1
-------
At 50°C:
Fraction Gypsum Saturation = (Ca) (S04) 263 + 47~j (8-2)
where
I = 3 [(Ca) + (Mg)] + (S04) (8.3)
= ionic strength of the liquor (g-mole/1), assuming the liquor
contains only Ca"1"*", Mg"*"*", S04=, and Cl" ions in solution.*
(Ca)
(Mg) = measured dissolved concentrations of total calcium, magnesium,
($64) and sulfate, respectively, g-mole/1iter.
Equations 8-1 and 8-2 can be used for simple, accurate, and convenient prediction
of gypsum saturation by those not having access to the modified Radian program.
*From the ionic balance: (Cl) = 2 [(Ca) + (Mg) - (S04)]. Therefore, I = 1/2
ZMfZj2 = 1/2 [4 (Ca) + 4 (Mg) + 4 (S04) + (Cl)] - 3*[(Ca) + (Mg)] + S04, where
M.J is the molarity of component i and Zj is its unit charge. Note that K and
Na concentrations are low at Shawnee and, therefore, have not been included in
Equation 8-3. However, preliminary evaluation of liquor compositions from
other limestone and lime installations has indicated that the effect of high
dissolved sodium is accounted for by adding the dissolved Na concentration
(g-mole/1iter) to the ionic strength, I.
8-2
-------
Equations 8-1 and 8-2 agree with the modified Radian program to within a standard
error of about 0.04 fraction saturation for the following ranges of variables:
Liquor pH: 4.0 - 9.0
Radian-predicted fraction of gypsum saturation: 0.2 - 3.0
Dissolved concentrations (m-mole/liter):
Calcium 4 - 140
Magnesium 0 - 600
Sulfate 10 - 400
Sulfite 0 - 100
Chloride 0 - 400
To the extent that the Radian program itself is accurate, Equations 8-1 and
8-2 are sufficiently accurate for limestone/lime scrubbing liquors containing
both magnesium and chloride ions up to 15,000 ppm.
8-3
-------
Section 9
SCRUBBER CHARACTERISTICS
This section is intended to acquaint the reader with the mechanical operating
characteristics of the TCA, venturi and spray tower scrubbers. The pressure
drop, turndown characteristics, and ranges of operating conditions for these
scrubbers are discussed. The information is taken from detailed findings
presented in earlier progress reports (References 1, 2, 3, 4, and 5),
9.1 TURBULENT CONTACT ABSORBER (TCA)
9.1.1 Description
The TCA was manufactured by Universal Oil Products (UOP). It operates with up
to three beds of low-density spheres, nominally 1-1/2 inches in diameter, free
to move between retaining grids. As the incoming flue gas contacts the slurry
in these beds, both S02 and particulates are removed. The cross-sectional
n ij
area of the TCA scrubber is 32 ft , over the scrubbing section and 49 ft£
across the mist eliminator section.
Figure 9-1 is a schematic of the scrubber. The chevron mist eliminator used
during the latest testing period is depicted to scale in Figure 9-2. The TCA
is capable of treating approximately 30,000 acfm (at 300°F) of flue gas from
9-1
-------
GAS OUT
MIST ELIMINATOR
WASH WATER
CHEVRON MIST
ELIMINATOR
RETAINING
BAR-GRIDS
GAS IN
o o o
flyP-2 £0j
y* 0°
o o
MIST ELIMINATOR
WASH LIQUOR
INLET SLURRY
MOBILE PACKING
SPHERES
i-
5'
H
APPROX. SCALE
EFFLUENT SLURRY
Figure 9-1. Schematic of Three-Bed TCA
9-2
-------
THREE-PASS, OPEN-VANE, 316L SS
CHEVRON MIST ELIMINATOR
(HORIZONTAL CONFIGURATION)
GAS FLOW
6 in.
Figure 9-2. Test Facility Mist Eliminator Configuration
9-3
-------
Boiler No. 10, approximately 10 MW of power plant capacity.
The boiler normally burns a medium to high sulfur bituminous coal producing
S02 concentrations of 1500 to 4500 ppm in the flue gas. Ductwork connections
are provided both upstream and downstream of the particulate removal equipment,
allowing scrubber operation with flue gas having either high fly ash loadings
(3 to 6 grains/dry scf) or low fly ash loadings (0.04 to 0.20 grain/dry scf).
9.1.2 TCA Pressure Drop and Holdup Characteristics
Pressure drop and liquid holdup tests were made during an April-June 1977
boiler outage with air and water and with 0, 5, 7.5, and 10 inches per bed (3
beds, 4 grids) of 6.5-gram, 1-5/8 inch nitrile foam spheres. Water flow rates
ranged from 19 to 44 gal/min-ft2. Superficial air velocities varied from 7.5
to 13 ft/sec in the pressure drop tests, and from 0 to 11.4 ft/sec in the
liquid holdup tests. The pressure drop across the three beds, including the
slurry spray nozzles, was measured between a point 28 inches below the bottom
bed, (35 inches directly above the inlet duct) and a point 40 inches above the
top bed (see Figure 9-1 for a TCA schematic).
Results of the pressure drop/flood tests are presented in Figures 9-3 through
9-6. Pressure drop increases with liquor flow rate and air velocity. Other
data collected during these tests indicated that flooding* usually occurred
at 8 to 10 inches t^O pressure drop for the three-bed TCA. Liquid holdup in
the scrubber ranged from 40 to 250 gallons.
The following equation for pressure drop across the three TCA beds and four
* Flooding is characterized by a large increase in pressure drop for a small
increase in gas velocity, and by large fluctuations in pressure drop at
constant gas velocity.
9-4
-------
* 3
I
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9.0 10.0 11.0
SUPERFICIAL AIR VELOCITY, fpi « 87° F
170
13.0
-I-
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14,000 16,000 18,000 20,000 22,000
AIR FLOW RATE, «cfm « 87° F
24.000
26.000
Figure 9-3.
TCA Bed Pressure Drop (3 Beds, 4 Grids) -
0 inches Total Bed Height of Nitrile Foam Spheres
9-5
-------
14
13
iax
11
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.s
BED PRESSURE DROI
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» 8.0 9.0 1OO 11.0 124 1&0
7
SUPERFICIAL AIR VELOCITY, «m • H° F
u.ooo ie,ooo 18.000 20,000 22^100
AIR FLOW RATE^cim • 86° F
24.000
29.000
Figure 9-4. TCA Bed Pressure Drop (3 Beds, 4 Grids) -
15 inches Total Bed Height of NltrMe Foam Spheres
9-6
-------
14 •
13
12 •
11 •
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9.0 10.0 11.0 12.0 13.0
SUPERFICIAL AIR VELOCITY, f pi 987° F
18.000 20.000 22.000 24.000 26.000
AIR FLOW RATE, acfm @ 87° F
Figure 9-5. TCA Bed Pressure Drop (3 Beds, 4 Grids) -
22.5 inches Total Bed Height of Nitrile Foam Spheres
9-7
-------
15
14 . •
13
12
11
* 10
Q
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0 43.8911/min-ft2 ^ REPLICATES
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7.0 8.0 9.0 10.0 11.0 12.0 13.0
SUPERFICIAL AIR VELOCITY, fp«099° F
I I 1 I 1 1 1
14.000 16.000 18.000 20.000 22.000 24.000 26,000
AIR FLOW RATE, wfm 0 99° F
Figure 9-6, TCA Bed Pressure Drop (3 Beds, 4 Grids) -
30 inches Total Bed Height of Nitrile Foam Spheres
9-8
-------
grids* was fitted to 164 air/water data points:
AP = (AP)NS + 0.0363 v Hs°'69 exp (0.014 L) (9-1)
with
(AP)NS = 0.095 v exp (0.021 L) (9-2)
where:
AP = TCA pressure drop for three beds and four grids, in H20**
(AP)NS = TCA pressure drop for four grids (no spheres), in H20**
v = superficial air velocity, ft/sec at 90°F
L = liquor flow rate per unit scrubber cross-sectional area,
gpm/ftz
Hs = total static bed height of 1-5/8 in. diameter 6.5-gram
nitrile foam spheres, in.
The fitted ranges of the variables in Equations (9-1) and (9-2) are given
below:
AP = 0.9 to 8.0 in. H20
v = 7.6 to 13.1 ft/sec
L = 19 to 44 gpm/ft2
Hs = 0 to 30 in.
All measured pressure drops in excess of 8.0 inches H20 were excluded from the
correlation because of incipient flooding. Any case for which Equation (9-1)
predicts a pressure drop greater than 8.0 inches H20 is likely to be in the
flooding region.
* The grids consist of 3/8-in. diameter bars with a center-to-center distance
of 1-1/4 inch, leaving 70 percent free area excluding support frames.
** Measured from below the bottom grid to above the top grid, including slurry
spray nozzles.
9-9
-------
Measured TCA bed pressure drops with spheres (107 data points) and the
corresponding predictions from Equation (9-1) are shown in Figure 9-7.
Equation (9-1) accounts for 96 percent of the variation in the data with
a standard error of estimate of 0.24 inches H20.
Measured TCA bed pressure drops without spheres (57 data points) and the
corresponding predictions from Equation (9-2) are shown in Figure 9-8.
Equation (9-2) accounts for 90 percent of the variation with a standard
error of 0.15 inches H20.
For the overall (spheres and no spheres) data, Equation (9-1) explains 99
percent of the variation with a standard error of 0.21 inches H20.
The form of Equation (9-1) was chosen to meet boundary constraints on pressure
drop for limiting values v, L, and Hs- For example, the equation predicts
zero pressure drop at zero gas velocity.
Scrubber liquid holdup ranged from 40 to 250 gallons over the range of condi-
tions studied. Reported volumes are accurate to +. 25 gallons. The following
summarizes scrubber holdup under typical operating conditions and the effect
on holdup of changing major process variables:
Typical operating conditions of 11.2 ft/sec, 210 gallons scrubber
37.5 gal/min-ftS and 15 inches total sphere holdup
height
Effect of air velocity increase from 7.5 to Holdup increase by
11.2 ft/sec 20-60 gallons
Effect of liquor rate increase from 18.8 to Holdup increase by
37.5 gal/min-ftz 40-120 gallons
Effect of sphere height increase from 0 to Holdup increase by
30 inches 70-110 gallons
9-10
-------
8
O
CM
X
Q.
O
oc
O
ai
oc
I
LLJ
CC
Q.
O
UJ
CD
Q
UJ
g
O
ui
OC
CL
7 •-
6 ••
5 -•
4 ••
MEASURED BED PRESSURE DROP, in. H2O
Figure 9-7. COMPARISON OF EXPERIMENTAL DATA AND PREDICTED
VALUES OF BED PRESSURE DROP - THREE-STAGE TCA
WITH 1-5/8 inch DIA.. 6.5 gram SOLID NITRILE FOAM
SPHERES
9-11
-------
00^
00
O
-------
9.1.3 TCA Turndown
In the TCA it has been shown repeatedly that variation in the flue gas flow
rate (gas velocity) does not significantly affect the S02 removal at a constant
slurry flow rate. Although the liquid-to-gas ratio increases when the gas
velocity is reduced, the gain in SC^ removal from higher liquid-to-gas ratio
is offset by the decreased sphere activity.
Because of the decreased sphere activity, prolonged operation of the TCA at
reduced gas velocity will result in caking of the spheres, especially under
conditions that give high scaling potential. Decreased sphere activity could
also result in channeling. The possibility of flue gas channeling is known to
be higher for larger units; uniform flow is harder to maintain where the ratio
of the scrubber diameter to the depth of sphere bed is greater. Therefore
caution should be used in extrapolating to larger units the observed flatness
of SC>2 removal response to change in gas velocity.
9.1.4 Spheres and Sphere Life
During more than six years of testing on the TCA, (March 1972 through June 1978)
several types of spheres were tested and evaluated for performance and reli-
ability. All spheres tested at Shawnee were purchased from Universal Oil Pro-
ducts (UOP).
The original batch of spheres supplied with the scrubber were 1-1/2 inch
polypropylene and polyethylene plastic spheres. Wear data on these indicated
a weight loss of about 27 percent after approximately 1000 hours of operation.
Continued erosion of the sphere shell resulted in the eventual collapse of
9-13
-------
these spheres and subsequent filling with slurry. These heavier slurry-filled
spheres settled to the bottom of the support grids, where they became immobile.
The next batch of spheres consisted of the 5-gram thermoplastic rubber (TPR)
spheres and high density polyethylene (HOPE) spheres. After 500 hours of
operation the TPR spheres lost about 2.6 percent of their original weight and
the HOPE spheres lost from 8 to 14 percent (as contrasted with an original
supplier's estimate for HOPE sphere life of approximately 2000 hours). About
one percent of the TPR spheres came apart at the seams. Continued operation
for approximately 2500 hours with the TPR spheres resulted in dimpling on one
side, about 2.4 percent seam failure, and an average weight loss of about 6
percent. Dimpled spheres, because of the reduced diameter, tended to fall
through the retaining bar grids.
The 5-gram TPR and HOPE spheres were replaced with 6-gram TPR spheres. Although
these heavier TPR spheres were expected to reduce the dimpling previously expe-
rienced with 5-gram spheres, a significant reduction did not occur. The failure
rate for the 6-gram TPR spheres is plotted in Figure 9-9. After 3800 hours of
testing approximately 11 percent of the spheres had failed from splitting at
the seams. The average weight losses for the unsplit spheres in each bed were
12.0 percent at the top, 9.2 percent in the middle, and 7.7 percent at the
bottom. Most of the testing was performed at 12.5 ft/sec scrubber gas velocity
and 15 percent solids.
All the TPR spheres were subsequently replaced with new 6.5-9ram nltrile rubber
solid foam spheres. After 240 hours of operation a sample was removed and
examined. The spheres still had their original color and looked clean,
although they had lost their smooth, new appearance. The surfaces were slightly
9-14
-------
IO
I
3.500
3.000
2,500
c/>
UJ
GC
«J
<
«• 2,000
111
NUMBER OF SPHERI
«
•
1.000
500 •
n
9 4 ft/sec SCRUBBER GAS VELOCITY
12.5 ft/sec _ _ 12.5ft/iec
CO
O
°^
0° y
O 1,500 SPHERES/BED
ADDED TO TOP 2 BEDS
0
o
o
0
0
o
o
CP°
o
00
0°
o
3 BEDS
o 10.000 SPHERES/BED
rCP SLURRY SOLIDS PERCENT = 15
00°
0°°
0 .,,.,.,
• 11
• 10
• 9
• 8
UJ
PERCENT SPHERE
3
2
1
0
500
1,000 1,500 2,000
TOTAL TIME.Hr
2,500
3,000
3,500
4,000
Figure 9-9. Failure Rate of 6-Gram TPR Spheres in Limestone/
Fly Ash Slurry Service
-------
roughened, open pores were visible under a microscope, and mold seams were
still apparent. They did not look wet, nor could water be squeezed from them,
but prior to drying they weighed approximately 9 percent more than new, unused
spheres. After drying for'3 days at 45°C to 60°C, comparison of the new and
used spheres showed, for the used:
Weight loss = 1 percent
Diameter loss = 9 percent
Volume loss = 25 percent
Because the mold seams were still visible and because there was little weight
loss after drying, it was presumed that the spheres had shrunk. After 574
hours of operation the spheres were again sampled. After acid washing and
drying they were unchanged from their previous condition at the end of 240
operating hours.
After 3 months of testing 6.5-gram nitrile foam spheres were replaced with new
6.3-gram nitrile foam spheres . The 6.3-gram foam spheres were tested for
3888 hours without significant failure. With the previously tested hollow TPR
spheres, over 11 percent of the spheres had failed at this service life (see
(Figure 9-9).
In the first 1773 hours of operation with the 6.3-gram foam spheres the losses
in diameter and weight were 12 percent and 4 percent, respectively. Continued
exposure for an additional 2115 hours resulted in a 23 percent diameter loss
and 21 percent weight loss. Figure 9-10 illustrates the spheres diameter loss
during the monitoring program. Comparison of the performance of these 6.5-gram
nitrile foam spheres with 6.3-gram nitrile foam spheres tested earlier indicated
a significant improvement in quality. External appearances of the 6.3-gram foam
spheres before and after exposure were the same noted for the 6.5-gram spheres.
9-16
-------
i
**j
1.8
1.6 ••
.£ 1.4 • •
of
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Ul
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1
I 1.0
0.8
0.6
O
A
GRID OPENING
500
O
A O
O POPULATION II
(INITIAL MIN. DIAMETER = 1.61 inches)
A POPULATION III
(INITIAL MIN. DIAMETER = 1.53 inches)
•f-
-I-
•f-
1000 1500 2000 2500
HOURS IN SERVICE
3000
3500
4000
Figure 9-10. Eros ion/Shrinkage Rate of Nitrile Foam Spheres
-------
The 6.3-gram nitrile foam spheres were then replaced with improved 6.5-gram
nitrile foam spheres. The wear rate on these spheres was carefully monitored
by sampling each bed and measuring the minimum diameters of 25 spheres.
Average weight measurements were also made of these samples, but were much
more variable.
The 6.5 gram foam spheres underwent an initial shrinkage* in minimum diameters
of 6 to 12 percent in the first 1000 hours of service. The subsequent shrink-
age rate declined to 0.05 inches per 1000 hours of service over the next 6700
hours of service. The average shrinkage rate over the total 7700 hours was
0.07 inch per 1000 hours.
The entire evaluation of sphere wear took place while operating with flue gas
with high fly ash loading, an environment more severe than when operating with
low fly ash loading.
9.1.5 Ceilcote Packing
An egg-crate type plate (packing support plate) manufactured by Ceilcote Company
was tested in the TCA in late November and early December 1977. The plate
dimensions were 2 ft x 2 ft x 2 inches with a 1-3/16 inch square opening, and
the material was fiberglass-filled polypropylene. Twenty-three layers of
Ceilcote plates (46 inches in height) were installed between the second and
third bar grids to provide an anticipated pressure drop of 8 inches H20 (actual
was lower, see Figure 9-11) at 30,000 acfm gas rate and 1200 gpm slurry flow
rate. This was typical of the pressure drop obtained under these flow rates
* Includes decrease in size due to abrasion.
9-18
-------
LIQUOR RATE
8 --
7 - -
6 - -
O
fM
5 - -
8
§
UJ
oc
t/i
ill
DC
o.
4
3 - -
2 - -
A
O
A
O
1,400 gpm
1,200 gpm
1,000 gpm
800 gpm
600 gpm
1 - -
CEILCOTEPLATE
PACKING:
HEIGHT -46 inches
LAYERS - 23
OPENING - 1 3/16 in. x 1 3/16 in.
SLURRY: SOLIDS CONC. - 15 wt. %
TEMPERATURE - 126 - 144° F
1 1 h-
18,000 20,000
22,000
24,000
26,000
28,000
30,000
GAS RATE, acfm @ 300 F
-4-
-4-
10
GAS VELOCITY, ft/sec @ 125°F
-h
11
12
Figure 9-11. PRESSURE DROP ACROSS 4 BAR GRIDS AND
23 LAYERS OF CEILCOTE SUPPORT PLATE PACKING
9-19
-------
for a three-bed, four-grid TCA with 5 inches static height of spheres per bed.
This arrangement was chosen to permit a direct comparison of scrubber perform-
ance with the plate packing and that with mobile spheres.
Under typical operating conditions of 30,000 acfm gas flow and 1200 gpm slurry
flow rate, S02 removal with the Ceilcote packing averaged 76 percent at 3200
ppm average inlet S02 concentration. The flue gas pressure drop was 7.2 inches
H20 (with 4 grids). Under similar operating conditions a three-bed, four-grid
TCA with 5 inches static height of 1-5/8 inches diameter solid nitrile foam
spheres per bed (about 8 to 9 inches H20 flue gas pressure drop) gives about
80 percent S02 removal (Reference 5, Section 14). Thus the Ceilcote plates
provided S02 removal performance comparable with that of the spheres.
At a reduced gas rate (18,000 acfm), average S02 removal for the plate scrubber
was 86 percent at an average inlet S02 concentration of 3050 ppm. Flue gas
pressure drop across the plates and four grids averaged about 2.9 inches H20.
Compared with this, a three-bed, four-grid TCA with 5 inches of spheres
per bed (about 4.5 inches H20 flue gas pressure drop) provides about 78 percent
S02 removal. Thus, when compared with a TCA unit operating with spheres, S02
removal was about the same at high gas rates and higher at low gas rates. Thus,
the plates demonstrated better turndown capacity. This was due to the absence
of any reliance on sphere activity, which is a strong function of gas rate.
Outlet particulate loading for the high gas rate run ranged from 0.038 to 0.046
and averaged 0.042 grain/dry scf. Particulate removal averaged 98.9 percent,
the same as under similar conditions for the TCA system with 5 inches of spheres
per bed (3 beds), where an average outlet particulate loading of 0.064 grain/dry
scf was observed. Comparable performance was observed at the low gas rate.
9-20
-------
No plugging occurred during tests with the Ceilcote packing. Minor scale
formation was observed along the edges of some of the plates. However, the
overall duration of the tests (326 hours total) was not sufficient to evaluate
reliability.
9.1.6 Range of Operating Conditions
This subsection addresses the range of operating conditions as they are deter-
mined by general mechanical considerations. Ranges of chemical parameters
such as pH, inlet SC^ concentration, chloride concentrations, etc., are dis-
cussed in Sections 3.2 and 4.2.
The major independent variables are:
• Gas flow rate (or gas velocity)
• Packing type and height
• Slurry flow rate.
The limits of gas flow rate are determined by two primary considerations. At
the low end, the gas flow rate should be adjusted to promote fluidization of
the sphere bed; at the high end, the gas flow rate should be regulated to pre-
vent flooding of the scrubber (see Section 9.1.2) and overloading of the mist
eliminator (re-entrainment of slurry dripping from the mist eliminator vanes).
Flooding the scrubber will result in excessive pressure drop and fan overload.
Overloading the mist eliminator will result in high outlet particulate loading
and additional fouling of the downstream equipment.
The range of gas flow tested on the TCA was 18,000 to 30,000 acfm @ 300°F. The
corresponding gas velocity of the saturated gas (at 125°F) was 7.5 to 12.5 ft/sec.
9-21
-------
The maximum slurry flow rate is determined primarily by the recirculating pump
capacity. However, at a given gas flow rate, the major constraint on slurry
flow rate is the pressure drop at which flooding occurs (see Figure 9-3 through
9-6). The range of slurry flow rates tested on the TCA was 600 to 1400 gpm.
The combination of the gas and slurry flow rate ranges tested at Shawnee re-
sulted in an L/G (liquid-to-gas) ratio range of 25 to 100 gal/mcf.
Two types of packings were tested on the TCA. Over 95 percent of the testing
was done using mobile spheres of various kinds (Section 9.1.4). The only
other type tested was Ceilcote egg-crate type packing (Section 9.1.5).
During testing with spheres the number of sphere beds was varied from 0 to 3,
and the sphere height/bed was varied from 0 to 10 inches (Section 9.1.2).
Egg-crate type packing was tested at a depth of 46 inches only.
The packing type, height, gas flow rate, and slurry flow rate interact with
each other and with the scrubber geometry in a complex manner to determine the
turndown characteristics. As noted earlier the Ceilcote plate packing demon-
strated better turndown capacity than the mobile spheres. This is expected
because the gas-slurry contact efficiency for spheres is a stronger function
of gas velocity than for plate packing.
9.2 VENTURI
9.2.1 Description
The adjustable-throat venturi scrubber in the venturi/spray tower system was
manufactured by Chemical Construction Company (Chemico). The venturi scrubber
9-22
-------
removes the bulk of the particulates. Because the residence time in the
venturi scrubber is low, S02 removal with lime/limestone slurry is inadequate.
Figure 9-12 (with major dimensions to scale) is a schematic of the scrubber.
Like the TCA scrubber, the venturi is capable of treating approximately 30,000
acfm of flue gas from Boiler No. 10. In this service it performs effectively
over the range of inlet S02 and particulates encountered at Shawnee.
Provision is made for separating the venturi effluent from the spray tower
effluent by incorporating a trapout device at the base of the spray tower.
This is further described in Section 13.1.7. Total independent operation of
either venturi or spray tower is not possible.
9.2.2 Pressure Drop
Pressure drop across the venturi scrubber is a function of the gas flow rate,
the slurry flow rate, and the annul us cross-sectional area (the annular space
between the venturi throat and the plug). The annul us cross-sectional area
is varied by changing the vertical position of the plug. This feature has been
utilized routinely at Shawnee to maintain constant pressure drop across the
venturi at various combinations of gas and slurry flow rates. The range of
pressure drop tested was 3 to 12 inches ^0.
The following equation has been fitted to the venturi air/water and soda-ash
pressure drop data (Reference 1, Section 12):
AP = 2.8 x 10'4 Vt2 + 7.5 x 10'5 Vt2*38 (L/G)0'897 (1/D)1*68 (9-3)
with:
9-23
-------
GAS OUT
CHEVRON MIST
ELIMINATOR
SPRAY TOWER
INLET SLURRY
MIST ELIMINATOR
'WASH WATER
MIST ELIMINATOR
WASH LIQUOR
ADJUSTABLE PLUG
VENTURISCRUBBER
VENTURI EFFLUENT SLURRY-^
APPROX SCALE
SPRAY TOWER
EFFLUENT SLURRY
FIGURE 9-12. SCHEMATIC OF VENTURI SCRUBBER AND SPRAY TOWER
9-24
-------
1 = 0.56 + 0.009Z
At = 1.8 + 0.048Z
where:
AP = pressure drop across venturi, inches H20
Vt = gas velocity at throat, ft/sec
L/G = liquid-to-gas ratio through scrubber, gal/mcf
1 = throat length, ft
D = venturi plug diameter = 3.2 ft. for the Chemico venturi
At = venturi throat area (used to calculate gas velociity), ft2
Z = percent opening of plug
The constant in the first term on the right-hand side of Equation 9-3 was
fitted to the "air only" (L=0) data. The four coefficents in the second term
on the right-hand side were fitted to the remaining data.
Equation 9-3 accounted for 97 percent of the variation of the air/water and
soda-ash data, with a standard error of estimate of 0.7 inch H20. Measured
and predicted (Equation 9-3) values of venturi pressure drop are compared in
Figure 9-13. Also shown in Figure 9-13, but not included in the fit of
Equation 9-3, is the pressure drop data for the early limestone factorial runs
(Reference 1).
The four coefficients in the second term on the right-hand side of Equation 9-3
were also fitted to the earlier limestone factorial data. The resultant equation
is:
AP = 2.8 x 10"4 Vt2 + 10.0 x 10'5 Vt2'46 (L/C)0'62 (1/D)1'36 (9-4)
9-25
-------
15
O
CM
x. 10
C.
O
6£.
0
CO
Sf
1 - 1 - 1
A AIR/WATER &AIR-S02/SODA ASH DATA
O SODA ASH/FLUE GAS DATA
O LIMESTONE FACTORIAL DATA
MEASURED PRESSURE DROP, In. H2O
Figure 9-13. Comparison of Experimental Data and Predicted Values
of Pressure Drop in the Chemico Venturi from Equation 9-3.
9-26
-------
15
O
c«
X
^c
^
0.
Q
LU
to
LU
a.
O
10 -•
y 5
O
LU
O LIMESTONE FACTORIAL DATA
5 10
MEASURED PRESSURE DROP, in. K
Figure 9-14. Comparison of Experimental Data and Predicted Values
of Pressure Drop in the Chemico Venturi from Equation 9-4.
9-27
-------
The equation accounts for 92 percent of the variation of the data. Measured
and predicted values of pressure drop are compared in Figure 9-14.
9.2.3 Venturi Scrubber Turndown
No problem has been encountered with the flue gas turndown in the venturi
scrubber over the range of gas and slurry flow rates tested at Shawnee. The
vertical position of the plug, which adjusts the cross-sectional area of the
annular space between the plug and the throat, can be varied to maintain a
constant pressure drop at a range of gas and slurry flow rates which far
exceeds that of practical interest or necessity.
It should be noted that venturi configurations other than that tested at
Shawnee, such as the rectangular throat design, can of course provide suffi-
cient gas pressure drop at the lowest expected turndown ratio for efficient
removal of the particulate matter.
9.2.4 Range of Operating Conditions
Independent variables during operation of the venturi scrubber are:
• Gas flow rate
• Slurry flow rate
• Annul us cross-sectional-area
Over the years the gas flow rate has ranged from 18,000 to 35,000 acfm, and
the slurry flow rate from 140* to 600 gpm. Except for minimum slurry flow
* The minimum slurry flow rate is dictated by the minimum controllable flow
rate on the recirculating pump used.
9-28
-------
conditions in which all slurry is introduced above the plug through a bull
nozzle, approximately three-fourths of the slurry is introduced via the bull
nozzle with the balance being fed via four tangential nozzles located along
the upper periphery of the scrubber (Figure 9-12).
The annul us cross-sectional area is varied by changing the position of the
adjustable plug, which varied the pressure drop. A pressure drop variation
of 3 to 12 inches HgO has been tested.
9.3 SPRAY TOWER
9.3.1 Description
The spray tower in the venturi/spray tower system was manufactured by Chemical
Construction Company (Chemico). It is operated with up to 4 slurry headers.
The top three headers, with 7 nozzles each, spray downward (countercurrent
to gas flow) whereas the bottom header, with 7 nozzles, usually sprays upward.
In the earlier test program during the mist eliminator reliability testing,
the bottom header sprayed downward to minimize the slurry entrainment. The
distance between the headers is about 4 ft. The empty cross-sectional area
p
of the spray tower in the scrubbing and mist eliminator sections is 50 ftr.
Figure 9-12 (drawn with major dimensions to scale) is a schematic of the scrubber.
The chevron mist eliminator used during the entire testing period is shown in
Figure 9-2. The scrubber performed effectively over the range of flue gas flow
rates and compositions encountered at Shawnee.
Provision is made for separating the venturi effluent from the spray tower efflu-
ent by incorporating a trapout funnel at the base of the spray tower. This is
9-29
-------
further described in Section 13.1.7. Tests have been made both with and with-
out the trapout funnel. Because of the physical layout of the flue gas duct-
work, independent operation of either venturi or spray tower is not possible.
9.3.2 Pressure Drop
Flue gas pressure drop across the four slurry headers in the spray tower was
measured in March, 1978, as a function of superficial gas velocity, total slurry
flow rate, and number and position of the headers in use. The lower pressure
tap was located 20 inches below the center-line of the bottom header and the
upper tap 7 inches above the center-line of the top header.
Figure 9-15 shows flue gas pressure drop as a function of superficial gas
velocity and slurry flow rate with all four spray headers in use. Figure 9-16
presents the effect of the number and position of spray headers on the flue
gas pressure drop at 14 gpm/ft^ total slurry flow rate.
Equation 9-5 is a correlation of flue gas pressure drop as a function of gas
and slurry flow rates for the case when all four slurry headers were used
(see Figure 9-15):
AP = 0.0062V 1>17 exp(0.084L) (9-5)
where:
AP = flue gas pressure drop across four spray headers, Inches F^O.
v = superficial gas velocity 1n the spray tower, ft/oec at 125°F
L - slurry flow rate to four headers, gpm/ft* of spray tower
cross-sectional area (Shawnee spray tower cross-sectional
area = 50 ft2)
Equation 9-5 accounts for 92 percent variation in the data with a standard
error estimate of 0.06 inch H20.
9-30
-------
1.4 -
1.2 •
CO
tc.
Ill
O
<
HI
I
O
a.
o
1.0 -
0.8 -
Q.
O
£0-6
tc
UJ
tc
O.
UJ
0.2 - -
SLURRY FLOW RATE,
gpm/ft2
• 28
Q 20
14
SPRAY HEADERS
USED
ALL 4
ALL 4
ALL 4
.
0.0
— * —
. 1 1 1 1 1
1 — 1 — 1 — • 1 — 1 —
4.0
5.0 6.0 7.0 8.0 9.0
SPRAY TOWER SUPERFICIAL GAS VELOCITY, ft/sec @ 125° F
10.0
Figure 9-15
THE EFFECT OF GAS VELOCITY AND SLURRY FLOW RATE ON THE
FLUE GAS PRESSURE DROP ACROSS THE FOUR SLURRY HEADERS
IN THE SPRAY TOWER
9-31
-------
1.4 - -
1.2 - -
CO
tc
tu
Z
1.0 --
0.8 --
.
O
OC
a
UJ
DC
IM
CO
3
tu
D
0.6 • •
0.2 --
0.0
T
T
SLURRY FLOW RATE,
gpm/ft2
14
14
14
SPRAY HEADERS
USED
TOP 2
ALL 4
BOTTOM 2
4.0
5.0 6.0 7.0 8.0 9.0
SPRAY TOWER SUPERFICIAL GAS VELOCITY, ft/»c O 125° F
10.0
Figure 9-16
THE EFFECT OF HEADER POSITION AND NUMBER OF HEADERS ON THE
FLUE GAS PRESSURE DROP AT 14 gpm/ft2
TOTAL SLURRY FLOW RATE
9-32
-------
The effects of header position and the number of headers on the pressure drop
P
were studied at 14 gpm/ft^ total slurry flow rate. Figure 9-16 indicates that
pressure drop was the highest when only the top two headers were used, next
highest with all four headers, and lowest with only the bottom two headers.
This could be explained by the fact that the slurry holdup in the spray tower
between the pressure taps is likely to be the highest when the top two headers
are used, and lowest when the bottom two headers are used.
9.3.3 Spray Tower Turndown
In addition to the advantage of open internal design, which minimizes the
scaling and plugging potential in slurry service, the spray tower has turndown
over an infinite range. The spray tower is also capable of operating at
higher-than-design gas velocity without flooding, subject to the limitations
of mist eliminator overloading and fan capacity. The minimum gas flow rate
of 18,000 acfm (4.8 ft/sec) at Shawnee was determined by the tightness of the
fan damper closure. Low gas flow rate should give better gas flow distribu-
tion. This would undoubtedly be true as well in a large scale unit.
9.3.4 Range of Operating Conditions
Important operating parameters for the spray tower are:
• Gas flow rate
• Slurry flow rate
• Number of slurry spray headers
• Header combinations
Unlike a TCA, the effect of gas flow rate (or liquid-to-gas ratio at constant
slurry flow rate) on the performance of the spray tower is quite significant
9-33
-------
(Figures 7-5 and 7-9). The level of gas flow affects the residence time of
the liquid droplets in the scrubber (via hold up), the residence time of the
gas in the scrubber, and the intensity of impact between the liquid droplets
and the gas molecules. At high gas flow rates the negative effect of the
lower gas residence time in the scrubber is offset by the increased intensity
of contact and higher liquid holdup. At Shawnee, gas flow ranged from 18,000
to 35,000 acfm (@ 300°F). The corresponding velocity of the saturated gas (at
125°F) was 4.8 to 9.4 ft/sec.
Generally in spray tower systems, absorption occurs primarily in the vicinity
of the spray nozzles before significant coalescence of slurry droplets takes
place. The effective absorption zone may have a radius as low as 12 Inches,
depending on the droplet size. For this reason spray towers are designed with
multiple headers containing several high efficiency, atomizing nozzles (see
Section 9.3).
At Shawnee the spray tower was operated with one to four headers. The slurry
flow per header ranged from 0 to 400 gpm. Combination of the gas and slurry
flow rate ranges resulted in an L/G (Iiqu1d-to-gas) ratio range of 15 to 110
gal/mcf. During testing all possible header combinations were evaluated.
Combinations using the upper headers (higher liquid holdup and residence time)
and higher flow per nozzle (better atomizatlon) provided better S02 removal
efficiency.
It should be noted that the Shawnee spray tower design is not optimized.
Optimization of the spray tower internal design has been planned in the future
program.
9-34
-------
Section 10
WATER BALANCES AROUND SCRUBBER SYSTEMS
The water balances around scrubber systems have been calculated in order to
determine the quantity of raw (makeup) water that can be used for the fresh
alkali slurry preparation, mist eliminator wash, and the process pump seals
in a closed-liquor-loop operation. Data from typical Shawnee lime and lime-
stone runs was used to calculate the makeup water requirements and to
investigate those factors which have an effect on the water balance.
10.1 FACTORS AFFECTING WATER BALANCES
The most significant factor affecting the water balance for closed-loop
Shawnee systems was water loss through evaporation (flue gas humidification).
The scrubber operating parameters which affected evaporation were gas rate
and temperature. For typical Shawnee operation at hot gas temperature
of 300°F, gas rates between 30,000 and 35,000 acfm (at 300°F), and scrubber
temperatures (wet bulb temperatures) between 125°F and 130°F, approximately
9 gpm is lost through evaporation, including an estimated 0.2 gpm entrainment.
Water losses with the discharged scrubber waste solids account for the
remainder of the makeup water requirements. These losses take two forms:
10-1
-------
• Free water discharged with the solids
• Water of hydration as CaS03*l/2H20 and CaS04*2H20
The waste solids discharge rate is a function of the rates of fly ash and S0?
removed and excess alkali added. The quantity of free water lost depends
upon the weight percent of solids in the waste sludge discharged. It is
greater for a limestone than for a lime system because the higher alkali
stoichiometries for limestone result in a higher solids discharge rate.
At Shawnee free water loss ranged from 0.7 to 7 gpm.
The water of hydration losses are dependent upon the degree of sulfite
oxidation. Because two molecules of water combine with calcium sulfate while
only half a molecule of water combines with calcium sulfite, more hydration
water is lost during forced oxidation operation. These losses range from
0.2 gpm without forced oxidation to 0.6 gpm with forced oxidation.
Tables 10-1 through 10-3 give eight examples of water balances calculated
from Shawnee operation at flue gas flow rates of 30,000-35,000 acfm at 300°F
(equivalent to 10 megawatts). A material balance computer program, which
is a part of the Design/Economics Computer Program being developed jointly by
TV A and Bechtel, was used to calculate the water balances (Reference 16).
The S02 inlet concentrations averaged 2550 ppm. Chloride content in coal was
assumed to be 0.05 weight percent. Makeup water requirements were calculated
for four limestone and four lime cases. The following conditions applied to
each alkali:
1. Forced oxidation with two-stage dewatering (clarifier
followed by either filter or centrifuge) and high fly ash.
2. No oxidation with two-stage dewatering and high fly ash.
10-2
-------
Table 10-1
SUMMARY OF WATER BALANCES FOR LIMESTONE RUNS
(1)
Test Conditions
Flue Gas Rate,
Macfro @ 300°F
Fly Ash Loading,
gr/wet scf
Percent solids
Recirculated
Percent Solids in
Discharged Sludge
SOo Removal, Percent
Limestone Stoich-
iometric Ratio,
moles Ca added/
mole S02 absorbed
Percent Sulfite
Oxidized
Scrubber Inlet pH
Water Output, gpm
Evaporation (2)
Hydrated Water in
Discharged Solids
Water in discharge
stream
Total
Water Input, gpm
Forced Oxidation
Clarifier & Filter
or Centrifuge
30-35
4.7
15
80
85
1.4
95
5.5
9
0.5
1.3
TO
Water in Limestone
Slurry (6Q% limestone)
Mist Eliminator Wash
Pump seal water (3)
Total
Dissolved Concentrations
of Liquor Species, ppm
Scrubber System
discharge pH
c
1.5
7.8
1.5
TO
7.60
1225
3175
320
6095
6635
No Oxidation
Clarifier A Filter
or Centrifuge
30-35
4.7
15
60
85
1.4
30
5.5
9
0.3
3.1
TO
1.5
9.4
1.5
7.60
1050
1295
230
3685
2705
No Oxidation
Clarifier Only
30-35
4.7
15
40
85
1.4
30
5.5
9
0.2
7.1
TO
1.5
14.8
0
"TO
7.60
920
575
185
2620
1200
(1) 30% excess air included
(2) including 0.2 gpm entrainment
(3) clarifier underflovj pump
10-3
-------
Table 10-2
SUMMARY OF WATER BALANCES FOR LIME RUNS
Test Conditions
Flue Gas Rate,
Macfm P 300°F (1)
Fly Ash Loading,
gr/wet scf
Percent solids
Recirculated
Percent Solids in
Discharged Sludge
S02 Removal, Percent
Lime Stoichiometric
Ratio, mole Ca++
added/mole S02
absorbed
Percent Sulfite
Oxidized
Scrubber Inlet pH
Water Output, gpm
Evaporation (2)
Hydrated Water in
Discharged Solids
Water 1n Discharge
Stream
Total
Water Input, gpm
Water to Lime Slaker
(2« lime)
Mist Eliminator Wash
Pump Seal Water (3)
Total
Forced Oxidation
Clarifier & Filter
or Centrifuge
30-35
4.7
8
80
90
1.05
95
7.0
9
0.6
1.2
TO
5.3
4.0
1.5
TO
Dissolved Concentrations
of Liquor Species, ppm
Scrubber System
discharge pH
ud
"9*:
so->*
s°r
cr
(1) 30% excess air included
(2)
7.40
2710
1380
165
2030
7175
No Oxidation
Clarifier & Filter
or Centrifuge
30-35
4.7
8
60
90
1.05
30
7.0
9
0.3
2.8
5.3
5.3
1.5
~I2TT
7.45
1600
570
160
1865
2970
No Oxidation
Clarifier Only
30-35
4.7
8
40
90
1.05
30
7.0
9
0.3
6.4
T5T7
5.3
10.4
0
"1577
7.55
1130
255
155
1735
1315
(3)
including 0.2 gpm entrainment
clarifler underflow pump
10-4
-------
Table 10-3
WATER BALANCES FOR RUNS WITH HIGH AND LOW FLY ASH LOADING
WITH FORCED OXIDATION AND TWO-STAGE DEWATERING
Test Conditions
Limestone High
Fly Ash
Flue Gas Rate,
Macfm 0 300°F (1)
Fly Ash Loading,
gr/wet scf
Percent sol ids
Recirculated
Percent Solids in
Discharged Sludge
SO 0 Removal , Percent
Alkali Stoichiometric
Ratio, moles Ca
added/mole S02 absorbed
Percent Sulfite
Oxidized
Scrubber Inlet pH
Water Output, gpm
Evaporation (2)
Hydrated water in
Discharged Solids
Water in Discharge
Stream
Total
Water Input, gpm
Alkali Makeup Water
Mist Eliminator Wash
Pump Seal Water (3)
Total
30-35
4.7
15
80
85
1.4
95
5.5
9
0.5
1.3
TO
1.5
7.8
1.5
TO
Dissolved Concentrations
of Liquor Species, ppm
Scrubber System
Discharge pH
Ca++
Mg++
S0o=
7.60
1225
3175
320
6095
6635
(1) 30% excess air included
(2) including 0.2 gpm entrainment
(3) clarifier underflow pump
Limestone Low
Fly Ash
30-35
0.2
8
80
85
1.4
95
5.5
9
0.5
0.8
TUTS"
1.5
7.3
1.5
7.60
1315
4820
405
8050
10,075
Lime High
Fly Ash
30-35
4.7
8
80
90
1.05
95
7.0
9
0.6
1.2
TO
5.3
4.0
1.5
7.40
2710
1380
165
2030
7175
Lime Low
Fly Ash
30-35
0.2
4
80
90
1.05
95
7.0
9
0.6
0.7
10.3
5.3
3.5
1.5
TO
7.30
3785
2190
170
2105
11,375
10-5
-------
3. No oxidation with clarifier only and high fly ash.
4. Forced oxidation with two-stage dewatering and low fly ash.
These cases are reviewed in Sections 10.2 through 10.5.
10.2 LIMESTONE SYSTEMS WITH HIGH FLY ASH LOADING
Water balances for typical limestone runs with high fly ash are presented in
Table 10-1. S02 removal for these runs averaged 85 percent with a limestone
stoichiometry of 1.4 moles Ca++ added/mole S02 absorbed. Fly ash loading
averaged 4.7 grains/wet scf (based on inlet gas containing about 8 percent
moisture), and the recirculated slurry solids were controlled at 15 weight
percent. With forced oxidation 95 percent of the sulfite was converted
to sulfate, whereas only 30 percent was oxidized without forced oxidation.
Discharged solids content averaged 80 weight percent with forced oxidation
and two-stage dewatering. Without forced oxidation, discharged solids con-
tent averaged 60 weight percent with two-stage dewatering and 40 weight
percent using the clarifier only.
10.2.1 Water Balances
Only 10.8 gpm makeup water was required for operation using two-stage dewater-
ing and forced oxidation. Evaporation* accounted for 9 gpm of the losses.
Another 1.8 gpm left the system with the discharged solids, 1.3 gpm of that
as free water and the remaining 0.5 gpm as hydration water. Raw (makeup)
water was supplied to the system at a rate of 1.5 gpm in the limestone slurry,
* In all cases discussed in this section evaporation includes about 0.2
gpm entrainment.
10-6
-------
1.5 gpm in the clarifier underflow pump seal water, with the remaining 7.8
gpm available for the mist eliminator wash.
Closed-loop scrubber operation without forced oxidation with two-stage dewa-
tering required 12.4 gpm of makeup water. Again, 9 gpm was lost to evaporation.
Free water in the discharge stream amounted to 3.1 gpm, and 0.3 gpm left the
system as hydrated solids. The limestone feed system supplied 1.5 gpm of the
raw water, the clarifier underflow pump supplied another 1.5 gpm as pump seal
water, and the mist eliminator wash supplied the remaining 9.4 gpm required.
Without forced oxidation, using only the clarifier for dewatering, a total
of 16.3 gpm left the system. This consisted of 9 gpm through evaporation,
7.1 gpm as free water with the discharged sludge, and 0.2 gpm with the
hydrated solids. Raw water was supplied at a rate of 1.5 gpm with the lime-
stone feed and 14.8 gpm with the mist eliminator wash. Since the system
used only one dewatering stage (clarifier only), seal water for the clarifier
underflow pump did not contribute to the system water balance.
10.2.2 Dissolved Solids Concentrations
Except for sulfate concentration which varied with magnesium concentration,
concentrations of dissolved species in the liquor in equilibrium with slurry
solids, such as calcium and sulfite, were only slightly affected by loop tight-
ness (percent solids in discharged sludge). Calcium and sulfite concentrations
decreased from 1225 ppm to 920 ppm and 320 ppm to 185 ppm, respectively, for
the tightest loop versus most open cases explored. However, highly soluble
species not in equilibrium with slurry solids, notably chlorides, decreased
in concentration from 6635 ppm to 1200 ppm as loop tightness decreased.
10-7
-------
10.3 LIME SYSTEMS WITH HIGH FLY ASH LOADING
Table 10-2 presents the water balances for typical lime runs with high fly
ash loading. S0£ removals averaged 90 percent at a lime stoichiometric ratio
of 1.05 moles Ca"1"1" added/mole S02 absorbed. Fly ash loading averaged 4.7
grains/wet scf (based on inlet gas containing about 8 percent moisture), and
the recirculated slurry solids were controlled at 8 weight percent. The
discharged solids averaged 80, 60, and 40 weight percent for forced oxidation
with two-stage dewatering, no forced oxidation with two-stage dewatering, and
no forced oxidation using only the clarifier, respectively.
10.3.1 Water Balances
Makeup water requirements for operation with forced oxidation and two-stage
dewatering amounted to 10.8 gpm. Evaporation accounted for 9 gpm of the
losses, with another 1.2 gpm leaving the system as free water and 0.6 gpm in
hydrated solids. Entering the system was 5.3 gpm with the slaked lime and
1.5 gpm through the clarifier underflow pump seals. This left the remaining
4.0 gpm available for the mist eliminator wash.
When oxidation was not forced, using two-stage dewatering, 12.1 gpm left
the system. Evaporation losses were again 9 gpm. Free water leaving the
system amounted to 2.8 gpm, and hydrated water leaving with the discharged
solids amounted to an additional 0.3 gpm. These losses were offset by 5.3
gpm entering with the slaked lime, 1.5 gpm with the clarifier underflow pump
seals, leaving the remaining 5.3 gpm with the mist eliminator wash.
When only the clarifier was used for dewatering and oxidation was not forced,
10-8
-------
15.7 gpm was needed to equalize the losses. Evaporation losses accounted for
9 gpm, free water left the system with the discharged solids at a rate of 6.4
gpm, and 0.3 gpm was lost with the hydrated solids. The lime slaker added 5.3
gpm to the system. The mist eliminator wash provided the remaining 10.4 gpm.
10.3.2 Dissolved Solids Concentrations
As with the limestone system, the concentrations of dissolved species in equili-
brium with slurry solids were relatively unaffected by loop closure. Calcium
concentration decreased from 2710 ppm to 1130 ppm, and sulfite decreased from
165 ppm to 155 ppm as the liquor loop became more open. Sulfate concentration
varied only slightly, from 2030 ppm to 1735 ppm, and was lower than the lime-
stone case because of the lower magnesium concentration. Similar to the lime-
stone cases, chlorides decreased in concentration from 7175 ppm to 1315 ppm
with decreasing loop tightness. The discharge slurry pH increased from 7.40
to 7.55 as the chloride concentration decreased.
10.4 LIMESTONE AND LIME SYSTEMS WITH LOW FLY ASH LOADING
The previous water balances for limestone and lime systems with high fly ash
were compared with similar systems where 96 percent of the fly ash was re-
moved upstream of the scrubber (Table 10-3). One limestone and one lime case
with low fly ash loading were studied under conditions of forced oxidation
with two-stage dewatering. Conditions were the same as for high fly ash,
except that the recirculated slurry solids concentrations were adjusted to
compensate for significantly less inert (fly ash) material. For the limestone
case 8 weight percent solids were in the recirculated slurry. Four weight
10-9
-------
percent solids were in the recirculated slurry for the lime case.
10.4.1 Water Balances
The makeup water requirements for the limestone run with low fly ash, shown
in Table 10-3, totaled 10.3 gpm. Evaporation accounted for 9 gpm of the
water leaving the system. An additional 1.3 gpm left the system, including
0.8 gpm in the discharge stream as free water and 0.5 gpm as hydration water
with the solids. This was balanced by adding 1.5 gpm to the system with the
limestone slurry, 1.5 gpm with the clarifier underflow pump seal water,
leaving the remaining 7.3 gpm to enter as the mist eliminator wash.
For the low fly ash lime system studied, the total makeup water requirement
was 10.3 gpm. Again, 9 gpm left the system through evaporation. Free water
left the system at a rate of 0.7 gpm and hydrated water at a rate of 0.6 gpm.
Water entered the system at a rate of 5.3 gpm with the lime feed, 1.5 gpm
through the clarifier underflow pump seal, leaving 3.5 gpm for the mist
eliminator wash sprays.
10.4.2 Dissolved Solids Concentrations
Dissolved species in equilibrium with slurry solids (calcium, sulfite, and
sulfate) were only slightly affected by the lack of inert solids in the scrub-
ber slurry. However, chloride concentration in the scrubber liquor increased
dramatically when the systems were run with low fly ash loading. For the
limestone case chlorides increased from 6635 ppm to 10,075 ppm when the fly
ash was removed prior to the scrubber. When lime was used, the chlorides rose
from 7175 ppm to 11,375 ppm when switching from high to low fly ash loading.
10-10
-------
10.5 SUMMARY
Scrubber system water balances were calculated for eight cases selected in
the detailed study, six with high fly ash loading, and two with 96 percent
of the fly ash removed prior to the flue gas entering the scrubber. Of the
eight cases studied, four were for limestone and four for lime.
Makeup water requirements are most strongly affected by evaporation to flue
gas, which accounted for 9 gpm for a 10 MW-equivalent system in all eight
cases studied. Free water leaving the system with the discharged solids
varied by a factor of ten, from 0.7 to 7 gpm depending on loop tightness and
fly ash loading. Hydrated water left with the discharged solids at a low
rate of 0.2 gpm without forced oxidation and at a high rate of 0.6 gpm when
oxidation was forced.
The concentration of dissolved species, in equilibrium with slurry solids,
namely calcium, sulfite, and sulfate, varied only slightly with loop tight-
ness. Highly soluble species such as chlorides were greatly affected by
loop tightness and fly ash loading. Chloride concentrations in the scrubber
liquor ranged from a high of 11,375 ppm for the tightest loop configuration
(low fly ash, 80 weight percent solids in discharged sludge) to a low of
1200 ppm for the least tight configuration (high fly ash, 40 weight percent
solids in discharged sludge).
10-11
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Section 11
MIST ELIMINATOR SYSTEMS
The mist eliminator serves the function of separating entrained slurry from
the flue gas leaving the scrubber. Thus, it minimizes the particulate
emission from the scrubber and also protects the downstream equipment, such
as the flue gas reheater and induced-draft fan, from fouling by scale and
soft solids deposits.
Scrubber operating conditions, mist eliminator configuration and placement,
and flushing sequences for washing solids off the mist eliminator surfaces
are all important parameters in achieving trouble-free mist eliminator
operation. Although it was not possible to examine every conceivable case
at Shawnee, extensive effort was spent from March 1972 through early 1976
to achieve reliable mist eliminator operation (References 1, 2, and 3).
Much of the early effort was devoted to identifying and learning how to
control two separate and distinct operating reliability problems. These
were scaling and soft, mud-type solids deposition on the scrubber walls and
internals, and especially in the relatively restricted areas of the mist
eliminators. Much of the early work was also conducted at a reduced gas
velocity using various combinations of mist eliminator washing techniques
and hardware configurations, including a wash tray upstream of the mist elim-
inator to intercept the entrained slurry. In fact, it was not recognized
11-1
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early in the program that scaling and mud-type solids deposition were indeed
separate problems, each with separate and distinct solutions. This fact
was not really apparent until methods were found to adequately control both.
In a lime or limestone based system, the most frequently encountered scaling
problem is due to gypsum crystals which precipitate on the scrubber internals
rather than outside the scrubber in the reaction tank. Proper selection of
operating parameters (such as liquid-to-gas ratio, reaction tank residence
time, pH, and percent solids in the recirculated slurry) to maintain a gypsum
saturation level in the scrubber below about 135 percent will prevent this
type of scaling (Sections 3 and 4). The use of infrequent (once every 4 to
8 hours) top sequential washing with fresh makeup water and low pressure
drop nozzles proved adequate at Shawnee for control of scaling in the mist
eliminator.
Identification of operating parameters, safe operating ranges, and mist elim-
inator washing techniques proved more difficult and time consuming for the
control of mud-type solids deposition which was superimposed over the scaling
problem. The use of a wash tray upstream of the mist eliminator to transfer
the mud-type deposits from the mist eliminator to an area where they could
more easily be removed by washing was only marginally successful and required
reduced gas flow rates. Washing techniques for the mist eliminator were
ultimately found without requiring a wash tray and at scrubber design gas
velocities, which limited restriction from these mud-type solids to less than
10 percent of the mist eliminator open area. These solid deposits did not
hinder the scrubber operation or cause shutdown for periodic cleaning. How-
ever, the real key to successful control of these mud-type solid deposits
was not found until well into the Advanced Test Program.
11-2
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During tests from October 1975 through mid-February 1976 to study methods
for improving limestone utilization (Reference 3), a strong correlation was
found between alkali utilization and the accumulation of the mud-type solids.
Above about 85 percent alkali utilization, the soft solids can easily be
removed even with very infrequent (once every 4 to 8 hours) washing with
fresh makeup water. In fact, an entirely clean system was maintained over
an extended period using only approximately one-fourth of the available
fresh makeup water (see Section 10 for available makeup water for mist elim-
inator wash). This important discovery was further confirmed at Shawnee
in subsequent tests with high alkali utilization and was also confirmed on
a different system at the TVA 1-MW Colbert pilot plant.
11.1 DESCRIPTION OF SHAWNEE MIST ELIMINATORS
The original mist eliminator used in the spray tower at the start of test-
ing in March 1972 was a three-pass, open-vane, chevron type made of eight-
gage, Type 316L stainless steel. Figure 9-2 shows the blade configuration
and dimensions for this mist eliminator. With the exception of a few
short tests with other types, this original design has been retained in the
spray tower during the entire test program.
Figure 9-12 is a schematic of the spray tower. As shown, the mist eliminator
is oriented for vertical gas flow. Provision is made for flushing both the
top side and the bottom side with makeup water and/or clear liquor. The
o
spray tower is circular in cross-section, with a 50 ft cross-sectional area
in both the scrubber and mist eliminator sections.
11-3
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Since July 1975 the TCA has employed the same mist eliminator design as
the spray tower. In the TCA, as shown in Figure 9-1, the mist elimimator is
located about 7 feet above the slurry spray header. The TCA is square with
a 32 ft^ cross-sectional area in the scrubber section which expands to 49 ft^
in the mist eliminator section. As with the spray tower, spray headers are
provided for washing both the top side and bottom side of the TCA mist
eliminator.
11.2 OTHER MIST ELIMINATOR CONFIGURATIONS TESTED AT SHAWNEE
Other types of mist eliminators tested at Shawnee are described below.
Experiences with these systems were not favorable. These types of mist elim-
inators were tested before it was found that, as mentioned previously, alkali
utilization has a strong effect on clean mist eliminator operation. Therefore,
it is not implied that these systems are not workable because of the unfavor-
able experiences at Shawnee. Performances of these units could have been
far better if the tests had been made at high alkali utilization.
11.2.1 Mist Eliminator with Wash Tray
The original TCA mist eliminator was a six-pass, closed-vane, stainless steel,
chevron mist eliminator. A Koch wash tray was later installed in November
1972 between the mist eliminator and the slurry spray nozzles to reduce the
amount of slurry solids reaching the mist eliminator. The most successful
washing configuration used for this system was washing the underside of the
mist eliminator continuously with a 60/40 mixture of makeup water and clari-
fied liquor at 15 to 25 gpm (0.3 to 0.5 gpm/ftz), and feeding the wash tray
11-4
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with the mist eliminator wash (which drained down onto the wash tray) plus
9 to 22 gpm of clarified liquor; the underside of the wash tray was continu-
ously washed with the wash tray effluent liquor. Initially, intermittent
steam sparging was used to clean the underside of the wash tray, but was
not successful.
This mist eliminator/wash tray system was tested in limestone service from
November 1972 through April 1975. The system operated reliably at 8.6 ft/sec
scrubber superficial gas velocity (5.6 ft/sec at the mist eliminator) and
15 percent slurry solids concentration. There were 1835 hours of operation
with only incidental soft solids deposits on the mist eliminator. However,
at 10 to 12 ft/sec scrubber superfical gas velocity, the mist eliminator re-
striction by soft solids stabilized at 10 to 15 percent but scale and solids
continued to buildup on the underside of the wash tray.
11.2.2 Two Mist Eliminators in Series
A system consisting of two identical three-pass, closed-vane, fiberglass-
reinforced plastic (FRP) mist eliminators in series, purchased from UOP, was
tested for five weeks in June-July 1975 in the TCA at 12.5 ft/sec scrubber
superficial gas velocity. Despite a variety of washing techniques, the
bottom mist eliminator could not be kept completely clean. With continuous
bottom wash using diluted clarified liquor and intermittent top wash using
makeup water for the lower mist eliminator (no wash for the upper mist
eliminator), solids accumulation stabilized at 10 to 15 percent restriction
of the lower unit and less than 5 percent restriction of the upper unit.
11-5
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11.2.3 Cone-Shaped Mist Eliminator
A cone-shaped, four-pass, closed-vane, 316 stainless steel, chevron mist
eliminator, fabricated by TVA, was unsuccessfully tested for about 3 months
(November 1974 through January 1975) in the spray tower. The sloped-vane
design of this mist eliminator supposedly should have given better drainage
of slurry and wash liquor. However, a continuous wash on the under side
at 0.7 gpm/ft^ did not keep the mist eliminator completely clean.
11.2.4 Mesh Pad on Top of Mist Eliminator
A York Demister 316 stainless steel mesh pad was placed above the three-
pass, open-vane, mist eliminator in the spray tower to determine if the
mesh pad had an effect on the outlet particulate mass loading during a
special particulate emission test series in November 1976. After 3 days
of operation the pad was 30 percent restricted with entrained solids, and
testing with the mesh pad was terminated. The mesh pad was not washed
during the test. No significant difference was observed in outlet mass
loading and mass removal efficiency with or without the York demister under
the same operating conditions.
11.3 FACTORS INFLUENCING CLEAN MIST ELIMINATOR OPERATION
A wide range of operating conditions were explored in the Advanced Test
Program while using the three-pass, open-vane, chevron mist eliminator in
both the TCA and the spray tower. This section discusses the parameters
tested and their effect on mist eliminator operation.
11-6
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11.3.1 Alkali Utilization
One of the most significant findings in the Advanced Test Program was that
alkali utilization (moles of S02 absorbed/mole of alkali feed) has a strong
influence on clean mist eliminator operation. At high alkali utilization
above about 85 percent, it is much easier to keep the mist eliminator clean
than at lower utilization. Residual alkali in the stationary slurry solids,
once deposited on the mist eliminator surfaces, continues to react with the
exit gas and forms products hard to wash off.
Fewer problems with fouling of mist eliminators have been experienced with
lime slurry systems. These normally operate at an alkali utilization of
about 90 percent, whereas limestone slurry systems usually operate at much
lower utilization values. However, it has been demonstrated at Shawnee
that a limestone slurry system operated at high utilization, despite the
accompanying reduction in S0£ removal efficiency, will experience equal
mist eliminator operability. This has been a major factor in redirecting
the Shawnee program toward the investigation of chemical additives to over-
come the loss of S02 removal when operating at low pH. However, there are
other means to improve alkali utilization, e.g., three tanks in series and
two-scrubber-loop operation.
11.3.2 Gypsum Saturation
As mentioned previously, proper selection of operating parameters, such as
liquid-to-gas ratio, reaction tank residence time, pH, and percent solids
in the recirculated slurry, to maintain a gypsum saturation level below about
135 percent will prevent gypsum scaling (Sections 3 and 4). This type of
11-7
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scaling in the mist eliminator is relatively easy to control by washing it
with fresh water and diluted clarified liquor unsaturated with gypsum.
11.3.3 Flue Gas Velocity
As the gas velocity in the scrubber increases, more slurry is entrained and
the load on the mist eliminator becomes greater. Furthermore, it becomes
more difficult for the captured slurry to drain from the mist eliminator
blades against the upflowing gas. Eventually, a g.'ts velocity is reached
that will re-entrain the slurry from the top edges of the mist eliminator.
At this reentrainment point, the mist eliminator efficiency is lost.
In neither scrubber could the velocity be increased to the point that re-
entrainment occurred. Because of the limited fan capacity, maximum
superficial gas velocity tested in the spray tower was 9.4 ft/sec. For
the TCA, the maximum superficial gas velocity in the scrubber section was
12.5 ft/sec. This was equivalent to 8.2 ft/sec in the enlarged mist elimi-
nator section. However, it is doubtful if the gas uniformly spread in the
expansion section from the scrubber to the mist eliminator.
11.3.4 Slurry Solids Concentration
As the slurry solids concentration increases, the load on the mist eliminator
increases. The majority of the Shawnee runs were made at 8 to 15 percent by
weight slurry solids concentration.
11-8
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11.3.5 Mist Eliminator Wash Systems
One of the most critical factors in maintaining reliable mist eliminator
operation is the washing system. Slurry solids intercepted by the mist eli-
minator must be flushed away or the solids will build up and plug the mist
eliminator. The amount of water available for washing the mist eliminator
is limited, by material balance, to water losses from the scrubbing system
(mainly flue gas humidification losses and losses with the disposed solids).
In a scrubbing system with a tightly closed water loop (Section 10) makeup
water is severely limited.
Over the operating life of the Shawnee Test Facility the mist eliminator
wash sequence and spray pattern have been continually refined. By June 1976
the wash sequences and spray patterns as detailed in Table 11-1 were being
used. Since that time plugging of any degree has been nearly eliminated.
These wash sequences take into consideration the available makeup water with
the tightly closed water loop at Shawnee.
The mist eliminators are, in their current mode, washed from both the bottom
and top sides. The primary wash is from the bottom side with only a periodic
flush from the top side. Because the TCA is square and the spray tower was
circular, a different arrangement of nozzles is used in each scrubber to
maintain full coverage. However, the wash sequence and specific wash rate
(gpm/sq.ft.) for the two scrubbers are identical. In all cases Type 316 stain-
less steel full-cone spray nozzles are used.
From June 1977 to June 1978 the venturi/spray tower mist eliminator was
cleaned once (December 1977) after 4183 hours of operation. At that time
11-9
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Table 11-1
MIST ELIMINATOR WASH SYSTEMS
Alkali
Alkali utilization
Scrubber system
Maximum flue gas rate, acfm 9 300°F
Lime or Limestone
Greater than S6 percent utilization
Spray Tower
35,000
TCA
30,000
Limestone
Less than 85 percent utilization
Spray Tower
35,000
TCA
30,000
I
o
Bottorcside H.E. Wash
Wash scheme /,»
Nozzle size and moder '
Number of nozzles
Nozzle location, inches below M.E.
Nozzle "On" time, min
Nozzle "Off" time, min
Total on/off sequence, hr
Nozzle AP, psi
Flow rate per nozzle, gpm
Total flow rate, gpm
Specific wash rate, gpm/ft'
Makeup water (continuous basis), gpm
Low Intermittent
1/2 G35W
10
10
6
234
4
50
7.5
75
1.5
1.9
Low Intermittent
1-1/4 H190WSQ
2
31
6
234
4
41
37.5
75
1.5
1.9
Continuous
1/2 635W
4
20
Continuous
21
5.0
zoU)
0.4
20(3)
Continuous
3/4 HH71WSQ
2
31
Continuous
20
20(3)
0.4
20(3)
Topside M.E. Wash
Wash scheme /•.<
Nozzle size and model
Number of nozzles
Nozzle location, inches above M.E.
Nozzle "On" time, min'2)
Nozzle "Off" time, min
Total on/off sequence, min
Nozzle AP, psi
Coverage area per nozzle, ft2
Flow rate per nozzle, gpm
Specific wash rate, gpm/ftz
Makeup water (continuous basis), gpm
Low Intermittent
3/4 H6W
6
16
4
76
80
13
15
8
0.53
0.4
Low Intermittent
3/4 HH71WSO
6
15
4
76
80
13
14.5
8
0.55
0.4
High Intermittent
3/4 H6W
6
16
3
7
10
13
15
8
0.53
2.4
High Intermittent
3/4 HH71WSQ
6
15
3
7
10
13
14.5
8
0.55
2.4
Notes:
(1)
(2
All nozzles are full cone type manufactured by Spraying Systems Co.
(2) Sequential wash with one nozzle activated at a time.
(3) Clarified liquor from dewatering system diluted with all available makeup water.
-------
the mist eliminator was 15 percent plugged due to a short-term malfunction
of the wash system. The venturi/spray tower rnist eliminator has operated
another 3308 hours since that time without plugging; in June 1978 the restric-
tion was less than 1 percent (Section 23.1.1, Reference 5).
The TCA mist eliminator was cleaned on June 21, 1978 when solids accumulations
on the ductwork above the mist eliminator broke loose and restricted the mist
eliminator by 12 percent. At that time, the mist eliminator had logged 7671
operating hours without cleaning.
Mist Eliminator Wash Scheme at High Alkali Utilization. When operating
under conditions giving a high alkali utilization, i.e., with lime and
limestone above about 85 percent alkali utilization (moles SC^ removed/mole
alkali added), a periodic flush with makeup water was all that was required
to maintain clean mist eliminator surfaces.
On the bottom side the mist eliminator was flushed intermittently for 6 min-
p
utes every 4 hours with makeup water at a specific wash rate of 1.5 gpm/ft
of mist eliminator cross-sectional area. Pressure drop across the nozzles
was about 40 to 50 psi.
On the top side a low intermittent sequential wash was used with 6 spray
nozzles, in which one nozzle was activated at a time for 4 minutes every 80
p
minutes at a specific wash rate of 0.5 gpm/ft . Pressure drop across the
nozzles was 13 psi.
Total makeup water consumption with this low intermittent wash scheme was
equivalent to only 2.3 gpm on a continuous basis. This level of makeup water
consumption was significantly less than the makeup water availability of 4-15
11-11
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gpm (Section 10), demonstrating the importance of high alkali utilization.
Typically at high alkali utilization and with this low intermittent wash
scheme, the mist eliminator remained clean and showed only minor dust-like
deposit.
Mist Eliminator Wash Scheme at Low Alkali Utilization. As the alkali
utilization decreases in limestone systems, the mist eliminator becomes
progressively more difficult to keep clean and a continuous underside wash
is required.
Generally, for runs with a limestone utilization below 85 percent, the bottom
side of the mist eliminator was washed continuously at a specific wash rate
of 0.4 gpm/ft^ using clarified liquor from the dewatering system diluted
with all available makeup water. Pressure drop across the nozzles was about
20 psi. Clarified liquor was used because of the limited availability of
makeup water in a closed-loop scrubbing system. Clarified liquor from the
dewatering system is normally saturated in dissolved solids and must be di-
luted with makeup water to prevent scaling of the mist eliminator. Propor-
tions as high as 80 percent clarified liquor and 20 percent makeup water
have been used with no apparent scaling. Even with this dilution factor,
assuming the undiluted clarified liquor is 100 percent saturated with gypsum,
the diluted liquor would be about 65 percent saturated with gypsum, which
is well below the incipient scaling point of 135 percent.
The top side wash was a high intermittent sequential wash with makeup water,
in which each of the 6 spray nozzles was activated in sequence for 3 minutes
n
every 10 minutes at a specific wash rate of 0.5 gpm/ft . Pressure drop
across the nozzles was 13 psi.
11-12
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All available makeup water was used with 2.4 gpm as top side wash and the
remainder as clarified liquor diluent to the bottom side wash.
Some mist eliminator restriction with soft solids was experienced with the
above described wash scheme at low limestone utilization. However, the
restriction would reach a steady-state level rarely above 10 percent and
usually below 5 percent.
11.4 OPERATING CHARACTERISTICS OF SHAWNEE MIST ELIMINATOR
11.4.1 Pressure Drop
Typical pressure drops across the three-pass, open-vane, 316L S.S. chevron
mist eliminator were as follows:
Gas Rate M.E. Superficial Gas Mist Eliminator
Scrubber acfm @ 300°F Velocity, ft/sec @ 125°F AP. in. H?0
TCA 30,000 8.2 0.4 to 0.6
20,000 5.5 0.1 to 0.2
Spray Tower 35,000 9.4 0.5 to 0.7
25,000 6.7 0.2 to 0.4
11.4.2 Entrainment
Of course, the cleanest of mist eliminators is of no significance if it
does not do its primary job of removing slurry entrainment. In April and
May 1977 air/slurry tests were performed on both the venturi/spray tower
and TCA systems in an attempt to determine the amount of slurry entrained
through the three-pass, open-vane mist eliminator. Conditions were less
11-13
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than ideal. The inlet air dust concentration was high, and traces of the
No. 2 reheater oil were noted in the TCA outlet. Corrections were made for
the presence of oil, but there was no way to determine how much the inlet
dust contributed to outlet mass emissions and how much came from entrainment.
The following outlet mass emissions were measured.
M.E. Superficial
Slurry Rate, Flue Gas Rate, Gas Velocity, Outlet Mass
Scrubber gpm acfm @ 300°F ft/sec @ 125°F
TCA
Venturi/
Spray Tower
1200
1400
30,000
35,000
8.2
9.4
0.001
0.001
- 0.005
- 0.003
The range of TCA outlet mass loading was obtained from 20 sets of data points
under 4 sets of test conditions, whereas the venturi/spray tower from 15 sets
of data points under 6 sets of test conditions. Although the data may not
be accurate because of the problems with dust and oil traces, a general idea
on the order of magnitude of slurry emission was obtained.
11-14
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Section 12
OPERATING CONSIDERATIONS
12.1 HOT GAS/COOLING SLURRY INTERFACE
Because of the complex, three-phase flow and simultaneous evaporation conditions
existing at the hot gas/cooling slurry interface, careful attention must be
given to the gas inlet duct design, cooling nozzle selection and arrangement,
and soot blower design.
At Shawnee the hot (300°F) flue gas feed is humidified before entering the
neoprene-lined TCA scrubber to reduce the gas temperature below 190°F, the
maximum permissible for liner protection. Normally, the gas temperature is
reduced to about 150°F. For the venturi scrubber inlet, cooling of the feed
gas is not required during normal operation; the venturi scrubber itself is
an efficient humidifying device.
The solids buildup problem experienced during the early days in the TCA inlet
duct was solved by careful selection of nozzle size and type, orientation,
location and the number of cooling slurry nozzles (Reference 1, Section 10.4).
This effort was supplemented with modification of the soot blower head (both
nozzles facing forward at a 45° angle), the soot blowing cycle (air blowing
during forward travel only) and installation of a Y-Strainer in the process
12-1
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slurry line to the cooling spray nozzles. With these modifications the wet-
dry interface was moved to within 12 inches of the scrubber entrance, from
where the accumulated solids could be easily blown into the scrubber and dis-
charged through the 48-inch downcomer for reslurrying in the effluent hold
tank.
12.2 FIELD LABORATORY pH MEASUREMENT
A detailed report covering the tests, recommendations, and subsequent results
of using improved procedures for laboratory pH measurement (in the field sam-
pling laboratory located on the scrubber structure) was issued in September
1976 (Reference 23). Discussion of in-line process pH meters (referred to
as "meter pH" as opposed to the "laboratory pH") can be found in Section 13.7.1
Measurement of laboratory pH in slurry liquor at the Shawnee Test Facility was
subject to frequent unexplained pH excursions, and there was a high rate of
pH electrode failure before the situation was brought under control in the
spring of 1976. This situation was tolerable during runs lasting many days
but became unacceptable during short-term factorial tests. These tests re-
quired changing the run conditions every 6 to 8 hours and controlling slurry
liquor pH within 0.1 pH unit.
An intensive study of the laboratory pH measurement procedure in February
and March 1976 revealed that variability of laboratory pH data in the past
was due primarily to thermal cycling (cold buffer to hot slurry) of the elec-
trodes and to fouling of the reference electrode junction by slurry solids.
An analysis of the problem produced a number of recommendations for improved
quality control, all of which were implemented.
12-2
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A fully enclosed heated and air conditioned field laboratory was constructed
on the scrubber structure to facilitate sampling. A pH meter (Fisher Model
520) with digital readout (to 0.001 pH unit) was used in the field laboratory
after March 1, 1976.
Use of laboratory-prepared (homemade) buffers was discontinued at the facility;
certified buffers with known temperature dependence were used for buffering
of all glass electrodes. More importantly, off-line electrodes were stored
at pH 4 in hot (50°C) solutions saturated with potassium chloride (KC1).
This method of storing electrodes between service periods had three important
functions:
• The hot (50°C) solution minimized thermal stress by holding the
electrodes at a constant temperature while on-line or off-line.
With this method of storage, repeated cycles of heating and cooling
were eliminated.
• The saturated solution of KC1 increased life expectancy of the
electrodes by preventing reference cell dilution.
• The low pH (pH 4) of the solution reduced reference junction
fouling by preventing buildup of acid-soluble solids on the
cell surfaces during storage. It also kept the glass membrane
sensitized.
The slurry liquor pH reading procedure was further improved by using two
electrodes (one for each scrubber system), switching the electrodes at the
beginning of each 8-hour shift, allowing a constant 4 minutes per reading
whether in the slurry or in the buffer, and renewing the buffer solution at
the beginning of each day shift.
Use of electrodes with rubber-stopper connections was discontinued following
the pH study at Shawnee. Uniloc and Broadley-James combination electrodes,
both with glass-to-glass seals, were used after March 1976. These electrodes
12-3
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performed well. Quality control criteria required an electrode to be discarded
either if it could not be zeroed at the correct buffer pH with the pH meter
control, or if it did not agree (within 0.2 pH unit in a slurry sample) with
two new electrodes used for comparison purposes. In addition, onsite personnel
were instructed to investigate the discrepancy if the field laboratory pH and
in-line process pH ("meter pH") values disagreed by more than 0.2 pH unit for
more than 2 hours.
The improved procedures outlined above were practiced at Shawnee after March
1976 with very good results. Electrode life was measured in months instead of
weeks, and virtually no problems or inexplicable pH variations were encountered.
12.3 REHEAT
An important consideration common to all wet scrubbing systems 1s the dispersal
of the wet scrubbed gas. The most common practice is to heat the wet gas to
impart buoyancy. Methods of reheat include direct oil-fired systems, steam
heated coils, and Indirect reheat systems in which the hot gas Is generated
in a separate combustion chamber and subsequently mixed with the flue gas.
At Shawnee the original direct oil-fired system was modified to an indirect
reheat system with an external oil-fired combustion chamber for improved
reliability (Section 13.3). The degree of reheat required varies with the
height of the stack, the nature of the surroundings, the efficiency of the
mist eliminators, the desire to minimize steam plume, the prevailing ambient
temperature and other meteorological conditions such as dew point, wind speed,
wind direction, etc. Common U.S. design practice has been to provide 50 to
75°F of reheat.
12-4
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At Shawnee, the reheater operation has never been optimized. The degree of
reheat is knowingly overkill at 125°F. This high level of reheat is main-
tained primarily to prevent $63 condensation, to protect the outlet ducting
and the induced draft fan, and to minimize the scrubber downtime due to
the failure of downstream equipment.
12-5
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Section 13
EQUIPMENT OPERATING EXPERIENCE DURING
LIME/LIMESTONE TESTING
This section summarizes the equipment operating experience during lime/lime-
stone testing during the Advance Testing Period from October 1974 through
June 1978, with both high and low fly ash loading in the flue gas, with and
without magnesium addition, and with and without forced oxidation. Readers
who are interested in more detailed information are referred to References
2 through 5.
13.1 SCRUBBER INTERNALS
13.1.1 Mist Eliminators
Descriptions of the mist eliminator systems tested and the results of those
tests have been summarized in Section 11.
13.1.2 TCA Grid Supports
The 3/8-inch diameter, Type 316L stainless steel grids, installed at 1-1/4
inch centers, were in slurry service for approximately 5 years with no
evidence of significant erosion. After 4 years two bars in the bottom grid
exhibited signs of corrosion. These bars were analyzed and determined to be
13-1
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Type 409 stainless steel, mistakenly installed during a sphere change.
13.1.3 TCA Spheres
Several types of spheres were tested on the TCA system. A summary of their
respective performances has been presented in Section 9.1.4.
13.1.4 TCA Slurry Nozzles
The four main slurry spray nozzles in the TCA are full-cone, open-type nozzles,
manufactured of Type 316 stainless steel by Spraco, Model 1969F. During 5
years in service, the nozzles provided excellent service both in terms of
wear and non-clogging characteristics. Over the years, only a small amount
of erosion occured at the discharge orifice. The insignificant wear rate
is attributed to the low pressure drop (about 5 psi) across the nozzles.
The three inlet gas cooling spray nozzles were manufactured by Bete, No.
ST32FCN (full-cone), with Stellite diffusers (spiral tip). After 11,600
hours of operation the diffusers of two nozzles were so eroded that only one
complete turn of the spiral tip remained. The three nozzles were replaced
with identical units.
13.1.5 Venturi Internals
The variable throat venturi scrubber (Figure 9-12), made of Type 316 stainless
steel, experienced both stress corrosion cracking and erosion during the
Advanced Testing Period, a continuing problem since 1972.
13-2
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Inspection after three years of testing (during the May 1975 boiler outage)
revealed stress cracking on the portion of the inlet duct that extends into
the venturi; a 4-inch wide half circle of duct had fallen off. An 8-inch
hairline crack was also discovered in the venturi housing at the point where
the bull nozzle entered the venturi. The stress cracking did not appear
serious and was repaired by welding. Severe erosion was also noted on the
plug shaft protection shroud and guide vanes. The erosion was severe enough
to require steps to prevent damage to the plug shaft itself. The most success-
ful repair method was to cover the affected areas with an expendable material
that could be replaced periodically. The most suitable material was neoprene,
which lasted up to 2000 hours.
After the May 1975 boiler outage two more pieces of the 40-inch duct extension
at the venturi inlet failed, and erosion of the bull nozzle, plug guide vanes,
and plug shaft sleeve flanges continued. To prolong the life of the guide
vanes and to test materials of construction, the vanes were covered with
metal wear plates or rubber shields (Reference 3, Appendix L).
In 1976, blisters were observed in the rubber lining of the 4-inch piping to
the tangential nozzles and the bull nozzle. One such blister was slit for
attempted repair with epoxy, but this technique was not successful. The
rubber was cut out, and the affected area was successfully repaired by coating
with epoxy.
In January 1977, minor repairs were made to the venturi plug guide vanes and
the shroud. Repairs were also made to the rubber lining in the venturi
flooded elbow. An inspection of the venturi in March 1977 showed serious
abrasion of a section of the guide vane structure that had previously been
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repaired. The protective rubber covering over the four guide vanes had failed
to varying degrees and was replaced with new covering. Maintenance also
included the replacement of the venturi bull nozzle in December 1977 and the
patch repair of the venturi inlet gas duct in February 1978. Solids or scale
deposits in the venturi or the flooded elbow were usually minor and were never
associated with mechanical or erosion problems. It should be emphasized that
solids buildup at the gas/slurry interface in the venturi entrance was also
never significant.
13.1.6 Spray Tower Slurry Nozzles
Two types of slurry nozzles were tested in the spray tower: Bete No. TF48FCN
Type 316 stainless steel nozzles and Bete No. ST48FCN Type 316 stainless steel
nozzles with Stellite diffusers. The "TF" nozzles were made out of one piece
of stainless steel whereas the "ST" nozzles consisted of three pieces: the
base and collar nut of Type 316 stainless and the diffuser of Stellite.
Eight Bete 316 stainless steel nozzles (No. TF4SFCN) were tested for 1565
hours on lime slurry with low fly ash loading. During the test period the
average flow rate per nozzle was 45 gpm at 10 psi pressure drop. Most of the
operation, approximately 1200 hours, was with 8 percent solids slurry. The
remainder was with 4 percent solids slurry. During the testing individual
nozzles lost from 0.93 to 2.43 percent of their initial weight due to erosion.
Most testing on the spray tower during the Advanced Test Program was with
Bete No. ST48FCN nozzles with Stellite diffusers. These nozzles were installed
in March 1974* They provided almost uninterrupted service till their removal
in 1976. Twenty-seven nozzles (7 nozzles/header on the top 3 headers and 6
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nozzles on the bottom header) were used during the 17,500-hour test period.
Only two nozzles had to be replaced during the test period.
In removing the Stellite diffusers for inspection at the end of the 17,500-
hour, the impact of the pipe wrench on the collar nut connecting the diffuser
to the base of the nozzle fractured ten of the diffusers near their tips.
Inspection of these nozzles revealed that the major portion of the nozzle wear
was confined to the diffusers. After 17,500 hours of testing the average
thickness of the diffuser decreased from 0.260 inch to 0.193 inch, which
represents a reduction of 26 percent. The maximum erosion of the base, mea-
sured by a diameter increase, was 20 percent after 10,685 hours of service.
New Stellite diffusers were installed in January 1977. In March 1977 after
a total of 2649 hours, 973 hours of which were in limestone service and 1676
hours in lime service, the diffusers were found to have negligible pitting
and relatively uniform wear as shown by measured thickness of the reference
area of four randomly selected diffusers:
4th level (upper) 0.253 inch
3rd level 0.223 inch
2nd level 0.220 inch
1st level (lower) 0.217 inch
These findings illustrate that flow rates through the four headers were
approximately equal with a possible reduced flow rate at the fourth level.
The metal used for these diffusers, Stellite VI, contains 25 percent chromium,
5 percent tungsten, 1 percent carbon, and 69 percent cobalt.
Service life of about 2 years for the ST48FCN nozzles is considered very
satisfactory under moderate pressure drop of about 10 psi. Occasional
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plugging by loose scales of these nozzles was experienced due to malfunction
of the strainers located upstream in the slurry line.
13.1.7 Spray Tower Trapout Funnel
Separation of slurry leaving the venturi scrubber from that leaving the spray
tower is necessary in some cases to achieve independent scrubber loops for
forced oxidation testing. This flow separation is accomplished by a large
trapout funnel installed in the spray tower below the bottom level of spray
nozzles (see Figure 6-1). Flue gas moves upward around the funnel periphery
through the one-foot annular space at the wall of the spray tower and is
then deflected over the funnel by an annular ring attached to the tower wall.
The annular ring also serves to direct falling slurry spray from above into
the trapout funnel. It should be noted that a trapout funnel is not neces-
sarily an efficient or practical mean of separating slurries in a full-scale
plant, but it was expedient at Shawnee. Widespread use of a trapout funnel
in full-scale plants would not be expected.
No evidence of corrosion was observed on the funnel, which was constructed
of Type 316L stainless steel.
During normal operation, accumulations of solids on the underside (gas side)
of the funnel were a common occurrence. After one limestone forced oxidation
run, nearly complete plugging occurred on one portion of the funnel. Solids
grew progressively on its outer edge until they were only a few inches from
the bottom of the deflector ring. No solids accumulated on the inside of
the funnel and no interference with slurry flow through the funnel downcomer
was noted.
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13.2 OXIDIZERS
13.2.1 Air Spargers
The slurry oxidation system (Section 6) consists of an air bubbler in the tank
bottom and a slurry agitator. The oxidation tanks are tall and thin (7 to 8
feet diameter x 20 feet high) to provide long air/slurry contact time.
The first air sparger was an octagonal ring with 130 1/8-inch holes pointed
downward and was installed near the bottom of the oxidation tank of the
venturi/spray tower system (see Figure 6-2). Inspection of the sparger
after 1745 hours of service revealed that 54 air holes were badly eroded, 33
were slightly eroded, and 65 were plugged with hard scale. This sparger was
replaced by a sparger ring of the same size but having 40 1/4-inch holes.
Inspection of the new sparger ring after 2400 hours of operation Indicated
that a spool piece connecting the sparger ring and the compressed air source
was completely eroded through and that most of the air had been escaping
from the holes in the spool piece. Type 304 stainless steel had been erro-
neously used as the spool piece material. Despite the non-uniform distribu-
tion of air through the spool piece, high oxidation efficiency was achieved
during this test period.
Based on this discovery, the air sparger ring was replaced with a 3-inch
diameter pipe extending to the center of the tank. Air was discharged down-
ward through a 3-inch elbow at the end of the pipe. Oxidation efficiency
continued to be high with this arrangement, indicating that the agitator
played a key role in providing air/slurry contact. The agitator used was
a 20 Hp axial down-flow agitator rotating at 56 rpm.
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The venturi/spray tower sparger ring with 40 holes of 1/4-inch diameter was
installed in the TCA oxidation tank (see Figure 6-8). The ring, constructed
of 316L stainless steel, was in good condition except for minor erosion
at the 1/4-inch air holes. A conventional tank agitator (37 rpm, 3 Hp) was
used for mixing. Despite marginal air/slurry contact with weaker agitation,
near complete oxidation was achieved with this configuration. Future tests,
designed to determine power requirements, will use a variable speed agitator.
13.2.2 Oxidation Air Compressors
A Worthington type VBB, size 14-1'2 x 9 inch, single cylinder air compressor
with 100 Hp motor was used for both venturi/spray tower and TCA systems during
the Advanced Test Program. The compressor selected was an oil-free, non-
lubricating type to avoid possible contamination of slurry by the oxidation
inhibitors in the oil.
Maintenance requirements were negligible. The cooling water jackets were
periodically flushed to remove soft scale.
13.2.3 Penberthy Eductor
An eductor is a device that passes a high velocity slurry through a constricted
nozzle into an eductor chamber and then through a moderately restricted jet
throat. In the chamber, the slurry creates a vacuum that draws ambient air
into the chamber via an entry pipe located at right angles to the slurry flow
path. The air is then entrapped and mixed in the slurry as the fluid leaves
the eductor chamber and passes through the jet throat.
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At Shawnee, a Penberthy Model ELL-10 Special eductor was tested. The materials
of construction were Stellite for the nozzle and a whirler inside the nozzle,
and neoprene-lined carbon steel for the eductor chamber and exit jet throat.
The eductor was normally operated at 1600 gpm slurry flow rate.
Test results indicated near-complete oxidation, but serious erosion prob-
lems were noted. The neoprene lining in the jet throat was chipped off
after only 620 hours of operation. After approximately 1800 hours of
operation, bare carbon steel was exposed. Tests were terminated after 2055
hours of operation when an epoxy patch failed. In view of cost disadvantage
compared to simple air sparge systems and severe erosion problems, further
testing of the eductor is not planned.
13.3 REHEATERS
Scrubbed flue gas was reheated to prevent acid condensation and corrosion in
the exhaust system, to facilitate analytical sampling, to protect the
induced-draft fans from solid deposits and droplet erosion, and to increase
plume buoyancy.
The original in-line, fuel-oil-fired units supplied by Hauck Mfg. Co. expe-
rienced frequent flameout and incomplete oil combustion. The Hauck reheaters
were modified in March 1974 (venturi/spray tower) and May 1975 (TCA) to
incorporate a fuel-oil-fired external combustion chamber manufactured by
Bloom Engineering Co. Both units operated reasonably well following the
modifications with only periodic flameout and minor electrical problems.
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13.4 INDUCED-DRAFT FANS
The Type 316L stainless steel fans at the Shawnee Test Facility are induced-
draft, centrifugal fans manufactured by Zurn Industries. Reliability was
fair to good during the Advanced Testing Period, with the only system
downtime being due to the following fan problems:
• Occasional cleaning of the fan, fan dampers, and duct
between the dampers and reheaters.
• Replacement of the I.D. fan outboard bearing and pillow
block, 8 times for the two fans.
• Replacement of the motor on the Beck damper position
control on five occasions.
• Servicing and adjusting the damper control linkage.
• Repairing a 4-inch hairline crack on the venturi/spray
tower fan rotor. The crack was successfully repaired
by welding with a Type 347 stainless steel rod and
grinding the weld smooth. Initial repair using a 316L
stainless steel welding rod was not successful.
13.5 PUMPS
13.5.1 Allen-Sherman-Hoff Pumps
The Allen-Sherman-Hoff centrifugal pumps are neoprene lined, slurry service
pumps equipped with Nelson liquid drive units. The pump packing was con-
ventional graphite-impregnated asbestos. The sleeves were chrome-plated
steel. Pump seals were air-flush type used to prevent excess water input
to the system.
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In light of the wide range of operating conditions experienced, it must be
acknowledged that the pumps provided satisfactory service and required only
moderate maintenance. The most frequent maintenance was repacking. Although
there was no apparent pattern associated with repacking frequency, the
following general trends were observed:
• Wide flow variation as dictated by changing test condi-
tions increased repacking frequency.
• Operation of a pump at the low-flow end of the pump curve
accelerated the frequency of packing problems.
Somewhat less frequent but routine pump maintenance included fluid change
in the vari-drive, replacement of the fluid cooler on the vari-drive, and
replacement of pump sleeves.
13.5.2 Moyno Pumps
Moyno pumps are positive displacement, variable speed pumps used primarily
for moving thick slurry at Shawnee. Five such pumps are employed as alkali
addition pumps. A larger sized Moyno is used to recirculate underflow slurry
in the TCA clarifier. The latter pump experienced limited service.
Moyno pump rotors are helical shaped and are made of chrome-plated steel for
abrasion resistance. Stators are rubber-lined with a double helical groove.
The most frequent maintenance problem was erosion of pump stators. An infre-
quent problem was the loss of pump capacity due to erosion of the rotor
surface after what appeared to be a chrome plating failure. The pumps were
oversized by a factor of two. They were allowed to wear until the required
flow could no longer be maintained. Typical operating life for a stator and
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rotor was 1000 and 2000 hours, respectively.
13.6 ALKALI ADDITION SYSTEMS
13.6.1 Lime
The slaked lime preparation system consists of a pebble lime storage silo,
a screw feeder, a Portec-Cahaba lime slaker, a slaked-lime holding tank and
associated feed pumps. Fresh water is used to slake the lime to a slurry
of approximately 20 weight percent solids. The system has exhibited good
reliability, once its early startup problems were overcome.
Over the years minor modifications have been made and some maintenance has
been performed. Activities worth noting were:
Modifications
• The original (vendor supplied) nozzles in the sprays for
the grit screen were replaced with more open nozzles to
increase the spray flow rate.
• The grit screen drive bearings (2 sets - 1-1/2 inch and
1-5/8 inch), were replaced with Dodge type E pillow
block bearings.
• Larger slaking water control valves and larger sprockets
for the lime screw feeder were installed to increase
capacity.
• The lime slurry sump pump start/stop float linkage was
replaced with an improved version to prevent dc.nage to
the mercury switch controls.
• An alarm was installed at the control board to notify
the operator of screw feeder stoppage.
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Maintenance
• The slaker (grit) screen has been replaced only 18 times
in nearly 7 years of operation since 1972. Carbon steel
screens tend to wear out from grit abrasion and from the
hydro chloric acid used periodically to remove carbonate
scaling on the screens.
• The slaker screen motor has been replaced twice, the drive
shaft once, the bearings once and the motor over-heat
detector once.
• The slaker process control elements have been cleaned and
serviced once, the unit painted once, and the air leaks
the lime silo baghouse repaired once.
13.6.2 Limestone
The limestone slurry preparation system consists of a limestone drying/grind-
ing system, four limestone bins, a weigh belt feeder, a limestone slurrying/
surge tank, and associated feed pumps. (The drying/grinding system came
from an earlier EPA Dry Limestone Injection Project which preceded the present
wet scrubbing program.)
For slurrying purposes, pulverized limestone from the grinding system is
pneumatically conveyed to a 1-day storage silo from where it is belt-fed into
the 400 gallon limestone slurry preparation tank. Slurry solids concentration
is controlled at nominal 60 weight percent.
In view of the system usage, it can be said to have provided acceptable perfor-
mance with moderate maintenance. Most of the maintenance has been asssociated
with the drying/grinding system. The major maintenance activities were as
follows:
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• Equipment vibration resulted in damage to the electronic
components circuit boards of the fuel oil and dryer
temperature controllers. New controllers with more
vibration resistant mounting were installed.
• Refractory in the burner section of limestone dryers was
patched in April, October, and November, 1977. Kaocrete B
has been used successfully.
• The Graham three-taper pin assembly in the variable speed
drive for the limestone dryer feedbelt was repaired and
was subsequently replaced.
t The oil atomizing air compressor for the limestone dryer
has been repaired once.
t The ball mill feeder circuit, magnetic starter for feed
belt motor, and fuel oil controller circuit board were
replaced.
t The gear box on the limestone mixer feedbelt has been
replaced once.
• The top impeller of the mixer in the limestone slurry
preparation tank has been adjusted and spaced properly on
the shaft to improve continuous mixing of the ground
limestone and water.
13.7 INSTRUMENT OPERATING EXPERIENCE
13.7.1 In-line pH Meters
Process pH is measured using Uniloc Model 312L submersible electrode assemblies
(See Section 12.2). These assemblies are manufactured by Universal Interloc,
Inc., of Santa Ana, California. Originally, Uniloc Model 320 flow-through
meters were used, but because of line plugging problems and frequent sensing
electrode breakage, use of these type sensors was abandoned.
Service requirements for the submersible assemblies consist of periodic
cleaning and buffering of the electrodes, generally every 2 or 3 days to
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ensure accuracy. Also, to minimize the service requirement, the instrument
electrodes are placed in water during scrubber outages. On infrequent occa-
sions the electrode assembly has failed due to assorted reasons, such as wet
electrical contacts or bad reference or sensing electrodes. The principal
continuing service requirement of the Model 321L pH meters has been scale
removal from the probes. The frequency of cleaning has depended on the
operating conditions of the scrubber and has ranged from once every few days
to once every few weeks. This scale causes measurement error and can be
removed with hydrochloric acid. All probes are also routinely rinsed with
water at least twice a week. A short test was conducted in April 1975 using
a continuous ultrasonic cleaner for the prevention of scale buildup. The
cleaner was effective at preventing heavy scale buildup.
To ensure the accuracy of the process pH meters, a laboratory pH measurement
(with a portable pH meter, see Subsection 12.2) is made once every two hours
for comparison purposes. This procedure enables pH control to be maintained
within _+ 0.2 pH units of the desired set point.
13.7.2 S02 Analyzers
A Du Pont Model 400 UV split-beam photometer, equipped with an automatic zero-
ing and air purging system (1 minute every 10 minutes frequency), is used to
measure S02 concentrations. The instrument has been accurate and reasonably
trouble-free. Maintenance requirements have been limited to cleaning the
sample cell and sample lines approximately once every 1 or 2 months and to
cleaning the particulate filter about once every 3 to 4 weeks. In addition,
the optical filter is calibrated twice per week, and the instrument is cali-
brated against the calibration gas once per week with a simultaneous check of
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the optical filter. Ultraviolet lamp failure has been the only component
problem and is caused by uncontrollable and momentary power fluctuations
resulting from switching of station power. An effective particulate filter
for the instrument is a cylindrical chamber constructed of a fine mesh screen.
The screen cylinder is surrounded by a solid protective cylinder. The gas
sample lines operated leak free; the lines are of heat traced Teflon tubing.
13.7.3 In-line 02 Analyzer
Oxygen concentration in the inlet flue gas is measured with a Teledyne Model
9500 meter which was put in service on June 15, 1977. The meter uses a micro-
fuel cell as the sensing element. Based on a year's operating experience
the overall sampling and instrumentation performance has not been satisfactory.
Pertinent problems included:
• Five fuel cell failures with a cell life range of 1 to
30 days.
0 Two sequence mechanism failures.
• Two solenoid valve failures.
• Freezing of instrument scrubbing water supply.
The unit operated for less than six weeks total time during the year of
testing.
The test facility currently uses four Thermox 02 analyzers which were installed
in November 1978 at inlets and outlets of the venturi/spray tower and TCA.
13.7.4 N02 Analyzer
Another Du Pont Model 400 UV photometer was modified by Du Pont technicians
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in 1976 to analyze for Nt^, which constitutes a small fraction of total NOX.
Over a 14-month period no useful data was obtained due to an erratic output
signal. Numerous modifications and checks have been performed by Du Pont
representatives but the source of the problem has not been located. The
installation is therefore judged to be a complete failure.
13.7.5 Magnetic Flowmeters
The original 1-1/2 inch Foxboro magnetic flowmeters, Series 1800, were lined
with Scothane that rapidly deteriorated in service. Subsequently, the meters
were relined with Adiprene-L. The new liners failed after periods ranging
from 3 to 9 months due to blister formation, subsequent erosion of the blister,
and eventual stripping away of the liner. It was then noticed that these
liners were tapered in thickness near the meter exit. The meters were relined
with Adiprene-L of uniform thickness in September 1975, after which no liner
failures were experienced. Larger meters (6 to 8-inch size) were lined with
neoprene. No difficulties with liner deterioration were experienced with
the neoprene-lined meters.
In 1976 Foxboro discontinued manufacture of the Series 1800 meters used at
Shawnee. The company now offers a more compact Series 2800. These Series
2800 magnetic flow meters, 1-1/2 inch or smaller, are lined with Teflon rather
than Adiprene-L. The Teflon liner has performed satisfactorily.
Periodic scale removal is required to maintain accuracy and sensitivity and
on infrequent occasions the magnetic converter requires maintenance. Satis-
factory meter accuracy is maintained by electrical purging once per shift
with the Foxboro Magnetic Flow Meter Electrode Cleaning Assembly. The elec-
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trode cleaning assembly applies line power voltage between the transmitter
electrodes and the transmitter tube. The current flow oxidizes away electrode
deposits and thus removes the condition of high resistance between electrodes
and the process liquid for normal accurate operations. The meters are
considered reliable, acceptably accurate, and easily serviced.
13.7.6 Density Meters
Both Dynatrol Model CL-10HY U-tube density meters and Ohmart radiation
density meters are used at Shawnee. Although the U-tube density meters are
preferred, both types of meters provide acceptably accurate and dependable
service. The instruments are used primarily for monitoring trends in slurry
density values. Initially the U-tube meters experienced plugging problems.
The cause was attributed to operator misjudgement in setting too low a flow
through the instrument. Improved performance has been noted after the opera-
ting personnel were properly trained.
13.7.7 Level Measurement
Three Brooks Magi ink 5300 Series level indicators were installed in three
scrubber effluent hold tanks for evaluation. The Brooks indicator consists
of a vertically mounted standpipe fastened externally or internally to the
side of a tank, with a bottom liquor inlet to the chamber. Slurry level
is detected by a donut-shaped float surrounding a small center pipe running
the length of the stilling chamber. A magnet inside the sealed center pipe
moves with the float and provides a level signal from its position.
The initial problem was solids buildup on the float, which led to eventual
immobilization. A liquor flush stream was installed in an effort to eliminate
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the problem, but the following difficulties continued:
• Dislodging an immobilized float occasionally uncoupled
the magnet.
• Altering the measurement range required the installation
of a new gear drive.
• Floating material caused occasional immobilization of
float.
• The flush system liquor stream impinged on the float
causing float depression and reading error. The
magnitude of the error was variable and depended on
the distance the purge stream free fell prior to
impingement on the float.
When working properly, the Brooks indicator measured slurry level in the efflu-
ent hold tank to within 6 inches. However, solids clogging the standpipe and
float were a common occurrence.
The most widely used level indicators were the Foxboro differential pressure
(atmosphere/tank pressure) Model 617 FEM with Teflon coated stainless steel
diaphragm. The instruments had three recurring problems:
• Deposits of mud or scale on the diaphragm caused false
readings. Cleaning of the diaphragm requires draining
of the tank.
a Changes in slurry density changed the indicated level.
• Transmitter electronics were sensitive to the ambient
temperature. Foxboro claims that the problem has been
corrected on newer models.
13.8 OTHER MATERIALS AND EQUIPMENT EVALUATION
During the advanced Test Period the following equipment and materials were
monitored:
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• Lining and piping
• Control valves
• Strainers
13.8.1 Lining and/or Coatings
Lining and/or coating materials for equipment at the Shawnee Test Facility
generally consist of neoprene (pipes, pumps, scrubber internal walls and
small tanks) or Flakeline 103 (large effluent hold tanks and clarifiers).
Flakeline 103 is a bisphenol-A polyester resin filled 25 to 35 percent with
glass flake and is manufactured by The Ceil cote Company.
Both neoprene lining and Flakeline coating have shown only minor erosion or
other deterioration. Whenever necessary, successful repairs have been made
using Epoxylite-203 (Epoxylite Corp., Anaheim, California), an epoxy resin
formulated with selected fillers. The resin was cured with Epoxylite1s
No. 301 amine hardener. For example, a patch on the venturi/spray tower
effluent hold tank agitator blade showed only ninor wear after more than
25,000 hours.
Testing of three test panels provided by Ceil cote Company was completed in
1976. Approximately one-third of the exposed surface of each panel was
covered with one of three Ceilcote formulations: Flakeline 103, Caroline
505AR and Flakeline 151. All three formulations on the test panel mounted
inside one of the TCA beds exhibited significant wear after 6634 hours of
exposure.
In a 1976 test, selected areas of neoprene lining, glass surfaces and stain-
less steel surfaces (mist eliminator vanes) were cleaned and McLube No. 1700
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coating was applied. This material is designed to keep ship hulls free of
barnacles, and it was hoped the material would prevent solids accumulation.
Results were unsatisfactory. The tops of coated mist eliminator vanes held
more solids than did some uncoated vanes in the immediate vicinity. It is
possible that the coating did not cure or dry exactly as desired.
Infrequent hardness measurements were made on areas of tower lining in contact
with spheres or areas receiving direct spray impingement. The range of Duro-
meter A hardness readings was 42 to 60 (at 65° to 90°F), as compared to 60
to 65 (at 73°F) original vendor's data. Higher temperature gives a lower read-
ing. Generally, the lining was in good condition although the surface where
scale was often removed exhibited scabs from chipping tools. There was no
evidence of rubber lining separation from the metal substrate.
A test panel (20 x 15 x 3/8 inches) supplied by Pullman Kellogg, made of
carbon steel and coated with fluoroelastomer CXL-2000, was installed in the
inlet gas duct of the TCA scrubber for the purpose of determining the ability
of the material to withstand the hot gas/slurry environment. It was arranged
to have cooling slurry spray impinge across its face. Inspection of the
panel after approximately 2000 hours in service showed that the coating had
failed along the exposed flanged edge allowing erosion of the carbon steel
substrate. Therefore, the material was judged to be unsatisfactory for the
conditions under which it was tested.
Results of extensive and thorough materials evaluation work at Shawnee are
included in the Five Reports on Corrosion Studies published by TVA (see Appen-
dices of References 1, 3, 4, and 5*).
Reference 1 contains two reports.
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13.8.2 Piping
After 5 years in service, blisters were observed in some sections of the
neoprene lined pipe. However, these blisters did not precipitate pipe
failures or blockage, and therefore did not lead to operating or maintenance
problems.
During a number of system modifications, sections of plastic pipe and fittings
were installed for evaluation in slurry service. Schedule 80 PVC 1120 (ASTM
D-1785) piping of 6-inch and 8-inch diameters was installed for the TCA re-
circulating slurry lines. Fittings were all of standard radius design. PVC
piping also served the venturi/spray tower oxidation tank system. Operation
with PVC piping has been satisfactory, with respect to corrosion and erosion,
over the limited time span of its use. However, some mechanical failures have
been experienced due to impact of heavy objects.
A section of U-shaped Bondstrand, fiberglass-reinforced 8-inch plastic pipe
was removed from service after approximately 8800 hours. It had been installed
in the suction line of the TCA recirculating slurry pump. There did not
appear to be significant wear of the pipe surface and the entire section was
judged to be in excellent condition.
A section of 8-inch polybutylene pipe, having the same configuration as the
Bondstrand pipe, was also installed in the suction line of the TCA recircula-
ting slurry pump. There was no evidence of erosion in the polybutylene pipe
after about 3550 hours of service.
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13.8.3 Valves
A Valtek 6-inch butterfly control valve was located in the spray tower
recirculating pump discharge line. Inspection after 3000 hours of service
revealed hairline cracks in the valve body and some slight disc erosion.
Flow rate control, at 700 to 800 gpm, was good. Inspection after 4853 total
service hours (1551 hours wide-open and 3302 hours in throttling service)
revealed small fissures in the body bore, up to 3/4 inch long, and a great
amount of erosion in the lower half of the valve body. The two deepest
grooves were 0.180 and 0.162 inch. In contrast to the body failure, the
Stellite-coated disc showed some slight waviness of the disc edge thickness.
Continued use of the valve resulted in further erosion of the valve body.
Previously observed grooves had deepened and the worst single hole located in
the disk plane was 0.28 inch deep. Thickness measurements at the outer edge
of the Stellite disk ranged from 0.22 to 0.24 inch.
A Fisher 2-inch Stellite butterfly control valve was originally installed in
September, 1976, on a slip-stream from the spray tower recirculating pump
discharge line. Inspection after 2 months of service indicated that the fish-
tail disc was in excellent condition. Only slight erosion or rounding of
sharp edges of the disk occurred, along with some slight pitting. Minor
pitting was seen on the leading (upstream) edge along the rear face. Pitting
was found to a greater extent on the back face than on the front face where
a few pits were seen. A magnifier was needed to see these shiny pits, which
were estimated to be 2 to 3 mils deep and 10 mils in diameter. The rear
half of the disc (trailing edge) where the fish tail was located appeared to
be in good condition. Minor erosion took place in the body of the valve in
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the plane of the closed disk position. The estimated maximum depth of wear
was 0.5 mm. The valve body appeared to be wearing faster than the disk in
throttling service. Six months after its installation, the valve was moved
from the venturi/spray tower to the TCA system.
A Durco 6-inch butterfly valve with a high-density polyethylene-coated disc
was located in the discharge line of the pump that fed the top two spray
tower headers. A total of 3700 hours of service with 8 percent slurry at
approximately 9 ft/sec slurry velocity through the valve (in full-open posi-
tion) resulted in a 4.5-mil loss of the disc coating thickness. This repre-
sented about 10 percent of the total coating thickness. The throat was in
good condition and there was no leakage through the valve when leak-tested
at 55 psig. A later inspection after approximately 8000 hours in slurry
service showed no further erosion of either the polyethylenecoated disc or
the valve body liner. All wetted surfaces were coated with a thin scale.
This valve is considered to be in excellent condition except for four small
irregular wear patterns at the disk edge probably caused by debris trapped at
the sealing edge during closure. The valve body liner of abrasion-resistant
polyethylene is in excellent condition. Measurements of the disk thickness
show no change or loss of the coating material. The valve service is pri-
marily in the open position.
The knife gate valves tested at Shawnee are Type 316 stainless steel Fabri-
Valves. There are a total of eight such valves in service: four on the
Hayward strainers on the TCA recirculating slurry pump (G-201) discharge and
the remainder on the Hayward strainers on the spray tower recirculating slurry
pump (G-204) discharge. Inspections were confined mainly to the four, 6-inch
13-24
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All four valves could be operated by the hand wheel after application of
grease onto the stems and into the knife gate slots. Observations specific
to each valve were:
• The valve on the downstream side of the north Hayward
strainer had very slight rounding of the knife gate at
the 6 o'clock position, slight erosion of the valve
body on the downstream edge at the 11 o'clock position,
and small amounts of scale on the downstream face of the
knife gate.
• The valve on the upstream side of the north Hayward
strainer had no bodily erosion and only slight rounding
of the knife gate at the 6 o'clock position. Thin,
smooth scale was found on the suction side. This valve
had a guide piece instead of a backup half-ring provided
in the other valves.
t The valve on the downstream side of the south Hayward
strainer had no bodily erosion and only slight rounding
of the sharp edge of the gate. The backup ring had a
couple of weld spots that had smoothed off.
• The valve on the upstream side of the south Hayward strain-
er had no noticeable erosion. White, hard 10 mil-thick
scale was on the upstream face.
The exterior bodies of all four valves appeared to be in good condition.
Operation of these valves without 0 rings had sometimes resulted in slight
leakage past the gate when the basket was being emptied, but this was not a
very serious problem. The deposition of hard scale on the gate was perhaps
the major factor that made the valve hard to operate and was the major contri-
butor to the failure of the 0-rings.
13.8.4 Strainers
Dual-basket in-line Elliott strainers were originally installed at the
discharge of the TCA and spray tower recirculating slurry pumps to alleviate
13-25
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the problem of slurry nozzles plugging with debris and other foreign materials.
During the May 1975 boiler outage each Elliott strainer was replaced by two
single-basket in-line Hayward Strainers mounted in parallel at the discharge
of each pump. The replacement of the Elliott strainers became necessary
because of the serious erosion that developed in the outlet necks. For the
Elliott strainer on the TCA pump discharge, erosion was also observed on edges
where the slide gate sealed each basket chamber. Inspection after approximately
3700 hours of service revealed that the iron body of the Elliot strainer was
severely eroded in several areas. The 316 stainless steel baskets (30-mil
thick with 3/8-inch-diameter perforations) had not eroded significantly.
Results of inspections of the 6-inch single-basket Hayward strainers on the
spray tower pump discharge after approximately 8000 hours of service were:
0 Erosion at several locations on the basket support
ledge. At two of the locations, where severe erosion
had occurred, about 80 percent of the ledge had
disappeared.
• Severe gouging, as much as 1/4 inch deep, of the
discharge throat was observed at two locations.
• Minor erosion along the inlet flange face, lower half
portion of Unit A.
• A triangular-shaped erosion spot 6 mm deep in the
discharge throat of Unit A.
0 Grooves up to 13 mm deep in the outlet throat of Unit B.
• Two erosion areas in the basket support flange.
• Basket of both units were in good condition.
For the two 8-inch single-basket Hayward strainers on the TCA pump discharge,
inspection after approximately 10,600 hours of service revealed:
13-26
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• A small erosion spot about 20 mm long at the bottom
of the discharge throat of one of the strainers.
• Some erosion of the basket support ledge of both strainers.
This erosion was not very extensive.
• Baskets of both units were in good condition.
Currently both types of strainers are in service. Neither type has shown to
be particularly better than the other.
13-27
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Section 14
FLUE GAS CHARACTERIZATION FOR PARTICULATE
AND SULFUR TRIOXIDE EMISSIONS
A series of tests were conducted on the TCA and venturi/spray tower systems
to determine the effect of the major operating variables on particulate mass
removal efficiency and size distribution, and on sulfuric acid vapor (SOg)
emissions. Additionally, the effect of slurry entrapment on scrubber
particulate emissions was estimated.
During the testing, the scrubber systems were supplied with flue gas from
Boiler No. 10 of the Shawnee Steam Plant, either directly from the boiler
(high fly ash loading) or after the electrostatic precipitator (low fly ash
loading). The flue gas inlet mass loading usually ranged from 3 to 6 grains/
dry scf (gr/dscf) at high fly ash loading, and from 0.04 to 0.20 gr/dscf at
low fly ash loading. More detailed information on the test results can be
found in References 4, 5, and 24.
14.1 PARTICULATE MASS REMOVAL EFFICIENCY
Particulate mass loading values were determined using a modification of EPA
Method Five. A Hi-Volume sampling train manufactured by the Acurex Corporation
was used.
14-1
-------
For both the TCA and venturi/spray tower systems, overall efficiency
increased with increasing pressure drop and decreased with increasing gas
flow rate (gas velocity). Also, outlet mass loadings were higher with a
continuous mist eliminator bottom wash using diluted clarified liquor, as
compared to an intermittent bottom wash with fresh water.
14.1.1 TCA System
At high fly ash loading, the TCA had mass removal efficiencies greater than
98 percent. Outlet mass loading averaged about 0.046 gr/dscf at a pressure
drop of 9 inches H20. The 1971 EPA New Source Performance Standard (NSPS)
for particulate emission of 0.10 lb/106 Btu corresponds to an outlet loading
of approximately 0.052 gr/dscf, assuming 30 percent excess air in the flue
gas. For pressure drops in excess of 7 inches ^0, the outlet loadings from
the TCA were generally below the level set by the 1971 NSPS.
At low fly ash loading, the TCA had removal efficiencies from 50 to 86
percent. Typical outlet mass loadings ranged from 0.018 to 0.032 gr/dscf,
which are well below the level specified by the 1971 NSPS.
However, the performance of the TCA at both high and low fly ash loading did
not meet the NSPS of 0.03 lb/106 Btu (corresponding to approximately 0.016 gr/
dscf) as revised in June 1979.
14.1.2 Venturi/Spray Tower System
At high fly ash loading, the venturi/spray tower system had removal efficien-
cies greater than 99 percent. Outlet mass loading averaged about 0.042 gr/dscf
for a total pressure drop of 16 inches H20, which is below the 1971 NSPS but
14-2
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above the revised 1979 NSPS.
With low fly ash loading, the venturi/spray tower system had removal effi-
ciencies from 80 to 99 percent. Typical outlet loadings ranged from 0.003
to 0.023 gr/dscf, which were well below the 1971 NSPS but met the revised
1979 NSPS only about half of the time.
14.2 PARTICULATE SIZE DISTRIBUTION
Particulate size distributions were measured with heated inertial impactors
located outside of the stack. A Brinks Model BMS-11 impactor was used for
inlet sampling and a Meteorology Research, Inc. (MRI) Model 1502 impactor
was used for outlet sampling.
14.2.1 TCA System
Mass removal efficiency on the TCA for flue gas with high fly ash loading
varied from about 10 to 60 percent for 0.1 micron particles to greater than
98 percent for particles larger than 5 microns. For the low fly ash loading
tests, removal efficiency was between 30 and 75 percent for 0.1 micron
particles and about 90 percent for particles larger than 5 microns.
For the high fly ash loading tests, emission of particles less than 2 microns
in diameter averaged 0.025 gr/dscf, except for a low gas rate run and a low
slurry rate run where the average was higher at 0.037 gr/dscf. This decreased
removal efficiency would be expected with slurry or gas turndown in a TCA
because of decreased sphere activity in the beds. Emission of particulates
with diameters greater than 2 microns averaged 0.028 gr/dscf, except for a
14-3
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run with a continuous mist eliminator bottom wash and a run with MgO addition
where the emissions averaged 0.055 and 0.038 gr/dscf, respectively. Emissions
during a low fly ash loading run averaged 0.003 gr/dscf for particles with
diameters less than 2 microns and 0.025 gr/dscf for particles with diameters
greater than 2 microns.
14.2.2 Venturi/Spray Tower System
Mass removal efficiency of the venturi/spray tower system for the flue gas
with high fly ash loading varied from 50 to 80 percent for 0.1 micron par-
ticles to greater than 99 percent for particles larger than 5 microns. For
the tests with low fly ash loading, removal efficiency was the same for 0.1
micron particles but decreased to approximately 95 percent for particles
larger than 5 microns. Within the ranges tested, the removal efficiency
appeared to be fairly independent of the levels of the independent variables,
such as gas rate, slurry rate, and pressure drop.
Mass emission of particles less than 2 microns diameter averaged 0.016
gr/dscf for the high fly ash loading tests. Emission of particles greater
than 2 microns averaged 0.006 gr/dscf for all tests except for a test with
MgO addition and a test where the venturi was operated at minimum pressure
drop. The data for these runs was not of sufficient quality to estimate a
mass emission for the greater than 2 micron diameter particulate. For a low
fly ash loading test, emissions for particles less than 2 microns in diameter
averaged 0.002 gr/dscf while emissions for particles greater than 2 microns
in diameter averaged 0.003 gr/dscf.
14-4
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14.3 SLURRY ENTRAINMENT
Non-dispersive infrared and thermo-gravimetric analysis of the participate on
a single outlet filter from a TCA test with low fly ash loading indicated that
emissions from entrained scrubber reaction products were in the range of 0.005
gr/dscf. This compares to an emission level in the range of 0.025 gr/dscf for
particles greater than 2 microns (or a total emission of 0.028 gr/dscf for all
size particles). Additionally, results from air/slurry entrainment tests on
the TCA (Section 11.4.2) indicated a slurry (40 percent fly ash and 60 percent
reaction products) entrainment value between 0.001 and 0.005 gr/dscf. These
results would indicate that less than 20 percent of the particulate emissions
from the scrubber systems are entrained reaction products.
Scanning Electron Micrographs (SEM) were taken of the scrubber outlet parti-
culate captured on the impactor third stage (7.8 to 9.3 microns cut size)
and sixth stage (1.1 to 1.2 micron cut size) during a venturi/spray tower
test. Very little emitted reaction products were visible on the sixth stage
(the deposits appeared to be all spherical fly ash) while crystals of
CaS03*l/2H20 (rosettes) were visible on stage three. These SEM photographs
suggest that the emitted scrubber slurry reaction products are concentrated
in the larger particle size fractions, i.e., greater than 2 microns.
Other testing has also indicated that the emitted reaction products are
concentrated in the larger size fractions. For example, continuous diluted
clarified liquor mist eliminator underwash in the TCA significantly increased
emissions only in the greater than 2 micron fraction range. Also, addition
of MgO to the scrubber liquor, which increases total dissolved solids,
resulted in an increase in emissions for the larger particle size fractions.
14-5
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14.4 SULFURIC ACID VAPOR (S03)
The vapor phase concentrations of sulfuric acid (S03) were measured using
a controlled condensation technique. S03 measurements on the TCA and venturi/
spray tower systems indicated that the percent S03 removal was independent
of the levels of the operating variables (e.g., pressure drop) and inlet
S03 concentration.
For the TCA system S03 emission concentrations ranged from zero to 16 ppm
with average removal ranging from 18 to 88 percent. For the venturi/spray
tower system, S03 emission concentrations ranged from zero to 14 ppm with
average removal ranging from 50 to 75 percent. The fact that the outlet S03
concentrations were always below the inlet concentrations indicated that the
scrubbing process did not contribute to S03 emissions.
14-6
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Section 15
WASTE SOLIDS DEWATERING AND HANDLING CHARACTERISTICS
At Shawnee the primary dewatering of the scrubber slurry occurs in the
clarifiers. Further dewatering of the clarifier underflow is usually
accomplished in the venturi/spray tower system by a rotary drum vacuum
filter and in the TCA system by a centrifuge. With these two pieces of
dewatering equipment in series with clarifiers, a very tight liquor loop
closure can be achieved.
15.1 CLARIFIERS
The clarifiers are conventional Dorr-Oliver solids contact units. Each has
a heavy duty rake and scraper mechanism supported from a bridge. The rake
and scraper have an automatic torque control lift mechanism. The venturi/
spray tower has a 20-foot diameter unit and the TCA has a 30-foot unit.
The clarifiers are operated primarily for their clarification capacity
rather than for their maximum thickening ability. In general, the underflow
solids concentrations are maintained between 30 and 35 weight percent when
operated with the filter or centrifuge downstream and between 35 and 40
weight percent when operated alone. When operating with underflow solids
concentrations in this range, there have been few problems with plugging
15-1
-------
of the underflow line. To avoid plugging when the scrubbers are down, the
clarifiers are put on total recycle, meaning that the underflow is routed
back to the clarifier inlet.
Early in the Advanced Test Program there were problems with unsatisfactory
clarity in the TCA overflow. The problem was corrected by extending the
feed well from 2 feet to 8 feet deep to provide a longer liquid up-flow
residence time and to minimize short-circuiting.
15.2 FILTER
An Ametek 3 ft x 6 ft rotary drum vacuum filter without cake wash is operated
at the facility for waste sludge dewatering and dissolved scrubbing additive
recovery. Cake discharge is achieved by a snap-blowback air cycle.
The feed to the filter (from clarifiers underflow) is typically 15 gpm with
30 to 35 weight percent solids content. The filtrate generally contains
less than 0.02 weight percent solids. The filter cake varies from 55 to 85
weight percent solids, depending mainly on whether the sludge is unoxidized
or oxidized (see Section 15.4).
Filter cloth life has been a major problem. Cloth life varies between 130
hours and 2100 hours. The major causes of failure are cloth blinding and
fraying. Although the reasons for these failures have not always been clear,
operating experience indicated a relationship between cloth life and the
technique by which the cloth is fitted to the drum. A carefully controlled
amount of looseness in the fit between the dividers appeared to be desirable
for cake discharge and non-blinding. The looseness evidently allows the
15-2
-------
cloth to "snap" the cake off when the air puff during the cake discharge
cycle is applied to the given filter cloth section. Two additional obser-
vations are that (1) oxidized sludge exhibited less tendency towards cloth
blinding and (2) the Ametek olefin cloth appears to provide the most satis-
factory service of those cloths tested. The reason for the better service
life of Ametek cloth is attributed to the looseness of weave. Results
from air permeability tests showed a correlation between higher initial
air permeability and longer cloth life. (Cloth permeability is a function
of the looseness of the weave.)
15.3 CENTRIFUGE
An 18 x 28 inch solid bowl continuous centrifuge manufactured by the Bird
Machine Co. is used to dewater scrubber waste sludge from the clarifier
underflow in the TCA system. Typical operating conditions consist of a
feed stream flow of 15 gpm at 30 to 35 weight percent solids, a centrate
of 0.1 to 3.0 weight percent solids, and a cake of 55 to 65 weight percent
solids for unoxidized slurry. A cake of 70 to 80 weight percent solids
is typical for oxidized slurry.
The abrasiveness of the feed slurry tends to wear certain components of the
centrifuge. As the centrifuge wear increases there is a gradual and con-
tinued increase of centrate suspended solids. Inspection of the centrifuge
over the course of the Advanced Test Period indicates that various compo-
nents have worn. These include conveyor tips (especially on the discharge
end and at the junction of the cylinder and the 10 degree section of the
conveyor), the cake plows, casing head plows, and the solids discharge
15-3
-------
head near the discharge ports. The hard facing materials on the centrifuge
consist of Stellite 1016 on the blade tips of the conveyor and Colmonoy #6
on the pushing faces of the conveyor. Table 15-1 summarizes the centrifuge
operation, wear, and repair.
Except for the gradual wear of the centrifuge parts and the resulting gradual
deterioration of the centrate clarity, the centrifuge has operated satis-
factorily (consistent solids content in the cake, with no plugging).
15.4 EFFECTS OF OPERATING CONDITIONS ON DEWATERING
The ability of the filter and centrifuge to dewater the scrubber slurry is
significantly affected by the degree of sulfite oxidation. Natural oxidation
of sulfite to sulfate in the scrubber system amounts to only 10 to 30 percent,
and calcium sulfite is the predominant material in the waste sludge. Forced
oxidation normally yields greater than 90 percent sulfite oxidation and
calcium sulfate is the predominant material in the waste sludge.
The primary purpose for oxidizing the scrubber solids is to improve waste
solids dewatering and disposal characteristics because, compared to sulfite
sludge, gypsum sludge is much easier to dewater, settles faster, and is
non-thixotropic. Dewatering characteristics of waste solids are routinely
monitored at the Shawnee Test Facility by cylinder settling tests and
vacuum funnel filtration tests (Buchner funnel tests).
Cylinder settling tests are performed in a 1000 ml cylinder containing a
rake which rotates at 0.17 rpm. The initial settling rate and ultimate settled
solids concentration are recorded as indices of dewatering characteristics.
15-4
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Table 15-1
SUMMARY OF CENTRIFUGE OPERATION, WEAR, AND REPAIR
Hours on stream
since last servicing
Wear sites revealed
by inspection
Repair made
1400
4750
4000
Conveyor blades worn off
Cake plows worn in out-
board area
Solids weir worn
Conveyor worn
Forward feed compartment
discharge ports eroded
Wear at center feed ports
Wear on plows at solids
discharge ends
Conveyor blades worn
Reapplication of hard
facing materials:
Stellite 1016
Colmonoy #6
Rotating unit sent to
factory for repair
Limited hardface welding
performed onsite
6460
Serious wear on conveyor
tips, especially discharge
end and at junction of
cylinder and 10° section
Wear at casing head plows
Wear at solids discharge
head
Major overhaul at
factory
Gear and bearing serviced
Rebuilt all worn conveyor
surfaces and discharge
ports
Added tungsten carbide
hardfacing to conveyor
tips
Replaced all seals, bushings,
case plows and discharge
ports as necessary
15-5
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The initial settling rate is a qualitative index of the solids settling
properties only. Design rates for sizing clarifiers have to take into consi-
deration the hindered settling rate as the solids concentrate. The ultimate
settled solids from the cylinder tests represents the highest achievable
solids concentration in a settling pond.
Funnel filter tests are performed in a Buchner funnel with Whatman No. 2
filter paper under a vacuum of 25 in. Hg. The funnel test results correlate
well with the Shawnee rotary drum vacuum filter results when the filter
cloth is not blinded. However, the funnel test cakes tend to have lower
solids concentrations.
Table 15-2 presents a summary of average values and ranges of all the cylin-
der settling and funnel filtration test data gathered. It shows the effect
of oxidation, fly ash loading, and additive concentration on initial set-
tling rate, ultimate settled solids, and funnel test cake solids.
The benefit of forced oxidation on the settling and dewatering characteris-
tics of the sludge are clearly evident. Looking first at runs without
magnesium addition, the initial settling rate for an oxidized slurry (0.9 -
1.2 cm/min average range) was much higher than unoxidized slurry (0.2 - 0.4
cm/min average range), regardless of whether it was with high or low fly
ash loading. With forced oxidation, the high settling rates were not depend-
ent on the oxidation scheme (one or two scrubber loop mode). Again exclud-
ing magnesium runs, the average ultimate settled solids and funnel test
solids were all between 70 and 76 weight percent for the oxidized slurry,
whereas for unoxidized slurry the ultimate settled solids and funnel test
solids were between 40 and 57 weight percent.
15-6
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Table 15-2
SUMMARY OF DEWATERING CHARACTERISTICS ON SHAWNEE SYSTEM BLEED
Oxidation
Yes
Yes
Yes
res
Yes
Yes
Yes
No
No
NO
No
No
No
No
Fly Ash
Loading
High
High
High
High
Hlgn
Low
Low
High
High
High
High
High
Low
Low
Alkali
LS
LS
LS
LS
L
LS
L
LS
LS
LS
L
L
LS
L
inn
Oxidation node t
l-loop 1
2- loop 1
-1«1 Settling Rate, On/ml n
Ivg: p Range
.1 0.6-1.3
.2 l.O-l.*'1'
Bleed Strew 0.4 0.3-0.6
2-1oop 0.8 0.2-1.2
2-loop 1
.0 0.8-1. Z
2-loop 0.9 0.6-1.2
2-loop 1
0
0
0
0
0
.2 0.4-2.4
.2 0.1-0.5
-2 0.1-0.4
.1 0.0-0.1
.2 0.2-0.5
.8 0.2-1.2
0.2 0.1-0.5
0
.4 0.1-0.9
Ultimate Settling Solids, wt*
Avg. Range
74 67-84
72 62-86
71 61-84
66 46-73
73 6\-85
74 61-87
70 60-81
54 41-67
45 30-60
41 32-46
50 48-66
42 31-52
43 33-54
40 30-55
Funnel Test Cake Solids, Wt* Sli
Avg.
76
72
73
70
71
73
76
57
57
55
53
52
50
45
Range Sol
73-80 15
65-88 15
71-76 15
46-76 15
64-78 15
64-82 15
64-83 15
48-66 15
45-64 15
47-69 15
51-55 15
43-63 8
41-59 15
40-50 8
(fry Effective Mg"
ids Concentration, ppei
0
0
5000
8000
0
0
0
0
5000
9000
0
2000
0
0
trt
Note: Values for forced oxidation runs are only from data where solids oxidation
Is greater than or equal to 90 percent.
(1) Oxldizer pH - 5.0. At pH 4.5 tue average Initial settling rate was
1.1, with a range of 0.6-0.9. At pH 5.5, the average Initial settling
rate was 1.1, with a range of 0.8-1.5.
-------
The initial settling rate of unoxidized slurry was probably limited by the
sulfite particles. In the case of oxidized slurry, the rate was probably
limited by the fly ash. Even in the case of slurry with low fly ash loading,
fly ash constituted about one weight percent of the solids.
The addition of magnesium primarily affected the initial settling rate. For
oxidized slurry with the 2-loop oxidation mode and with 8000 ppm effective
magnesium ion concentration, the average initial settling rate, the ultimate
settled solids, and the funnel test cake solids were all slightly lower than
those for oxidized slurry without magnesium. The initial settling rate for
bleed stream slurry was about half that of other oxidized slurries. The
ultimate settled solids and funnel test cake solids were in the same range
as those with other oxidized slurries.
The effect of magnesium was more pronounced for unoxidized slurry. For a
limestone slurry with high fly ash loading, the average initial settling
rate was 0.20 cm/min with no magnesium and 0.05 cm/min with 9000 ppm effective
magnesium. Thus, the addition of magnesium decreased the settling rate by
a factor of four. The ultimate settled solids were also somewhat lower for
slurries with magnesium. The funnel test cake solids were about the same.
In the presence of magnesium, the initial settling rate (but not the ultimate
settled solids) was affected due to the increase in liquor viscosity and
density (resulting from increased total dissolved solids).
On the rotary drum vacuum filter, cake solids concentration is always above
80 percent with oxidized slurry. This is true regardless of whether addi-
tives are present or not. As would be expected, the filter performance is
not affected by the reduction in initial settling rate. Unoxidized cake from
15-8
-------
the drum filter averages about 50 to 65 weight percent solids. The unoxi-
dized solids tend to be thixotropic, like quicksand, while the oxidized
solids are more like moist soil.
On the centrifuge, cake solids concentration ranged from 65 to 75 weight
percent with oxidized slurry and ranged from 55 to 65 weight percent solids
with unoxidized slurry.
Generally, there is a significant reduction in the quality of slurry settling
and dewatering characteristics when the oxidation drops below about 90 percent
although the data are sparse for some of the test blocks.
The data thus far generated clearly illustrate the benefits of forced oxida-
tion with respect to increased initial solids settling rate, ultimate settled
solids, and funnel test cake solids, as well as the performance of the de-
watering equipment.
15-9
-------
Section 16
ANALYTICAL REQUIREMENTS
To control system parameters and to develop advanced theoretical models by
which lime/limestone S02 scrubbing systems may be described, routine analyses
of scrubber slurry streams are performed. The test facility has a fully
staffed and equipped laboratory capable of performing all the required analy-
ses. The type and frequency of these analyses are listed in Table 16-1. A
complete description of the analytical procedures used for these analyses
can be found in Reference 6.
16.1 GENERAL TEST SCHEDULE
Presented in Table 16-1 is a list of the location and frequency of samples
taken and the type of analysis performed on each sample. Basically, the
scrubber inlet slurry streams are analyzed for all components every 8 hours.
Variables essential to scrubber operation and control are determined more
frequently; pH is read every 2 hours, percent solids in the recirculating
slurry is determined every 4 hours, and any additive whose concentration is
to be controlled is determined every 2 hours.
Scrubber outlet streams are analyzed once every 8 hours for the liquor phase
only. This is done to gather data for scrubber characterization. Percent
16-1
-------
Table 16-1
TYPE AND FREQUENCY OF SAMPLE ANALYSES
Sample Location
Type of Analysis
Frequency
of Sampling
Venturi Inlet
Spray Tower Inlet
TCA Inlet
Complete solids and liquor analysis
Weight percent solids of slurry
pH of slurry
Additive (if any)
Mn or Fe (venturi and spray tower
inlet only)
Every 8 hours
Every 4 hours
Every 2 hours
Every 2 hours
Every 8 hours
Venturi Outlet
Spray Tower Outlet
TCA Outlet
Complete liquor analysis
Mn or Fe (TCA outlet only)
Every 8 hours
Alkali Feed
Weight % solids
Clarifier Underflow Weight % solids
Every 2 hours
Every 4 hours
Filter
Weight % solids in filtrate
Weight % solids in filter cake
Every 4 hours
Every 4 hours
Centrifuge
Weight % solids in centrate
Weight % solids in centrifuge cake
Every 4 hours
Every 4 hours
Special Tests
Buchner Funnel filtration test
Cylinder settling test
Every 24 hours
Every 24 hours
16-2
-------
solids in alkali feed, a controlled input, are determined every 2 hours.
Thickener underflow percent solids concentration is determined every 4 hours.
The percent solids in the filter and centrifuge cakes is determined every 4
hours to document the dewatering equipment performance and to facilitate
material balance calculations.
Special tests are also performed by laboratory personnel. These include a
Buchner Funnel filtration test and a cylinder settling test once a day to
characterize the slurry solids dewatering properties. The laboratory also
conducts special analyses, as needed, on samples such as scrubber scale and
solids deposits, recheck samples, etc.
16.2 LABORATORY STAFFING
A 24-hour day is divided into three 8-hour shifts. Each shift has a basic
staff of two laboratory technicians, and a shift supervisor who performs more
complicated analytical tests. During the day shift, there are three additional
persons: a support chemist who is responsible for developing procedures for
special tests as well as providing samples for quality assurance tests, the
laboratory supervisor, and a third laboratory technician who performs special
tests as required.
16.3 QUALITY ASSURANCE
The primary method for ensuring reliability of analytical data is the daily
evaluation of analytical results by the onsite staff and by Bechtel personnel
16-3
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in San Francisco. Ionic imbalance and the general reasonableness of results
are used as the measure of acceptability. During the Advanced Test Program,
solids analyses with an ionic imbalance greater than +_ 8.5 percent and liquor
analyses with an ionic imbalance greater than _+ 15 percent (_+ 20 percent prior
to August 18, 1976) were rejected. The solids ionic imbalance limit of +_ 8.5
percent was based on the results of about 300 solids analyses performed prior
to December 12, 1975. In these analyses, the average Ionic imbalance was
_+ 3.5 percent, with a standard deviation of 2.5 percent. Thus, ± 8.5 percent
ionic imbalance included approximately 95 percent of the solids analysis
results. The liquor ionic imbalance values for 60 analyses performed in
July 1976 had an average of _+ 6.4 percent and a standard deviation of 4.4
percent. Thus, _+ 15 percent ionic imbalance included 95 percent of the
liquor analysis results.
The results of the analysis of liquor and solids standards were used to
monitor both the accuracy (closeness between the true and the experimentally
determined values) and the precision (reproducibility) of analytical results.
In addition, a TVA program for interlaboratory comparison of analytical results
was initiated. Selected quality assurance samples were routinely sent to the
TVA General Analytical Laboratory 1n Muscle Shoals, Alabama, after their
analysis at the Shawnee Test Facility laboratory.
16-4
-------
Section 17
REFERENCES
1. Bechtel Corporation, EPA Alkali Scrubbing Test Facility; Summary of
Testing through October 1974, EPA Report No. EPA-650/2-75-047, June 1975.
2. Bechtel Corporation, EPA Alkali Scrubbing Test Facility: Advanced
Program. First Progress Report, EPA Report No. EPA-600/2-75-050, September
1975.
3. Bechtel Corporation, EPA Alkali Scrubbing Test Facility: Advanced
Program. Second Progress Report. EPA Report No. EPA-600/7-76-008, Septem-
ber 1975.
4. Bechtel Corporation, EPA Alkali Scrubbing Test Facility; Advanced
Program. Third Progress Report, EPA Report No. EPA-600/7-77-105, September
1977.
5. Bechtel National, Inc.. EPA Alkali Scrubbing Test Facility: Advanced
Program. Fourth Progress Report. EPA Report No. EPA-600/7-79-244a & b,
November 1979.
6. Bechtel Corporation, Shawnee Test Facility Laboratory Procedurees Manual.
March 1976.
17-1
-------
7. A. V. Slack, G. A. Hollinden, Sulfur Dioxide Removal from Haste Gases.
Noyes Data Corporation, Park Ridge, New Jersey (1975), P. 52.
8. R. H. Borgwardt, "Increasing Limestone Utilization in FGD Scrubbers,"
presented at the 68th AIChE Annual Meeting, Los Angeles, November 16-19,
1975.
9. P. V. Danckwerts. Gas-Liquid Reactions. McGraw-Hill, San Francisco,
California (1970), p. 260.
10. Bechtel Corporation, EPA Alkali Scrubbing Test Facility: Monthly Progress
Report for Period May 1 to May 31. 1977. June 24, 1977, Section 4.
11. Radian Corporation, Experimental and Theoretical Studies of Solid Solu-
tion Formation in Lime and Limestone S02 Scrubbers - Volume 1., Final
Report. EPA Report No. EPA-600/2-76-273a, October 1976.
12. D. Ottmers, Jr., J. Phillips, C. Burklin, W. Corbett, N. Phillips, and
C. Shelton, A Theoretical and Experimental Study of Lime/Limestone Wet
Scrubbing Process EPA Report No. EPA-650/2-75-006, December 1974.
13. R. H. Borgwardt, "EPA/RTP Pilot Studies Related to Unsaturated Operation
of Lime and Limestone Scrubbers," Proceedings: Symposium on Flue Gas
Desulfurization - Atlanta. November 1974. Volume 1. EPA Report No. EPA-
650/2-74-126a, December 1974.
14. J. W. Barrier, et al, "Comparative Economics of FGD Sludge Disposal,"
presented at the 71st Annual Meeting of the Air Pollution Control Associa-
tion, Houston, Texas, June 25-30, 1978.
17-2
-------
15. R. H. Borgwardt, Sludge Oxidation In Limestone FGD Scrubbers. EPA Report
No. EPA-600/7-77-061, June 1977.
16. R. L. Torstrick, L. J. Henson, and S. V. Tomlinson, "Economic Evaluation
Techniques, Results, and Computer Modeling for Flue Gas Desulfurization,"
Proceedings: Symposium on Flue Gas Desulfurizatlon - Hollywood, FL.
Volume I. EPA Report No. EPA-600/7-78-058a, March 1978.
17. T. K. Sherwood and R. L. Pigford, Absorption and Extraction. 2nd Ed.,
McGraw-Hill Book Company, Inc., New York, 1952, p. 127 and pp. 273-4.
18. Radian Corporation, A Theoretical Description of the Limestone Injection-
Wet Scrubbing Process. Volume 1. Final Report. NAPCA Contract No. CPA-
22-69-138, June 9, 1970.
19. Bechtel Corporation, EPA Alkali Scrubbing Test Facility: Sodium Carbonate
and Limestone Test Results. EPA Report No. EPA-650/2-73-013, August 1973.
20. R. H. Borgwardt, Limestone Scrubbing at EPA Pilot Plant. Progress Report
No. 6, January 1973.
21. J. M. Potts, et al., "Removal of Sulfur Dioxide from Stack Gases by
Scrubbing with Limestone Slurry: Small-Scale Studies at TVA," Proceed-
ings: Second International Lime/Limestone Wet-Scrubbing Symposium - New
Orleans. LA. November 1971. Volume 1. EPA Publication No. APTD - 1161,
June 1972.
22. R. J. Gleason, "Limestone Scrubbing Efficiency of Sulfur Dioxide in a
Wetted Film Packed Tower in Series with a Venturi Scrubber," Proceedings:
Second International Lime/Limestone Wet-Scrubbing Symposium - New Orleans.
LA. November 1971, Volume 1. EPA Publication No. APTD - 1161, June 1972.
17-3
-------
23. Bechtel Corporation, pH Study at the Shawnee Test Facility - Phase II.
September 1976.
24. R. G. Rhudy and H. N. Head, "Results of Flue Gas Characterization Testing
at the EPA Alkali Wet-Scrubbing Test Facility," presented at the Second
Fine Particle Scrubber Symposium, New Orleans, LA, May 2-3, 1977.
17-4
-------
APPENDIX A
CONVERTING UNITS OF MEASURE
A-l
-------
CONVERTING UNITS OF MEASURE
Environmental Protection Agency policy is to express all measurements
in Agency documents in metric units. In this report, however, to avoid
undue costs or lack of clarity, English units are used throughout.
Conversion factors from English to metric units are given below:
To Convert From
scfm (60°F)
cfm
°F
ft
ft/hr
ft/sec
ft?
ftz/tons per day
To
nm3/hr (0°C)
mj/hr
°C
m
m/hr
m^sec
-/metric tons
gal/mcf
gpm
gpm/ft^
gr/scf
in.
in. H20
Ib
Ib-moles
Ib-moles/hr
Ib-moles/hr ft2
Ib-moles/min
psia
1/m3
1/min
1/miD/m2
gm/m3
cm
mm Hg
gm
gm-moles
gm-moles/min
gm-moles/min/rrr
gm-moles/sec
kilopascal
Multiply By
1.61
1.70
(°F-32)/1.8
0.305
0.305
0.305
0.0929
0.102
0.134
3.79
40.8
2.29
2.54
1.87
454
454
7.56
81.4
7.56
6.895
A-2
-------
APPENDIX B
DATABASE SUMMARY
B-l
-------
DATABASE SUMMARY
The NOMAD database system can be used to print reports of selected data.
The run summary table reports for the period October 1974 through June 1978
are presented in this appendix.
The following codes and abbreviations are used in describing the operating
conditions and the system configuration:
• Alkali type
L = lime
LS = limestone
• Fly ash and MgO addition
Y = yes
N = no
Spray tower header configuration
1 = lowest spray bank
2 = second lowest
3 = second highest
4 = highest
• Mist eliminator system configuration
1-3P/OV = one three-pass, open-vane mist eliminator
2-3P/CV = two three-pass, closed-vane mist eliminator
• Mist eliminator wash, bottom/top
C = continuous
I = intermittent
S = sequential
Dewatering system
CL = clarifier
CE = centrifuge
F = filter
LAM = Lamella inclined plate settler
e.g., CL/CE = clarifier and centrifuge in series
B-2
-------
• Alkali addition point
DNC = downcomer
EHT = effluent hold tank
t TCA total bed height is given in inches for 3 beds
• TCA sphere type
FOAM = 1 5/8-inch solid nitrile foam spheres
TPR = 1 1/2-inch hollow thermoplastic rubber spheres
The analytical point designations for slurries are as follows:
1805 = venturi/spray tower bleed stream oxidation tank
1815 = venturi inlet
1816 = spray tower inlet
1825 = spray tower outlet
1851 = venturi outlet
2816 = TCA inlet
2825 = TCA outlet
2831 = inlet to Penberthy air eductor
2832 = TCA oxidation tank (first of two series tanks)
B-3
-------
VST RUN DEFINITION
RUN
NO.
VFG-1A
VFG-1B
VFG-1C
VFG-1D
VFG-1E
VFG-1F
VFG-1G
VFG-1I
VFG-1P
VFG-1Q
601-1A
601-1B
601-1C
602-1A
603-1A
604-1A
605-1A
606-1A
607-1A
60-8-1 A
609-1A
610-1A
611-1A
612-1A
613-1A
614-1A
614-1B
615-1A
615-1B
616-1A
617-1A
618-1A
619-1A
620-1A
621-1A
622-1A
623-1A
624-1A
625-U
626-1A
627-1A
628-U
628-18
629-1 A
RUN
REP
FLAG
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
A
A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
START
DATE
10/10/76
10/20/76
10/29/76
11/02/76
1 1/06/76
11/10/76
11/18/76
11/22/76
11/27/76
//
10/09/73
11/17/73
12/15/73
03/15/74
04/02/74
04/26/74
07/31/74
08/07/74
08/15/74
08/21/74
09/20/74
10/02/74
10/25/74
11/13/74
11/14/74
11/15/74
11/16/74
11/15/74
11/16/74
11/15/74
11/14/74
11/21/74
12/19/74
01/10/74
01/18/75
01/30/75
03/12/75
03/19/75
06/20/75
07/09/75
08/05/75
08/16/75
09/18/75
04/28/76
START
TIME
1550
1734
1330
2215
2215
2200
1600
1530
1305
N/A
1420
2300
2300
2000
1200
1300
0800
0500
2000
130O
1800
1600
1500
1900
1040'
0300
1500
1200
0500
2100
2010
1900
1800
1245
1500
1900
,1400
1300
1900
1400
1300
1100
1300
1800
END
DATE
10/18/76
10/29/76
11/02/76
11/06/76
11/10/76
11/18/76
11/21/76
11/27/76
12/04/76
//
11/17/73
12/15/73
01/08/74
04/01 /74
04/19/74
07/15/74
08/06/74
08/14/74
08/20/74
09/17/74
10/02/74
10/13/74
11/11/74
11/14/74
11/14/74
11/15/74
11/18/74
11/15/74
11/16/74
11/16/74
11/14/74
12/02/74
01/02/75
01/17/74
01/23/75
03/05/75
03/19/75
04/23/75
07/09/75
08/04/75
08/13/75
09/18/75
10/07/75
05/12/76
END
TIME
0530
0830
2215
2215
2200
0815
1518
1300
0715
N/A
2300
2300
2200
0500
oaoo
0100
0800
1600
0800
0800
0700
0700
1 100
1040
2010
1200
0745
2015
1500
0500
2320
0700
1300
0745
0800
0800
0900
0900
0900
0800
1100
0800
0800
0800
HOURS
ON
STRM
182
207
87
96
96
124
71
117
157
N/A
666
912
575
393
395
1828
141
170
108
610
277
253
392
16
10
9
41
8
10
8
3
235
327
163
113
787
162
823
319
569
187
717
426
266
FACT
OR
TIME
T
T
T
T.
T
T
T
T
T
N/A
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
RUN COMMENTS
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
STEADY STATE NOT ACHIEVED
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
B-4
-------
VST RUN DEFINITION
RUN
NO.
630-1 A
631-1A
632-1 A
633-1 A
634-1 A
635-1A
636-1 A
637-1 A
638-1 A
639-1 A,
640-1 A
641-1A
642-1 A
643-1 A
701-1A
702-1 A
703-1 A
704-1 A
705-1 A
706-1A
707-1A
708-1A
709-1 A
71 0-1 A
711-1A
711-18
712-1A
712-18
713-1A
714-1A
715-1A
716-1A
717-1A
718-1A
801-1A
801-2A
802-1A
803-1 A
804-1 A
805-1 A
806-1 A
806-1 B
806-1 C
806-10
RUN
REP
FLAG
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
0
N/A
N/A
N/A
N/A
N/A
START
DATE
05/12/76
05/18/76
05/28/76
06/05/76
06/19/76
07/16/76
07/28/76
08/06/76
08/17/76
08/24/76
09/02/76
09/09/76
09/15/76
09/27/76
10/09/75
10/14/75
10/19/75
11/03/75
11/07/75
11/13/75
1'./*l/'75
11/26/75
12/06/75
12/12/75
12/24/75
12/30/75
01/02/76
01/07/76
01/08/76
01/19/76
01/26/76
01/27/76
01/28/76
07/03/76
01/04/77
II
01/24/77
02/04/77
02/10/77
02/18/77
02/23/77
02/25/77
02/27/77
03/01/77
START
TIME
1000
1 145
1815
1000
1700
1710
1830
1315
1726
1455
1555
1430
1430
1250
1800
1700
0900
2000
1600
1900
1600
1400
1700
1400
1300
1200
1200
1500
0900
1600
1800
1700
1400
1530
1420
N/A
1550
1400
1210
1620
1440
1 130
0815
1500
END
DATE
05/18/76
05/24/76
06/04/76
06/14/76
07/02/76
07/26/76
08/04/76
08/12/76
08/24/76
09/01/76
09/09/76
09/14/76
09/27/76
10/05/76
10/12/75
10/17/75
11/01/75
11/06/75
11/13/75
11/21/75
11/26/75
12/02/75
12/12/75
12/22/75
12/30/75
01/02/76
01/07/76
01/08/76
01/10/76
01/26/76
01/27/76
01/28/76
02/05/76
07/15/76
01/15/77
II
02/04/77
02/10/77
02/18/77
02/23/77
02/25/77
02/27/77
03/01/77
03/03/77
I
END
TIME :
0800
1345
0245
0530
23'',:.
0813
1256
0735
0547
0550
05t5
1656
0525
1203
1900
2000
2200
1300
0800
0700
1300
0700
0700
0700
1200
11 CC
1100
0800
1200
0700
1700
1000
0800
1000
1255
N/A
0805
0730
0205
0800
1130
0815
1415
0800
HOURS
ON
STRM .
142
145
151
212
319
190
164
137
174
183
157
120
249
191
73
60
319
66
136
180
118
138
134
234
144
71
11S
18
52
157
23
18
181
235
263
N/A
256
138
151
112
45
45
54
41
FACT
OR
TIME
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
N/A
T
T
T
T
T
T
T
T
RUN COMMENTS
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
THIS IS AN ABSORBENT DEPLETION RUN
N/A
N/A
N/A
PH DROPPED DRASTICALLY
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
B-5
-------
VST RUN DEFINITION
RUN
NO.
807-1A
808-1A
809-1A
810-1A
811-1A
812-1A
813-1A
B14-U
B15-1A
816-1A
B17-1A
818-1A
819-1A
819-1B
820-1 A
820-1 B
820-1C
821-1A
822-1 A
822-1 B
823-1A
824-1 A
825-1 A
826-1 A
827-1 A
828-1 A
828-1 B
829-1 A
830-1 A
851-1A
852-1 A
853-1 A
854-1 A
855-1 A
856-1 A
857-1 A
858-1 A
859-1 A
859- 1B
859- 1C
859-10
860-1 A
861-1A
862-1 A
RUN
REP
FLAG
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
START
DATE
03/03/77
03/06/77
08/12/77
08/18/77
OB/25/77
09/02/77
//
09/08/77
09/15/77
09/28/77
10/18/77
10/26/77
11/01/77
12/08/77
03/01/78
04/04/78
04/13/78
04/19/78
04/25/78
05/05/78
05/12/73
05/23/78
05/30/78
06/09/73
//
//
//
//
//
03/10/77
03/15/77
03/18/77
03/25/77
06/21/77
06/28/77
07/07/77
07/13/77
07/20/77
07/25/77
07/28/77
OB/02/77
OB/05/77
10/06/77
10/11/77
START
TIME
1630
1015
1510
1355
1245
1 108
N/A
1620
1320
1005
1110
1155
1655
1032
2030
1230
1230
1545
1440
0740
1630
1435
1900
1335
N/A
N/A
N/A
N/A
N/A
1450
1422
1550
1525
1510
1300
1416
1355
1440
1000
0800
0750
1330
1125
1300
END
DATE
03/06/77
03/09/77
08/18/77
08/25/77
09/02/77
09/08/77
//
09/15/77
09/28/77
10/04/77
10/26/77
11/01/77
12/08/77
12/15/77
04/04/78
04/10/78
04/19/78
04/25/78
05/05/78
05/10/78
05/23/78
05/30/78
06/09/78
06/19/78
//
//
//
//
//
03/15/77
03/18/77
03/25/77
04/01/77
06/28/77
07/07/77
07/12/77
07/20/77
07/25/77
07/28/77
OB/02/77
OB/05/77
08/11/77
10/11/77
10/18/77
END
TIME
1015
C330
.-J20
0735
0410
0752
N/A
0746
0730
0820
0727
0735
0850
0739
0800
0505
0815
0750
0740
0455
0800
0800
0800
1925
N/A
N/A
N/A
N/A
N/A
0750
1550
0815
1315
1300
0815
2150
0810
1000
0800
0750
1330
0537
0825
0720
HOURS
ON
STRM
66
65
137
162
184
141
N/A
136
306
142
188
141
840
126
462
137
134
136
232
85
205
15*»
229
246
N/A
N/A
N/A
N/A
N/A
110
74
161
166
158
209
128
162
115
70
120
72
133
117
162
FACT
OR
TIME
T
T
T
T
T
T
N/A
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
N/A
N/A
N/A
N/A
N/A
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
RUN COMMENTS
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
SOLIDS SAMPLES ARE BEING RUN BY
N/A WET METHOD BEGINNING 0730
N/A ON 9-16-77
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
900GPM TO TOP 2 HDRSdtOOGPM TOTAL
N/A TO ST) 7/2-7/5/77. HIGHER S02
N/A REMOVAL
N/A
N/A
N/A
N/A
N/A
N/A
N/A
B-6
-------
VST RUN DEFINITION
RUN
NO.
863-1A
864-1 A
865-1 A
866-1 A
867-1 A
RUN
REP
FLAG
N/A
N/A
N/A
N/A
N/A
START
DATE
12/16/77
01/20/78
01/25/78
02/14/78
02/21/78
START
TIME
1615
1309
1008
1030
1430
END
DATE
01/20/78
01/25/78
02/14/78
02/21/78
02/27/78
END
TIME
1241
0755
0835
0855
0820
HOURS
ON
STRM
779
115
254
159
137
FAC1
OR
TIME
T
T
T
T.
T
• RUN COMMENTS
N/A
N/A
N/A
N/A
N/A
•B-7
-------
VST SYSTEM CONFIGURATION
NO. OF
RUN SCRUBBER
NO. STAGES
VFG-1A
VFG-1B
VFG-1C
VFG-1D
VFG-1E
VFG-1F
VFG-1G
VFG-1 I
VFG-1P
VFG-1Q
601-1A
60 1-1 B
601-1C
602-1 A
6D3-1A
00 604-1A
' 605-1 A
00 606-1 A
607-1A
608-1A
609-1A
610-1A
611-1A
612-1A
613-1A
614-tA
614-18
615-1A
615-1B
6 16-1 A
617-1A
618-1A
619-1A
620-1A
621-1A
622-1 A
623-1 A
624-1 A
625-1 A
626- « A
627-1A
628-1 A
628-1 B
629-1 A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
S.T.
HEADER
CONFIG
1234
1234
1234
1234
1234
NONE
1234
1234
1234
N/A
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
NONE
1234
1234
1234
1234
NONE
NONE
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
NO-OP
HOLD
TANKS
1
i
N/A
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
M. Ei
SYSTEM
CONFIG
1-3P/OV
1-3P/OV
1-3P/QV
1-3P/OV
1-3P/OV
1-3P/OV
CHE+YRK
1-3P/OV
1-3P/OV
N/A
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
SLOPED
SLOPED
SLOPED
SLOPED
SLOPED
SLOPED
SLOPED
SLOPED
SLOPED
SLOPED
SLOPED
SLOPED
SLOPED
1-3P/OV
1-3P/OV
I-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
M.E.
WASH
B/T
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
N/A
I
I/
I/
I/
I/
I/
11
c/
I/
I/
i/c
i/c
c/
c/
c/
C/
c/
c/
c/
c/
c/
c/
I/
c/
c/
I/
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
SPARGER NO. OF
DE- OXID HOLE HOLES
WATER CONFIG DIAM. , IN
SYSTEM FLAG INCHES SPARGER
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
N/A
CL/F
CL/FI
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL
CL/F
CL/P
CL/F
CL/CE
CL/CE
CL/CE
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
K'/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
SPARGE
TANK ALK
AGIT ADDN
ATOR PT.
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
N/A
EHT
EHT
EHT
EHT
EHT
DNC
DNC
DNC
DNC
DNC
DNC
EHT
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
EHT
DNC
DNC
DNC
PRESCRUB
ALKALI
ADDITION RUN
POINT NO.
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
VFG-1A
VFG-1B
VFG-1C
VFG-1D
VFG-1 E
VFG-1 F
VFG-1G
VFG-1 I
VFG-1 P
VFG-1Q
601-1A
601-1B
601-1C
602-1A
603-1A
604-1A
605-1A
606-1A
607-1A
608-1A
609-1A
610-1A
611-1A
612-1A
613-1A
614-1A
614-1B
615-1A
615-1B
616-1A
617-1A
61B-1A
619-1A
620-1A
621-1A
622-1A
623-1A
624-1A
625-1A
626-1 A
627-1A
628-1A
628- 1B
629-1 A
-------
VST SYSTEM CONFIGURATION
CO
i
NO. OF
RUN SCRUBBER
NO. STAGES
630-1 A
631-1A
632-1 A
633-1A
634-1 A
635-1 A
636-1A
637-1 A
638-1 A
639-1 A
640-1 A
641-1A
642-1 A
643-1 A
701-1A
702-1 A
703-1A
704-1 A
705-1A
706-1A
707-1A
708-1A
709-1 A
710-tA
71 1-1A
711-1B
712-1A
712-1B
713-1A
714-1A
71S-1A
716-1A
717-1A
718-1A
B01-1A
B01-2A
802-1 A
803-1 A
804-1 A
805-1 A
806-1A
806-18
806-1C
806-10
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
2
2
2
2
2
2
2
2
2
2
S.T.
HEADER
CONFIG
1234
34
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1 34
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
N/A
1234
1234
1234
1234
1234
1234
1234
1234
NO. OF
HOLD
TANKS
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
N/A
1
1
M.E.
SYSTEM
CONFIG
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
N/A
t-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
M.E.
WASH
B/T
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
c/i
C/I
C/I
C/I
C/I
C/I
C/I
I/I
I/I
I/I
I/I
I/I
I/I
N/A
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
DE-
WATER
SYSTEM
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/CE
CL/F
CE
CE
CE
CL/F
CL/F
CL/F
CL/F
CE
CE
CE
CE
CE
CE
CE
CE
CE
CE
CE
CL/F
CL/F
N/A
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
OX ID
CONFIG
FLAG
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
2
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
SPARGER NO. OF
HOLE HOLES
DIAM., IN
INCHES SPARGER
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
0.125
0.126
0.125
0.125
0.125
0.125
0.125
0.125
0.126
0.125
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
130
130
130
130
130
130
130
130
130
130
SPARGE
TANK ALK
AGIT ADDN
ATOR PT.
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
ONC
ONC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
DNC
EHT
N/A
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
PRESCRUB
ALKALI
ADDITION RUN
POINT NO.
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
ONC
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
630-1A
631-1A
632-1A
633-1A
634-1 A
635-1A
636-1 A
637-1 A
638-1 A
639-1A
640-1A
641-1A
642-1 A
643-1 A
701-1A
702-1A
703-1A
704-1 A
705-1 A
706-1 A
707-1A
708-1A
709-1 A
710-1A
711-1A
711-1B
712-1A
712-1B
713-1A
714-1A
715-1A
716-1A
717-1A
718-1A
801-1A
801-2A
B02-1A
803-1 A
804-1 A
805-1 A
806-1 A
806-18
806- 1C
806-10
-------
VST SYSTEM CONFIGURATION
CO
i
NO. OF
RUN SCRUBBER
NO. STAGES
807-1A
808-1A
809-1A
810-1A
811-1A
812-1A
813-1A
814-1A
815-1A
816-1A
817-1A
818-1A
819-1A
819-18
820-1A
820-18
820-1C
821-1A
822-1A
822-1B
823-1A
824-1A
825-1A
826-1A
827-1A
828-1A
828-18
829-1A
830-1A
851-1A
852-1A
853-1 A
854-1 A
855-1A
856-1 A
857-1A
858-1A
859-1 A
859-18
859-1C
859-1 D
860-1 A
861-1A
862-1 A
2
2
2
2
2
2
N/A
2
2
2
2
2
N/A
N/A
2
2
2
1
2
2
1
1
1
1
N/A
N/A
N/A
N/A
N/A
2
2
2
2
2
2
2
2
2
2
2
2
2
2
2
S.T.
HEADER
CONFIG
1234
1234
1234
1234
1234
1234
N/A
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
N/A
1234
1234
1234
1234
1234
1234
N/A
N/A
N/A
N/A
N/A
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
NO. OF M.E.
HOLD SYSTEM
TANKS CONFIG
1 -3P/OV
H
3
3
3
Q
N/A
3
3
3
3
I
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
4/A
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/DV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
N/A -3P/OV
N/A N/A
N/A N/A
N/A N/A
N/A N/A
N/A N/A
1 1-3P/OV
1 1-3P/OV
1 1-3P/OV
1 1-3P/OV
3
3 1-3P/OV
3 1-3P/OV
3 1-3P/OV
3 1-3P/OV
3 1-3P/OV
3 1-3P/OV
3 1-3P/OV
3 1-3P/OV
3 1-3P/OV
3 1-3P/OV
M.E.
WASH
B/T
I/I
I/I
C/I
C/I
C/I
C/I
N/A
C/I
C/I
C/I
C/I
C/I
C/I
C/I
C/S
c/s
C/S
c/s
c/s
c/s
c/s
c/s
c/s
c/s
N/A
N/A
N/A
N/A
N/A
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
DE- OXID
WATER CONFIG
SYSTEM FLAG
CL/F
CL/F
CL/F/L
CL
CL
CL/F
N/A
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F/L
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/R
CL/F
N/A
N/A
N/A
N/A
N/A
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
4
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
1
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
SPARGER NO. OF
HOLE HOLES
DIAM., IN
INCHES SPARGER
0.125
0.125
0.250
0.250
0.250
0.250
N/A
0.250
0.250
0.250
0.300
0.300
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
0.125
0.125
0.125
0.125
0.250
0.250
0.250
0.250
0.250
0.250
0.250
0.250
0.250
0.300
0.300
130
130
40
40
40
40
N/A
40
40
40
1
1
N/A
N/A
1
1
N/A
1
1
1
1
1
1
1
N/A
N/A
N/A
N/A
N/A
130
130
130
130
40
40
40
40
40
40
40
40
40
1
1
SPARGE
TANK ALK
AGIT ADDN
ATOR PT.
Y
Y
Y
Y
Y
Y
N/A
Y
Y
Y
Y
Y
N/A
N/A
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
N/A
N/A
N/A
N/A
N/A
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
N/A
N/A
EHT
EHT
EHT
EHT
EHT
EHT
N/A
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
N/A
N/A
N/A
N/A
N/A
DNC
DNC
DNC
DNC
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
N/A
PRESCRUB
ALKALI
ADDITION RUN
POINT NO.
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
807-1A
808-1 A
809-1 A
810-1 A
81 1 -1 A
812-1 A
813-1 A
814-1A
815-1 A
816-1 A
817-1 A
81 8—1 A
819-1 A
819-18
820-M A
820-1 B
820-1C
821-1 A
822-1 A
822-1 B
823-1A
824-1A
825-1 A
826-1 A
827-1A
828-1A
828-1B
829-1A
830-1A
851-1A
852-1A
853-1A
854-1A
855-1A
856-1 A
857-1 A
858-1 A
859-1 A
859-1B
859-1C
859-1 D
860-1A
861-1A
862-1 A
-------
VST SYSTEM CONFIGURATION
RUN
NO.
863-1 A
864-1 A
865-1 A
866-1 A
867-1A
NO. OF
SCRUBBER
STAGES
N/A
N/A
N/A
N/A
2
S.T.
HEADER
CONFIG
1234
1234
1234
1234
1234
NO. OF
HOLD
TANKS
N/A
N/A
N/A
N/A
N/A
M.Ei
SYSTEM
CONFIG
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
M.E.
WASH
B/T
I/I
I/I
I/I
I/I
i/s
DE-
WATER
SYSTEM
CL/F
CL/F
CL/F
CL/F
CL/F
OXID
CONFIG
FLAG
N/A
N/A
N/A
N/A
N/A
SPARGER
HOLE
DIAM. ,
INCHES
N/A
N/A
N/A
N/A
N/A
NO. OF
HOLES
IN
SPARGER
N/A
N/A
N/A
N/A
1
SPARGE
TANK
AGIT
ATOR
N/A
N/A
N/A
N/A
Y
ALK
ADDN
PT.
EHT
EHT
EHT
EHT
EHT
PRESCRUB
ALKALI
ADDITION
POINT
N/A
N/A
N/A
N/A
DNC
RUN
NO.
863-1A
864-1A
865-1A
866-1 A
867-1 A
oo
i
-------
VST OPERATING CONDITIONS
CO
ro
RUN
NO.
VFG-1A
VFG-1B
VFG-1C
VFG-1D
VFG-1E
VFG-1F
VFG-1G
VFG-1I
VFG-1P
VFG-10
601-1A
601-16
60 1 - 1 C
602-1A
603-1A
604-1A
60 5-1 A
606-1 A
607-1A
608-1A
609-1A
610-1A
61 1-1A
612-1A
613-1A
614-1A
614-1B
615-1A
61 5-1 B
61 6-1 A
61 7-1 A
61 8-1 A
619-1A
620-1A
621-1A
622-1A
623-1A
624-1A
625-1 A
626-1 A
627-1A
62S-1A
628-1 B
629-1A
ALK
TYPE
L
L
L
L
L
L
L
L
L
N/A
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
FLY
ASH
Y
N
Y
Y
Y
Y
Y
Y
Y
N/A
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
MGO
Y
N
N
N
N
N
N
N
N
N/A
N
N
N
N
N
N
N
N
N
N
N
N
Y
Y
Y
Y
Y
Y
Y
Y
Y
N
N
N
N
N
N
N
N
N
N
N
N
Y
PRESCRUB
PH VENTURI
CONTR PH CONTR
POINT POINT
7.00
8.0C
8.00
8.00
8.00
8.00
8.00
8.00
8.00
N/A
8.00
8.00
8.00
8.00
8.00
8.00
9.00
8.00
8.00
8.00
8.00
8.00
7.00
6.00
6.00
6.00
6.00
7.00
7.00
7.00
6.00
8.00
8.00
8.00
8.00
8.00
8.00
8.00
8.00
8.00
8.00
5.00
5.00
6.00
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
GAS
RATE
ACFM
35000
35000
35000
20000
35000
35000
35000
35000
35000
N/A
25000
25000
25000
25000
25000
25000
25000
25000
25000
25000
25000
25000
25000
25000
25000
25000
' 25000
25000
25000
25000
25000
25000
25000
250CO
25000
25000
25000
30000
30000
35000
35000
30000
30000
35000
GAS
VEL
FPS
9.4
9.4
9.4
5.4
9.4
9.4
9.4
9.4
9.4
N/A
b.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
5.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
8.0
8.0
9.4
9.4
8.0
8.0
9.4
VEN
LIO
RATE
GPM
600
600
600
600
375
600
600
600
140
N/A
600
600
600
600
eqo
100
100
100
600
600
600
600
600
600
600
100
100
100
100
600
100
100
600
600
600
600
600
600
600
600
600
600
600
600
S.T.
LIO
RATE
GPM
1400
1400
1400
1400
1400
0
1400
1400
1400
N/A
1200
1200
1200
1200
1200
200
200
200
200
200
1200
1200
1200
1200
0
1200
1200
1200
1200
0
0
1200
1200
1200
1200
1200
1200
1200
1200
1400
1400
1600
1600
1400
VEN
L/G
GAL/
MACF
21 .4
21 .4
21 .4
37.4
13.4
21 .4.
21 .4
21 .4
5.0
N/A
29.9
29.9
29.9
29.9 •
29.9
5.0
5.0
5.0
29.9
29.9
29.9
29.9
29.9
29.9
29.9
5.0
5.0
5.0
5.0
29.3
5.0
5.0
29.9
29.9
29.9
29.9
29.9
24.9
24.9
21.4
21 .4
24.9
24.9
21.4
S.T.
L/G
GAL/
MACF
49.8
49.8
49.8
87.2
49.8
0.0
49.8
49.8
49.8
N/A
59.8
59.8
5918
59.8
59.8
59.8
59.8
59.8
59.8
59.8
59.8
59.8
59.8
59.8
0.0
59.8
59.8
59.8
59.8
0.0
0.0
59.8
59.8
59.8
59.8
59.8
59.8
49.8
49.8
49.8
49.8
66.5
66.5
49.8
PRESCRUB
SOLID VEN NOW %
RECIRe SOLIDS
NOM % RECIRC
8.0
8.0
8.0
8.0
8.0
8.0
8.0
15.0
8.0
N/A
8.0
8.0
8.0
8.5
15.0
8.0
8.5
8.5
8.0
8.5
8.5
8.0
8.5
8.0
8.0
8.0
8.0
8.0
8.0
8.0
8.0
8.0
8.5
60.0
8.5
8.0
8.0
8.5
8.0
8.0
15.0
10.0
9.0
8.0
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
SOLIDS
DISCH
RANGE
%
48-57
42-62
53-60
51-57
45-63
59-64
51-54
52-55
55-60
N/A
20-52
N/A
20-52
42-48
46-54
50-60
48-52
18-23
50-55
48-58
47-52
43-48
44-49
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
16-21
53-60
N/A
57-61
50-62
53-60
48-58
55-60
52-60
52-56
51-55
52-56
52-60
RUN
NO.
VFG-1A
VFG-1B
VFG-1C
VFG-1D
VFG-1E
VFG-1F
VFG-1G
VFG-1I
VFG-1P
VFG-10
601-1 A
601-1B
601-lft
602-1A
603-1A
604-1 A
605-1A
606-1 A
607-1 A
608-1 A
609-1 A
610-1 A
61 1-1 A
612-1A
613-1A
614-1 A
614-1 B
615-1 A
615-1B
616-1 A
617-1 A
618-1 A
619-1 A
620-1 A
621- A
622- A
623- A
624- A
625- A
626- A
627- A
628- A
628-1 B
629-1 A
-------
VST OPERATING CONDITIONS (CONTINUED)
CO
I
RUN
NO.
VFG-1A
VFG-1B
VFG-1C
VFG-1D
VFG-1E
VFG-1F
VFG-1G
VFG-1I
VFG-1P
VFG-1Q
601-1A
601-18
601-1C
602-1A
603-1 A
604-1 A
605-1A
606-1 A
607-1A
608-1A
609-1A
610-1A
611-1A
612-1A
613-1A
614-1A
614-1B
615-1A
615-18
616-1A
617-1A
618-1A
619-1A
620-1 A
621-1 A
622-1A
623-1 A
624-1A
625-1 A
626-1 A
627-1 A
628-1 A
628-18
629-1 A
VEN
D.P.
IN.
H20
9.0
9.0
9.0
9.0
5.3
9.0
9.0
9.0
3.6
N/A
9.0
9.0
9.0
9.0
9.0
1.3
1.8
2.1
9.0
9.0
9.0
9.0
9.0
9.0
9.0
1.7
2.5
2.0
2.7
9.0
1.7
1 .8
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
S.T.
D.P.
IN.
H20
4.0
4.3
4.5
1 .4
4.2
3.5
4.6
4.5
3.9
N/A
2.7
2.7
2.7
2.5
2.2
1.5
1.5
1.3
2.2
3.4
2.5
2.6
2.2
3.1
2.2
2.0
2.8
2.8
2.6
2.4
1.4
2.1
2.4
3.3
2.7
2.8
2.5
3.2
3.1
5.6
5.7
3.3
N/A
4.6
M.E. SYSTEM
D.P. RANGE
IN.H20
0^44-0.49
0.45-0.50
0.45-0.50
0.11-0.15
0.43-0.50
0.37-0.45
0.79-1 .75
0.38-0.44
0.35-0.42
N/A
0.16-1 .26
N/A
0.16-1 .26
0. 19-0.27
0.16-0.33
0.20-1 .25
0.23-0.28
0.23-0.31
0.75-0.85
0.22-0.44
0.23-0.28
0.20-0.33
0.55-0.60
0.55-0.75
0.67-0.69
0.71-0.83
0.93-2.76
0.80-0.84
0.89-0.91
0.89-0.91
1.79-0.89
0.50-0.60
0.60-1 .10
0.55-0.80
0.63-0.70
0.20-0.70
0.17-0.20
0.95-1 .05
0.15-0.30
0.37-0.40
0.37-0.42
0.08-0.45
0.10-0.40
0.40-0.55
SPARGE
EFFLU TANK VENTURI SPARGE
RES RESID DESUP TANK TANK
TIME TIME RES TIME LEVEL
WIN MIN. MIN. FEET
3.0
12 .0
12.0
12 .0
12 .0
20.0
12 .0
12.0
12.0
N/A
12.0
12.0
12-0
12.0
12.0
17.0
17.0
17.0
12.0
12.0
24.0
24.0
6.0
6.0
18.0
8.3
8.3
8.3
18.0
18.0
18.0
12.0
12.0
12.0
12.0
17.0
17 .0
17.0
12.0
12.0
20.0
12.0
12.0
3.0
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
.N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
•N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
M/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
OXID EDUCTOR
AIR CIRCUL
RATE RATE
SCFM GPM
N/A'
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
BLEED
TO OX
TANK
GPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
BLEED
OXID
TANK
PH
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
H2S04
RATE
GPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
RUN
NO.
VFG-1 A
VFG-1 B
VFG-1C
VFG-1 D
VFG-1 E
VFG-1 F
VFG-1G
VFG-1 I
VFG-1 P
VFG-10
601-1 A
601-18
601-1C
602-1 A
603-1A
604-1 A
605-1A
606-1 A
607-1A
608-1 A
609-1 A
610-1A
611-1 A
612-1A
613-1A
614-1A
614-18
615-1A
615-1 B
616-1A
617-1A
618-1A
619-1A
620-1 A
621-1A
622-1 A
623-1 A
624-1 A
625-1 A
626-1A
627-1 A
628-1 A
628-18
629-1 A
-------
VST OPERATING CONDITIONS
00
i
RUN
NO.
630-1 A
631-1A
632-1A
633-1 A
634-1 A
635-1 A
636-1 A
637-1 A
638-1A
639-1A
640-1A
641-1A
642-1A
643-1 A
701-1A
702-1A
703-1A
704-1A
705-1A
706-1A
707-1A
708-1 A
709-1A
710-1A
711-1A
711-18
712-1A
712-18
713-1A
714-1A
715-1A
716-1A
717-1A
718-1A
801-1A
801 -2A
802-1A
803-1 A
804-1 A
805-1A
806-1A
806-1 B
806-1C
806-10
ALK
TYJ>E
L
L
L
L
L
L
L
L
L
L
L
L
L
L
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
N/A
LS
LS
LS
LS
LS
LS
LS
LS
FLY
ASH
Y
Y
Y
Y
N
N
N
N
N
N
N
N
N
N
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
N
Y
N/A
Y
Y
Y
Y
Y
Y
Y
Y
MGO
Y
Y
Y
Y
N
N
N
N
N
Y
Y
Y
Y
Y
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
Y
Y
Y
Y
N
N
N/A
N
N
N
N
N
N
N
N
PRESCRUB
PH VENTURI
CONTR PH CONTR
POINT POINT
7.00
7.00
7.00
7.00
8.00
8.00
8.00
8.00
8.00
7.00
7.00
7.00
7.00
7.00
5.90
5.90
5.90
5.90
5.50
5.20
N/A
N/A
N/A
N/A
5.60
N/A
N/A
N/A
5.20
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
4 .50
4.50
5.00
5.00
5.00
5.00
4 .50
4.50
4.50
4.50
GAS
RATE
ACFM
35000
35000
35000
25000
35000
35000
25000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
25000
N/A
25000
25000
25000
25000
25000
25000
25000
25000
GAS
VEL
FPS
9.4
9.4
9.4
6.7
9.4
9.4
6.7
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
9.4
6.7
N/A
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
VEN
LIO
RATE
GPM
600
600
140
140
600
600
600
600
600
600
600
140
140
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
400
N/A
400
600
600
600
600
600
600
600
S.T.
LIO
RATE
GPM
1400
700
1400
1400
1400
1400
1400
1400
1400
1400
1400
1400
1050
1400
1600
1400
1400
1400
1500
1400
1400
1400
1400
1400
1400
1400
1400
1400
1400
1400
0
0
1400
1400
13DO
N/A
1400
1400
1400
1400
1400
1400
1400
1400
VEN
L/G
GAL/
MACF
21 .4
21.4
5.0
7.0
21 .4
21 .4
29.9
21.4
21 .4
21.4
21.4
5.0
5.0
21.4
21 .4
21.4
21 .4
21 .4
21 .4
21 .4
21 .4
21 .4
21.4
21 .4
21.4
21 .4
21 .4
21.4
21 .4
21 .4
21.4
21 .4
21.4
21.4
19.9
N/A
19.9
29.9
29.9
29.9
29.9
29.9
29.9
29.9
S.T.
L/G
GAL/
MACF
49.8
24.9
49.8
69.8
49.8
49.8
69.8
49.8
49.8
49.8
49.8
49.8
37.4
49.8
57.0
49.8
49.8
49.8
53.4
49. B
49.8
49.8
49.8
49.8
49.8
49.8
49.8
49.8
49.8
49.8
0.0
0.0
49.8
49.8
64.8
N/A
69.8
69.8
69.8
69.8
69.8
69.8
69.8
69.8
PRESCRUB
SOLID VEN NOW X
RECIRC SOLIDS
NOW X RECIRC
8.0
8.0
8.0
8.0
4.0
8.5
8.0
8.0
4.0
4.0
8.0
8.0
8.0
8.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
8.0
8.0
N/A
8.0
8.0
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
SOLIDS
DISCH
RANGE
%
50-56
53-59
52-56
49-53
51-65
42-52
42-46
44-50
47-59
44-54
48-51
45-50
45-57
41-46
58-63
58-65
60-67
59-65
53-66
54-75
58-73
59-65
61-65
57-63
59-65
56-62
60-63
N/A
59-60
57-62
56-66
70-73
53-59
50-61
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
RUN
NO.
630-1 A
631-1A
632-1 A
633-1 A
634-1 A
635-1 A
636-1 A
637-1 A
638-1 A
639-1 A
640-1 A
641-1 A
642-1 A
643-1 A
701-1A
702-1 A
703-1 A
704-1 A
705-1 A
706-1 A
707-1 A
708-1 A
709-1 A
710-1 A
711-1A
71 1-1B
712-1 A
712-1 B
713-1 A
714-1A
715-1A
716-1A
717-1 A
718-1 A
801-1 A
801-2A
802-1 A
803-1 A
804-1 A
805-1 A
806-1 A
806-1 B
806-1 C
806-10
-------
VST OPERATING CONDITIONS (CONTINUED)
RUN
NO.
630-1A
631-1A
632-1A
633-1A
634-1A
635-1A
636-1A
637-1A
638-1A
639-1A
640-1 A
641-1A
642-1 A
643-1 A
701-1A
702-1A
703-1A
704-1A
705-1A
706-1 A
707-1 A
708-1A
709-1A
710-1A
71 1-1A
711-18
712-1A
712-1B
713-1A
714-1A
715-1A
716-1A
717-1A
718-1A
801-1A
801-2A
802-1 A
803-1A
804-1A
6'.5-1A
806-1A
806-18
806-1C
806-10
VEN
D.P.
IN.
H20
9.0
9.0
2.8
1 .6
9.0
9.0
9.0
9.0
9.0
9.0
9.0
3.6
3.5
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
N/A
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
S.T.
D.P.
IN.
H20
4.4
4.5
4.3
2.1
4.0
4.3
2.0
4.0
3.7
4.2
4.5
3.2
3.5
4.0
5.7
5.3
5.5
5.6
5.6
5.9
5.5
6.0
5.0
5.7
6.6
6.0
5.9
6.4
5.8
6.1
4.5
4.4
5.6
4.0
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
M.E. SYSTEM
D.P. RANGE
IN.H20
0.40-0.50
0.40-0.48
C. 43-0. 45
0.21-0.24
0.46-0.51
0.46-0.51
0.23-0.26
0.45-0.48
0.45-0.48
0.47-0.59
0.45-0.52
0.48-0.51
0.48-0.51
0.41-0.48
0.35-0.70
0.35-0.60
0.30-0.40
0.35-0.76
0.35-0.43
0.30-0.40
0.25-0.43
0.43-0.55
0.33-0.40
0.33-0.40
0.35-0.40
0.33-0.38
0.36-0.40
0.35-0.40
0.38-0.40
0.33-0.40
0.35-0.40
0.35-0.40
0.25-0.50
0.47-0.52
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
EFFLU
RES
TIME
MIN
3.0
3.0
3.0
3.0
12.0
12.0
12.0
3.0
3.0
3.0
3.0
3.0
3.0
3-0
20.0
20.0
20.0
20.0
20.0
12.0
12.0
12.0
12.0
12.0
6.0
6.0
6.0
6.0
6.0
6.0
20.0
20.0
6.0
12.0
19.4
N/A
18.0
18.0
18.0
18.0
18 .0
18.0
18.0
18.0
SPARGE
TANK VENTURI
RESID DESUP TANK
TIME RES TIME
MIN. MIN.
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
17.0
17.0
17.0
1 .3
1.3
1.3
1.3
1 .3
1 .3
1 .3
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
7.0
7.0
7.0
4.7
4.7
4.7
4.7
4.7
4.7
4.7
SPARGE
TANK
LEVEL
FEET
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
18.0
18.0
18.0
18.0
18.0
18.0
18.0
18.0
18.0
18.0
CXID
AIR
RATE
SCFM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
400
400
400
400
400
400
250
150
100
50
EDUCTOR
CIRCUL
RATE
GPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
1590
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
BLEED
TO OX
TANK
GPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
BLEED
OXID
TANK
PH
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
S/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
H2S04
RATE
GPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
RUN
NO.
630-1A
631-1 A
632-1A
633-1A
634-1A
635-1 A
636-1 A
637-1A
638-1 A
639-1A
640-1 A
641-1 A
642-1 A
643-1 A
701-1 A
702-1 A
703-1 A
704-1 A
705-1A
706-1 A
707-1 A
708-1 A
709-1 A
710-1 A
711-1A
71 1-1B
712- A
712- 8
713- A
714- A
715- A
716-1 A
717-1A
718-1 A
801-1 A
801-2A
802-1 A
803-1 A
804-1A
805-1 A
806-1A
806-18
806-1 C
806-10
-------
VST OPERATING CONDITIONS
CO
i
RUN
NO.
807-1A
808-1 A
809-1 A
810-1A
81 1-1A
812-1A
813-1A
B14-1A
815-1A
816-1A
B17-1A
818-1A
819-1A
819-1B
820-1A
820-18
820-1C
821-1A
822-1A
822-18
823-1A
824-1 A
825-1 A
826-1 A
827-1A
828-1A
828-1 B
829-1A
830-1A
851-1A
852-1A
853-1 A
854-1 A
855-1 A
856-1 A
857-1 A
858-1A
859-1 A
859-18
859-1C
859-1D
860-1A
861-1 A
862-1 A
ALK
TYPE
LS
LS
LS
LS
LS
LS
N/A
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
N/A
N/A
N/A
N/A
N/A
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
FLY
ASH
Y
Y
N
N
N
N
N/A
N
N
N
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
N/A
N/A
N/A
N/A
N/A
Y
Y
Y
Y
N
N
N
N
N
N
N
N
N
N
Y
MGO
N
N
N
N
N
N
N/A
N
N
N
N
N
N
N
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
N/A
N/A
N/A
N/A
N/A
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
PRESCRUB
PH VENTURI
CONTR PH CONTR
POINT POINT
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
5.50
5.50
5.50
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
8.00
8.00
8.00
8.00
8.00
8.00
8.00
8.00
8.00
8.00
8.00
4.50
4.$0
4.50
5.00
5.50
5.50
N/A
5.50
5.50
5-50
5.50
5.50
N/A
N/A
5.50
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
4.50
4.50
4 .50
5.20
4.50
5 .00
5.50
5.50
5.50
5.50
5.50
5.50
5.50
5.50
5.50
GAS
RATE
ACFM
25000
25000
25000
25000
25000
25000
N/A
25000
35000
35000
35000
35000
N/A
N/A
35000
35000
35COO
3SOOO
35000
35000
18000
35000
18000
26500
N/A
N/A
N/A
N/A
N/A
25000
25000
25000
25000
25000
25000
25000
25000
25000
25000
25000
25000
25000
25000
35000
GAS
VEL
FPS
6.7
6.7
6.7
6.7
6.7
^6.7
N/A
6.7
9.4
9.4
9.4
9.4
N/A
N/A
9.4
9.4
9.4
9.4
9.4
9.4
4.8
9.4
4.8
7.1
N/A
N/A
N/A
N/A
N/A
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
6.7
9.4
VEN
LIO
RATE
GPM
600
600
600
.600
600
600
N/A
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
N/A
N/A
N/A
N/A
N/A
600
160
600
600
600
600
600
600
600
600
600
600
600
600
600
S.T.
LIO
RATE
GPM
1400
1400
1400
1400
1400
1400
N/A
1400
1400
1400
1400
1600
1600
1600
1600
1600
1600
N/A
1600
1600
1600
1600
1600
1600
N/A
N/A
N/A
N/A
N/A
600
1400
1400
1400
1400
1400
1400
1400
1400
1400
1400
1400
1400
1400
1400
VEN
L/G
GAL/
MACF
29.9
29.9
29.9
29.9
29.9
29.9
N/A
29.9
21 .4
21 .4
21 .4
21 .4
N/A
N/A
21 .4
21 .4
21 .4
21 .4
21 .4
21 .4
41 .5
21 .4
41 .5
28.2
N/A
N/A
N/A
N/A
N/A
29.9
8.0
29.9
29.9
29.9
29.9
29.9
29.9
29.9
29.9
29.9
29.9
29.9
29.9
21.4
S.T.
L/G
GAL/
MACF
69.8
69.8
69.8
69.8
69.8
69.8
N/A
69.8
49.8
49.8
49.8
57.0
N/A
N/A
57.0
57.0
57.0
N/A
57.0
57.0
110.8
57.0
110.8
75.2
N/A
N/A
N/A
N/A
N/A
29.9
69.8
69.8
69.8
69.8
69.8
69.8
69.8
69.8
69.8
69.8
69.8
69.8
69.8
49.8
PRESCRUB
SOLID VEN NOW %
RECIRC SOLIDS
NOM X RECIRC
N/A
N/A
7.8
8.0
8.0
7.0
N/A
8.4
8.4
7.6
8.8
9.6
10.0
15.2
6.0
8.2
10.5
N/A
8.0
5.6
13.3
14. 1
14.7
15.2
N/A
N/A
N/A
N/A
N/A
15.0
15.0
15.0
15.0
7.3
7.8
7.8
15.2
7.2
7.6
7.3
7.0
7.0
7.2
17.3
15.0
15.0
15.0
15.0
15.0
15.0
N/A
15.0
15.0
15.0
15.0
15.0
N/A
N/A
15.0
15.0
15.0
15.0
15.0
15.0
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
15.0
15.0
15.0
15.0
15.0
15.0
15.0
8.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
SOLIDS
DISCH
RANGE
%
N/A
N/A
72-88
37-55
38-52
80.92
N/A
84-92
82-92
81-91
82-89
82-89
83-91
82-89
82-83
78-86
55-71
N/A
80-90
80-89
79-87
80-90
82-88
80-88
N/A
N/A
N/A
N/A
N/A
74-B8
65-80
73-83
75-83
62-88
75-90
70-86
72-90
64-83
69-86
64-77
52-57
74-89
82-90
82-89
RUN
NO.
807-1 A
808-1 A
809-1 A
810-1A
81 1-1 A
812-1A
813-1 A
814-1 A
815-1 A
816-1 A
817-1 A
818-1A
8 19-1 A
'81 9-1 B
820-1 A
820-18
820-1C
821-1A
822-1 A
822-18
823-1A
824-1 A
825-1 A
826-1 A
827-1 A
828-1 A
828-1 B
829-1 A
830-1 A
851- A
852- A
853- A
854- A
855- A
856- A
857-1A
858-1 A
859-1 A
859-18
859-1 C
859-1 D
860-1 A
861-1A
862-1 A
-------
VST OPERATING CONDITIONS (CONTINUED)
CO
i
RUN
NO.
807-1A
B08-1A
809-tA
810-1A
811-1A
812-1A
813-1A
814-1A
815-1A
816-1A
817-1A
B18-1A
819-1A
819-1B
820-1A
820-1 B
820-1C
821-1A
822-1A
822-1 B
823-1A
824-1A
825-1A
826-1A
827-1 A
828-1A
828-1 B
829-1 A
830-1A
851-1A
852-1 A
853-1A
854-1A
855-1A
856-1 A
857-1A
858-1A
859-1 A
859-1 B
859-1 C
859-1 D
060-1 A
861-1A
862-1A
VEN
D.P.
IN.
H20
9.0
9.0
9.0
9.0
9.0
9.0
N/A
9.0
9.0
9.0
9.0
9.0
6.2
7.3
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
N/A
N/A
N/A
N/A
N/A
9.0
2.6
4.7
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
9.0
S.T.
D.P.
IN.
H20
N/A
N/A
2.8
2.7
2.6
2.9
N/A
3.0
7.0
6.8
6.3
6.0
4.6
5.3
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
4.5
1.3
2.4
4.5
2.9
3.1
2.7
2.5
2.8
3.2
3.0
2.8
2.8
3.2
6.4
M.E. SYSTEM
D.P. RANGE
IN.H20
N/A
N/A
0.29-0.35
0.29-0.32
0.30-0.34
0.31-0.36
N/A
0.32-0.38
C. 53-0. 76
c :.,e-o.7a
0.55-C.66
0.57-0.68
0.18-0.86
0.24-0.82
0.52-0^68
0.58-0.66
0.43-0.72
N/A
0.42-0.56
0.41-0.52
0.14-0.23
0.39-0.62
0. 17-0.34
0.39-0.54
N/A
N/A
N/A
N/A
N/A
0.24-0.30
0.23-0.29
0.24-0.30
0.24-0.30
0.32-0.36
0.31-0.36
0.31-0.35
0.31-0.35
0.30-0.34
0.28-0.32
0.30-0.31
0.30-0.32
0.30-0.33
0.27-0.32
0.55-0.64
EFFLU
RES-
TIME
MIN
18.0
18.0
13.4
13.4
13.4
13.4
N/A
13.4
13.4
13.4
16.8
14.7
14.7
14.7
14.7
14.7
14.7
14.7
14.7
14.7
11 .2
11 .2
11 .2
11 .2
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
18.0
18-0
18.0
18.0
18.0
18.0
18.0
18.0
12.6
18.0
18.0
SPARGE
TANK VENTURI
RESID DESUP TANK
TIME RES TIME
MIN. MIN.
1 .3
1 .3
1 .3
1 .3
1 .3
1 .3
N/A
8.8
8.8
11.3
11.3
11.3
N/A
N/A
1 .3
1 .3
1 .3
1 .3
1 .3
1 .3
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
11.3
42.0
.3
.3
.3
.3
.3
.3
.3
.3
.3
.3
.3
1 .3
1 .3
4.7
4.7
4.7
4.7
4.7
N/A
N/A
4.7
4.7
4.7
4.7
4.7
N/A
N/A
4.7
4.7
4.7
4.7
4.7
4.7
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
4.7
17.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
4.7
SPARGE
TANK
LEVEL
FEET
18.0
18.0
18.0
18.0
18.0
18.0
N/A
14.0
14.0
18.0
18.0
18.0
N/A
N/A
18.0
18.0
18.0
18.0
18.0
18.0
18.0
18.0
18.0
18.0
N/A
N/A
N/A
N/A
N/A
18.0
18.0
18.0
18.0
18.0
18.0
18.0
18.0
18.0
18.0
18.0
18.0
18.0
18.0
18.0
OXID EDUCTOR
AIR CIRCUL
RATE RATE
SCFM GPM
N/A
150
150
150
150
150
N/A
150
210
210
210
210
N/A
N/A
210
150
N/A
210
210
210
110
210
110
210
N/A
N/A
N/A
N/A
N/A
150
150
150
150
150
150
150
150
150
150
100
N/A
150
150
210
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
BLEED
TO OX
TASK
GPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
BLEED
OXID
TANK
PH
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
H2S04
RATE
GPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
RUN
NO.
807-1 A
808-1 A
809-1A
810-1 A
81 1-1 A
812-1 A
813-1 A
814-1 A
815-1A
816-1A
817-1 A
818-1A
819-1A
819-18
820-1A
820-18
820-1C
821-1A
822-1 A
822-18
823-1 A
824-1 A
825-1 A
826-1 A
827-1 A
828-1A
828-18
829-1 A
830-1A
851-1A
852-1 A
853-1 A
854-1 A
855-1 A
856-1 A
857-1 A
858-1 A
859-1 A
859- 1B
859-1 C
859-1 D
860-1 A
861-1A
882-1 A
-------
VST OPERATING CONDITIONS
RUN
NO.
863-1 A
864-1 A
B65-1A
866-1 A
867-1 A
ALK
TYPE
L
L
L
L
L
FLY
ASH
Y
Y
Y
Y
Y
MGO
N
N
N
N
N
PH
CONTR
POINT
7.80
7.80
7.80
7.80
7.80
PRESCRUB
VENTURI
PH CONTR
POINT
N/A
N/A
N/A
N/A
5.50
GAS
RATE
ACFM
N/A
35000
35000
35000
35000
GAS
VEL
FPS
N/A
9.4
9.4
9.4
9.4
VEN
LIO
RATE
GPM
600
600
600
600
600
S.T.
LIO
RATE
GPM
1600
1600
1600
1600
1600
VEN
L/G
GAL/
MACF
N/A
21.4
21.4
21.4
21.4
S.T.
L/G
GAL/
MACF
N/A
57.0
57.0
57.0
57.0
SOLID
RECIRC
NOM X
10.4
9.5
10.1
9.9
11.8
PRESCRUB
VEN NOM %
SOLIDS
RECIRC
N/A
N/A
N/A
N/A
15.0
SOLIDS
DISCH
RANGE
X
80-89
81-88
76-84
78-84
83-88
RUN
NO.
863-1 A
864-1 A
865-1 A
866-1 A
867-1 A
CO
I
00
-------
VST OPERATING CONDITIONS (CONTINUED)
RUN
NO.
863-1A
864-1 A
865-1A
866-1A
867-1A
VEN
D.P.
IN.
H20
5.6
9.0
9.0
9.0
9.0
S.T.
D.P.
IN.
H20
5.0
6.3
6.0
7.4
N/A
M.E. SYSTEM
D.P. RANGE
IN.H20
0.06-0.61
0.48-0.68
0.56-0.78
0.61-0.75
0.66-0.82
EFFLU
RES
TIME
WIN
14.7
14.7
14.7
14.7
14.7
SPARGE
TANK
RESID
TIME
MIN.
N/A
N/A
N/A
N/A
8.8
VENTURI
DESUP TANK
RES TIME
MIN.
N/A
N/A
N/A
-N/A
4.7
SPARGE
TANK
LEVEL
FEET
N/A
N/A
N/A
N/A
14.0
OXID
AIR
RATE
SCFM
N/A
N/A
N/A
N/A
210
EDUCTOR
CIRCUL
RATE
GPM
N/A
N/A
N/A
N/A
N/A
BLEED
TO OX
TANK
GPM
N/A
N/A
N/A
N/A
N/A
BLEED
OXID
TANK
PH
N/A
N/A
N/A
N/A
N/A
H2S04
RATE
GPM
N/A
N/A
N/A
N/A
N/A
RUN
NO.
863-1 A
864-1 A
865-1 A
866-1 A
867-1 A
GO
-------
VST ANALYTICAL RUN SUMMARY (GASES)
RUN
NO.
VFG-1A
VFG-1B
VFG-1C
VFG-1D
VFG-1E
VFG-1F
VFG-1G
VFG-1 I
VFG-1P
VFG-10
601-1A
601-1 B
601-1C
602-1A
603-'. A
604-1A
605-1A
606-1A
607-1A
608-1A
609-1A
610-1A
61 1-1A
612-1A
613-1A
614-1A
614-18
615-1A
615-1B
616-1A
617-1A
618-1A
619-1A
620-1A
621-1 A
622-1A
623-1A
624-1 A
625-1A
626-1A
627-1 A
628-1 A
628- IB
629-1 A
AVG
S02
IN
PPM
3044
2951
2916
3206
3168
3329
3042
3112
3184
2433
3742
3225
3130
2987
2912
2813
2941
2730
2891
3083
2768
2746
3038
2724
2778
2812
2772
3020
3038
3314
3356
3428
2682
3074
2484
3020
3067
3165
2758
2789
2517
2833
3009
3244
MIN
S02
IN
PPM
2560
2520
2520
2800
2760
2400
2080
2600
2400
2240
3480
2280
2480
2240
2400
1840
2720
2160
1860
1320
2240
2040
2440
2260
1960
2400
2200
2720
2680
2800
2520
2600
1200
2240
2000
2120
2240
2200
2000
1440
1280
1 120
1600
2320
MAX
S02
IN
PPM
3560
3520
3360
3680
3600
3840
3400
3720
3880
2600
4040
3920
386D
3720
3520
7400
32CO
3120
3160
3900
3440
3720
3700
3120
3520
3320
3600
3680
3760
3720
3920
4040
3960
3940
3440
3840
3740
4000
3200
3680
3840
4040
3860
4280
AVG
S02
OUT
PPM
204
709
738
324
784
2233
475
600
1019
766
632
133
619
426
510
478
559
681
363
479
323
188
44
588
555
394
466
740
1365
1362
1326
970
424
496
306
563
492
704
547
557
418
474
448
625
MIN
S02
OUT
PPM
40
540
520
120
440
1520
100
380
680
620
340
30
120
180
340
50
200
420
60
20
100
50
7
130
320
200
280
600
800
920
540
500
35
150
170
230
210
275
80
BO
30
20
50
180
MAX
S02
OUT
PPM
900
1000
1000
940
1 140
2760
620
900
1540
860
860
320
920
660
740
1080
810
880
470
1000
520
520
120
1720
1060
540
760
1140
2020
1620
1840
1520
1060
740
650
1050
800
1250
960
960
1240
1 170
980
1050
AVG
S02
REM
X
92
73
71
88
72
25
83
78
64
64
81
95
77
84
80
81
79
72
86
83
87
92
98
76
77
84
81
73
50
54
56
68
83
82
87
79
82
75
78
78
84
83
84
78
MIN
502
REM
67
68
67
66
65
20
79
70
56
62
76
89
69
78
76
59
70
67
83
67
82
82
96
33
61
79
73
66
40
47
47
57
65
76
79
66
75
62
67
67
64
67
72
69
MAX
S02
REM
99
76
78
95
85
48
95
85
70
71
90
99
96
93
85
98
92
79
96
98
95
97
100
94
88
91
88
80
68
64
82
83
98
93
91
89
90
88
96
94
98
98
97
95
AVG
MAKE
PER
PASS
MMOL
/L
10.5
8.0
7.8
6.0
9.6
10.3
9.3
9.1
9.9
N/A
21 .5
21 .7
17.3
17.8
16.6
9.3
9.5
8.0
7.3
7.5
7.1
7.5
8.8
6.1
1 1 .5
12.6
1 1 .9
1 1 .7
8.1
9.6
10.0
9.6
6.5
7.4
6.3
7.1
7.4
8.4
7.6
8.1
7.6
6.7
7.3
9.5
MIN
MAKE
PER
PASS
MMOL
/u
7.4
7.1
7.0
4.3
8.1
8.7
7.3
7.9
7.9
N/A
20.5
14.4
13.1
13.0
14.3
6.1
8.7
6.8
5.3
3.8
5.8
5.6
7.1
2.6
8.2
10.8
9.7
10.1
7.1
8.5
8.3
7.9
3.3
6.1
5.3
5.5
5.9
6.7
6.0
4.6
4.1
3.0
4.2
7.0
MAX
MAKE
PER
PASS
MMOL
/L
13.0
9.2
8.8
7.2
11 .2
21 .7
10.1
10.5
11.1
N/A
23.2
26.9
23.7
21.1
19.1
28.2
10.7
8.9
8.2
9.1
8.7
9.6
10.7
8.1
14.7
15.4
5.0
3.9
0.1
1 .2
4.4
11 .4
9.1
9.4
8.0
9.4
9.4
10.6
9.4
9.9
11 .6
9.1
9.2
13.2
AVG
02
IN
5.6
8.9
6.0
5.6
6.3
5.8
5.1
5.1
5.8
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
MIN
02
IN
3.6
7.0
4.4
4.0
4.3
4.7
4.2
3.4
3.8
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
VA
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
MAX
02
IN
8.5
12.8
11 .5
6.7
10.2
8.1
5.6
7.0
7.5
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
AVG
N02
IN
PPM
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
MIN
N02
IN
PPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
MAX
N02
IN
PPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
AVG
BOIL
LOAD
MEGA
WATT
139
142
149
138
141
152
140
143
141
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
54
N/A
N/A
N/A
5
N/A
N/A
MIN
BOIL
LOAD
MEGA
WATT
100
1 14
138
94
80
142
101
101
90
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
54
N/A
N/A
N/A
5
N/A
N/A
MAX
BOIL
LOAD
MEGA
WATT
150
150
156
156
156
155
153
152
150
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
54
N/A
N/A
N/A
5
N/A
N/A
-------
VST ANALYTICAL RUN SUMMARY (GASES)
RUN
NO.
630-1 A
631-1A
632-1A
633-1A
634-1A
635-1 A
636-1 A
637-1A
638-1A
639-1A
640-1A
641-1A
642-1A
643-1 A
701-1A
702-1A
703-1A
704-1A
705-1A
706-1A
707-1A
708-1A
709-1A
710-1A
711-1A
711-1B
712-1A
712-1B
713-1A
714-1A
715-1A
716-1A
717-1A
718-1A
801-1A
801-2A
802-1A
803-fA
804-1A
805-1A
806-1 A
806-1 B
806-1 C
806-10
AVG
S02
IN
PPM
3101
2920
2766
2993
2517
2602
2955
2998
2604
2688
2972
2647
2597
2556
2928
3058
3069
3407
3192
3146
3576
3275
3566
3328
3117
2954
3216
2980
2987
2935
3566
3540
3096
2411
3481
N/A
3439
3145
3221
3426
3340
2820
3236
3103
MIN
S02
IN
PPM
2120
2240
2040
2200
1480
1700
2320
2680
2000
2080
2560
2200
2200
2000
2440
2760
2120
2560
2480
2480
2680
2320
2860
2280
2520
2460
2560
2600
2680
2240
3200
3240
2660
2120
2780
N/A
2780
2640
2460
3000
3000
2520
3000
2700
MAX
S02
IN
PPM
3880
3920
3360
3600
3760
3600
3560
3520
3100
3200
3600
3000
3240
2920
3160
4060
4220
4400
3960
3840
4400
4150
4470
4000
3840
3640
3880
3400
3600
3880
3720
3800
3640
2680
3920
N/A
4060
3520
3840
4130
3840
3320
3480
3320
AVG
S02
OUT
PPM
219
753
481
219
558
512
412
792
523
346
560
293
706
64
327
404
1171
438
510
1029
656
770
659
405
557
526
384
220
700
270
2242
2840
363
532
1177
N/A
1142
999
861
702
816
658
771
583
MIN
S02
OUT
PPM
50
200
140
60
220
130
22C
5-5G
220
0
320
80
120
20
220
200
720
320
260
480
400
320
400
100
340
380
240
100
500
70
2100
2480
100
360
820
N/A
630
620
500
430
660
540
660
460
MAX
SO2
OUT
PPM
440
1600
1020
560
1020
1300
740
-. c -in
760
800
800
800
1020
320
400
840
-.820
600
780
1480
1120
1480
1040
780
960
840
600
500
840
720
2360
3160
850
800
1680
N/A
1800
1900
1180
1000
1000
880
840
680
AVG
S02
REM
91
71
80
91
76
79
84
70
78
86
79
87
70
97
87
85
57
85
82
63
79
74
79
86
80
80
86
92
73
89
29
11
87
75
62
N/A
63
64
70
77
73
74
73
79
MIN
S02
REM
85
55
64
82
68
60
77
66
73
72
74
69
61
88
85
77
47
78
72
53
68
60
70
77
71
72
83
84
68
78
22
3
71
66
52
N/A
50
37
64
69
70
71
70
77
MAX
S02
REM
99
93
93
.98
85
92
89
78
88
100
86
97
94
99
91
92
68
90
89
83
84
87
85
96
87
83
91
96
81
98
33
17
96
82
74
N/A
78
77
80
84
77
77
76
82
AVG
MAKE
PER
PASS
MMOL
/L
10.6
11.9
10.8
9.5
7.0
7.5
6.6
7.9
7.5
8.5
8.7
1 1 .2
11.3
9.2
8.7
9.7
6.6
10.8
9.3
7.4
10.6
9.0
10.5
10.7
9.3
8.8
10.3
10.2
8.2
9.8
13.0
4.8
10.0
6.8
6.8
N/A
6.4
5.4
6.0
7.0
6.4
5.5
6.3
6.5
MIN
MAKE
PER
PASS
MMOL
/L
7.1
9.7
8.7
6.9
4.6
5.8
5.5
7.3
6.3
6.9
7.9
8.1
9.4
7.2
7.4
9,1
4.4
7.8
7.4
4.9
8.1
6.9
8.6
7.6
7.5
7.6
8.1
9.2
7.2
7.6
8.8
1 .1
8.4
6.2
5.3
N/A
5.2
3.3
4.7
5.7
5.5
5.0
5.8
5.6
MAX
MAKE
PER
PASS
MMOL
/L
14.1
17.4
13.0
11 .0
9.7
8.9
7.8
8.8
8.4
10.3
11 .0
13.7
16.3
10.6
9.4
11 .6
8.5
14.1
1 1 .6
10.6
13.0
11 .4
13.1
12.6
11 .7
10.0
11 .9
11 .0
10.9
13.7
14.7
7.3
11 .8
7.2
7.9
N/A
7.8
6.4
7.8
8.4
7.2
6.2
6.8
7.1
AVG
02
IN
N/A
N/A
N/A
N/A
N/A
N/A
8.7
7.5
8.0
8.3
7.9
9.5
8.1
8.6
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
6.1
N/A
6.2
6.6
7. 1
6.3
5.3
5.4
5.9
6.2
MIN
02
IN
X
N/A
N/A
N/A
N/A
N/A
N/A
7.8
6.0
6.3
6.4
6.5
6.0
4.2
6.2
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
4.0
N/A
4.5
5.3
6.1
3.8
5.0
4.2
4.8
6.0
MAX
O2
IN
N/A
N/A
N/A
N/A
N/A
N/A
9.5
9.0
10.5
9.2
10.2
10.2
12.5
10.0
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
8.5
N/A
8.5
7.8
9.5
7.7
6.0
6.6
6.8
6.7
AVG
N02
IN
PPM
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
MIN
N02
IN
PDM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
MAX
N02
IN
PPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
AVG
BOIL
LOAD
MEGA
WATT
N/A
N/A
N/A
N/A
N/A
N/A
139
144
140
139
134
136
142
139
N/A
N/A
N/A
N/A
N/A
N/A
• N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
143
N/A
143
131
139
147
132
136
148
144
MIN
BOIL
LOAD
MEGA
WATT
N/A
N/A
N/A
N/A
N/A
N/A
113
128
100
103
105
100
115
110
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
100
N/A
100
93
92
125
50
100
148
124
MAX
BOIL
LOAD
MEGA
WATT
N/A
N/A
N/A
N/A
N/A
N/A
149
148
150
148
148
163
149
148
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
165
N/A
152
164
153
151
160
150
150
150
-------
VST ANALYTICAL RUN SUMMARY (GASES)
RUN
NO.
807-1 A
808-1 A
809-1 A
810-1A
81 1-1A
812-1A
813-1A
814-1A
815-1A
816-1A
817-1A
818-1A
819-1A
819-1B
820-1A
820-1B
820-1C
821-1A
822-1A
822-1 B
823-1A
824-1 A
825-1A
826-1A
827-1 A
828-1A
828-1 B
829-1 A
830-1 A
851-1A
852-1A
853-1 A
854-1A
855-1 A
856-1A
857-1 A
858-1A
859-1A
859-1B
859-1C
859-10
860-1A
861-1A
862-1A
AVG
S02
IN
PPM
3348
2831
2435
2657
2570
2341
2520
2401
2493
2352
2478
25S4
2996
2977
2279
2412
2820
1720
2758
2378
2507
2627
2458
2731
N/A
N/A
N/A
N/A
N/A
3267
3328
3430
3215
2370
2515
2662
2773
2964
2720
2656
2693
2265
2708
2637
MIN
S02
IN
PPM
2920
2640
2060
1840
2200
1960
2520
1920
1860
1980
1920
1840
2320
2680
1280
1760
2320
1720
2360
1920
2320
2320
1400
2000
N/A
N/A
N/A
N/A
N/A
2920
2960
2640
2680
1480
2240
2480
2360
2760
2560
2320
2480
1960
2080
2080
MAX
S02
IN
PPM
3720
3080
2720
3480
3240
2900
2520
2640
3260
2760
3080
3080
3600
3280
3240
2920
3520
1720
3300
2840
2960
2840
2860
3240
N/A
N/A
N/A
N/A
N/A
3840
3720
3920
'680
3080
2880
2840
3100
3240
3000
3360
3040
2700
3200
3080
AVG
S02
OUT
PPM
651
601
416
424
377
172
220
196
307
330
403
340
408
427
80
148
256
1340
259
220
139
285
135
272
N/A
N/A
N/A
N/A
N/A
676
904
720
531
384
302
391
432
223
222
198
233
120
215
385
MIN
S02
OUT
PPM
400
480
250
160
180
90
220
80
120
200
200
160
160
150
10
60
100
1340
40
80
20
120
30
90
N/A
N/A
N/A
N/A
N/A
440
540
380
240
120
180
280
280
130
180
110
140
80
90
180
MAX
S02
OUT
PPM
780
840
520
660
700
300
220
400
540
680
640
470
660
580
520
280
450
1340
600
320
240
540
300
560
N/A
N/A
N/A
N/A
N/A
960
1200
920
880
640
460
480
560
440
280
440
320
200
440
640
AVG
S02
REM
X
78
76
81
82
83
92
90
91
86
84
82
85
84
84
96
93
89
14
89
89
93
87
93
89
N/A
N/A
N/A
N/A
N/A
77
70
76
81
82
86
83
82
91
91
91
90
94
91
84
MIN
S02
REM
75
67
76
75
75
88
90
83
75
72
76
81
77
79
82
89
83
14
80
86
91
78
87
79
N/A
N/A
N/A
N/A
N/A
72
61
73
73
77
79
81
80
85
90
85
87
92
85
77
MAX
S02
REM
X
82
81
87
90
92
95
90
95
93
89
88
91
93
94
99
96
96
14
98
95
99
95
99
95
N/A
N/A
N/A
N/A
N/A
83
80
84
90
91
92
88
88
95
92
95
94
96
96
92
AVG
MAKE
PER
PASS
MMOL
A
7.0
5.7
5.2
5.8
5.7
5.7
N/A
5.8
8.0
7.4
7.5
7.5
N/A
N/A
7.4
7.6
B.6
N/A
8.3
7.2
4.1
7.8
. 4.0
6.2
N/A
N/A
N/A
N/A
N/A
11 .1
7.9
7.0
7.0
5.2
5.8
5.9
6.1
7.2
6.6
6,5
6.5
5.7
6.6
8.2
MIN
MAKE
PER
PASS
MMOL
A
6.3
5.0
4.7
4.4
5.0
4.9
N/A
4.9
6.2
6.0
6.3
5.5
N/A
N/A
4.2
5.7
7.5
N/A
7.3
6.2
3.8
6.7
2.4
4.9
N/A
N/A
N/A
N/A
N/A
10.6
6.8
5.9
6.4
3.6
5.2
5.4
5.3
6.8
6.3
5.7
6.2
5.0
5.2
6.5
MAX
MAKE
PER
PASS
MMOL
/L
7.7
6.3
5.7'
7.6
6.9
6.8
N/A
6.4
9.9
8.8
8.8
8.8
N/A
N/A
10.5
9.2
11.1
N/A
9.8
8.4
4.7
8.9
4.7
7.4
N/A
N/A
N/A
N/A
N/A
12.3
9.1
7.7
7.7
6.3
6.6
6.2
6.7
7.7
7.1
7.6
7.2
6.6
7.7
9.4
AVG
02
IN
X
6.1
3.2
9.1
7.7
8.5
7.5
7.3
7.3
8.4
8.8
6.9
6.5
7.3
8.5
7.2
6.5
6.7
6.0
6.6
7.4
8.2
7.3
8.5
8.8
N/A
N/A
N/A
N/A
N/A
5.9
5.5
5.1
5.3
10.8
9.5
9.1
6.8
7.8
10.3
9.0
8.1
8.4
8.6
7.6
MIN
02
IN
X
4.2
5.3
6.2
5.8
7.5
6.7
7.3
6.0
7.2
8.0
5.5
5.0
2.4
6.5
6.0
5.7
5.0
6.0
5.6
5.0
6.4
6.0
6.0
7.0
N/A
N/A
N/A
N/A
N/A
5.2
4.0
4.0
4.5
9.5
7.8
8.0
5.2
7.0
9.5
8.0
7.0
7.5
8.0
5.5
MAX
02
IN
X
8.3
19.2
10.5
8.8
10.6
8.8
7.3
8.5
10.6
10.8
8.9
7.8
9.0
10.0
8.3
9.0
9.9
6.0
10.0
10.0
10.0
10.0
10.0
10.0
N/A
N/A
N/A
N/A
N/A
6.7
8.2
7.0
6.1
11 .5
15.1
11 .5
8.1
8.6
11 .1
10.3
9.2
10.5
9.8
9.1
AVG
N02
IN
PPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
MIN
N02
IN
PPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
MAX
N02
IN
PPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
AVG
BOIL
LOAD
MEGA
WATT
134
144
137
117
126
143
152
122
143
136
130
144
144
143
130
130
136
126
147
139
112
138
139
139
N/A
N/A
N/A
N/A
N/A
131
135
136
146
104
136
134
142
137
1 12
130
142
133
133
139
MIN
BOIL
LOAD
MEGA
WATT
110
120
88
94
94
100
152
92
95
95
82
108
103
106
74
50
96
126
96
102
102
96
93
94
N/A
N/A
N/A
N/A
N/A
50
93
59
120
95
105
10
115
98
86
97
125
92
99
105
MAX
BOIL
LOAD
MEGA
WATT
149
152
154
155
154
153
152
152
156
154
151
154
156
155
158
154
155
126
158
158
138
154
154
157
N/A
N/A
N/A
N/A
N/A
152
159
156
150
112
152
151
154
152
153
150
152
153
154
154
-------
VST ANALYTICAL RUN SUMMARY (GASES)
RUN
NO.
863-1 A
864-1A
865-1A
866-1 A
867-1 A
AVG
SOS
IN
PPM
2902
2187
2280
2030
2196
MIN
S02
IN
PPM
2160
1600
1400
1160
840
MAX
S02
IN
PPM
4000
2580
3040
3260
3320
AVG
S02
OUT
PPM
333
106
251
91
261
MIN
S02
OUT
PPM
20
40
20
10
10
MAX
• S02
OUT
PPM
880
250
620
300
680
AVG
502
REM
X
87
94
89
95
88
MIN
SD2
REM
X
71
87
77
89
76
MAX
SD2
REM
%
99
98
99
99
99
AVG
MAKE
PER
PASS
MMQL
/L
N/A
7.0
6.7
6.5
6.4
MIN
MAKE
PER
PASS
MMOL
/L
N/A
5.2
4.6
3.9
2.8
MAX
MAKE
PER
PASS
MMOL
/L
N/A
8.3
8.3
10.2
9.2
AVG
02
IN
%
9.1
N/A
N/A
6.7
9.0
MIN
t)2
IN
%
4.5
N/A
N/A
5,0
8.5
MAX
02
IN
X
12.5
N/A
N/A
8.5
10.0
AVG
N02
IN
PPM
N/A
N/A
N/A
N/A
N/A
MIN
N02
IN
PPM
N/A
N/A
N/A
N/A
N/A
MAX
N02
IN
PPM
N/A
N/A
N/A
N/A
N/A
AVG
BOIL
LOAD
MEGA
WATT
134
96
88
57
66
MIN
BOIL
LOAD
MEGA
WATT
8
60
20
52
65
MAX
BOIL
LOAD
MEGA
WATT
156
130
156
62
68
ro
i
ro
Co
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA
CONCENTRATIONS IN LIQUID, PPM
DO
i
r\>
ANALY CA-M-
RUN TICAL
NO. POINT AVQ MIN MAX
VFG-1A 1816 207 67 764
VFG-1B 1816 1265 606 2570
VFQ-1C 1816 2217 2020 2475
1825 2797 25103280
VFG-1D 1816 1678 1225 2340
1825 1690 1260 2230
VFG-1E 1816 1637 1270 2060
1825 1777 1330 2230
VFG-1F 1818 2188 1850 2800
1825 2506 2090 3540
VFG-1G 1816 2278 2050 2650
1825 2412 2050 2669
VFG-1I 1816 1708 1260 2110
1825 1791 1415 2120
VFG-1P 1816 1560 1350 1840
1825 1803 1570 2145
VFG-1Q 1816 415 264 555
60 1-1 A 1815 682 240 853
1825 325 325 325
601-1 B 1815 334 289 402
1825 467 335 678
601-1C 1815 814 779 853
1825 733 697 760
602-1 A 1815 2325 768 3512
1816
1825 2108 1120 2744
603-1A 1815 2829 2300 3287
1816 2940 2940 2940
1825 2782 2325 3014
604-1 A 1816 3209 1307 4325
1825 3011 2180 3390
605-1A 1816 2188 2085 2345
1825 2246 2190 2325
606-1 A 1816 1343 1237 1475
607-1A 1816 1712 1592 1895
1825 1950 1950 1950
608-1 A 1816 3039 1975 4539
609-1A 1816 8601 2080 3024
610-1A 1816 3417 2635 3920
611-1A 1816 262 50 498
612-1A 1816 610 610 610
618-1A 1815 1752 1250 2255
1816 1136 1060 1250
AVG
3333
352
565
641
572
575
531
561
538
573
638
653
705
718
695
704
14
79
32
39
46
90
78
91
103
186
1 17'
215
382
252
51
53
123
195
230
338
325
126
4097
3449
84
79
MG++
MIN
333
163
493
578
463
466
400
467
427
487
549
569
635
625
529
527
8
27
32
26
38
82
75
19
36
152
117
147
101
146
36
40
102
152
230
203
266
24
2980
3449
66
66
MAX
4089
585
697
687
600
614
665
695
634
691
737
780
779
777
1065
1047
22
98
32
45
52
98
81
155
150
215
117
239
798
346
74
62
160
306
230
525
451
285
6600
3449
103
89
AVG
994
62
104
807
59
248
80
695
74
1 106
130
602
52
530
68
943
21
7
7
11
45
7
35
143
538
68
176
200
81
352
48
488
54
59
648
53
29
78
1613
352
28
20
S03-
MIN
22
0
45
542
13
45
22
294
0
0
45
180
22
226
22
316
0
2
7
3
8
2
11
16
168
24
176
56
8
88
16
416
8
16
648
8
8
24
320
352
24
6
MAX
1945
203
361
972
180
723
135
1289
226
1447
203
1040
113
814
135
1379
56
16
7
23
81
16
56
656
1 184
136
176
560
272
568
80
568
128
152
648
152
64
200
5488
352
32.
32.
AVG
6524
1724
1418
1674
720
762
729
911
1140
1350
624
678
719
1051
1108
1518
182
215
346
216
168
186
261
2074
1524
1654
1715
1874
1629
2168
1488
1859
1925
2001
2182
1731
1420
1188
10906
12225
2435
2070
S04«
MIN
1368
1166
882
1295
238
164
352
369
649
586
201
263
475
614
723
728
140
171
346
181
76
179
218
590
517
1534
1715
1486
665
1573
1192
1698
1180
1542
2182
1141
1210
796
7419
12225
1441
1441
MAX
7899
2228
1803
2111
1460
1743
1326
1507
2150
1899
1010
1385
1204
1607
1622
2017
220
347
346
276
249
192
299
5254
2332
1763
1715
2615
2502
2795
1965
2053
2237
2440
2182
2249
1689
1596
14245
12225
3430
2477
AVG
3982
1818
4326
4475
3923
3951
3537
3552
4285
4253
4805
4776
4248
4137
3730
3743
620
1 168
460
475
666
1373
1193
3065
2913
4688
4555
4355
5647
4729
3048
2977
1707
2458
2524
4907
4160
5558
3187
3545
1400
992
CL-
MIN
531
265
3811
4254
3545
3634
3102
2836
3722
3722
4343
4254
381 1
3634
3013
3190
443
440
460
360
440
1280
1160
1276
1240
3758
4555
3474
1914
3226
2907
2942
1560
2056
2524
2978
3970
4821
2269
3545
1170
567
MAX
4963
4526
5229
4697
4431
4343
4343
4343
5672
5406
5672
5229
4786
4875
4077
4343
775
1440
460
620
980
1440
1230
3959
3956
5318
4555
5176
7658
5318
3190
3013
2127
2907
2524
8627
4325
6098
4396
3545
1630
1630
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA (CONTINUED)
RUN
NO.
VFG-1A
VFG-1B
VFG-1C
VFG-1D
VFG-1E
VFG-1F
VFG-1G
VFG-1I
VFQ-1P
VFG-1Q
601-1A
601-1 B
601-1C
602-1 A
60 3-1 A
604-1 A
605-1 A
606-1 A
607-1 A
608-1 A
60 9-1 A
610-1A
611-1A
612-1A
61 8-1 A
ANALY
TICAL
POINT
1816
1816
1816
1625
1616
1825
1816
1825
1816
1825
1816
1825
1616
1825
1816
1825
1816
1815
1825
1815
1825
1815
1825
1815
1816
1825
1815
1816
1825
1816
1825
1816
1825
1816
1816
1825
1816
1816
1816
1816
1816
1815
1816
AVG
6.96
7.99
8.00
4.76
7.96
5.24
8.02
4.85
7.93
4.59
7.97
5.03
7.99
4.84
7.94
4.72
8.02
8.04
5.20
8.21
5.16
7.95
5.07
8.00
5.25
8.05
8.20
5.43
7.96
6.00
9.02
5.00
8.00
8.09
5.10
8.05
5.00
7.05
7.04
8.40
PH
MIN
6.45
7.79
7.86
4.62
7.87
4.87
7.83
4.29
7.82
4.35
7.73
4.81
7.86
4.53
7.49
4.50
7.79
7.85
5.20
8.10
4.60
7.85
4.90
7.55
4.90
8.00
8.20
4.85
5.30
4.95
8.90
4.90
7.80
7.80
5.10
7.65
5.00
6.90
7.04
8.40
TOTAL IONS,
MAX
7.07
8.21
8.17
4.95
8.08
5.58
8.16
5.20
8.00
4.79
8.29
5.45
8.25
5.12
8.14
4.91
8.50
8.40
5.20
8.30
5.45
8.10
5.30
8.70
5.70
8.10
8.20
7.80
9.30
8.90
9.10
5.10
8.30
8.30
5.10
8.40
5.00
~
7.30
7.04
8.40
AVG
15119
5268
8731
10514
7086
7366
6653
7635
8401
9971
8655
9504
7609
8406
7311
8862
1295
2155
1172
1106
1389
2475
2304
7930
7403
9840
9825
9762
11 295
10914
7065
7852
5304
6589
7753
10382
8723
10595
20208
20181
5780
4377
MIN
2512
2501
7656
9709
6007
6190
5367
6250
7348
8637
8268
8809
6588
7671
6011
7517
939
884
1172
916
1082
2427
2234
2805
4190
8232
9825
8574
4540
7553
6518
7740
4457
6058
7753
7385
7890
9535
16133
20181
4486
4113
PPM
MAX
18076
9580
9666
11244
8777
9530
7585
9121
10223
12775
9532
10425
8955
9668
8094
9547
1579
2535
1172
1353
1853
2535
2339
13224
9907
10880
9825
10815
14368
12217
7343
8051
5806
7269
7753
15504
9381
11279
28310
20181
7075
4532
PERCENT
GYPSUM
SATURATION
AVG
21
94
89
110
42
45
42
54
73
88
39
55
39
57
57
81
14
15
24
15
12
14
19
164
1 19
132
143
146
123
167
123
152
132
139
153
129
105
100
37
94
180
139
MIN MAX
7 87
51 128
56 115
85 134
13 94
10 109
21 74
21 88
45 126
40 131
13 65
18 89
25 71
34 93
37 87
43 109
11 18
12 25
24 24
13 20
6 18
13 15
16 23
48 402
43 186
119 140
143 143
118 196
52 183
123 204
101 159
139 169
84 153
112 168
153 153
99 161
80 131
74 130
5 79
94 94
108 253
108 161
PERCENT
IONIC
IMBALANCE
AVG MIN
4.2 -10.1
4.9 -10.2
3.$ -7.2
7.1 0.3
5.7 -9.7
1.9 -10.1
9.7 0.8
1.8 -7.7
7.9 -1.5
0.9 -6.9
11.6 3.6
6.4 -2.7
8.6 2.2
1 .2 -13.6
6.8 -16.9
-5.6 -17.8
5.8 -7.1
4.5 -12.7
-7.5 -7.5
8.5 1.4
13.7 7.1
11.2 7.4
7.2 3.8
-2.9 -15.0
-6.6 -15.3
0.2 -2.1
-1.6 -1.6
-0.1 -12.6
2.8 -15.6
-2.7 -11 .3
2.0 -5.8
-9.4 -11 .0
-10.0 -18.2
-5.9 -11 .4
-8.2 -8.2
5.9 -14.5
8.5 -4.3
2.3 -5.7
-2.8 -18.4
-15.6 -15.6
2.9 -9.2
-8.9 -14.2
MAX
13.6
14.6
14.3
14.6
12.9
12.5
15.0
11.6
14.6
14.9
15.0
13.9
14.7
10.5
14.2
11.9
14.6
18.1
-7.5
17.1
20.0
18.1
10.3
11.5
0.0
3.0
-1.6
13.7
18.7
3.6
6.2
-8.4
18.9
3.4
-8.2
17.5
15.6
5.8
17.1
-15.6
15.0
-3.2
B-25
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA
CONCENTRATIONS IN LIQUID, PPM
00
i
ro
ANALY CA++
RUN TICAL
NO. POINT AVQ MIN MAX
618-1A 1825 1651 1565 1737
619-1A 1816 1943 1505 2277
1825 2045 16'85 2518
620-1A 1815 1440 1440 1440
1816 1602 1440 1765
1825 1590 1575 1605
621-1A 1816 1750 1750 1750
B22-1A 1816 2378 1935 2810
1825 2632 2275 3215
623-1 A 1816 2350 2055 2680
1825 2714 2709 2719
624-1 A 1816 2395 1690 3360
1825 2611 2050 3644
625-1 A 1816 3038 1215 4280
1825 3433 3090 4160
626-1A 1816 2608 2150 4000
1825 3043 2589 3680
627-1 A 1816 2490 2076 3186
1825 2630 2630 2630
628-1 A 1816 1958 1115 2859
1825 2108 1485 3110
628-1 B 1816 2357 1755 3370
1825 2334 1965 2574
629-1 A 1816 644 223 924
630-1 A 1816 268 106 600
631-1A 1816 585 106 1182
632-1A 1816 229 141 461
633-1A 1816 177 83 569
634-1A 1816 1950 1356 2530
635-1 A 1816 2260 1890 2679
636-1A 1816 2140 1490 2690
637-1 A 1816 1712 1200 1975
638-1A 1816 2008 1400 2380
639-1 A 1816 602 37 1233
640-1 A 1816 714 459 986
641-1A 1816 171 61 840
642-1A 1816 444 79 1178
1825 2090 2090 2090
643-1A 1816 122 76 282
701-1A 1818 2232 1940 2579
1825 2985 2985 2985
702-1 A 1816 1943 1630 2110
1825 1910 1910 1910
AVQ
86
246
292
200
218
377
169
260
275
232
266
229
260
146
147
225
215
93
92
271
262
297
322
3771
3923
4560
4589
4067
332
639
650
604
609
3301
3126
3702
4001
163
3700
437
459
529
518
MG++
MIN
85
109
131
200
200
206
169
45
219
188
275
61
125
65
32
165
173
51
92
115
138
227
302
2809
3179
3539
4009
3579
28
515
597
539
491
2759
2809
3319
3490
163
3159
392
459
447
518
MAX
88
355
418
200
237
549
169
339
328
292
298
380
467
216
199
270
244
190
92
364
339
382
347
5349
4949
5889
5459
4649
587
753
689
700
751
4139
3639
4069
4459
163
4389
465
459
634
518
AVQ
1005
107
680
22
63
479
28
71
746
65
520
65
807
76
489
76
741
60
40
75
393
47
626
849
633
482
783
1124
66
97
75
92
119
871
181
1372
553
760
1064
41
64
61
24
S03-
MIN
912
16
456
22
22
454
28
8
352
16
352
8
664
16
248
16
440
8
40
4
56
0
544
90
180
113
316
271
13
36
22
22
22
81
45
316
135
760
474
8
64
32
24
MAX
1099
384
816
22
104
504
28
544
1272
176
68)8
176
968
144
736
312
992
208
40
328
760
144
672
2216
1492
1221
1402
2103
226
226
226
316
226
3121
407
1922
1786
760
1470
72
84
88
24
AVQ
118f
192f
2351
1830
1891
1618
1841
1609
1820
1351
1828
1190
1454
1368
1762
1307
1490
717
617
1434
1995
1180
1310
9783
7610
8102
7252
8205
1370
1494
1422
1469
1995
8251
7903
6827
8164
880
6765
440
752
411
383
S04«
MIN
513
907
2098
1630
1829
950
1841
1015
1213
1020
1817
493
695
917
1264
633
596
181
617
749
1194
793
1036
6803
5910
5806
5543
6055
261
339
499
1125
1386
4591
6996
8250
5965
880
4779
329
752
278
383
MAX
1862
3397
2565
1830
1953
2283
1841
2578
2337
1672
1840
1759
2002
2258
2295
2072
2121
1199
617
2350
2568
1940
1509
13619
10220
9446
8193
9496
2994
2442
2072
1740
2391
10214
9049
7987
10549
880
9115
596
752
520
383
AVQ
1134
3018
2956
2202
2129
2109
2535
3758
3859
3470
3775
3972
4044
4582
4939
4772
4720
4248
4644
3340
3149
4199
4019
3887
5636
7428
71 19
5051
3408
4627
4282
3363
3616
3363
3699
4788
5798
2942
4669
4935
4928
4735
4573
CL-
MIN
709
2623
2694
2202
2056
1985
2535
2481
3368
3155
3687
2659
2552
1311
3864
3687
4183
3368
4644
1595
2517
3226
3474
3013
4609
5672
6381
4431
1950
4077
3545
2747
2925
2304
3013
3994
4526
2942
3545
4857
4928
4360
4573
MAX
1560
3613
3432
2202
2202
2233
2535
4538
4467
3793
3864
5495
5495
6209
5850
6523
5282
5318
4644
4254
3935
5548
4715
5140
6381
9218
8509
5850
4343
5300
4963
3722
4077
4431
4520
6381
7622
2942
6027
5034
4928
5176
4573
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA (CONTINUED)
RUN
NO.
618-1A
61 9-1 A
620-1 A
621-1A
622-1 A
623-1 A
624-1 A
625-1 A
626-1 A
627-1 A
628-1 A
626-18
629-1 A
630-1 A
631-1A
632-1A
633-1 A
634-1A
635-1 A
636-1 A
637-1A
63B-1A
639-1 A
640-1 A
641-1A
642-1 A
643-1 A
701-1A
702-1 A
ANALY
TICAL
POINT
1825
1816
1825
1615
1816
1825
1816
1B16
1825
1616
1825
1816
1825
1816
1825
1816
1825
1816
1825
1816
1825
1816
1825
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1825
1816
1816
1825
1816
1825
AVQ
4.88
7.76
5.05
8.00
5.15
7.73
5.03
7.99
5.03
3.02
4.93
8.15
4.80
8.02
4.67
8.07
5.50
7.56
5.00
7.80
4.95
5.98
6.94
6.98
6.98
7.03
8.01
8.02
8.01
7.92
7.95
6.99
7.06
7.00
6.98
4.80
6.96
5.66
5.65
5.84
5.10
PH
MIN
4.85
7.40
4.90
8.00
5.00
4.60
4.65
7.20
4.90
7.20
4.60
7.45
4.55
7.55
4.40
7.80
5.50
6.30
4.59
6.90
4.90
5.64
6.17
6.79
6.45
6.86
7.66
6.32
7.79
6.57
7.69
6.91
6.87
6.75
6.55
4.80
6.59
5.80
5.65
5.75
5.10
MAX
4.90
8.10
5.20
8.00
5.30
8.70
5,30
8.60
5.15
8.40
5.20
9.00
5.35
9.30
5.00
8.25
5.50
8.55
5.40
8.30
5.00
6.15
7.12
7.12
7.36
7.28
8.16
8.65
8.24
8.79
8.20
7.19
7.96
7.15
7.23
4.80
7.15
5.90
5.65
5.95
5.10
TOTAL
AVG
5141
7404
8486
5812
6036
6290
6448
8240
9513
7650
9301
8038
9345
9382
10943
9375
10390
7843
8274
7285
8108
8270
8825
19046
18238
21267
20115
18763
7157
9162
8613
7180
8383
16214
15651
16885
18990
7044
16351
8267
9387
7826
7600
IONS, PPM
MIN MAX
5079
6666
7787
5812
5811
5535
6448
6481
8504
6896
9065
5836
6957
4001
9611
7414
9525
6381
8274
5218
6343
6663
8079
15517
15864
16491
18721
16992
4301
7567
6689
5888
6457
12251
14210
15484
16124
7044
14220
7971
9387
7033
7600
5203
8853
9114
5812
6261
7045
6448
10076
10441
8442
9538
11055
12094
12394
12610
12483
11631
9730
8274
8965
9B55
11081
9424
24621
20750
25544
22450
20703
9836
10476
10045
8190
9091
17921
17382
18173
22217
7044
19367
8687
9387
8436
7600
PERCENT
GYPSUM
SATURATION
AVG MIN MAX
91
134
157
122
128
96
133
119
136
103
136
91
111
113
148
104
118
61
54
100
141
87
94
• 76
27
53
19
18
93
91
86
79
115
71
60
15
46
70
11
31
56
26
25
43 139
65 247
141 166
122 122
122 134
.69 123
133 133
81 181
96 178
30 125
138 138
41 135
57 153
80 181
106 185
51 159
52 163
16 103
54 54
46 167
78 194
57 148
76 105
28 114
11 77
9 1 10
9 41
7 60
18 184
21 148
27 132
59 102
76 138
3 136
46 1 10
5 73
6 135
70 70
5 30
23 43
56 56
18 35
26 25
PERCENT
IONIC
IMBALANCE
AVG MIN
10.8 6.7
-4.9 -19.5
-14.0 -17.5
-9.5 -9.5
0.1 -9.5
7.5 5.1
-5.1 -5.1
2.6 -12.3
-3.8 -12.5
10.0 2.6
4.2 -0.2
3.5 -9.3
-5.0 -18.9
5.0 -8.2
-0.3 -7.1
0.1 -11 .3
-5.5 -19.9
2 . 1 -6.3
1.2 1.2
-0.2 -18.8
-5.9 -15.7
2.2 -15.4
-5.2 -13.9
3.3 -8.5
1.7 -15.3
4.4 -8.6
5.4 -3.0
1.6 -14.4
-1.1 -18.9
1.6 -9.2
5.7 -1.0
2.4 -7.6
2.8 -6.5
6.2 -2.1
6.8 -4.3
0.6 -6.3
1.3 -10.1
2.9 2.9
3.6 -8.2
2.1 -6.9
18.9 18.9
0.6 -9.4
4.7 4.7
MAX
14.8
10.9
-11.6
-9.5
9.6
9.9
-5.1
15.7
11.2
16.6
8.6
18.2
17.5
17.8
7.8
19.4
11.5
9.5
1.2
17.3
10.5
17.2
7.0
12.2
19.7
11.4
15.6
11.4
17.3
11.9
16.9
8.7
14.3
14.3
14.9
6.4
9.0
2.9
12.6
12.8
18.9
13.9
4.7
B-27
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA
CONCENTRATIONS IN LIQUID, PPM
CO
l
ro
CO
RUN
NO.
703-1A
704-1 A
705-1A
706-1A
707-1A
708-1 A
709-1 A
710-1A
711-1A
71 1-1B
712-1A
712-18
713-1A
714-1A
715-1A
716-1A
717-1A
718-1A
801-1A
802-1 A
803-1 A
804-1 A
80S-1A
806-1 A
806- IB
ANALY
TICAL
POINT
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
CA-M-
AVQ MIN MAX
3044 2665 3609
2595 1880 3395
1473 1000 2185
1805 1465 2295
1575 1070 2015
1680 1220 2140
1096 565 2045
947 504 2277
1669 1035 2155
2473 1733 3059
1613 1060 2749
2516 2140 2879
611 208 1200
801 730 872
1057 1057 1057
622 396 1260
2386 2100 2810
1254 1015 1567
842 278 1300
1075 810 1297
1483 1310 1667
1607 1280 2110
1308 1025 1610
1324 1015 1635
1876 1510 2315
2094 1725 2560
1674 1455 1940
1683 1430 2080
2264 1920 2695
2277 2010 2719
1663 1520 1890
1669 1480 1870
2453 2190 2920
2231 1970 2495
663 374 1480
618 378 1385
2378 2150 2540
2060 1920 2315
392 335 450
389 325 440
2203 2025 2490
2202 1910 2440
AVG
626
737
590
672
905
817
792
774
646
650
761
876
5035
5569
5769
4962
594
615
350
396
673
700
486
483
702
784
549
534
784
875
582
576
897
1 104
460
450
1 112
1224
393
385
1232
1248
MG++
MIN
426
527
491
582
777
529
737
109
297
355
699
783
4129
4759
5769 '
3839
447
420
158
364
634
586
401
379
503
639
455
443
659
587
485
519
829
899
409
389
1 021
1 121
367
367
1111
1 145
MAX
841
1053
657
757
1082
924
875
949
849
771
800
947
6509
6379
5769
5719
711
723
438
418
722
861
609
601
873
859
589
585
853
1011
641
637
971
1251
561
565
1243
1325
419
407
1313
1313
AVG
114
99
83
168
141
108
59
87
96
106
84
96
1279
1864
6468
1768
1 10
65
221
389
410
24
197
273
462
24
264
333
311
22
132
173
386
13
67
80
334
16
93
101
350
15
S03*
MIN
16
56
48
24
50
32
16
32
16
72
40
88
520
1304
6468
472
31
1 1
45
260
147
0
33
90
45
0
90
67
22
0
45
79
22
0
22
22
45
0
33
45
11
0
MAX
320
160
136
376
264
240
112
184
384
144
176
104
3634
2425
6468
3778
316
814
407
565
588
124
508
701
882
67
1334
1537
531
90
248
316
836
67
180
226
565
33
226
135
497
45
AVG
1464
733
754
2370
945
1181
882
784
1456
1412
520
2188
14310
13377
13890
15955
1870
2158
1575
2016
2535
2159
2229
2282
2545
1904
2257
2277
2334
1928
1974
1995
2298
1950
815
744
2363
2059
733
707
2330
2042
S04»
MIN
988
240
476
1390
421
695
529
410
905
440
360
1951
9584
12544
13890
11535
1670
1819
768
1326
2106
1915
1904
1938
1807
1690
1916
1807
2078
1711
1666
1713
1937
1789
525
444
1949
1931
434
559
2101
1855
MAX
2084
1535
1111
2745
1533
1568
1326
1455
2039
1971
825
2644
18053
14210
13890
20144
2277
2508
2428
2468
2809
2633
2627
2740
3020
2195
2914
3004
2697
2513
2424
2359
2788
2272
1883
1666
3012
2337
901
906
2573
2194
AVG
6207
5849
3847
3871
4410
4580
3651
3350
3726
5326
4935
5530
5241
5761
5743
3176
4519
2359
1118
1329
2773
3405
1979
1955
3494
4677
2839
2756
4728
5360
3204
3150
5529
6025
1745
1687
6202
5970
1 125
1070
6108
6481
CL-
MIN
5247
4928
3190
3580
4041
4006
3155
3013
2623
2978
3900
4609
3651
5424
5743
1595
3722
1373
265
1107
2282
2481
1240
1329
2260
3988
2659
2397
361 1
4121
2836
2747
4742
5052
1196
1063
5872
5717
1019
975
5850
5694
MAX
6878
6736
4538
4290
4644
5347
4538
3900
4821
6559
6594
6452
6771
6098
5743
5530
5229
3168
1506
1484
3257
4697
2747
2747
4697
5894
3190
3190
5827
6204
3900
3877
6293
6470
2902
2792
6603
6381
1 196
1152
6603
7046
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA (CONTINUED)
RUN
NO.
703-1A
704-1A
705-1A
706-1A
707-1A
708-1 A
709-1A
710-1A
711-1A
711-18
712-1A
712-18
713-1A
714-1A
715-1A
716-tA
717-1A
718-1A
801-1A
802-1 A
803-1 A
804-1 A
605-1 A
808-1 A
806-18
ANALY
TICAL
POINT
1816
1316
1816
1816
1816
1816
1816
1816
1316
1316
1816
1816
1816
1816
1316
1816
1816
1816
1815
1816
1825
1851
1815
1816
1825
18S1
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
AVG
5.21
5.79
5.72
5.37
5.76
5.65
5.85
6.01
5.65
5.58
5.80
5.24
5.56
5.43
4.98
5.45
5.91
4.57
5.76
5.61
3.94
4.96
5.55
5.29
4.36
5.09
5.57
4.43
5.07
5.79
4.43
4.92
6.06
4.36
4.62
6.16
3.65
4. S3
PH
MIN
5.08
5.58
5.35
5.10-
5.60
5.50
5.65
5.86
5.46
5.57
5.63
5.14
5.33
5.30
4.96
5.03
5.33
3.63
5.43
5.19
3.43
4.00
5.27
4.20
3.96
4.66
4.66
3.79
4.79
5.12
3. 86
4.65
5.69
4.04
4.48
6.06
3. 54
4.45
MAX
5.32
5.99
6.00
5.70
5.85
5.85
5.99
6.19
5.88
5.60
6.10
5.36
5.85
5.55
4.98
5.70
6.94
4.95
6.12
5.98
4.40
5.33
5.95
5.95
4.98
5.79
5.83
4.99
5.40
5.99
4.75
S.28
6.20
4.68
4.79
6.25
3.82
4.61
TOTAL
AVG
11666
10239
6926
9067
8174
8565
6665
6129
7759
10158
8092
11393
26628
27533
32767
26633
9518
6552
4163
5270
8001
8046
6310
6418
9208
9705
7710
7703
10642
10715
7691
7703
11608
11636
3940
3762
12709
11667
2817
2731
12568
12344
IONS, PPM
MIN MAX
10498
8393
5765
7929
6737
7124
5412
4957
6332
7142
6471
10549
19402
26192
32767
23004
8636
5337
1594
4025
7559
6493
5249
5127
7732
8738
7012
6496
9101
9927
7199
7044
10792
10079
2861
2745
12246
11300
2649
2573
12128
11479
12687
12597
8581
9910
9215
9826
8835
7671
9686
12697
10859
12546
30524
28874
32767
30845
10361
7375
5864
6177
8367
9720
7774
7788
10725
11254
9598
9956
11948
11697
8692
8734
12800
12312
7009
6650
12957
12139
3086
2904
13248
13042
PERCENT
GYPSUM
SATURATION
AVG MIN MAX
100
48
41
125
44
60
36
31
78
90
26
123
84
96
125
92
117
99
75
101
120
107
113
117
133
104
124
126
130
105
107
109
127
97
33
29
119
93
23
22
109
95
70 147
12 106
21 72
72 158
17 83
29 86
16 71
11 118
44 123
27 127
16 36
116 1 36
27 168
84 109
125 125
63 153
1 06 1 36
86 126
30 126
63 128
104 129
94 138
92 139
100 145
103 152
96 119
103 164
98 175
117 152
93 136
88 133
90 133
111 157
88 107
18 100
16 86
94 149
89 102
12 32
16 31
98 118
91 101
PERCENT
IONIC
IMBALANCE
AVG MIN
0.6 -11 .9
7.1 -8.6
0.7 -1t .9
-8.3 -18.1
6.9 -t.2
0.7 -6.8
1.6 -9.4
2-9 -8-2
2.1 -17.6
0.2 -3.2
-2.6 -12.4
H>.2 -1.3
-6.4 -19.0
1.9 -7.8
-14.9 -14.9
-5.6 -18.2
-0,3 -15.9
2.6 -14.5
4.4 -3.8
-0.4 -12.1
-5 . 7 -9.6
0.8 -12.3
2.0 -12.5
-0.2 -13.2
-4.8 -14.9
2.3 -11 .9
-0.5 -14.5
-1.1 -14.6
-2.6 -14.5
1.2 -9.1
0.5 -6.9
0.6 -6.8
-4.4 -9.9
0.8 -3.6
12-9 0.8
12.4 4.4
-5.3 -7.5
1.6 -0.3
9.6 4.6
11.8 6.9
-2.9 -6.2
-0.3 -4.9
MAX
14.9
15.6
13.3
12.2
17.7
12.4
16.6
14.6
19.4
7.8
6.1
1.7
7.2
11.6
-14.9
9.3
18.7
11.2
14.4
8.3
-1.1
9.5
13.4
6.7
8.1
7.8
8.0
5.4
5.8
10.6
5.0
7.7
0.4
4.6
19.3
18.3
-2.6
4.6
12.9
16.6
2.1
4.6
B-29
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA
CONCENTRATIONS IN LIQUID, PPM
co
OJ
o
RUN
NO.
806-1 B
806-1 C
806-1 D
807-1 A
808-1 A
809-1 A
810-1A
811-1A
81 2-1 A
813-1A
814-1A
ANALY
TICAL
POINT
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1325
1851
CA++
AVG MIN MAX
615 153 706
632 459 736
2314 2015 2574
1905 1880 1955
560 360 694
563 366 721
2044 1975 2135
2027 1860 2140
308 293 335
304 290 341
2252 2100 2360
1908 1810 2005
153 137 169
165 155 175
2030 1960 2125
1566 1415 1715
220 220 220
210 210 210
1670 1500 1850
2830 2095 3489
1816 1705 1950
1915 1740 2780
2857 2385 3799
1873 1140 2385
1455 1245 1775
1473 1275 1815
2039 1620 2584
1492 1125 1880
1262 1015 1690
1261 1040 1610
1558 1090 1955
1531 1320 1745
1213 1042 1375
1236 1022 1370
1668 1430 1950
1420 1420 1420
1350 1350 1350
1320 1320 1320
1645 1645 1645
1524 1370 1790
1281 1140 1440
1241 1065 1375
1584 1385 1900
AVG
384
378
1267
1 170
315
310
1 189
1 192
397
376
1204
1020
333
341
1032
1 1 14
266
266
1104
1294
711
733
1283
1 141
639
644
1 145
1032
594
593
1044
1 137
788
788
1 133
1167
877
822
1 189
1386
866
855
1340
MG++
MIN
345
350
1161
1151
213
217
1167
1151
367
324
1 145
899
324
333
973
975
266
266
967
1087
611
630
924
977
544
537
974
567
312
309
799
1012
607
617
892
1167
877
822
1189
1027
612
682
1132
MAX
409
401
1331
1207
365
359
1231
1269
453
411
1273
1079
343
349
1101
1197
266
266
1191
1459
789
992
1544
1342
719
784
1324
1169
757
762
1249
1389
1012
1014
1322
1167
877
822
1189
1509
1022
992
1464
AVG
101
86
250
15
101
180
276
129
116
107
698
553
158
124
990
19
45
45
325
35
98
167
149
25
88
110
280
44
108
124
473
67
109
148
342
50
137
137
525
28
126
127
332
S03=
MIN
67
11
0
11
56
67
22
1 1
90
67
260
192
124
124
554
0
45
45
214
0
33
67
0
0
13
33
113
0
56
67
243
5
67
67
22
50
137
137
525
4
73
79
158
MAX
180
203
520
22
135
452
441
294
158
158
949
995
226
124
1492
45
45
45
429
101
217
746
443
88
191
214
814
113
169
203
938
237
147
294
621
50
137
137
525
67
226
248
633
AVG
1423
1543
2429
2250
1277
1192
2604
2277
684
664
2601
2931
559
4.02
3063
2469
931
973
2807
1834
2002
2113
2116
2171
21 19
2133
2425
2551
2277
2276
2627
2692
2518
2508
2872
2861
2705
2603
3008
3000
2561
2596
3219
504*
MIN
968
1076
2012
2012
670
506
2285
969
548
517
1522
2463
349
364
2701
2227
931
973
2609
1668
1792
1895
1775
1836
1860
1919
2023
2134
2032
1932
2141
2483
2300
2290
2106
2861
2705
2603
3008
2549
2310
2311
2607
MAX
1772
1949
2864
2581
1702
1691
3020
2933
813
801
3319
3622
856
441
3966
2813
931
973
3338
2004
2131
2508
2480
2652
2388
2424
2727
3074
2608
2737
3202
2905
2806
2936
3407
2861
2705
2603
3008
3348
3062
2990
3695
AVG
11 14
1088
6580
5538
970
904
5569
5273
993
974
5469
4317
693
786
4480
4257
310
310
4368
7147
3562
3740
7001
4952
2653
2679
4983
3601
2149
2134
3649
4056
2528
2564
41 12
4015
2969
2836
4210
4442
2761
2720
4439
CL-
MIN
975
975
5805
5335
930
886
5406
4609
930
886
5140
3900
531
731
4010
3811
310
310
3855
6204
3235
3279
6248
3900
2215
2082
3988
3190
1684
1817
3146
3368
1950
1950
3545
4015
2969
2836
4210
4121
2570
2481
4157
MAX
1240
1258
7179
5761
1041
930
5938
5539
1196
1240
5717
4697
797
842
4830
5052
310
310
5008
8509
3811
6364
8331
6260
3545
3456
6337
4298
2481
2526
4343
4564
3057
3146
4609
4015
2969
2836
4210
5273
3057
2947
5273
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA (CONTINUED)
RUN
NO.
806- IB
806- 1C
806-10
807-1 A
80B-1A
809-1 A
81 0-1 A
81 1-1 A
812-1A
B13-1A
81 4-1 A
ANALY
TICAL
POINT
1816
182S
1851
1815
1616
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
18S1
AVG
6.08
3.76
4.49
6.01
3.67
4.53
6.16
4.23
4.48
6.28
4.34
4.53
6.33
3. 56
4.50
5.72
3.34
5.09
5.81
4.23
5.50
6.02
4.59
5.58
5.92
4.84
5.91
5.85
5.25
5.60
5.95
5.88
4. 87
PH
WIN
5.95
3.58
4.31
5.87
3.36
4.46
6.12
4.11
4.41
6.21
4.25
4.41
6.33
3.32
4.40
5.57
2.82
4.83
5.48
3.70
5.25
5.77
3.62
5.15
5.39
4.43
5.91
5.85
5.25
5.32
5.69
5.77
4.04
MAX
6.24
4.00
4.57
6.15
4.03
4.61
6.20
4.36
4.57
6.35
4.49
4.64
6.33
3.92
4.69
5.85
4.09
5.73
5.98
5.07
5.74
8.10
5.06
6.23
6.05
5.40
5.91
5.85
5.25
6.12
6.19
6.08
4.95
TOTAL
AVG
3706
3795
13203
11238
3295
3217
12053
11286
2574
2501
12611
11101
1969
1894
11986
9786
1850
1880
10630
13318
8307
8787
13587
10321
7055
7143
11037
8868
6493
6489
9513
9636
7263
7350
10275
9681
8157
7836
10745
10576
7715
7657
11113
PERCENT
GYPSUM
IONS, PPM SATURATION
MIN MAX AVG MIN MAX
3122
3031
12304
10906
2507
2434
11745
10224
2388
2278
11882
10336
1838
1893
11661
91 10
1B50
1880
9896
11831
7604
7885
12480
8806
6220
6247
9799
7795
5823
5736
8660
8940
6204
6269
9213
9681
8157
7836
10745
9968
7297
7323
10655
4140 56
4280 62
13825 115
11708 99
3960 53
3914 50
12798 117
12334 103
2823 18
2865 18
13379 123
11749 134
2148 9
1896 8
12744 144
1 06 1 5 98
1850 24
1880 24
11274 115
15322 96
8683 106
13357 113
15963 111
11987 95
8208 103
8396 104
12701 111
9458 102
7020. 105
7519 106
10417 106
10254 104
8015 101
8098 102
11147 116
9681 104
8157 110
7836 108
10745 118
11274 104
8274 102
7993 102
11B41 115
32 77
37 78
102 136
90 113
21 72
24 73
103 139
45 131
16 22
16 21
74 156
112 165
6 14
7 9
127 183
92 109
24 24
24 24
108 132
83 116
95 113
101 132
101 127
73 1 09
93 115
93 1 1 7
91 131
87 146
90 146
88 135
92 125
91 118
80 1 19
60 129
87 138
104 104
110 110
108 108
118 118
92 122
86 131
85 124
103 137
PERCENT
IONIC
IMBALANCE
AVG MIN
1.7
0.5
-4.3
0.2
-0.7
1.5
-2.6
6.4
11.1
9.9
-0.4
-2-1
6.3
13-3
-7.4
5.9
17.9
14.1
-1.6
5-1
5.6
4.4
3.4
3.8
6.0
5-6
1.7
5-2
4.0
3.8
-0.5
1.8
2.0
1.6
-1,6
-0.5
0-4
0-3
-4-4
4.3
3.5
1.8
-2.1
-9.3
-9.0
-8.4
-3.9
-14.7
-12.1
-8.1
1 .7
7.3
2.6
-2.9
-4.7
-6.5
8.7
-12.3
1 . 1
17.9
14.1
-4.0
-6.1
-3.0
-8.9
-6.1
-7.3
-5.5
-14. 1
-13.3
-6.6
-13.5
-13.3
-14.1
-11 .3
-6.2
-4.9
-13.7
-0.5
0.4
0.3
-4.4
-12.1
-12.5
-8.5
-10.7
MAX
9.0
10.3
-0.4
2.9
14.5
14.5
0.4
14.3
14.0
13.7
5.2
3.1
14.4
17.9
-4.7
14.2
17.9
14.1
2.6
11.9
11 .8
10.6
11.7
11.6
14.0
14.1
9.5
14.6
14.5
14.1
13.4
12.0
9.1
7. 1
13.5
-0.5
0.4
0.3
-4.4
12.2
11.7
9.7
6.3
B-31
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA
CONCENTRATIONS IN LIQUID, PPM
OJ
ro
ANALY
RUN TICAL
NO. POINT
815-1A 1815
1816
1825
1851
816-1A 1815
1816
1825
1851
817-1A 1815
1816
1825
1851
818-1A 1815
1816
1825
1851
819-1A 1815
1816
1825
1851
819-1B 1815
1816
1825
1851
820-1A 1815
1816
1325
1851
820-18 1815
1816
1851
820-1C 1815
1816
1825
1851
821-1A 1815
1825
1851
822-1 A 1815
1816
1825
1851
822- IB 1815
AVG
2013
1565
1609
2165
2361
1767
1790
2475
3332
1970
1984
3560
3616
2071
2084
3836
3521
2202
2215
3722
3475
2356
2338
3704
617
569
569
672
705
638
761
941
613
627
978
674
554
724
713
663
711
744
740
CA++
MIN MAX
1445 2540
1240 1835
1245 2035
1660 2599
2150 2525
1610 1850
1620 1975
2245 2705
2970 3560
1680 2180
1725 2220
3199 3939
2980 4300
1900 2340
1895 2275
3230 4500
2460 4509
1700 2975
1670 3029
2700 5110
2729 4490
1985 2825
2000 2749
3009 4509
522 902
156 786
274 930
561 802
646 880
508 922
698 912
820 1214
234 974
285 992
894 1204
674 674
554 554
724 724
586 832
482 900
564 890
614 842
652 1044
AVG
1614
1095
091
560
950
173
199
1933
1560
831
795
1574
1774
903
914
1745
2275
1241
1239
2290
2455
1361
1332
2460
9422
5551
4046
9315
9425
5566
9279
9294
5534
5459
9217
9599
2980
9639
10466
6098
6181
10466
9190
MG++
MIN MAX
1 297 2059
929 1409
914 1352
1224 1904
1 564 2274
974 1344
1074 1377
1 764 2144
1374 1934
719 947
687 867
1339 1814
1499 1994
812 989
827 972
1399 1949
1 659 2854
782 1644
719 1637
1 664 2844
2324 2629
1212 1502
1 182 1497
2194 2704
8119 11539
3879 6559
2929 5719
7979 11119
8499 10239
4459 6369
7599 10199
8159 10059
4989 6319
4969 6039
7939 10019
9599 9599
2980 2980
9639 9639
9460 11640
5180 7240
4760 7320
9460 11460
7680 10420
AVG
42
125
137
434
26
129
147
349
24
92
95
284
28
100
120
312
27
110
123
353
25
118
126
325
50
1435
1228
429
950
1419
1584
5583
1559
1809
6275
113
283
1130
735
1684
2053
1 148
411
S03=
MIN
5
0
45
45
1 1
90
101
158
0
45
33
79
4
39
67
45
0
45
33
1 1
1 1
67
22
135
1 1
554
260
45
33
780
407
4466
972
1108
4862
1 13
283
1 130
57
226
509
226
57
MAX
9»
361
200
746
45
180
260
508
45
226
180
520
67
158
203
610
90
203
214
701
56
169
226
520
226
4387
3912
1 040
1877
2259
2962
6672
2307
3573
7633
113
283
1 130
4207
3053
3279
2544
1018
AVG
2667
2540
2584
2881
2597
2460
2422
2861
1945
1874
1948
2418
2010
1942
1931
2447
2183
2126
2157
2497
2446
2352
2416
2845
35289
20131
14624
35350
31530
18596
31232
26473
16871
16765
26277
29452
11617
29262
31348
18700
18407
31340
28339
S04*
MIN
2310
2302
2316
2019
2404
2180
1432
2483
1747
1525
1753
1876
1715
1765
1545
1900
1844
1738
1712
1591
2180
2157
2170
2440
28208
13972
8120
31 121
28391
15815
2781 1
23859
14258
13518
23982
29452
1 1617
29262
26732
14987
14677
26856
24184
MAX
2960
2934
3058
3453
2913
2773
2890
3298
2109
2133
2797
2877
2174
2120
2172
2883
2484
2710
2623
3037
2576
2619
2795
3184
43308
25842
21396
43672
34224
20255
34078
30382
18843
18894
29257
29452
11617
29262
36468
21813
21618
33511
30567
AVG
6060
3832
3818
6010
7651
4616
4628
7665
8701
4391
4404
8839
9452
4838
4876
9579
10892
6150
6135
10993
10432
6045
5963
10480
2765
1384
1698
2769
4168
1830
4237
4435
2352
2352
4753
6647
1553
6603
6871
3517
3512
6938
5752
CL-
MIN MAX
4609 7622
2925 4653
2836 4857
4520 7401
6913 8420
4254 4919
4254 4963
6825 8376
8261 9041
3900 4830
3767 4963
8509 9306
8243 10769
4387 5406
4405 5247
8154 10725
8509 13118
5008 8110
4875 8420
8863 13251
9395 11434
5495 6913
5362 6913
8863 11966
1861 3634
709 1684
1019 2082
1817 3589
2836 6293
1373 2836
2747 6337
3988 5052
2041 2570
2041 2526
4254 7223
6647 6647
1553 1553
6603 6603
3905 8165
2751 4171
2796 4171
3994 8254
5236 6346
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA (CONTINUED)
RUN
NO.
81 5-1 A
816-1A
817-1A
818-1A
819-1A
819-18
820-1A
820-18
820-1 C
821-1A
822-1 A
822- IB
ANALY
TICAL
POINT
1815
1816
1B25
1851
1815
1616
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1851
1815
1816
1825
1851
1815
1825
1851
1815
1816
1825
1851
1815
AVG
5.60
5.83
5.63
4.61
5.50
5.74
5.60
4.52
5.56
5.91
5.78
4.66
5.55
5.90
5.76
4.70
5.45
5.86
5.68
4.49
5.45
5.87
5.71
4.40
5.56
6.05
6.79
4.80
5.18
5.89
5.00
4.76
5.87
5.69
4.58
4.00
9.10
5.46
5.15
5.74
5.59
4.86
5.06
PH
MIN
4.94
5.62
5.00
3.85
5.25
5.50
5.27
4.18
5.29
5.77
5.57
4.36
5.27
5.82
5.60
4.28
5.07
5.56
5.32
4.12
5.16
5.78
5.45
3.78
4.58
5.40
6.79
3.36
4.91
5.66
4.69
4.68
5.66
5.57
4.48
4.00
9.10
5.46
4.30
5.60
5.30
4.00
4.50
MAX
6.33
6.04
5.90
5.74
6.17
5.87
5.79
5.08
5.79
6.04
6.00
4.91
5.75
6.04
5,98
5.70
5. 98
6.12
6.02
4.83
5.79
6.00
5.99
4.71
6.40
6.89
6.79
5.66
5.41
6.10
5.91
4.94
6.03
5.90
4.70
4.00
9.10
5.46
5.60
6.00
6.10
5.50
5.50
TOTAL
AVG
12619
9303
9392
13264
14857
10313
10340
15556
15893
9301
9376
16982
17273
10042
10133
18267
19448
12129
12170
• 20426
19356
12532
12469
20371
48468
29152
22279
48880
47119
28168
47433
47027
27070
27157
47810
46785
17074
47635
50480
30833
31039
50986
44777
IONS,
MIN
10820
7925
7939
10595
14013
9436
9136
14578
15018
8480
8233
16280
15270
9219
9423
16206
15744
10023
9950
17132
17454
11459
11419
17960
39465
21471
16845
43687
42301
23437
40267
43439
24320
24360
44861
46785
17074
47635
47010
25051
24780
47518
38897
PPM
14741
10702
11062
15131
15590
10643
10782
16621
16508
10247
10335
17659
19170
10951
10801
1 9989
22874
15325
15591
23914
21396
13631
13712
22305
59431
36326
30027
58388
50069
32213
51035
49727
29389
29830
51191
46785
17074
47635
57322
34651
34807
55566
48549
PERCENT
GYPSUM
SATURATION
AVG MIN MAX
103
102
106
118
102
103
101
115
103
98
103
131
106
too
100
132
101
99
101
118
108
109
1(2
130
121
97
89
132
125
101
135
145
91
94
150
112
91
119
118
100
104
123
122
87 115
90 119
90 127
90 139
91 12
92 28
62 21
98 33
93 15
84 14
93 51
103 145
91 120
92 112
80 110
110 171
80 120
85 119
80 122
83 155
97 130
100 122
104 128
117 139
101 169
27 147
46 1 16
108 165
113 153
85 148
121 152
123 215
32 154
37 154
130 204
112 112
91 91
119 119
100 143
75 152
86 138
108 149
111 177
PERCENT
IONIC
IMBALANCE
AVG MIN
5.7
5.5
6.0
1.5
6.1
3.3
4.6
2.8
6.3
3.9
1.5
3.4
9.1
2.7
3.1
5.1
7.2
0.6
0.6
5.6
12.0
7. 1
6.1
10.7
0.3
-1.6
-5.4
-1.8
3.0
3.9
0.4
0.5
6.8
5.0
-2.7
3.7
-6.0
1.8
4.7
1.7
2.7
3.6
5.1
-14.8
-0.5
-4.4
-10.5
-9.2
-3.4
-1 .2
-2.6
-1 .7
0.1
-4.3
-5.8
5.2
-2.3
-1 .8
-2.9
-9.0
-9.4
-14.9
-7.9
7.7
0.3
-3.6
1 .6
-10.8
-15.1
-14.8
-14.7
-2.3
-3.9
-8.7
-10.0
-2.2
-1 .2
-12.7
3.7
-6.0
1 .8
-2.7
-12.7
-5.3
-4.5
-2.9
MAX
14.8
13.2
14.8
13.4
14.6
10.7
14.8
7.7
14.6
12.8
6.5
14.1
14.4
8.2
8.2
10.6
15.0
10.7
11.6
14.9
15.0
14.9
14.3
14.9
12.8
12.2
8.8
9.6
9.6
13.9
8.6
7.5
13.2
9.6
3.8
3.7
-6.0
1.8
14.2
10.2
15.0
12.9
11.6
B-33
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA
CONCENTRATIONS IN LIQUID, PPM
RUN
NO.
822-1 B
823-1 A
824-1A
825-1 A
826-1 A
851-1 A
852-1 A
853-1 A
854-1 A
855-1 A
856-1 A
ANALY
TICAL
POINT
1816
1825
1851
1805
1816
1825
1851
1805
1816
1825
1851
1805
1816
1825
1851
1805
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
AVG
782
859
756
653
881
893
952
504
605
643
711
624
655
693
755
669
705
741
805
1447
1152
1145
1541
1577
867
848
1971
1569
1243
1206
1744
1664
1086
1042
1819
1046
853
917
1202
1277
958
964
1455
CA++
MIN MAX
532 136
586 160
646 1 1 2
580 ' 770
640 150
652 128
630 1234
450 588
506 778
514 928
574 982
510 806
538 792
546 860
566 940
590 842
614 1040
610 1046
666 1152
1355 1570
1000 1360
928 1278
1300 1675
1405 1990
747 1037
632 1075
1650 2425
1115 1790
1065 1440
1005 1415
1080 2095
1345 1950
766 1445
800 1460
1420 2210
884 1285
795 922
842 1026
1140 1280
964 1605
830 1160
832 1130
1207 1638
AVG
5985
5870
9243
5820
5870
5830
5902
6160
6125
6116
6237
6648
6550
6404
6613
6514
6353
6314
6388
1141
704
740
1167
1203
714
747
1306
1355
865
904
1349
1314
891
925
1337
304
78
176
290
565
224
272
565
MG++
MIN
4720
4580
8360
5270
5170
5020
5050
5100
5220
5300
5500
5800
5230
5300
5600
5330
5270
5530
500n
1040
632
667
1038
1 119
627
599
1229
1119
667
739
1079
1071
721
755
955
236
44
71
249
425
127
141
446
MAX
6720
6720
10160
6340
6450
6280
6470
7200
7540
7420
7460
7640
7520
6990
7760
7780
8300
7360
7740
1240
790
788
1378
1323
837
851
1395
1479
1011
1035
1463
1507
973
1015
1559
372
121
419
375
766
369
424
760
AVG
3279
3479
997
67
5446
5503
5933
104
5173
5605
5888
220
2618
2739
3047
267
2917
3030
3380
39
76
222
194
22
54
277
980
35
62
228
313
33
58
229
384
24
35
217
314
91
57
233
448
503 =
MIN
961
1300
113
23
1561
1402
1742
23
2431
2940
3506
23
905
1 131
1538
23
565
509
735
8
22
64
8
0
22
56
723
0
32
22
22
0
0
45
22
0
1 1
27
226
11
11
113
57
MAX
4184
4410
1809
170
8481
8029
8594
498
9838
10178
10178
837
4693
4693
5089
1402
4184
4750
5145
88
1 12
336
336
56
147
520
1379
316
124
429
995
192
147
474
1007
56
64
475
386
304
102
392
937
AVG
17352
17026
28294
19889
16628
16653
16833
21002
17495
17127
17421
23187
21049
20909
21215
21265
18978
18993
19047
2502
1932
1978
2920
2718
1374
1435
3102
2683
1933
2132
2997
2598
1557
1605
3075
1986
1515
1728
2088
1952
1629
1763
2113
S04*
MIN
12516
12245
24166
17299
12712
12506
13176
18299
14717
13373
13692
20929
17360
18295
17775
17446
16476
15529
16116
2180
1450
1672
2469
2369
1 107
1092
2761
2285
1526
1602
2280
2189
1077
1152
2681
1720
1356
1509
1875
1628
1461
1448
1692
MAX
19765
19823
32498
21952
20248
19389
20019
25100
21323
21773
21934
25379
24282
24267
23904
23630
22226
24059
24729
2852
2296
2354
3592
3050
1593
1775
3492
2899
2421
2701
3418
2917
2305
2342
3805
2331
1647
19B2
2545
2608
1852
2106
2333
AVG
3324
3247
5825
2534
2566
2545
2597
2698
2653
2681
2729
3628
3475
3378
3509
3955
3899
3848
3921
3705
2383
2355
3802
3961
2254
2264
4487
4190
2671
2609
4198
4325
2860
2835
4456
989
461
569
1088
2063
880
837
2111
CL-
MIN
2751
2574
5192
2174
2263
2263
2263
2308
2263
2352
2352
2973
2973
1420
2751
3106
2973
2973
2929
3461
2130
2176
3373
3567
2038
2038
4343
3767
2481
2399
3722
3456
2082
2082
3412
801
244
244
826
1373
531
531
1462
MAX
3816
3728
6346
2840
2840
2840
2929
3018
2929
2973
3106
5414
4038
3994
3994
4571
4526
4482
4526
3951
2531
2529
4128
4564
2437
2437
4742
4675
3102
2947
4764
4963
3057
3057
4919
1418
621
976
1420
3106
1487
1397
3106
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA (CONTINUED)
RUN
NO.
822-1 8
823-1 A
824-1 A
825-1 A
826-1 A
851-1A
852-1 A
853-1 A
854-1 A
85S-1A
856-1 A
ANALY
TICAL
POINT
1816
1825
1851
1805
1816
1825
1851
1805
1816
1825
1851
1805
1816
1825
1851
1805
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
AVG
5.53
5.40
4.66
6.30
5.25
5.15
4.85
5.91
5.24
5.15
4.80
5.67
5.45
5.37
5.11
5.46
5.35
5.29
5.02
4.43
7.88
3.60
5.63
7.83
4.28
4.80
8.03
5.48
4.92
5.05
8.02
5.64
3.82
4.71
8.11
5.61
3.60
5.10
8.07
5.41
3.64
PH
MIN
5.40
5.20
4*. 00
5.94
4.94
4.84
4.40
5.80
4.90
4.80
4.50
5.30
5.10
5.00
4.70
5.20
5.10
5.00
4.70
4.11
7.65
3.30
5.04
6.57
3.87
4.19
7.57
5.16
3.37
4.62
7.70
5.31
3.03
4.44
7.99
5.31
3.32
4.37
7.82
5.25
3.05
MAX
6.30
6.10
5.10
6.80
5.70
5.70
5.30
6.10
5.50
5.50
5.10
6.00
6.00
6.00
7.00
5.80
5.60
5.50
5.20
4.63
8.25
4.03
6.11
8.28
4.56
5.37
8.29
6.02
5.65
5.50
8.21
6.12
4.50
5.14
8.30
6.21
4.36
5.50
8.30
5.68
4.64
TOTAL
AVG
30896
30654
45463
29162
31582
3161 1
32408
30685
32267
32386
33201
34531
34566
34350
35364
32919
33097
33169
33790
9066
6367
6566
9853
9759
5404
5712
12138
10117
6921
7224
10878
10213
6597
6781
11364
4420
2980
3648
5057
6036
3798
4115
6781
IONS, PPM
MIN MAX
23535
23474
41085'
25985
26603
27553
28500
26880
28542
28474
29025
31687
29809
31209
32039
28172
28178
28345
28213
8851
5966
6117
9172
9209
4892
4763
11073
9291
6203
6439
10064
8687
5186
5482
9499
3779
2707
2915
4726
4888
3129
3316
5900
35251
35436
50798
31357
34095
34305
35690
35748
37544
37818
38748
37590
3791 1
37432
38967
36819
37121
37205
38984
9513
6861
7215
10867
10430
6023
6516
12939
10727
8064
8416
11780
11364
7814
8126
12579
4990
3321
4320
5780
7511
4780
5102
8094
PERCENT
GYPSUM
SATURATION
AVG MIN MAX
111
121
124
106
121
123
131
84
86
90
99
107
104
1 11
119
107
105
110
119
94
81
81
111
104
49
50
130
97
77
81
114
99
58
57
121
106
100
102
118
94
94
96
108
77 168
86 1 74
102 193
90 1 22
94 166
99 169
96 174
74 103
69 1 17
58 127
77 170
86 134
89 1 30
91 139
98 154
92 136
84 157
90 171
93 188
90 102
59 107
60 98
98 128
90 1 17
43 58
33 71
103 159
82 105
56 98
58 101
85 132
82 1 18
35 96
37 97
104 165
91 123
97 107
88 1 13
113 129
80 126
89 1 13
84 1 10
87 121
PERCENT
IONIC
IMBALANCE
AVG MIN
0.3
-0.1
3.9
5.8
-3.9
-4.8
-6.1
4.1
-5.3
-5.8
-5.8
-1.1
-4. 1
-5.3
-4.9
2.7
-2.3
-2.7
-3.4
9.5
8.4
7.4
4.3
9.7
12.2
6.9
-0.1
12.3
15.1
11.2
8.9
11.8
13.3
10.4
5.3
12.3
9.5
5.9
5.2
10.6
11.4
8.1
6.1
-11.6
-12.7
-5.0
-2.8
-11 .2
-13.2
-14.7
-5.6
-14.5
-14.4
-16.8
-10.3
-11 .4
-14.9
-11 .9
-13.6
-17.5
-18.3
-13.8
5.7
1 .5
4.9
0.5
0.9
7.9
-9.3
-8.5
5.1
8.6
5.5
-10.2
2.2
9.5
2.0
-8.6
-1 .1
0.0
-4.8
-9.2
1 .7
6.1
1.4
-4.0
MAX
8.9
11.5
14.7
12.9
6.4
4.2
2.5
11.2
7.0
10.1
10.0
8.5
5.4
2.6
7.0
11.7
14.0
8.1
6.2
14.3
10.7
9.5
6.4
14.7
18.0
14»3
3.7
18.8
19.4
17.2
15.6
15.2
16.5
19.2
13.6
14.5
15.6
13.9
12-4
14.8
18.0
14.2
15.8
B-35
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA
CONCENTRATIONS IN LIQUID, PPM
C3
i
Co
ANALY
RUN TICAL
NO. POINT
857-1A 1815
1816
1825
1851
858-1 A 1815
1816
1825
1851
859-1 A 1815
1816
1825
1851
859-18 1615
1816
1625
1851
859-1 C 1815
1816
1825
1851
859-10 1815
1816
1825
1851
860-1 A 1815
1816
1825
1851
861-1A 1815
1816
1825
1851
862-1A 1815
1816
1825
1851
863-1 A 1815
1816
1825
1851
864-1A 1815
1816
1825
CA++
AVG MIN MAX
1782 1582 2005
1210 10.42 1345
1219 1042 1330
1953 1710 2195
2443 1895 3354
984 845 1117
988 850 1115
2611 2060 3400
2116 1910 2345
1350 1217 1507
1340 1170 1567
2332 2110 2584
2007 1830 2160
1441 1335 1552
1466 1430 1547
2180 1855 2400
2317 1905 2825
1437 1382 1500
1424 1350 1477
2497 2175 2925
2265 2125 2560
1229 1042 1445
1203 1030 1517
2324 2100 2480
2799 2310 3479
1489 1230 1725
1507 1277 1637
2811 2210 3660
2689 2355 3270
1791 1420 2000
1789 1570 1970
2825 2340 3695
3244 2739 3960
1484 1195 1755
1461 1185 1690
3456 2970 4399
3003 2600 3850
1962 1680 2380
2002 1675 2450
3207 2580 4339
3214 2920 3629
2196 1990 2355
2148 2010 2490
AVG
838
446
466
863
1063
300
332
1064
957
569
588
936
1045
595
614
1016
944
602
602
948
1013
594
576
1028
1 145
596
620
1 134
1833
1030
1082
1845
1877
687
716
1884
2342
1310
1315
2339
2442
1420
1405
MG+H
MIN
737
365
385
735
805
257
285
803
772
473
511
797
964
509
582
909
867
529
528
849
824
550
474
919
1007
483
529
974
1564
964
967
1579
1354
499
514
1449
1849
1 157
1 149
1459
2224
1332
1320
h
MAX
924
519
528
947
1227
350
399
1214
1112
656
661
1019
1122
670
664
1129
1009
679
697
1044
1064
668
622
1084
1249
682
702
1259
2054
1107
1224
2029
2259
954
994
2209
2949
1492
1569
2884
2630
1484
1474
AVG
64
88
332
505
20
47
212
427
99
78
194
837
33
63
304
514
87
51
256
922
90
54
86
762
22
39
49
265
38
91
116
265
29
85
181
455
36
80
353
471
26
84
208
S03=
MIN
1 1
22
67
67
0
22
49
316
67
45
67
610
0
1 1
248
226
16
22
4
746
45
33
33
678
0
11
11
169
1 1
22
67
33
0
22
33
203
4
22
56
22
8
22
56
I
MAX
158
147
497
927
45
85
452
576
192
101
429
1062
56
128
361
757
180
90
497
1108
113
79
180
859
45
67
79
395
90
124
158
542
67
135
339
678
237
147
882
1368
36
167
441
AVG
1987
1761
1823
2116
2057
1595
1710
2144
1856
1222
1380
2127
2140
1772
1880
2339
1912
1715
1771
1995
2126
946
881
2271
1852
1317
1374
2097
2227
1972
2131
2504
2255
1782
1890
2632
2579
2398
2638
2929
2499
2332
2439
S04-
MIN
1836
1627
1657
1420
1767
1151
1264
1764
1695
880
903
1980
1982
1670
1722
2092
1712
1562
1459
1760
1986
606
560
2004
1721
1111
1 162
1883
1960
1445
1508
1 146
1963
1468
1520
2266
2161
1973
1990
2052
2305
2075
2137
MAX
2272
1970
2022
2563
2567
1939
1954
2434
2057
1698
2123
2369
2239
1932
2052
2496
2096
1889
2219
2292
2351
1420
1751
2543
2109
1565
1654
2473
2379
2492
2690
3042
2660
2107
2356
2955
2925
4088
5043
5850
2667
2534
2732
AVG
3627
1840
1815
3701
5146
1243
1259
5270
4537
2785
2745
4517
4390
2566
2516
4312
4872
2731
2687
4991
4877
2954
2912
4930
6515
3060
3063
6417
8150
4512
4513
8163
9031
3191
3153
9140
10013
5362
5296
10072
10920
5937
5929
CL-
MIN MAX
2969 4210
1462 2348
1396 2082
3102 4210
4165 6736
1019 1373
1063 1471
4165 7312
4298 4875
2681 2925
2614 2880
4165 4875
4165 4609
2348 2836
2348 2614
3722 4697
4099 5938
2481 3102
2508 2969
4099 6160
4742 5052
2836 3146
2809 3102
4786 5074
5406 7888
2437 3545
2419 3678
5052 7977
6958 8996
4121 4830
4033 4830
7418 9041
7489 10858
2526 4033
2481 4033
7622 11389
8863 12763
4254 6390
3825 6301
9041 12187
10193 11538
5503 6257
5717 6204
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA (CONTINUED)
RUN
NO.
857-1 A
858-1 A
859-1 A
859-1 B
859- 1C
859-10
860-1 A
861-1A
862-1 A
863-1 A
864-1 A
ANALY
TICAL
POINT
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1625
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
AVQ
5.38
8.03
5.54
4.27
5.51
7.98
5.40
3.64
5.49
8.10
4.58
5.49
8.01
4.02
5.60
8.01
4.56
5.36
7.93
4.60
5.52
8.04
3.78
5.49
7.83
5.86
3.26
5.54
8.01
5.78
4.30
5.60
7.81
4.89
4.24
5.59
7.84
PH
MIN
4.71
7.83
5.11
3.45
5.33
6.90
5.02
2.98
5.29
8.00
4.37
5.12
7.78
3.17
5.23
7.70
4.44
4.89
7.42
4.41
5.36
7.90
3.40
5.20
6.79
5.12
2.89
5.17
7.66
5.17
4.00
4.90
5.95
3.79
3.40
5.41
7.53
MAX
6.21
8.28
6.70
6.62
5.75
8.45
5.66
4.41
5.66
8.29
4.77
5.65
8.32
4.64
6.41
8.19
4.68
5.58
8.12
4.75
5.75
8.21
4.35
5.98
8.20
6.37
4.29
5.71
8.36
7.46
4.52
7.04
8.16
5.31
4.89
5.78
8.16
TOTAL
AVQ
8404
5408
5721
9244
10854
4232
4566
1 1642
9695
6072
6317
10885
9777
6535
6872
10523
10275
6619
6826
11505
10520
5863
5744
11462
12496
6593
6706
12884
15187
9532
9768
15838
16746
7350
7522
17888
18556
11425
11919
19610
19713
12286
12428
IONS,
MIN
7546
4843
4950
7692
9350
3576
3901
9984
9422
5602
5452
10594
9380
6087
6493
9442
9265
6427
6544
10531
10230
5234
5287
11090
10740
5572
5779
10818
13352
6282
8533
14698
14320
6066
6199
15632
16467
10232
10361
17787
18544
11495
11905
PPM
MAX
9180
5978
6170
10451
13232
4846
5135
13838
10152
6794
7330
11168
10308
7074
7145
10969
11703
6992
7168
12986
10998
6805
7184
11972
14508
7320
7703
15440
16712
10454
1071 1
17785
19473
8910
9540
21198
21622
14200
14380
22704
20658
12722
13006
PERCENT
GYPSUM
SATURATION
AVG MIN MAX
98
91
93
107
107
86
89
115
95
63
69
114
102
90
95
117
102
87
89
110
110
47
43
117
101
69
72
114
97
90
94
111
109
87
90
131
107
102
112
126
106
102
106
90 1 10
83 100
84 1 02
75 132
96 131
60 103
62 102
101 136
88 102
47 89
46 104
105 130
97 108
86 98
89 105
102 126
96 112
80 95
72 1 12
104 118
98 126
28 71
30 90
103 36
93 09
57 86
59 91
105 28
93 08
60 20
69 22
57 143
94 131
74 98
75 106
107 144
89 130
80 175
84 214
91 240
95 116
90 112
96 123
PERCENT
IONIC
IMBALANCE
AVG MIN
9.9
8.4
3.7
6.4
11 .6
8.5
3.2
8.0
10.3
9.0
5.5
2.6
11.8
10.8
7.2
7.3
9.7
8.1
3.6
1 .3
8.8
8.0
7.1
0.1
7.0
9.5
tO. 4
3.3
5.6
4.8
4.9
3.8
7.7
4.0
2.4
4.5
7.0
6.2
2.7
4.1
5.7
8.1
4.3
-1 .4
-8.5
-15.2
-4.8
4.8
-1 .6
-5.3
-2.5
0.9
-0.6
-15.0
-8.6
8.4
7.5
1 .6
3.7
5.7
2.0
-6.0
-7.8
7.4
0.3
-0.6
-5.9
-2.9
5.8
4.0
-5.7
-1 .8
-4.3
-2.8
-6.0
2.5
-3.8
-2.3
1 .4
-11 .9
-13.7
-8.4
-9.4
2.0
4.7
1.4
MAX
14.2
13.6
11.9
13.7
14.4
14.1
11 .2
13.5
14.9
13.9
13.1
12.2
14.6
12.5
13.0
14.3
14.6
14.8
9.8
9.4
11.4
10.4
12.9
4.6
11.4
14.6
14.3
5.9
12.8
11.2
11.4
13.1
12.2
9.4
11.0
11.2
14.8
13.9
19.4
14.8
14.0
13. B
9.4
B-37
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA
CONCENTRATIONS IN LIQUID, PPM
DO
U>
CO
RUN
NO.
864-1 A
865-1 A
866- 1 A
867-1 A
ANALY
TICAL
POINT
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
AVQ
3328
2667
1807
1840
2869
2330
1647
1576
2478
1768
1240
1238
18S4
CA-M-
MIN MAX
2879 3649
2340 3199
1620 2070
1575 2110
2230 3489
2010 2980
1445 2050
1400 1775
2070 3039
1540 2245
1080 1455
1085 1410
1620 2050
AVG
2439
1609
993
997
1599
1701
882
876
1674
1800
905
909
1793
MG++
MIN
2239
1444
902
902
1469
1549
742
732
1484
1539
814
772
1579
MAX
2640
1854
1107
1102
1834
1884
969
977
1904
2174
992
999
2019
AVG
340
66
91
359
544
51
83
164
467
41
78
274
373
S03«
MIN
56
11
33
22
11
11
33
33
40
0
45
67
33
MAX
576
169
203
735
1029
214
147
508
1402
90
124
689
768
AVG
2793
2195
2116
2314
2509
2364
2004
2046
2730
2706
2218
2320
3094
S04»
MIN
2592
2109
2022
1867
2234
2103
1732
1731
2204
2459
2074
1978
2710
MAX
3091
2281
2291
2598
2800
2650
2293
2476
3387
3190
2413
2505
3388
AVG
1 1059
8029
4451
4449
8087
8077
4259
4256
8058
6692
3367
3357
6797
CL-
MIN
10370
7268
3722
3767
7090
7179
4077
4077
7090
6027
3013
3013
6204
MAX
11715
9041
4875
4875
9138
9484
4609
4520
9306
7241
3634
3678
7090
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA (CONTINUED)
RUN
NO.
864-1 A
865- 1 A
866-1 A
B67-1A
ANALY
TICAL
POINT
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
AVQ
4.38
5.58
7.82
4.53
5.56
7.84
4.56
5. 55
7.82
4.38
PH
MIN
3.92
5.41
7.45
4.08
4.95
7.40
4.00
5.40
6.77
4.04
MAX
5.91
5.90
8.14
5.66
7.75
9.02
4.90
5.90
9.12
4.68
TOTAL
AVG
20580
15090
9733
10225
16147
15003
9185
9214
15910
13473
8048
8342
14384
IONS,
MIN
19553
13989
8799
9193
14619
13917
8461
8381
14791
12390
7409
7561
13427
PPM
MAX
21457
16310
10419
11088
1761 1
16672
10087
101 18
16991
14814
8590
9163
15098
PERCENT
GYPSUM
SATURATION
AVG MIN
121 108
102 95
98 91
107 91
120 103
98 90
92 85
92 85
117 100
91 84
86 81
89 78
106 97
MAX
137
116
108
118
137
109
102
105
142
102
100
98
114
PERCENT
IONIC
IMBALANCE
AVG
2.5
3.2
5.2
0.1
-0.6
-2.4
0.9
-3.6
-6.9
2.2
0.9
-3.5
-3.8
MIN
-1 .9
-8.9
-4.2
-8.1
-11 .8
-12.4
-5.1
-12.5
-13.5
-2.1
-5.1
-13.0
-9.1
MAX
9.0
13.0
12.6
9.5
11 .0
9.5
10.5
3.9
5.2
10.8
5.8
4.5
1.6
B-39
-------
RUN SUMMARY
SOLIDS ANALYTICAL DATA
CONCENTRATIONS IN SOLIDS, WT X
RUN
NO.
VFG-1A
VFG-1B
VFG-1C
VFG-1D
VFG-1E
VFG-1F
VFG-1G
VFG-1I
03 VFG-1P
t
0 VFG-1Q
601-1A
601-1B
601-1C
602-1 A
603-1 A
604-1 A
605-tA
606-1 A
607-1 A
608-1 A
609-1 A
610-1A
611-1A
612-1A
618-1A
ANALY
TICAL
POINT
1816
1816
1816
1825
1816
1825
1816
1825
1816
1825
1816
1825
1816
1825
1816
1825
1816
1815
1825
1815
1825
1815
1825
1815
1816
1825
1815
1816
1825
1816
1825
1816
1825
1816
1816
1825
1816
1816
1816
1816
1816
1815
1816
AVG
0.49
2.43
1.50
2.85
2.20
1.16
3.1 1
2.1 0
1.76
3.75
2.40
2.52
2.85
2.61
3.16
2.36
2.45
2.78
2.59
2.79
2.07
2.05
2.28
2.74
1.33
0.67
1.89
1.73
C02
MIN
0.19
1.49
0.54
1.37
0.88
0.33
2.03
1.52
1.33
2.82
1.64
1.25
2.14
1 .98
3.16
1.28
2.45
1.04
1.73
1.80
1.63
1.30
1.34
2.01
0.68
0.60
1.60
1.48
S02 SO 3 CAO
MAX AVG MIN MAX AVG MIN MAX AVG MIN MAX
0.77 25.72 12.84 29.68 2.97 0.02 5.93 26.40 13.03 30.50
4.12 36.67 33.48 38.65 2.90 0.16 7.61 39.27 35.69 42.62
2.47 22.36 18.82 32.55 2.47 0.55 4.01 24.40 20.36 34.83
4.95 22.62 17.73 25.69 1.81 0.03 7.38 26.22 21.75 30.13
4.73 23.01 18.82 26.42 3.52 0.33 9.23 26.03 21.35 29.37
2.25 16.30 12.66 23.91 2.18 0.12 6.52 18.18 15.21 27.51
3.90 21.26 14.04 25.69 1.83 0.26 3.89 24.57 18.13 28.24
2.80 22.97 19.72 26.79 4.42 1.00 8.07 27.24 25.61 28.66
2.58 20.73 18.09 25.44 2.61 0.06 6.05 23.27 19.76 26.97
4.31 40.35 38.36 43.43 4.88 0.47 10.11 41.69 40.22 43.37
3.96 19.54 15.12 23.06 5.56 1.30 14.01 23.75 19.38 27.70
9.46 19.04 12.56 22.29 5.87 2.86 10.24 23.03 19.31 33.93
3.96 18.44 15.95 23.06 6.28 3.26 9.37 24.04 23.02 25.25
3.63 21.10 16.85 25.37 5.81 0.84 11.49 25.31 22.76 27.14
3.16 22.29 22.29 22.29 5.49 5.49 5.49 26.99 26.99 26.99
3.41 20.73 17.36 23.51 5.36 1.26 8.77 24.07 22.30 26.08
2.45.22.17 22.17 22.17 3.36 3.36 3.36 23.90 23.90 23.90
8.92 20.33 15.30 24.00 5.28 0.72 10.99 26.38 19.90 29.60
3.90 19.95 16.70 22.90 5.53 3.46 11.23 26.35 25.10 28.40
•
8.14 20.81 19.30 22.20 5.37 3.80 6.98 27.04 25.70 31.70
2.50 21.40 19.20 24.10 6.24 3.95 8.50 27.36 26.80 28.60
3.11 20.42 16.10 22.70 6.44 3.88 10.59 25.15 22.88 28.30
3.00 20.73 14.10 23.90 6.75 3.55 15.71 24.94 23.90 26.38
4.01 20.46 17.20 23.50 6.13 2.76 8.10 24.91 23.31 26.71
1.92 23.82 19.73 26.30 6.95 1.92 9.94 26.19 23.34 27.79
0.74 19.45 17.20 21.70 7.77 6.46 9.07 22.47 22.01 22.93
2.28 18.48 17.10 20.56 6.12 3.23 9.39 24.16 22.62 25.94
2.17 18.09 14.90 20.60 8.70 5.94 11. BO 22.71 20.62 25.51
WT X
AVG
2.52
0.16
2.97
2.40
2.86
4.42
3.48
4.77
2.93
0.22
3.83
3.80
3.63
3.60
3.67
3.66
3.90
3.54
4.03
4.12
IN SLURRY
MIN MAX
2.23
0.04
2.58
2.24
2.50
3.72
3.20
3.83
2.40
0.15
2.90
3.17
3. 18
3.27
3.00
2.75
3.09
3.00
3.20
3.66
2
0
3
2
3
5
3
5
3
0
7
4
4
4
4
4
5
4
4,
.85
.28
.36
.55
.24
.97
.77
.72
.30
.28
.04
.34
.09
.25
.50
. 1 1
.40
.07
.85
4.56
WT X IN <
AVG MIN
8.6
8.4
8.7
8.0
8.4
8.9
8.3
14.6
8.6
15.0
8.1
7.9
7.9
8.7
8.6
15.2
15.0
8.4
8.5
8.3
8.4
8.2
8.5
9.0
7.8
7.8
8.4
8.3
7.6
7.8
8.1
7.3
8.0
7.3
7.2
8.3
7.5
14.4
7.0
2.0
7.0
7.7
8.6
13.3
15.0
6.8
7.5
7.5
7.9
6.5
7.9
7.4
7.3
6.2
7.3
7.3
5LURR'
MAX
13.3
9.1
9.8
8.5
8.9
15.0
8.9
15.9
13.4
15.6
9.4
9.0
8.8
10.0
8.6
16.9
15.0
15.2
9.3
9.0
9.4
9.4
9.1
12.1
8.4
9.3
9.7
9.7
-------
RUN SUMMARY
SOLIDS ANALYTICAL DATA (CONTINUED)
RUN
NO.
VFG-1A
VFG-1B
VFG-1C
VFG-1D
VFG-1E
VFG-1F
VFG-1G
VFG-1I
VFG-1 P
VFG-1Q
801-1A
601-18
601-1C
602-1 A
603- 1 A
604-1 A
605-1 A
606-1 A
607-1 A
606-1 A
609-1 A
610-1A
611-1A
612-1A
618-1A
ANALY
TICAL
POINT
1816
1816
1816
1825
1816
1825
1816
1825
1816
1825
1816
1625
1816
1825
1816
1825
1816
1815
1825
1815
1825
1815
1825
1815
1816
1825
1815
1816
1825
1816
1825
1816
1825
1816
1816
1825
1816
1816
1816
1816
1816
1815
1816
PERCENT
SULFITE
OXIDATION
AVG MIN MAX
8.3
S.B
7.9
5.9
10.3
9.3
6.3
13.4
9.1
8.7
18.4
20.0
21.4
18.0
16.5
17. 2
10.8
17.1
18.2
17.2
18.9
20.2
20.6
19.3
18.9
24. S
20.8
27.8
0.1
0.4
2.3
0.1
1 .3
0.6
0.8
2.9
0.2
0.9
4.4
10.6
10.2
2.6
16.5
4.2
10.8
2.6
11.0
12.2
12.5
12.1
11.0
9.4
5.5
19.2
11.7
19.3
17.4
14.5
12.1
25.0
24.3
20.5
13.1
24.5
21.0
17.4
38.0
38.3
31.1
34.5
16.5
28.8
10.8
32.2
35.0
22.1
26.2
33.8
47.1
27.4
27.7
29.7
30.5
36.0
STQICHIOMETRIC
RATIO
AVG MIN MAX
1.03
1 .09
1.09
1.17
1.12
1.10
1.21
1.12
1.11
1.12
1.15
.1.15
1.18
1.15
1.17
1.14
1.14
1.17
1.16
1.17
1.11
.12
.13
.16
.07
.04
.12
.10
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
.01
.OS
.03
.09
.05
.02
.12
.08
.07
.09
.10
.08
.13
.11
.17
.07
.14
.06
.10
.10
.09
.OB
.07
.11
.04
.03
.10
.08
1 .09
1.16
1.19
1.28
1.30
1.20
1.35
1.16
1.17
1 .14
1.25
1.52
1.25
1.23
1.17
1.21
1.14
1.59
1.22
1.50
1.14
1.18
1.18
1.25
1.10
1.04
1.14
1.12
PERCENT
IONIC
IMBALANCE
AVG MIN MAX
4.5
5.0
4.9
5.8
2.5
4.9
3.0
5.0
4.4
-4.4
-1.4
-4.2
-0.5
-2.3
-1.5
-3.6
-4.1
5.1
6.5
5.6
5.9
0.4
-3.4
-3.2
-4.7
-3.8
5.3
-6.3
-3.5
-2.6
-2.6
1 .1
-6.1
-0.4
-2.6
1.4
-3.3
-6.5
-8.5
-8.5
-6-7
-8.1
-1.5
-7.5
-4.1
-6.8
2.6
1.9
3.0
-8.4
-7.5
-8.5
-8.4
-5.9
-0.2
-8.5
7.9
8.4
7.7
8.4
7.6
8.3
7.4
8.2
8.1
-1 .1
7.0
8.2
5.2
8.5
-1.5
7.3
-4.1
8.5
8.4
7.0
7.8
8.1
2.8
1 .7
-0.8
-1.6
7.1
-2.3
B-41
-------
RUN SUMMARY
SOLIDS ANALYTICAL DATA
CONCENTRATIONS IN SOLIDS, WT X
CD
RUN
NO.
618-1A
619-1A
620-1 A
621-1A
622-1A
623-1A
624-1 A
625-1A
626-1 A
627-1A
628-1 A
628-18
629-1 A
630-1 A
631-1A
632-1A
633-1 A
634-1 A
635-1 A
636-1 A
637-1 A
638-1 A
639-1A
640-1A
641-1A
642-1 A
643-1 A
701-1A
702-1 A
ANALY
TICAL
POINT
1825
1816
1825
1815
1816
1825
1816
1816
1825
1816
1825
1816
1825
1816
1825
1816
1825
1816
1825
1816
1825
1816
1825
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1825
1816
1816
1825
1816
1825
AVO
2.15
1.86
2.16
1.91
2.36
1.82
1.91
1.70
2.33
1.85
1.92
0.45
0.73
0.63
0.58
1.01
3.83
3.00
3.08
. .67
1 .81
1.30
1.33
1.26
0.81
1.15
7.59
8.98
C02
MIN
0.97
1.35
1.79
0.88
1.83
0.73
1.25
1.15
1.20
0.48
1 .09
0.11
0.43
0.27
0.37
0.58
2.51
1.70
1.76
1.18
0.44
0.28
0.94
0.62
0.32
0.67
5.21
6.99
MAX
4.83
2.56
2.51
3.76
2.87
3.06
2.39
2.51
3.72
6.55
3.00
1.26
1.10
1.21
0.86
1.33
6.43
5.17
3.68
2.30
2.47
2.10
1 .80
1.74
1.28
1.91
10.25
10.51
S02 S03 CAO
AVG MIN MAX AVG MIN MAX AVG MIN MAX
18.89 13.50 22.80 9.46 7.02 13.33 24.55 21.61 28.10
16.89 16.90 21.30 5.96 4.14 9.17 23.17 21.64 24.14
17.22 16.00 18.30 6.48 4.71 7.57 22.64 21.94 23.43
19.78 14.20 23.80 6.33 2.00 9.79 23.63 21.48 27.20
22.41 20.80 24.40 4.71 2.68 6.77 24.58 23.52 25.24
19.97 14.80 25.90 6.70 2.09 10.32 23.73 19.16 26.93
19.19 15.40 23.50 7.68 3.82 11.62 25.00 19.87 29.28
18.60 14.20 24.10 7.16 4.36 11.78 23.73 21.10 29.45
20.22 16.70 23.42 4.99 3.63 8.03 24.28 22.90 25.00
19.23 13.00 22.80 7.16 3.74 10.78 23.40 21.10 26.62
20.22 15.fi" 24.70 6.82 4.33 9.47 24.31 21.58 26.70
23.43 18.00 27.30 8.05 3.40 14.10 26.10 23.00 30.00
24.33 19.40 31.10 5.59 3.18 9.16 25.75 22.50 29.30
21.34 15.90 26.90 6.27 2.08 9.93 24.04 20.00 29.50
22.23 19.60 29.10 5.42 3.23 9.95 23.75 21.70 27.20
25.34 21.00 28.90 5.14 3.08 8.01 26.66 23.40 29.30
35.56 28.90 40.40 4.17 0.51 11.16 38.16 34.20 43.40
35.79 28.20 40.10 10.48 2.21 19.26 42.44 39.50 45.30
35.84 32.60 39.45 9.74 3.55 18.78 43.24 39.50 46.96
37.90 36.30 39.09 9.21 2.54 15.43 42.66 40.81 44.04
35.81 33.29 37.64 9.42 1.49 16.67 39.97 36.33 44.23
35.87 26.62 42.29 14.82 5.25 25.92 41.54 33.23 46.88
37.22 32.75 38.91 14.93 7.46 23.43 43.54 40.25 46.03
40.87 35.65 43.11 7.68 1.42 15.27 42.13 39.55 45.37
38.71 35.47 41.98 8.24 0.48 13.78 40.15 36.14 43.53
40.64 38.18 42.34 10.70 2.81 13.61 43.79 39.80 45.61
20.47 17.30 23.10 4.90 1.67 6.53 30.58 28.06 32.90
23.27 20.00 26.00 1.60 0.77 2.35 32.67 29.76 35.14
WT X
AVG
3.63
4.10
4.23
3.87
3.59
3.96
3.52
3.92
7.36
4.46
4.05
3.66
3.79
3.97
3.97
3.55
0.93
0.87
0.58
0.15
0.03
0.06
0.33
0.09
0.20
0.14
5.71
5.20
IN SLURRY
MIN MAX
3.00
3.00
3.90
3.12
3.08
3.05
2.12
2.72
7.35
3.07
3.12
2.56
3.00
2.56
2.80
2.83
0.42
0.02
0.01
0.07
0.01
o.ot
0.02
0.03
0.03
0.05
4.60
4.67
4.33
4.73
4.84
4.55
4.07
6.09
4.61
5.06
7.36
6.34
4.61
5.12
4.47
5.23
4.90
4.80
1 .47
1 .78
1 .29
0.35
0. 10
0.30
1 .34
0.16
0.85
0.44
6.23
5.44
WT X IN £
AVG MIN
7.9
8.3
8.3
8.2
8.0
8.6
8.1
8.5
15.1
9.6
9.0
8.9
8.6
8.4
8.2
8.3
4.3
8.3
8.3
8.3
4.6
3.9
8.3
8.1
8.1
8.1
16.2
15.2
6.6
6.9
7.9
6.4
7.2
6.9
4.5
7.5
14.6
•
6.7
7.6
6.9
7.4
5.6
7.5
7.1
3.4
7.2
7.7
7.7
3.6
0.0
7.7
7.5
6.3
7.2
14.4
14.8
>LURR'
MAX
9.4
9.5
9.4
9.6
8.9
13.8
9.4
9.6
15.9
12:5
10.2
13.3
9.7
9.7
9.3
10.2
6.1
9.3
9.1
9.2
8.1
5.5
9.4
8.5
9.0
8.8
18.6
15.9
-------
RUN SUMMARY
SOLIDS ANALYTICAL DATA (CONTINUED)
RUN
NO.
618-1A
619-1A
620-1A
621-1A
622-1A
623-1A
624-1A
62S-1A
626-1 A
627-1A
628-1A
628-1 B
629-1A
630-1 A
631-1A
632-1 A
633-1A
634-1 A
635-1 A
636-1 A
637-1 A
638-1 A
639-1 A
640-1 A
641-1A
642-1 A
643-1 A
701-1A
702-1A
ANALY
TICAL
POINT
1825
1816
1825
1815
1816
1825
1816
1816
1825
1816
1825
1816
1825
1816
1825
1816
1825
1816
1325
1816
1825
1816
1825
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1825
1816
1816
1825
1816
1825
PERCENT
SULFtTE STOICHIOMETRIC
OXIDATION RATIO
AVQ MIN MAX AVG MIN MAX
28.9
20.1
23.2
20.5
14.4
21 .3
24.4
23.8
16.8
23.1
21.4
21.4
15.6
19.0
16.2
13.9
8.5
18.5
17.6
16.0
16.9
24.6
24.1
13.0
14.3
17.3
16.1
5.4
19.8
13.6
17.2
6.5
8.1
6.5
11.9
13.1
11.2
12.7
12.3
10.3
9.0
7.5
8.2
7.9
1.0
4.5
6.7
5.1
3.1
9.8
13.4
2.6
1.0
5.1
5.5
2. a
1
44.1 1
29.1 1
27.5 1
35.6 1
19.8 1
30.6 1
36.6 1
39.8 1
27.8 1
39.8 1
28.8 1
31.3
21 .9
33.3
27.2
19.6
20.7
35.3
31.2
24.4
26.7
43.8
36.4
25.5
23.7
-21.3-
22.2
8.6
.12
.12
.14
.11
.13
.10
.11
.10
.14
.11
.11
.02
.04
.04
.03
.05
.15
.10
.10
.05
.06
.04
.04
.04
.03
.03
.46
1.94
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
.06
.08
.11
.05
.10
.04
.07
.07
.08
.03
.06
.00
.02
.01
.02
.03
.09
.05
.06
.04
.02
.01
.03
.02
.01
.02
.30
.38
1 .26
1.17
1 .17
1 .20
1 .16
1 .18
1.13
1.18
1.25
1 .44
1.17
1.07
1 .07
1 .08
1.05
1 .06
1.26
1 .21
1.12
1.08
1.09
1 .05
1.05
1.05
1.04
1.06
1.67
1.70
PERCENT
IONIC
IMBALANCE
AVG MIN MAX
-5.5
0.4
1.2
-2.3
-5.5
-3.2
1.1
1 .1
0.5
-3.5
-2.6
-2.3
-1 .4
0.7
-0.9
-1 .5
-2.2
-0.1
2.6
2.1
-0.7
-4.6
-2.8
-1 .5
-1 .4
-1.7
-1.5
-1.1
-8.2
-4.8
-2.2
-8.5
-8.1
-8.5
-7.7
-8.3
-7.7
-8.0
-7.5
-7.8
-8.4
-4. 1
-6.4
-6.3
-8.3
-7.5
-6.3
-6.0
-8.3
-8.2
-8.3
-4.3
-5.7
-6.1
-7.7
-8.2
-2.7
3.7
3.9
6.6
-1 .9
4.7
7.9
7.5
7.9
4.9
8.3
6.3
3.9
7.3
4.4
4.2
7.6
7.6
7.7
e.o
7-9
1 .7
2.9
3.2
5.4
2.0
6.4
7.4
B-43
-------
RUN SUMMARY
SOLIDS ANALYTICAL DATA
CONCENTRATIONS IN SOLIDS, WT %
DO
I
RUN
NO.
703-1A
704-1 A
705-1A
706-1 A
707-1 A
708-1A
709-1 A
710-1A
71 1-1A
7 1 1 - 1 B
712-1A
712-1B
713-1A
714-1A
715-1A
716-1A
717-1A
718-1A
801-1A
802-1A
803-1 A
804-1 A
805-1 A
806-1 A
806- IB
ANALY
TICAL
POINT
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1616
1816
1816
1816
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
AVG
0.88
7.85
4.02
2.62
5.77
4.03
5.72
7.66
4.85
5.93
9.1 1
8.66
2.02
5.04
5.67
4.60
6.34
0.68
5.00
1.72
9.03
1.54
8.87
1.17
9.91
1.33
11.11
0.64
6.80
0.43
C02
WIN
0.05
2.18
' 2.97
0.38
3.30
0.84
3.60
1.02
2.36
2.75
4.93
1.23
1.25
3.23
5.28
1.98
1.47
0.02
1.87
0.16
2.69
0.44
1.49
0.10
5.61
0.33
6.12
0.22
4.78
0.22
S02 503
MAX AVG MIN MAX AVQ WIN MAX AVG
1.97 19.82 14.30 23.10 5.18 2.84 9.30 21.00
11.15 18.13 14.00 22.00 4.62 1.66 11.09 29.63
6.15 24.56 20.30 27.90 2.78 0.59 5.79 28.60
5.27 20.04 19.50 20.50 5.57 3.70 7.05 23.75
8.31 22.60 18.00 24.30 3.19 0.73 6.39 27.49
6.64 21.87 20.30 23.90 5.27 2.74 7.35 26.37
9.57 22.53 19.70 26.10 3.71 2.00 5.99 28.16
10.80 20.93 17.30 25.40 3.12 0.06 7.25 29.82
7.31 20.90 16.40 25.30 3.40 1.03 6.59 25.92
7.98 18.18 15.00 23.90 3.83 1.90 5.22 26.16
11.54 19.78 16.70 24.20 3.38 1.78 5.25 30.27
19.25 19.31 13.30 22.30 2.11 0.03 3.98 28.32
4.46 19.15 16.50 22.20 4.96 2.52 7.27 22.84
7.55 21.21 18.80 23.70 4.61 1.65 6.66 27.24
6.05 18.18 15.10 21.30 3.43 1.58 4.44 26.17
16.76 20.79 2.30 25.30 5.83 1.25 13.03 27.94
10.43 29.45 22.70 32.70 12.18 6.56 20.78 43.40
2.80 1.74 0.18 16.28 14.61 2.17 40.09 13.12
9.13 32.69 7.60 39.45 7.24 0.97 46.43 41.77
6.32 0.55 0.00 1.75 15.54 5.02 29.48 13.82
15.28 28.14 19.54 35.47 7.41 2.14 12.97 42.17
•
4.07 0.56 0.18 1.09 16.02 9.46 22.40 13.64
13.39 27.13 19.90 32.57 7.33 3.05 17.19 41.87
1.92 0.42 0.00 0.98 16.24 5.52 29.57 13.64
16.50 28.26 22.26 31.85 6.32 1.38 11.44 42.94
3.11 0.30 0.01 1.44 18.55 12.76 24.05 15.51
15.89 28.36 23.16 35.77 4.68 1.46 13.75 43.59
0.90 0.21 0.01 0.53 21.00 14.97 33.23 15.54
9.90 33.54 28.95 36.91 4.27 0.15 8.97 42.30
0.66 0.28 0.15 0.36 17.87 8.78 30.59 13.12
CAO
MIN
16.05
22.54
22.82
19.78
23.81
22.20
25.66
22.90
23.98
23.17
27.96
21.80
21.64
24.68
24.46
22.91
38.70
4.20
36.47
6.85
36.86
8.09
37.72
5.90
40.28
10.18
40.96
10.95
41.22
6.98
MAX
22.31
33.89
30.92
27.05
29.40
28.30
30.30
34.40
28.30
28.75
32.84
36.00
24.74
31 .75
28.04
33.64
49.80
36.68
44.01
24.23
45.41
18.80
44.44
23.38
46.32
19.06
46.17
24.08
43.63
21.34
WT X
AVG
8.07
5.94
5.72
7.11
6.09
6.13
6.03
5.69
6.64
6.93
5.69
5.85
7.18
6.11
7.69
6.24
0.77
7.95
0.22
5.70
0.25
7.28
0.23
7.78
0.46
6.45
0.61
7.03
0.48
7.15
IN SLURRY
MIN MAX
7.10
4.17
4.70
5.56
5.35
5.1 1
4.56
2.97
5.75
6.40
5.04
4.99
6.45
4.85
5.94
4.03
0.06
5.62
0.16
0.54
0.11
4.31
0.15
6.15
0.24
5.46
0.22
5.24
0.33
5.95
10.
7.
6.
9.
7.
7.
6.
7.
7.
7.
6.
6.
7.
7.
8.
8.
3.
10.
0.
10.
0.
10.
0.
11.
0.
8.
1.
8.
0.
8.
30
73
52
43
56
98
99
53
50
76
25
71
73
26
29
54
11
00
31
08
57
46
27
11
89
44
23
82
62
35
WT X IN S
AVG MIN
15.2
15.3
14.8
15.0
15.1
14.7
15.0
15.0
14.7
15.0
15.3
15.3
14.1
1-5.0
16.4
15.4
7.7
14.9
5.9
14.6
5.9
14.9
5.1
14.9
7.4
14.4
14.5
14.6
15.2
15.0
14.4
13.8
13.9
14.1
14.3
14.2
13.4
7.9
13.0
13.7
14.6
13.9
12.9
13.5
14.9
13.7
3.9
10.3
3.7
10.9
4.6
11.3
2.4
12.0
5.9
10.9
7.4
13.2
14.1
13.0
;LURR>
MAX
17.3
16.3
15.6
16.4
16.0
15.4
16.6
17.4
16.2
15.8
16.3
16.7
15.3
16.3
18.7
17.5
8.8
22.6
10.0
16.8
8.0
17.8
7.1
17.0
10.0
16.7
17.6
15.8
16.0
16.4
-------
RUN SUMMARY
SOLIDS ANALYTICAL DATA (CONTINUED)
RUN
NO.
703-1A
704-1A
705-1 A
706-1A
707-1A
708-1 A
709-1 A
710-1A
711-1A
71 1-1B
712-1A
712-18
713-1A
714-1A
715-1A
716-1A
717-1A
718-1A
801-1A
802-1 A
803-1 A
804-1 A
805-1A
806-1 A
806-1 B
ANALY
TICAL
POINT
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1816
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
PERCENT
SULFITE
OXIDATION
AVG MIN MAX
17.5
17.0
8.2
18.1
10.2
16.2
11.6
10.7
11.7
14.8
12.1
8.4
17.2
14.9
13.1
20.6
24.7
87.6
14.6
94.9
17.4
95.8
17.6
96.5
15.1
97.9
11.6
98.6
9.3
97.6
9.2
5.7
1.8
13.2
2.5
8.4
6.4
0.2
3.5
6,0
6.5
0.1
9.4
5.5
6.5
3.9
14.3
22.1
2.0
78.8
6.1
91.7
7.4
86.0
4.1
90.1
4.3
96.8
0.3
95.8
34.2
38.8
16.2
21 .7
22.1
22.1
18.2
24.1
24.1
21 .5
18.1
19.3
25.6
21.4
18.7
80.0
42.1
98.8
83.0
100.0
32.7
98.2
34.8
100.0
24.5
99.9
32.2
100.0
19.9
99.3
STOICHIOMETHIC
RATIO
AVG MIN MAX
.05
.53
.22
.15
.34
.22
.33
.48
.30
.42
.59
.65
.13
.30
.40
1.33
1 .24
1 .10
i .19
1.23
1 .40
1.17
1 .41
1.14
1 .44
1.14
1.52
1.06
1.27
1.06
1 .00
1 . 13
1 .15
1 .02
1 .20
1 .05
1 .19
1 .06
1 .15
1.16
1 .28
1 .08
1 .07
1 .18
1 .35
1.11
1 .05
1 .00
1 .06
1 .01
1 .10
1 .05
1 .05
1 .01
1 .22
1 .03
1 .23
1 .02
1 .19
1 .01
1.13
1.86
1.36
1.31
1.52
1.38
1.62
1.73
1.49
1.62
1.77
2.70
1.32
1.49
1.42
3.19
1.41
1.66
1.40
1.85
1.84
1.50
1.72
1.31
1.88
1.37
1.95
1.07
1.40
1.13
PERCENT
IONIC
IMBALANCE
AVG MIN MAX
-5
1
-0
-4
-6
-6
-5
-1
-3
-0
-3
-3
0
-3
2
-0
2
3
4
1
2
-0
4
2
2
3
3
-1
3
-1
.3
.6
.1
.5
.9
.1
.2
.5
.6
. 1
.4
.3
.1
.7
.4
.8
.2
.2
. 1
.9
.0
.2
.0
.9
.7
.5
.0
.0
.1
.5
-8.5
-4.1
-7.6
-7.8
-8.4
-7.8
-8.5
-6.9
-8.3
-7. 1
-7.4
-8.2
-5.6
-8.1
-7,6
-6.5
-7.9
-7.6
-3.6
-7.9
-4.1
-7.3
-4.0
-6.7
-2.9
-2.3
-6.7
-4.3
-2.7
-5.6
1 .7
7.8
6.8
0.6
-3.4
-4.7
3.3
7.4
2.8
7.8
3.7
8.0
5.7
8.3
8.1
7.5
8.0
8.4
8.5
7.9
8.2
7.3
7.6
7.8
7.1
7.6
7.9
3.0
7.6
3.2
B-45
-------
RUN SUMMARY
SOLIDS ANALYTICAL DATA
CONCENTRATIONS IN SOLIDS, WT X
RUN
NO.
806-18
B06-1C
806-1 D
807-1 A
808-1 A
809-1 A
810-1A
811-1A
81 2-1 A
813-1A
814-1A
ANALY
TICAL
POINT
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
AVG
6.22
0.30
6.54
1.18
8.52
1.86
8.63
0.26
5.10
0.44
6.51
1.12
8.19
1 .04
9.51
5.54
17.96
5.59
14.27
4.13
15.16
C02
MIN
5.50
O.X>5
4.34
0.76
7.72
1.10
7.09
0.05
2.80
0.00
3.41
0.09
3.02
0.17
5.13
0.49
9.84
5.59
14.27
1.07
6.06
S02 S03 CAO
MAX AVG MIN MAX AVG MIN MAX AVG MIN MAX
6.86 32.98 24.13 36.19 8.49 4.21 20.31 43.07 41.42 44.15
0.53 0.51 0.01 1.27 21.44 15.37 27.81 16.01 11.63 20.25
9.65 32.09 29.46 35.76 8.55 4.07 12.41 43.09 41.62 45.12
1.87 6.57 3.07 11.37 16.32 13.76 20.05 19.13 15.16 22.00
9.94 31.88 27.14 35.47 6.58 2.79 11.20 44.16 41.83 45.66
2.91 22.93 21.29 25.29 5.33 2.20 10.75 26.50 24.21 27.96
11.14 33.74 31.82 36.90 2.26 0.31 4.42 42.29 40.94 44.08
0.52 0.40 0.17 0.72 25.62 14.92 30.49 19.29 11.46 23.83
7.05 32.77 26.60 38.36 6.50 2.19 13.34 39.73 37.04 41.88
1.04 0.68 0.18 1.44 39.63 25.24 50.00 28.49 20.71 33.97
9.35 28.34 23.88 "3.17 10.56 2.37 23.06 41.68 37.97 49.38
3.80 0.81 0.14 2.20 41.91 33.75 65.77 31.59 27.14 45.85
12.98 27.92 23.02 32.93 9.44 2.94 14.04 42.29 37.38 44.94
2.84 1.27 0.05 9.62 50.29 41.97 65.74 37.18 30.24 49.02
12.18 27.64 22.44 33.29 11.41 4.52 17.96 44.63 40.23 50.00
11.38 0.87 0.15 2.20 42.55 34.36 67.46 39.02 30.71 58.22
27.08 21.89 14.54 29.31 9.14 3.12 13.56 47.71 42.70 51.80
5.59 2-.02 2.02 2.02 37.83 37.83 37.83 36.88 36.88 36.88
14.27 24.40 24.40 24.40 12.06 12.06 12.06 46.90 46.90 46-90
8.93 0.53 0.00 1.80 40.31 34.58 51.93 33.30 28.37 39.58
24.42 23.56 18.09 28.61 11.05 4.83 24.82 46.69 42.25 57.99
WT %
AVG
0.66
6.35
0.25
3.70
0.43
4.85
0.55
5.47
0.49
0.47
0.08
0.53
0.14
0.68
0.18
0.60
0.07
0.31
0.11
IN SLURRY
MIN MAX
0.64
5.74
0.04
2.53
0.16
4.20
0.52
4.94
0.48
0,20
0.02
0.28
0.00
0.40
0.11
0.26
0.03
0.25
0.07
0.
6.
0.
4.
0.
5.
0.
6.
0.
0.
0.
0.
0.
1 .
0.
1 .
0.
0.
0.
68
95
45
87
69
43
59
00
50
73
13
98
26
86
40
01
10
37
16
WT X IN S
AVG MIN
14.5
14.7
14.2
14.4
15.9
14.6
17. 1
15. 1
15.5
14.8
7.9
14.9
8.4
14.7
8.0
16.3
6.9
13.9
6.3
14.6
8.2
13.9
14.0
13.3
13.6
15.4
12.9
16.0
14.3
14.5
•
12.9
7.3
12.2
6.5
12.4
6.9
14.6
5.6
13.9
6.3
12.4
6.1
•LURR1
MAX
15.5
15.9
15.0
16.3
16.5
15.8
17.8
15.9
16.2
16.1
8.4
17.5
14.6
16.3
9.1
19.5
10.1
13.9
6.3
15.9
9.2
-------
RUN SUMMARY
SOLIDS ANALYTICAL DATA (CONTINUED)
RUN
NO.
806- IB
806- 1C
806- 1D
807-1 A
808-1 A
809-1 A
810-1A
811-1A
81 2-1 A
81 3-1 A
814-1A
ANALY
TICAL
POINT
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
PERCENT
SULFITE
OXIDATION
AV6 WIN MAX
17.1
96.9
17.3
67.5
14.2
15.4
5.0
97.8
13.7
97.8
21.7
97.6
21.)
97.2
24.4
97.6
24.9
93.7
28.3
98.4
26.0
8.5
91.4
9.5
50.1
6.2
6.5
0.7
94.3
5.1
93.3
5.8
92.5
8.3
78.9
13.9
94.4
9.3
93.7
28.3
95.1
12.8
40.2
99.9
25.2
83.7
22.5
28.4
9.3
99.3
27.7
99.4
37.2
99.6
30.6
99.9
37.4
99.5
37.3
93.7
28.3
100.0
46.0
STOICHIOMETRIC
RATIO
AVG MIN MAX
1.23
1.03
1.25
1 .09
1.33
1.10
1.36
1.02
1 .20
1.02
1.27
1.05
1.35
1 .04
1.39
1.24
1.96
1.25
1.61
1.19
1.74
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
.20 1.
.00 1
.15 1
.05 1
.29 1
.06 1
.27 1
.00 1
.09 1
.00 1
.10 1
.00 1
.13 1
.01 1
.17 1
.02 1
.37 2
.25 1
.61 1
.05 1
.19 2
.25
.05
.41
.14
.40
.16
.49
.03
.30
.06
.50
.18
.67
.09
.66
.46
.70
.25
.61
.41
.39
PERCENT
IONIC
IMBALANCE
AVG MIN MAX
0.7
0.9
1.5
2.3
1.8
1.3
0.4
3.1
-1.5
2.9
0.1
1 .9
-1 .5
0.8
3.5
-1 .6
4.0
-2.3
-2.1
-2.1
-1 .3
-4.4
-1.9
-2.1
-1.1
-5.8
-4.4
-0.9
-2.0
-7.9
-2.8
-7.7
-7.7
-8.2
-7.1
-6.4
-8.4
4.0
-2.3
-8.0
-8.2
3.9
3.8
7.8
,5.0
5.8
6.5
5.4
8.4
2.3
6.1
8.4
7.2
8.2
4.5
6.9
8.4
5.5
4.0
-2.3
6.6
8.4
B-47
-------
RUN SUMMARY
SOLIDS ANALYTICAL DATA
CONCENTRATIONS IN SOLIDS, WT X
RUN
NO.
815-1A
816-1A
817-1A
818-1A
7 B19-1A
-pa
OO
819-1B
820-1 A
820-18
820-1C
821-1A
822-1A
822-1 B
ANALY
TICAL
POINT
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1851
1815
1816
1825
1851
1815
1825
1851
1815
1816
1825
1851
1815
AVG
8.29
16.46
4.36
13.13
2.61
12.45
3.18
12.98
3.41
13.12
2.90
12.78
1.19
11.59
1.87
11.36
4.46
11.92
2.47
3.28
13.92
1.11
C02
MIN
1 .33
6.01
1.40
4.51
1.48
9.66
1.67
5.94
O.B6
7.53
1.92
9.49
0.10
2.42
1.10
6.67
3.02
8.78
2.47
0.20
7.00
0.10
MAX
20.24
23.84
9.66
16.74
4.23
15.32
5.42
16.92
8.71
20.54
4.48
15.79
3.96
19.02
2.72
16.16
6.12
14.46
2.47
10.40
24.60
4.00
AVG
0.89
20.18
0.70
22.17
0.51
24.33
0.43
23.69
0.48
23.59
0.41
23.87
0.38
20.49
1.62
24.82
15.13
24.80
0.09
1.18
22.61
0.45
SO2
MIN
0.08
12.97
0.08
19.18
0.04
19.67
0.08
15.61
0.00
16.28
0.17
20.26
0.08
14.88
0.08
18.83
12.12
22.80
0.09
0.20
12.50
0.20
MAX
3.61
28.98
2.17
27.87
1.35
28.04
0.86
31.70
3.32
30.10
1.21
28.68
2.08
31.85
4.56
29.66
19.03
27.58
0.09
12.00
28.90
1.10
503 CAO
AVG MIN MAX AVG MIN MAX
33.80 20.17 43.53 35.21 30.00 41.19
8.18 0.22 16.78 44.95 39.43 50.29
38.87 33.79 43.25 33.41 30.53 36.51
10.06 6.57 17.02 43.42 39.02 45.62
22.49 11.00 29.12 19.56 10.84 23.99
7.82 3.52 14.05 42.77 40.99 45.75
26.71 21.12 31.15 23.34 20.03 26.68
7.52 3.95 11.53 42.73 38.85 45.75
26.34 13.15 36.37 23.39 16.45 28.87
7.70 1.95 15.18 43.36 39.81 46.31
25.16 18.43 29.73 22.26 17.69 25.07
6.89 4.71 11.41 42.55 40.96 44.32
25.26 19.51 30.35 19.88 13.65 26.86
10.76 3.82 19.15 39.29 35.11 44.77
23.68 17.96 28.41 20.14 15.43 24.13
6.47 2.33 10.30 40.56 38.90 42.11
10.45 7.85 13.40 25.23 22.38 28.86
7.73 3.69 10.52 41.57 39.84 42.53
14.99 14.99 14.99 13.36 13.36 13.36
21.00 6.90 29.33 19.28 10.40 27.30
7.65 3.38 17.70 41.59 39.60 45.90
22.19 18.45 26.28 16.67 12.70 19.90
WT X
AVG
0.61
0.18
0.57
0.19
6.67
0.56
4.88
0.49
4.55
0.49
4.99
0.50
5.60
0.51
5.75
0.60
5.70
0.73
9.28
6.42
0.53
6.23
IN SLURRY
MIN MAX
0.32
0.07
0.26
0.15
5.00
0.40
3.17
0.34
1 .92
0.15
2.89
0.37
3.22
0.04
4.36
0.50
4.53
0.64
9.23
4.80
0.50
4.30
1 .34
0.40
0.77
0.29
13.55
0.84
7.20
0.69
8.67
1 .01
8.01
0.73
9.77
0.65
7.89
0.70
6.98
0.80
9.28
8.40
0.70
8.90
WT X IN SLURRY
AVG MIN MAX
14.8
8.4
14.8
7.8
16.0
8.9
14.9
^.5
15.0
10.0
15.2
9.6
14.7
5.8
14.6
8.3
15.2
10.5
16.3
14.4
7.9
13.3
12.8
6.0
13.2
5.0
14.5
7.8
13.7
8.6
11 .8
7.1
13.5
8.5
11.4
2.2
11 .3
7.5
13.9
9.4
16.3
12.0
6.5
10.3
1 7.0
9.9
16.6
9.5
19.4
9.8
16.0
10.9
17.4
13.0
16.7
10.5
18.8
8.5
18.7
9.6
17.6
11.7
16.3
17.9
10.3
15.2
-------
RUN SUMMARY
SOLIDS ANALYTICAL DATA (CONTINUED)
RUN
NO.
815-1A
816-1A
81 7-1 A
818-1A
819-1A
819-18
820-1 A
820-1 B
820- 1C
821-tA
822-1 A
822-1 B
ANALY
TICAL
POINT
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1851
1815
1816
1825
1851
1815
1825
1851
1815
1816
1825
1851
1815
PERCENT
SULFITE
OXIDATION
AVG MIN MAX
96.7
24.5
97.8
26.4
96.7
20.4
98.1
20.7
97.7
20.7
98.0
16.8
98.1
29.7
92.3
17.3
35. 8
19.8
99.3
93.1
21.0
97.8
87.8
0.7
92.8
17.9
90.7
9. -8
96.5
10.1
85.9
6.2
93.5
13.9
88.2
11.9
79.1
6.4
27.8
10.2
99.3
31.5
11.6
93.8
99.7
42.0
99.8
37.7
99.8
34.8
99.7
35.8
100.0
40.6
99.2
31.1
99.6
50.7
99.5
26.0
46.9
26.1
99.3
99.0
38.7
98.8
STOICHIOMETRIC
RATIO
AVG MIN MAX
1 .49
1.98
1.21
1.65
1.23
1.60
1.22
1.65
1.24
1.66
1.21
1.64
1.08
1.63
1.13
1.57
1.28
1 .56
1.30
1.27
1.83
1.09
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
.06
.23
.06
.17
.09
.44
.11
.25
.05
.31
.12
.41
.01
.09
.07
.30
.19
.40
.30
.01
.29
.01
2.66
2.81
1.51
1.89
1.46
1.85
1.40
2.00
2.10
2.17
1.43
1.80
1.26
2.24
1.19
1.95
1.39
1.75
1.30
1.86
3.10
1.33
PERCENT
IONIC
IMBALANCE
AVG MIN MAX
0.4
1.3
-0.1
0.4
-0.1
0.2
0.7
0.3
0.7
1.3
2.5
1 .3
1.1
-2.5
-1.4.
-0.4
-4.0
-1 .8
-2.7
-3.5
-3.1
-4.3
-8.3
-7.6
-7.3
-6.5
-8.2
-8.5
-6.7
-6.9
-8.1
-7.2
.
-6.9
-5.7
-7.1
-8.3
-8.1
-8.1
-8.0
-8.5
-2.7
-8.0
-7.8
-8.3
6.7
6.4
5.9
7.0
7.8
7.8
7.1
7.0
7.8
7.2
8.1
7.2
8.2
5.8
8.3
7.2
3.1
7.0
-2.7
4.5
6.5
3.4
B-4?
-------
RUN SUMMARY
SOLIDS ANALYTICAL DATA
CONCENTRATIONS IN SOLIDS, NT X
RUN
NO.
822-1 B
823-1A
•
824-1A
825-1 A
826-1 A
CD
1
tn
0
851-1A
852-1A
853-1 A
854-1 A
855-1A
856-1 A
ANALY
TICAL
POINT
1816
1825
1851
1805
1816
1825
1851
1805
1816
1825
1851
1805
1816
1825
1851
1805
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
AVQ
12.46
13.67
15.29
9.58
10.74
6.44
6.71
8.52
8.06
0.24
3.65
0.57
3.28
0.46
3.76
0.31
4.11
0.30
3.95
0.29
4.39
C02
MIN
9.20
7.40
7.70
6.10
7.60
3.10
3.30
2.20
3.90
'0.11
3.14
0.11
2.86
0.15
2.93
0.05
3.47
0.04
1.82
0.00
3.77
S02 SO 3 CAO
MAX AVG MIN MAX AVG MIN MAX AVG MIN MAX
15.70 22.09 18.10 26.40 B.12 3.40 13.90 40.30 37.90 42.90
20.50 0.32 0.20 0.50 14.98 7.38 20.35 28.61 24.40 32.80
19.20 1.51 0.40 3.20 11.69 6.65 16.80 29.06 23.70 33.90
14.40 0.35 0.10 0.70 15.48 4.45 24.95 23.14 14.70 26.90
15.90 7.46 2.90 10.70 8.67 4.33 12.10 25.83 22.80 28.50
10.80 0.44 0.10 1.30 21.23 8.58 28.85 22.85 15.80 27.60
10.90 13.44 8.00 17.70 10.79 7.48 16.70 27.43 24.60 31.90
15.80 0.62 0.10 3.10 19.58 8.18 28.05 24.63 16.30 29.20
13.20 15.25 10.00 22.60 7.67 3.75 12.90 28.65 22.40 32.10
0.51 0.54 0.36 0.73 22.18 17.46 28.52 17.30 13.74 22.13
4.41 35.12 30. BZ 39.05 7.26 3.37 14.68 43.29 41.28 45.41
1.78 3.34 0.01 15.91 19.65 10.12 32.98 18.42 9.16 25.99
4.23 35.67 33.66 36.91 6.73 2.71 12.99 42.66 37.95 44.63
1.87 0.66 0.01 1.38 21.47 10.12 32.80 17.05 8.88 24.76
4.95 35.39 26.06 37.30 8.95 3.53 28.09 44.24 41.26 51.65
1.15 0.64 0.07 2.53 21.27 8.38 32.98 16.01 6.13 24.27
4.79 35.80 31.39 39.09 6.19 2.28 12.22 42.85 40.96 44.43
0.65 0.57 0.15 1.08 48.64 45.53 57.61 34.73 31.62 42.74
5.28 35.07 31.03 36.71 9.41 3.23 13.60 42.06 40.29 43.66
•
1.02 0.72 0.24 2.21 35.58 25.96 50.74 26.05 20.83 39.49
5.80 35.82 32.91 37.24 6.28 3.08 12.42 42.46 38.52 44.71
r*\* i L/
WT %
AVG
0.43
4.90
4.38
8.02
5.49
6.22
5.05
5.75
5.07
6.07
0.35
5.89
0.39
8.59
0.37
7.05
0.14
0.93
0.05
1.58
0.24
1 I"%J\J k.WUUU*7 |
IN SLURRY
MIN MAX
0.30
3.50
3.00
4.90
4.70
3.40
4.30
4.30
3.80
5.70
0.11
5.85
0.37
6.12
0.19
5.32
0.12
0.32
0.00
0.11
0.02
0.70
8.30
5.80
14.10
6.80
10.20
5.80
13.30
6.20
6.44
0.73
5.92
0.42
11 .63
0.93
8.76
0.19
1 .53
0.09
8.08
0.77
,?UL.& U,
WT % IN !
AVG MIN
5.6
15.4
13.3
19.7
14.1
16.3
14.7
16.2
15.2
15.2
5.9
15.6
9.1
15.4
6.2
15.1
6.1
14.7
7.2
15.3
7.8
4.
13.
10.
15.
12.
10.
13.
12.
12.
13.
5.
1 1 .
6.
12.
5.
12.
5.
12.
6.
12.
7.
6
4
6
4
9
1
3
1
8
9
6
5
4
9
2
4
3
3
7
5
1
> r
>LURR
MAX
7.6
18.1
15.6
21 .5
16.5
22.1
16.1
23.6
17.7
16.5
6.3
17.7
10.6
17.0
7.2
16.9
7.8
16.8
8.4
16.7
8.2
-------
RUN SUMMARY
SOLIDS ANALYTICAL DATA (CONTINUED)
RUN
NO.
822- 1B
823-1 A
824-1 A
825-1 A
826-1 A
B51-1A
852-1 A
853-1 A
854-1 A
855-1 A
856-1 A
ANALY
TICAL
POINT
1816
1825
1851
1805
1816
1825
1851
1805
1816
1825
1851
1805
1816
1825
1851
1805
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
PERCENT
SULFITE
OXIDATION
AVQ MIN MAX
22.5
97.2
86.1
96.2
48.6
97.3
39.4
96.0
28.8
97.0
14.1
84.8
12.9
96.2
16.3
96.2
12.0
98.5
17.6
97.5
12.2
10.8
92.2"
73.3
84.4
24.4
88.1
25.3
82.2
11.7
95.2
6.9
36.1
5.9
92.6
7.0
86.0
4.8
97.2
6.8
94.8
6.3
34.8
98.8
95.1
99.0
75.7
99.5
62.6
99.5
48.9
97.9
27.6
99.9
23.6
99.9
38.8
99.4
23.7
99.6
26.0
99.1
22.5
STOICHIOMETRIC
RATIO
AVG MIN MAX
1 .65
2.90
3.17
2.79
2.12
1 .63
1 .45
1 .93
1 .58
1 .02
1 .13
1 .04
1 .12
1 .05
1 .13
1 .03
1 .15
1 .01
1 .14
1.01
1 .16
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
.45
.65
.79
.44
.71
.20
.22
.18
.25
.01
.10
.02
.10
.01
.10
.00
.13
.00
.06
.00
.13
1 .91
5.66
4.39
6.57
2.94
3.13
1.79
4.27
2.23
1.03
1.17
1.10
1.16
1.19
1.19
1.09
1.18
1.02
1.18
1.05
1.20
PERCENT
IONIC
IMBALANCE
AVQ MIN MAX
-1 .6
1.5
0.3
-0.9
-1 .8
-2.5
-1.5
-2.0
-1 .3
5.8
6.5
5.4
6.0
5.1
5.1
0.6
4.5
-0.8
-0.7
0.6
2.5
-7.4
-3.4
-5.9
-6.9
-7.7
,•
-7.3
-8.0
-8.2
-8.5
3.9
3.3
1 .6
3.6
1 .1
-8.3
-7.2
-0.2
-5.2
-7.9
-5.2
-6.2
4.9
8.0
7.2
3.7
5.1
6.8
8.1
7.7
6.5
8.4
7.7
7.4
8.2
7.5
8.5
6.1
7.8
6.0
7.5
7.7
7.9
B-51
-------
RUN SUMMARY
SOLIDS ANALYTICAL DATA
CONCENTRATIONS IN SOLIDS, WT %
I
in
RUN
NO.
B57-1A
858-1 A
859-1 A
B59-1B
859- 1C
859-1D
860-1 A
861-U
862-1 A
863-1 A
864-1 A
ANALY
TICAL
POINT
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
185t
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
AVG
0.07
3.64
0.45
3.52
0.95
4.43
0.17
4.24
1.04
4.33
2.95
4.89
0.20
5.05
0.21
4.41
0.29
2.97
0.26
2.95
0.19
3.27
C02
MIN
0.00
2.81
0.00
3.02
0.35
3.13
0.00
3.47
0.36
3.57
2.25
3.96
0.00
4.67
0.00
3.14
0.00
2.37
0.05
1.19
0.05
2.69
S02 SO 3 CAO
MAX AVG MIN MAX AVG MIN MAX AVG MIN MAX
0.27 0.91 0.19 3.25 37.65 24.66 53.50 27.58 18.81 38.73
4.12 35.50 33.19 38.04 5.28 1.92 10.41 41.95 40.69 43.78
1.45 0.63 0.00 2.15 36.33 28.07 54.10 26.24 19.87 39.39
4.21 36.56 31.53 39.09 7.49 2.11 24.26 43.50 41.59 48.86
1.87 8.15 3.86 11.40 36.07 25.41 54.94 34.34 26.10 40.87
4.95 37.67 34.74 39.55 4.88 1.04 15.65 43.75 41.67 47.07
0.46 0.51 0.00 1.64 43.75 29.95 57.72 32.28 21.94 40.40
5.11 34.75 34.02 35.83 6.32 2.57 9.45 42.86 42.14 43.68
1.60 10.95 4.34 15.20 29.63 23.13 42.69 31.33 21.63 40.61
5.34 34.83 32.21 36.94 11.13 7.05 14.32 43.77 42.48 44.99
4.15 28.24 23.16 31.74 16.68 10.76 24.70 41.42 38.25 43.18
5.55 37.87 36.19 39.45 5.34 1.43 9.91 44.69 40.54 47.39
0.88 0.65 0.00 1.80 47.07 27.50 69.82 33.88 20.36 49.23
5.44 36.54 34.56 38.47 5.15 2.17 10.97 44.16 40.68 45.21
0.44 0.65 0.06 2.17 44.14 43.16 45.27 31.93 31.01 33.29
5.80 33.92 29.68 36.39 9.36 5.50 17.04 42.39 41.17 44.02
0.91 0.50 0.19 1.66 23.37 8.02 28.98 17.04 6.61 20.00
3.65 33.97 31.85 36.54 9.33 6.84 11.80 39.95 38.82 41.34
2.02 0.74 0.03 6.42 26.49 16.60 34.00 19.78 12.10 25.07
6.49 31.34 25.69 37.60 10.41 2.51 17.83 38.58 34.00 42.11
0.38 0.31 0.09 0.71 21.40 13.61 27.89 15.48 10.77 19.92
3.86 27.56 25.31 32.42 11.17 8.01 14.01 36.49 34.49 36.56
WT %
AVG
0.68
0.05
0.21
0.09
0.11
0.11
0.39
0.08
0.34
0.22
0.32
0.03
0.40
0.05
0.22
0.06
6.35
0.93
5.23
0.55
7.33
0.93
IN SLURRY
MIN MAX
0. 18
0.03
0.08
0.02
0.05
0.02
0.28
0.02
0.07
0.03
0.29
0.02
0.25
0.02
0.02
0.01
5.21
0.49
2.25
0.02
5.12
0.49
1.32
0.08
0.39
0.18
0.19
0.20
0.49
0.14
0.55
0.30
0.35
0.03
0.56
0.08
0.32
0.16
10.22
1 .52
8.21
0.84
9.38
1 .20
WT % IN S
AVG MIN
14
7
7
15
14
7
14
7
15
7
14
7
15
7
14
7
14
17
15
10
15
9
.8
.7
.7
.3
.1
.2
.6
.6
.2
.3
.2
.1
.5
.0
.3
.3
.9
.2
.3
.4
.9
.5
10.0
7.2
6.5
13.3
12.6
6.8
13.7
7.3
12.9
6.9
•
13.8
6.6
12.4
6.3
13.3
7.0
13.8
12.7
13.3
8.7
13.8
9.0
,LURR'
MAX
18.2
8.6
8.8
16.7
15.6
7.6
16.1
7.8
16.8
7.7
14.6
7.5
26.7
7.7
16.5
7.9
15.9
19.7
17.7
12.1
17.6
10.1
-------
RUN SUMMARY
SOLIDS ANALYTICAL DATA (CONTINUED)
RUN
NO.
857-1 A
858-1 A
859-1 A
859-1 B
8S9-1C
859-1 D
860-1 A
861-1 A.
862-1 A
863-1 A
864-1 A
ANALY
TICAL
POINT
1815
1816
1825
1851
1B15
1816
1825
1851
1815
1616
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1616
1825
1851
1815
1816
1825
1851
1815
1816
1825
PERCENT
SULFITE STOICHIOMETRIC
OXIDATION RATIO
AVG MIN MAX AVG MIN MAX
96.9
10.6
97.8
13.5
77.2
9.0
98.6
12.6
68.5
20.3
31.9
10.0
98.3
10.0
98.2
18.0
97.2
18.0
96.7
20.9
98.1
24.5
87.6
.4.0
91 .5
4.1
68.0
2.1
96.6
5.4
57.4
13.5
22.5
2.8
95.8
4.4
94.1
11.4
90.9
13.8
72.7
5.1
94.8
18.4
99.
20.
100.
35.
91 .
25.
100.
. 17.
81.
25.
46.
17.
100.
20.
99.
31.
99.
22.
99.
35.
- • -
99.
30.
3 1
1 1
0 1
7 1
9 1
8 1
0 1
7 1
1 1
4 1
0 1
4 1
0 1
2 1
8 1
5 1
1 1
9 1
8 1
7 1
-
6 1
1 1
.00
.13
.02
.12
.04
.16
.01
.16
.04
.15
.10
.17
.01
.18
.01
.16
.02
.11
.02
.11
.02
.13
1 .00
1 .10
1 .00
1 .09
1 .01
1 .11
1 .00
1 .12
1 .02
1 .13
1 .08
1 .14
1 .00
1 .16
1 .00
1 .11
1 .00
1 .09
1 .00
1 .04
1 .00
1 .10
1.02
1.16
1.07
1.14
1.08
1.18
1.02
1.19
1.07
1.17
1.14
1.19
1.02
1.20
1 .02
1.20
1.07
1.13
1.16
1.25
1.03
1.16
PERCENT
IONIC
IMBALANCE
AVG MIN MAX
1 .2
6.0
-1 .5
4.1
2.1
3.9
3.2
6.1
-0.7
-0.1
3.0
3.5
0.2
4.9
0.5
1.2
-0.8
-0.3
1 .2
0.2
-0.1
1.0
-6.5
2.1
-7.7
-6.1
-5.8
-3.2
-3.9
3.1
-7.0
-7.2
-4.3
0.0
-7.2
0.9
-5.0
-3.3
-7.5
-5.6
-8.4
-8.3
-5.7
-5.2
7.6
8.4
2.5
7.5
7.8
7.5
7.0
8.5
4.8
7.2
7.0
6.1
6.4
7.5
3.9
6.8
7.7
7.6
8.1
7.4
5.6
7.4
B-53
-------
RUN SUMMARY
SOLIDS ANALYTICAL DATA
CONCENTRATIONS IN SOLIDS, WT %
ACID INSOLUBLES,
SOLIDS,
RUN
NO.
864-1 A
865-1 A
866-1 A
867-1 A
ANALY
TICAL
POINT
1851
1815
1816
1825
1851
1815
1816
1825
1851
1815
1816
1825
1851
AVQ
0.30
2.59
0.34
3.39
0.19
3.05
C02
MIN
0.11
1.86
0.11
1.32
0.08
2.31
MAX
0.60
3.59
0.88
6.44
0.43
4.12
AVG
2.50
28.04
2.36
27.35
0.38
30.85
502
MIN
0.36
23.88
0.08
23.52
0.08
28.10
MAX
9.41
31 .85
10.04
31 .49
i .07
33.66
AVG
22.56
12.45
24.87
11.50
28.78
9.53
503
MIN
16.37
9.02
20.71
7.85
23.46
6.66
MAX
28.36
16.34
33.97
15.83
31 .85
12.25
AVG
18.69
36.47
19.95
36.45
21 .43
37.29
CAO
MIN
13.64
35.37
15.60
33.36
16.09
35.81
MAX
21 .96
38.03
24.62
38.28
23.95
39.59
WT %
AVG
5.92
0.88
4.93
0.77
4.31
0.75
IN SLURRY
MIN MAX
4.23
0.58
2.51
0.53
3.03
0.50
8.51
1 .64
7.03
1 .10
5.74
0.95
WT X IN S
AVG MIN
15.4
10.1
15.5
9.9
14.5
11 .7
13.7
8.6
14.2
8.7
12.9
7.9
iLURR'
MAX
17.2
12.2
16.9
11.1
15.6
14.6
-------
RUN SUMMARY
SOLIDS ANALYTICAL DATA (CONTINUED)
RUN
NO.
ANALY
TICAL
POINT
PERCENT
SULFITE
OXIDATION
AVG WIN
STOICHIOMETRIC
RATIO
MAX AVG WIN MAX
PERCENT
IONIC
IMBALANCE
AVG MIN MAX
864-1A 1851
865-1A 1815
1816
1825
1851
866-1A 1815
1816
1825
1851
867-1A 1815
1816
1825
1851
87.8
26.3
90.4
25.2
98.4
19.8
59.9
18.5
62.9
16.7
96 .-0
14.1
98.4 1.02 1
35.0 1.10 1
01 1
07 1
04
14
99.5 1.02 1.01 1.05
32.1 1.14 1.05 1.28
99.7 1.01 1
25.9 1.121
01
09
1 .03
1 .17
1.7 -6.1
-0.3 -4.0
0.2 -7.6
0.3 -7.3
3.0 -4.4
-0.8 -6.7
6.6
4.4
6.3
5.8
7.6
3.5
B-55
-------
TCA RUN DEFINITION
CD
RUN
NO.
TFG-2A
TFG-2B
TFG-2C'
TFG-2D
TFG-2E
TFG-2F
525-2A
526-2A
527-2A
528-2A
529-2A
530-2A
531-2A
532-2A
533-2A
534-2A
535-2A
535-28
536-2A
537-2A
538-2A
539-2A
540-2A
541-2A
542-2A
543-2A
544-2A
545-2A
546-2A
547-2A
548-2A
549-2A
550-2A
551-2A
552-2A
553-2A
554-2A
555-2A
556-2A
557-2A
558-2A
559-2A
560-2A
561-2A
RUN
REP
FLAG
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
START
DATE
02/28/77
02/04/77
02/1 0/77
02/15/77
02/1 9/77
02/23/77
10/24/73
11/21/73
01/1 8/74
02/06/74
02/26/74
03/28/74
05/1 0/74
07/1 7/74
08/06/74
09/03/74
09/1 2/74
12/04/74
12/31/74
01/1 5/75
01/24/75
03/07/75
03/2 1/75
03/25/75
03/28/75
04/01/75
04/04/75
04/15/75
06/03/75
06/18/75
06/23/75
06/27/75
07/02/75
07/08/75
07/1 0/75
07/19/75
07/25/75
07/29/75
08/01/75
08/05/75
03/15/75
09/05/75
09/23/75
09/30/75
START
TIME
1330
0530
1310
1730
1505
1515
1600
1800
1800
2300
1300
1 100
1000
1600
1700
1400
1700
1 100
2000
1600
1600
1700
1700
1500
1400
0900
1 100
1100
2300
1500
2000
1600
1600
1500
1700
1600
1900
1600
1400
1700
1400
1400
1000
1700
END
DATE
03/03/77
02/10/77
02/14/77
02/19/77
02/23/77
02/28/77
11/15/73
01/10/74
01/24/74
02/26/74
03/07/74
04/17/74
06/26/74
07/29/74
08/21/74
09/08/74
12/04/74
12/30/74
01/15/75
01/21/75
02/21/75
03/21/75
03/25/75
03/28/75
04/01 /75
04/03/75
04/15/75
04/21 /75
06/17/75
06/23/75
06/27/75
07/02/75
07/08/75
07/10/75
07/14/75
07/21/75
07/28/75
08/01/75
08/05/75
08/13/75
09/02/75
09/22/75
09/29/75
10/06/75
END
TIME
1807
0530
1025
1505
1515
0750
0500
0800
0700
0800
1000
1200
0700
'0800
1 100
2100
1100
0700
0800
0900
0500
1300
1200
0900
0900
0800
0800
0700
0700
0700
0700
0700
0700
0500
0700
1000
0700
0700
0700
0600
0700
0500
0700
0700
HOURS
ON
STRM
76
128
93
93
96
112
517
1 190
133
425
213
476
1088
258
332
100
1835
490
328
137
562
278
90
65
91
47
269
133
207
112
71
112
119
39
86
42
60
63
89
181
398
384
142
135
FACT
OR
TIME
T
T
T
T.
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
RUN COMMENTS
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
STEADY STATE NOT ACHIEVED
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
AIR PURPOSELY INTRODUCED INTO SYSTEM TO DETERMINE EFFECT ON OXIDATION
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
-------
TCA RUN DEFINITION
CO
RUN
NO.
562-2A
562-28
563-2A
564-2A
565-2A
566-2A
567-2A
568-2A
569-2A
569-28
570-2A
571-2A
571-2B
572-2A
573-2A
575-2A
576-2A
576-2B
577-2A
578-2A
579-2A
580-2A
581-2A
582-2A
583-2A
583-2B
5S4-2A
585-2A
586-2A
587-2A
588-2A
589-2A
590-2A
590-2B
591-2A
592-2A
593-2A
594-2A
601-2A
602-2A
603-2A
604-2A
605-2A
606-2A
RUN
REP
FLAG
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
7
N/A
7
N/A
N/A
N/A
N/A
N/A
N/A
START
DATE
10/06/75
10/30/75
11/06/75
11/14/75
11/21/75
11/26/75
12/03/75
12/09/75
12/16/75
12/19/75
12/23/75
12/29/75
01/02/76
01/02/76
01/09/76
01/15/76
01/17/76
01/22/76
01/22/76
01/29/76
01/29/76
02/01/76
02/04/76
02/1 1/76
04/15/76
04/21/76
05/03/76
05/14/76
05/20/76
05/31/76
06/16/76
06/21/76
01/24/78
02/02/78
03/27/78
04/05/78
04/21/78
05/02/78
07/01/76
07/12/76
07/19/76
07/28/76
08/05/76
08/13/76
START
TIME
1500
1500
1300
1500
1900
1400
1400
1400
1500
1300
1000
1100
1100
2200
0800
1400
1300
0400
1700
1300
2200
1200
1700
1400
1745
1545
2145
1 145
1300
1445
0945
1515
1347
1255
1345
1220
1135
1710
2045
1630
2330
1600
2115
1245
END
DATE
10/30/75
11/06/75
11/14/75
11/19/75
11/26/75
12/03/75
12/09/75
12/16/75
12/19/75
12/23/75
12/29/75
01/02/76
01/02/76
01/09/76
01/11/76
01/17/76
01/22/76
01/22/76
01/29/76
01/29/76
02/01/76
02/01/76
02/11/76
02/12/76
04/21/76
05/01/76
05/14/76
05/20/76
05/25/76
06/14/76
06/21/76
07/01/76
01/26/78
02/06/78
04/05/78
04/21/78
05/02/78
05/06/78
07/12/76
07/18/76
07/26/76
08/04/76
08/13/76
08/18/76
END
TIME
0700
0700
0700
0700
0700
1100
0700
0700
0800
0800
0900
10CO
2100
0800
0400
1200
0400
0600
0700
2100
1200
2300
1400
0700
0500
1100
0800
0745
0500
0530
01 15
0515
1010
0900
1220
0730
0825
1955
0545
1210
2035
0533
1235
1416
HOURS
ON
STRM
495
134
182
113
109
166
138
162
66
97
144
96
11
154
45
47
112
3
159
9
62
12
164
18
131
230
236
140
110
295
107
200
45
92
207
293
260
99
177
137
165
158
170
122
FACT
OR
TIME
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
RUN COMMENTS
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
THIS IS AN ABSORBENT
N/A
N/A
N/A
N/A
THIS IS AN ABSORBENT
N/A
THIS IS AN ABSORBENT
N/A
THIS IS AN ABSORBENT
N/A
THIS IS AN ABSORBENT
SUSPECTED AIR LEAK V]
SUSPECTED AIR LEAK V]
N/A
SUSPECTED AIR LEAK VI
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
SUSPECTED AIR LEAK VI
N/A
SUSPECTED AIR LEAK VI
DEPLETION RUN
DEPLETION RUN
DEPLETION RUN
DEPLETION RUN
DEPLETION RUN
iA DOWNCOMER INTO
:A DOWNCOMER INTO
:A DOWNCOMER INTO
A DOWNCOMER INTO
A DOWNCOMER INTO
D-204 EHT CAUSED HIGH OXIDATION
D-204 EHT CAUSED HIGH OXIDATION
D-204 EHT CAUSED HIGH OXIDATION
D-204 EHT CAUSED HIGH OXIDATION
D-204 EHT CAUSED HIGH OXIDATION
-------
TCA RUN DEFINITION
RUN
NO.
607-2A
608-2A
608-2B
609-2A
610-2A
61 1-2A
61 2-2A
613-2A
614-2A
615-2A
616-2A
617-2A
618-2A
618-2B
619-2A
620-2A
621-2A
622-2A
622-28
623-2A
co 624-2A
i 625-2A
g 701-2A
702-2A
703-2A
704-2A
705-2A
706-2A
707-2A
708-2A
709-2A
710-2A
711-2A
712-2A
713-2A
714-2A
714-2B
715-2A
716-2A
717-2A
718-2A
719-2A
801-2A
801-28
RUN
REP
FLAG
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
7
N/A
7
7
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
START
DATE
08/19/76
09/03/76
09/06/76
09/1 3/76
09/24/76
10/07/76
10/1 2/76
10/1 8/76
10/22/76
10/28/76
1 1/05/76
11/15/76
02/06/78
02/13/78
02/17/78
03/02/78
03/17/78
05/08/78
05/12/78
05/1 9/78
06/08/78
1 1/1 0/78
11/24/76
12/06/76
12/13/76
12/21/76
01/04/77
01/1 4/77
03/04/77
03/09/77
03/15/77
03/17/77
03/24//7
03/28/77
06/15/77
08/30/77
09/07/77
10/07/77
10/14/77
10/20/77
11/24/77
12/01/77
06/24/77
06/28/77
START
TIME
1427 ,
1235
2250
1045
1 100
1600
1433
1604
1356
1300
0800
1705
0900
1240
1400
1200
0935
1830
1400
1600
1235
1510
1900
1500
1610
2030
1210
1 3SO
1350
1450
0000
1405
1349
1550
1305
1200
2000
1439
1300
1408
1200
1705
1 145
1715
END
DATE
09/02/76
09/06/76
09/13/76
09/24/76
10/07/76
10/12/76
10/18/76
10/21 /76
10/28/76
11/03/76
11/13/76
1 1/22/76
02/13/78
02/17/78
03/02/78
03/06/78
03/27/78
05/12/78
05/19/78
05/31/78
06/19/78
01/25/79
12/06/76
12/13/76
12/20/76
01/04/77
01/14/77
01/04/77
03/09/77
03/14/77
03/17/77
03/24/77
03/28/77
04/02/77
06/24/77
09/07/77
09/09/77
10/14/77
10/20/77
11/21/77
11/30/77
12/09/77
06/28/77
06/30/77
END
TIME
1645
2250
0715
0300
1350
0500
0905
1110
0845
1213
1000
0825
1240
0735
0815
2145
0810
1400
1600
0520
1735
0855
0800
1300
1050
0830
0812
0530
0730
2400
0737
0744
1135
1300
1145
2020
0800
0735
0325
0820
0625
0755
1715
1600
HOURS
ON
STRM
212
84
151
259
280
111
138
67
139
1 10
174
158
162
88
306
106
239
91
125
271
269
1652
277
162
162
324
236
339
113
128
56
162
93
117
202
201
36
161
135
747
143
res
102
47
FACT
OR
TIME
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
RUN COMMENTS
SUSPECTED AIR
SUSPECTED AIR
N/A
N/A
N/A
SUSPECTED AIR
SUSPECTED AIR
SUSPECTED AIR
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
LEAK VIA DOWNCOMER INTO D-204 EHT CAUSED HIGH OXIDATION
LEAK VIA DOWNCOMER INTO D-204 EHT CAUSED HIGH OXIDATION
LEAK VIA DOWNCOMER INTO D-204 EHT CAUSED HIGH OXIDATION
LEAK VIA DOWNCOMER INTO D-204 EHT CAUSED HIGH OXIDATION
LEAK VIA DOWNCOMER INTO D-204 EHT CAUSED HIGH OXIDATION
-------
TCA RUN DEFINITION
RUN
NO.
802-2A
803-2A
804-2A
805-2A
806-2A
807-2A
808-2A
809-2A
810-2A
811-2A
DO 812-2A
i, 813-2A
Co 814-2A
815-2A
816-2A
817-2A
818-2A
818-2B
819-2A
820-2A
821-2A
RUN
REP
FLAG
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
START
DATE
07/01/77
07/08/77
07/15/77
07/22/77
07/28/77
OB/02/77
08/10/77
08/17/77
OB/24/77
09/09/77
09/16/77
09/23/77
09/29/77
12/09/77
12/14/77
12/16/77
12/23/77
12/30/77
01/06/78
01/13/78
05/31/78
START
TIME
1308
1401
1042
1250
1305
1505
1 140
1525
1410
1157
1010
2205
1000
0950
1315
1430
0740
1210
1401
1200
1655
END
DATE
07/07/77
07/15/77
07/22/77
07/28/77
08/02/77
08/10/77
08/17/77
08/23/77
OB/29/77
09/16/77
09/22/77
09/29/77
10/04/77
12/14/77
12/16/77
12/23/77
12/30/77
01/05/78
01/13/78
01/24/78
06/08/78
END
TIME
1135
1042
0820
0820
0800
0810
0510
2050
2355
0738
0735
0735
0910
1115
1430
0740
1210
0740
1200
0805
0735
HOURS
ON
. STRM
142
165
166
140
115
185
162
149
130
164
141
130
119
75
48
161
131
140
164
259
182
FACT
OR
TIME
T
T
T
T.
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
T
RUN COMMENTS
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
SOLIDS SAMPLES ARE BEING RUN BY WET METHOD BEGINNING 0730 ON 9-16-77
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
-------
TCA SYSTEM CONFIGURATION
RUN
NO.
TFG-2A
TFG-2B
TFG-2C
TFG-2D
TFG-2E
TFG-2F
525-2A
526-2A
527-2A
528-2A
529-2A
530-2A
531-2A
532-2A
533-2A
534-2A
535-2A
535-28
536-2A
537-2A
538-2A
539-2A
540-2A
541-2A
542-2A
543-2A
544-2A
545-2A
546-2A
547-2A
548-2A
549-2A
550-2A
551-2A
552-2A
553-2A
554-2A
555-2A
556-2A
557-2A
558-2A
559-2A
560-2A
561 -2A
TCA
NO.
BEDS
3
3
3
3
3
3
3
3
2
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
TCA
TOT
BED
HGT
15.0
15.0
15.0
15.0
15.0
15.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
TCA
SPHERE
TYPE
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
H/T
HOPE
HOPE
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
HOPE
HOPE
HOPE
HOPE
HOPE
HOPE
HOPE
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
NO. OF
HOLD
TANKS
1
3
3
3
3
3
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
M: E.
SYSTEM
CONFIG
1-3P/OV
1 -3P/OV
1-3P/OV
1 -3P/OV
1-3P/OV
1 -3P/OV
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
KT-6P/C
2-3P/CV
2-3P/CV
2-3P/CV
2-3P/CV
2-3P/CV
2-3P/CV
2-3P/CV
1-3P/OV
1-3P/OV
T-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
M.E.
WASH
B/T
I/I
I/I
C/I
C/I
C/I
C/I
NONE
NONE
NONE
NONE
NONE
NONE
NONE
c/
c/
c/
c/
c/
c/
c/
c/
c/
c/
c/
c/
c/
c/
c/
I/I
I/I
C/I
C/I
C/I
C/I
C/I
I/I
I/I
C/I
C/I
C/I
C/I
C/I
C/I
C/I
DE-
WATER
SYSTEM
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL/F
CL/F
CL/F
CL/F
CL/F
CL
CL/F
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
OXID
CONFIG
FLAG
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
ALK
ADDN
PT.
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
RUN
NO.
TFG-2A
TFG-2B
TFG-2C
TFG-2D
TFG-2E
TFG-2F
525-2A
526-2A
527-2A
528-2A
529-2A
530-2A
531-2A
532-2A
533-2A
534-2A
535-2A
535-28
536-2A
537-2A
538-2A
539-2A
540-2A
541-2A
542-2A
543-2A
544-2A
545-2A
546-2A
547-2A
548-2A
549-2A
550-2A
551-2A
552-2A
553-2A
554-2A
555-2A
556-2A
557-2A
558-2A
559-2A
560-2A
561 -2A
B-60
-------
TCA SYSTEM CONFIGURATION
TCA
RUN NO.
NO. BEOS
562-2A
562-28
563-2A
564-2A
565-2A
566-2A
567-2A
568-2A
569-2A
569-2B
570-2A
571-2A
571-28
572-2A
573-2A
575-2A
576-2A
576-28
577-2A
57S-2A
579-2A
580-2A
58 1-2 A
582-2A
583-2A
583-2B
584-2A
585-2A
586-2A
587-2A
588-2A
589-2A
590-2A
590-2B
591-2A
592-2A
593-2A
594-2A
601-2A
602-2A
603-2A
604-2A
605-2A
606-2A
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
TCA
TOT
BED
HGT
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
17.0
17.0
17.0
17.0
24.0
24.0
15.0
14.5
14.0
13.5
0.0
13.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
14.5
14.5
14.5
14.0
14.0
14.0
TCA NO. OF M.E.
SPHERE HOLD SYSTEM
TYPE TANKS CONFIG
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
N/A
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
1 1-3P/OV
1 1-3P/OV
1 1-3P/OV
1
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
1
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
1
1 1-3P/OV
1 1-3P/OV
1 1 -3P/OV
1 1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
M.E.
WASH
B/T
C/I
C/I
C/I
C/I
C/I
C/I
C/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/
I/
I/
I/
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
i/s
I/S
i/s
i/s
I/I
I/I
I/I
I/I
I/I
I/I
DE- OXID
WATER CONFIG
SYSTEM FLAG
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL/CE
CL
CL
CL/CE
CE
CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
ALK
A DON
PT.
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
-
EHT
EHT
EHT
EHT
-
EHT
-
EHT
-
EHT
-
EHT
EHT
ONC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
EHT
EHT
EHT
EHT
DNC
DNC
EHT
DNC
DNC
DNC
RUN
NO.
562-2A
562-28
563-2A
564-2A
565-2A
566-2A
567-2A
568-2A
569-2A
569-28
570-2A
571 -2A
571-28
572-2A
573-2A
575-2A
576-2A
576-28
577-2A
578-2A
579-2A
580-2A
581-2A
582-2A
583-2A
583-28
584-2A
585-2A
586-2A
587-2A
588-2A
589-2A
590-2A
590-28
591 -2A
592-2A
593-2A
594-2A
601-2A
602-2A
603-2A
604-2A
605-2A
606-2A
B-61
-------
TCA SYSTEM CONFIGURATION
RUN
NO.
607-2A
608-2A
608-28
609-2A
610-2A
611-2A
612-2A
613-2A
614-2A
615-2A
616-2A
617-2A
618-2A
618-2B
619-2A
620-2A
621-2A
622-2A
622-28
623-2A
624-2A
625-2A
701-2A
702-2A
703-2A
704-2A
705-2A
706-2A
707-2A
708-2A
709-2A
710-2A
711-2A
712-2A
713-2A
714-2A
714-2D
715-2A
716-2A
717-2A
718-2A
7 19-2 A
801-2A
801-28
TCA
NO.
BEDS
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
N/A
N/A
3
3
TCA
TOT
BED
HGT
13.5
13.5
13.5
13.5
13.0
12.5
2.5
2.0
2.0
1.5
1 .0
5.0
5.0
5.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
14.0
15.0
14.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
21 .0
30.0
22.5
N/A
N/A
15.0
15.0
TCA NO. OF
SPHERE HOLD
TYPE TANKS
FOAM 1
FOAM 1
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM N/J
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
N/A
N/A
FOAM
FOAM
: M . E .
SYSTEM
5 CONFIG
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
1 -3P/OV
1 -3P/OV
1-3P/OV
1-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
1 -3P/OV
\ -3P/OV
1 -3P/OV
1 -3P/OV
1
3
3
3
1 1-3P/OV
1 1-3P/OV
1 1-3P/OV
1 -3P/OV
1 -3P/OV
3 -3P/OV
1 -3P/OV
1 -3P/OV
1 1-3P/OV
3 1-3P/OV
3 1-3P/OV
3 1-3P/OV
1 1-3P/OV
1 1-3P/OV
1 1-3P/OV
1 1 -3P/OV
M.E.
WASH
B/T
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/S
i/s
I/S
I/S
i/s
I/S
I/S
I/S
I/I
I/I
I/I
I/I
I/I
I/I
I/I
I/I
C/I
C/I
c/s
C/I
C/I
C/I
C/I
I/I
C/I
C/I
DE-
WATER
SYSTEM
CL/CE
CL/CE
CL/CE
CL/CE
CL/F
CL/F
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL/CE
CL
CL/CE
CL/CE
CE
CL/CE
CL/CE
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
LAM
CL
CL
CL
CL
CL
CL
CL
OXID
CONFIG
FLAG
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
2
N/A
ALK
ADDN
PT.
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
DNC
EHT
DNC
DNC
DNC
DNC
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
RUN
NO.
607-2A
608-2A
608-28
609-2A
610-2A
61 1-2A
612-2A
613-2A
614-2A
615-2A
616-2A
617-2A
618-2A
618-28
619-2A
620-2A
621-2A
622-2A
622-28
623-2A
624-2A
625-2A
701-2A
702-2A
703-2A
704-2A
705-2A
706-2A
707-2A
708-2A
709-2A
710-2A
711-2A
712-2A
713-2A
714-2A
714-28
715-2A
716-2A
717-2A
718-2A
719-2A
801-2A
801-2B
B-62
-------
TCA SYSTEM CONFIGURATION
TCA
RUN NO.
NO. BEOS
802-2A
803-2A
804-2A
805-2A
806-2A
807-2A
808-2A'
809-2A
810-2A
811-2A
812-2A
813-2A
814-2A
815-2A
8 16-2 A
817-2A
818-2A
818-2B
819-2A
820-2A
821-2A
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
TCA
TOT
BED
HGT
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
22.0
22.0
22.0
22.0
22.0
22.0
15.0
TCA NO. OF M;E.
SPHERE HOLD SYSTEM
TYPE TANKS CONFIG
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
1 1-3P/OV
1
1
^
1
1
2
2
2
2
2
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
-3P/OV
1 1-3P/OV
1 1-3P/OV
1-3P/OV
1-3P/OV
1-3P/OV
1 -3P/OV
1 -3P/OV
1-3P/OV
1 1-3P/OV
1 1-3P/OV
M.E.
WASH
B/T
C/I
C/I
C/I
C/I
C/I
C/I
C/I
C/I
C/I
C/I
C/I
C/I
C/I
C/I
C/I
C/I
C/I
C/I
C/I
C/I
i/s
DE- OXID
WATER CONFIG
SYSTEM FLAG
CL
CL
CL
CL
CL
CL
CL
CL/F
CL/F
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL/CE
N/A
N/A
N/A
N/A
N/A
3
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
4
ALK
ADDN
PT.
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
N/A
N/A
EHT
RUN
NO.
802-2A
803-2A
804-2A
805-2A
806-2A
807-2A
808-2A
809-2A
810-2A
811-2A
812-2A
813-2A
814-2A
815-2A
816-2A
817-2A
818-2A
818-2B
819-2A
820-2A
821-2A
B-63
-------
TCA OPERATING CONDITIONS
ro
I
en
RUN
NO.
TFG-2A
TFG-2B
TFG-2C
TFG-2D
TFG-2E
TFG-2F
525-2A
526-2A
527-2A
523-2A
529-2A
530-2A
531-2A
532-2A
533-2A
534-2A
535-2A
535-2B
536-2A
537-2A
538-2A
539-2A
540-2A
541-2A
542-2A
543-2A
544-2A
545-2A
546-2A
547-2A
548-2A
549-2A
550-2A
551-2A
552-2A
553-2A
554-2A
555-2A
55S-2A
557-2A
558-2A
559-2A
560-2A
561-2A
ALK
TYPE
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
FLY
ASH
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
MGO
Y
N
N
N
N
N
N
N
N
N
N
N
Y
Y
Y
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
PH
CONTR
POINT
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
5.80
5.80
5.80
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
5.40
5.40
N/A
5.40
5.40
5.50
5.50
5.50
5.50
5.50
5.50
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
GAS
RATE
ACFM
30000
30000
30000
20000
30000
30000
25000
20500
20500
20500
2C.SOO
20500
20500
20500
20500
20500
20500
20500
24000
24000
24000
28800
28800
28800
28800
28800
20500
28800
30COO
30000
30000
30000
30000
30000
30000
30000
22500
22500
22500
30000
30000
30000
30000
30000
GAS
VEL
FPS
12.5
12.5
12.5
8.4
12.5
12.5
10.4
8.6
8.6
8.6
8.6
8.6
8.6
8.6
8.6
8.6
8.6
8.6
0.0
0.0
0.0
2.0
2.0
2.0
12.0
12.0
8.6
12.0
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
9.4
9.4
9.4
12.5
12.5
12.5
12.5
12.5
TCA
LIQ
RATE
GPM
1200
1200
1200
12
600
1200
1200
1200
1200
1200
1200
1200
1200
1700
1200
1200
1200
1200
1200
1400
1400
1000
1000
1000
1000
1000
1200
1000
1000
1000
1000
1000
1000
1000
1200
1200
1200
1200
1200
1200
1200
1200
1200
1200
TCA
L/G
GAL/
MACF
49.8
49.8
49.8
0.7
24.9
49.8
59.8
72.9
72.9
72.9
72.9
72.9
72.9
103.3
72.9
72.9
72.9
72.9
62.3
72.7
72.7
43.3
43.3
43.3
43.3
43.3
72.9
43.3
41.5
41.5
41.5
41.5
41.5
41.5
49.8
49.8
66. S
66.5
66.5
49.8
49.8
49.8
49.8
49.8
SOLID
RECIRC
NOW X
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
8.0
8.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
1 5.0
13.0
15.0
15.0
15.0
15.0
15.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
15.0
15.0
15.0
SOLIDS
DISCH
RANGE
%
50-55
30-39
32-42
35-42
37-43
34-42
31-42
35-47
34-39
25-33
30-47
30-43
35-42
32-43
29-38
30-40
34-42
34-42
32-43
33-40
31-40
40
40
40
40
40
35-40
35-40
35-44
35-43
22
30
37-41
39-41
38-41
32-37
36-40
25
31-45
39-44
34-42
36-42
36-41
37-44
TCA
D.P.
IN.
H20
6.6
9.2
8.6
4.8
4.9
6.8
6.0
4.5
4.7
5.1
5.1
4.9
5.4
4.6
4.7
4.3
4.3
4.4
5.4
6.1
6.3
6.8
6.4
6.5
6.9
6.7
5.3
5.3
8.6
7.4
7.0
6.4
6.4
6.6
7.7
8.6
5.2
5.2
5.0
7.4
7.5
7.6
7.6
7.4
M.E. SYSTEM
D.P. RANGE
IN.H20
0.44-0.50
0.56-0.60
0.49-0.60
0. 17-0.24
0.49-0.56
0.43-0.49
N/A
0.15-0.26
0.30-1 .00
0. 16-0.20
0. 19-0.23
0. 17-0.25
0.19-0.35
0. 15-0.19
0.17-0.25
0. 15-0.20
0. 10-0.20
0.15-0.20
0.30-0.40
0.40-0.55
0. 15-0.25
0.33-0.50
0.50-0.53
0.50-0.65
0.48-0.50
0.50-0.53
0. 15-0.20
0.40-0.45
0.65-0.80
0.65-1 .10
0.58-Q.65
0.58-0.65
0.66-0.83
0.66-0.80
0.6B-0.75
0.31-0.36
0. 18-0.40
0. 18-0.23
0.16-0.23
0.36-0.44
0.37-0.43
0.38-0.43
0.38-0.42
0.35-0.40
RUN
NO.
TFG-2A
TFG-2B
TFG-2C
TFG-2D
TFG-2E
TFG-2F
525-2A
52G-2A
527-2A
528-2A
529-2A
530-2A
531-2A
532-2A
533-2A
534-2A
535-2A
535-2B
536-2A
537-2A
538-2A
539-2A
540-2A
541-2A
542-2A
543-2A
544-2A
545-2A
546-2A
547-2A
548-2A
549-2A
550-2A
551-2A
552-2A
553-2A
554-2A
555-2A
556-2A
557-2A
558-2A
559-2A
560-2A
561 -2A
-------
TCA OPERATING CONDITIONS (CONTINUED)
RUN
NO.
TFG-2A
TFG-2B
TFG-2C
TFG-2D
TFG-2E
TFG-2F
525-2A
526-2A
527-2A
528-2A
529-2A
530-2A
531-2A
532-2A
533-2A
534-2A
535-2A
535-28
536-2A
537-2A
53S-2A
539-2A
540-2A
541-2A
542-2A
543-2A
544-2A
545-2A
546-2A
547-2A
548-2A
549-2A
550-2A
551 -2A
552-2A
553-2A
554-2A
555-2A
556-2A
557-2A
558-2A
559-2A
560-2A
561-2A
EFFLU TCA LOW PH
RES TANK RES
TIME TIME
WIN WIN.
12.0
12.0
12.0
12.0
24.0
12.0
10.0
10.0
10.0
12.0
12.0
12.0
12.0
12.0
12.0
12.0
15.0
15.0
20.0
20.0
20.0
25.0
15.0
15.0
15.0
15.0
17.0
25.0
15.0
15.0
15.0
15.0
15.0
15.0
15. JO
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
OXID EDUCTOR BLEED BLEED
AIR CIRCUL TO OX OXID H2S04
RATE RATE TANK TANK RATE
SCFM GPM GPM PH GPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
RUN
NO.
TFG-2A
TFG-2B
TFG-2C
TFG-2D
TFG-2E
TFG-2F
525-2A
526-2A
527-2A
528-2A
529-2A
530-2A
531-2A
532-2A
533-2A
534-2A
535-2A
535-2B
536-2A
537-2A
538-2A
539-2A
540-2A
541-2A
542-2A
543-2A
544-2A
545-2A
546-2A
547-2A
548-2A
549-2A
550-2A
551-2A
552-2A
553-2A
554-2A
555-2A
556-2A
557-2A
558-2A
559-2A
560-2A
561-2A
B-65
-------
TCA OPERATING CONDITIONS
CO
i
cr>
cr>
RUN
NO.
562-2A
562-2B
563-2A
564-2A
565-2A
566-2A
567-2A
568-2A
569-2A
569-2B
570-2A
571-2A
571-2B
572-2A
573-2A
575-2A
576-2A
576-2B
577-2A
578-2A
579-2A
580-2A
581-2A
582-2A
583-2A
583-28
584-2A
585-2A
586-2A
587-2A
588-2A
589-2A
590-2A
590-28
591-2A
592-2A
593-2A
594-2A
601-2A
602-2A
603-2A
604-2A
605-2A
606-2A
ALK
TYPE
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
L
L
L
L
L
L
FLY
ASH
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
MGO
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
Y
Y
Y
Y
Y
Y
Y
N
N
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
PH
CONTR
POINT
N/A
5.90
N/A
5.20
5.20
5.90
N/A
5.50
5.50
5.50
N/A
N/A
N/A
5.20
5.50
5.50
5.70
N/A
N/A
N/A
5.20
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
5.40
N/A
N/A
N/A
N/A
N/A
N/A
7.00
7.00
7.00
7.00
7.00
8.00
GAS
RATE
ACFM
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
28000
28000
30000
30000
30000
30000
30000
30000
20500
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
20500
30000
• GAS
VEL
FPS
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
11 .7
11 .7
12.5
12.5
12.5
12.5
12.5
12.5
8.6
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
8.6
12.5
TCA
LIO
RATE
GPM
1200
1200
1200
1200
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1200
1200
1200
1200
1200
900
1200
1200
1200
1200
1200
1200
1200
1200
900
1200
1200
1200
1200
900
1200
900
TCA
L/G
GAt/
MAC F
49.8
49.8
49.8
49.8
41 .5
41 .5
41 .5
41.5
41 .5
41.5
41 .5
41 .5
41 .5
41 .5
41.5
41 .5
41.5
41.5
41 .5
41.5
41 .5
41 .5
53.4
53.4
49.8
49.8
49.8
37.4
49.8
49.8
72.9
49.8
49.8
49.8
49.8
49.8
37.4
49.8
49.8
49.8
49.8
37.4
72.9
37.4
SOLID
RECIRC
NOW %
15.0
15.0
15.0
15.0
15.0
15.0
15.0
1 5.0
15.0
15.0
15.0
15.0
1 5.0
1 5.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
15.0
8.0
15.0
15.0
13.8
14.7
14.4
15.0
14.8
15.1
8.0
15.0
a.o
8.0
8.0
8.0
SOLIDS
DISCH
RANGE
X
37-43
34-46
36-46
38-45
34-43
34-44
37-43
38-46
33-44
37-44
34-41
34-42
-
34-47
34*-43
35-39
37-42
-
39-43
-
40-45
-
35-42
N/A
33-41
55-64
32-61
33-36
36-37
30-55
60-68
52-61
62-70
56-60
54-60
51-59
52-62
53-54
54-60
57-60
58-63
58-62
51-59
57-62
TCA
D.P.
IN.
H20
7.6
8.3
8.0
7.9
7.7
9.4
9.2
9.3
8.4
7.9
7.5
7.0
N/A
6.7
6.9
6.6
7.5
N/A
8.8
N/A
9.7
N/A
N/A
N/A
9.5
10.0
9.0
7.8
3.5
10.3
5.4
8.8
11.4
10.5
10.6
8.9
7.2
8.0
8.7
8.3
8.3
7.3
4.8
6.7
M.C. SYSTEM
D.P. RANGE
INI.H20
0.35-0.43
0. 35-0.43
0.40-0.43
0.38-0.45
0.30-0.35
0.30-0.40
0.35-0.38
0.33-0.40
0.25-0.35
0.30-0.35
0.30-0.35
0.33-0.35
-
0.30-0.40
0.30-0.35
0.30-0.38
0.35-0.40
-
0.35-0.41
-
0.45-0.55
-
0.28-0.35
N/A
0.45-0.53
0.45-0.53
0.45-0.55
0.53-0.58
0.52-0.60
0.45-0.52
0.18-0.25
0.45-0.52
0.40-0.48
0.42-0.52
0.45-0.60
0.52-0.60
0.49-0.66
0.51-0.56
0.47-0.52
0.49-0.51
0.49-0.53
0.52-0.88
0.25-0.32
0.51-0.56
RUN
NO.
562-2A
562-2B
563-2A
564-2A
565-2A
56G-2A
567-2A
563-2A
569-2A
569-2B
570-2A
571-2A
571-28
572-2A
573-2A
575-2A
576-2A
576-28
577-2A
578-2A
579-2A
580-2A
581-2A
58.T-2A
583-2A
583-2B
584-2A
585-2A
586-2A
587-2A
588-2A
589-2A
590-2A
590-2B
591 -2A
592-2A
593-2A
594-2A
601-2A
602-2A
603-2A
604-2A
605-2A
606-2A
-------
TC& OPERATING CONDITIONS (CONTINUED)
RUN
NO.
562-2A
562-2B
563-2A
564-2A
565-2A
56S-2A
567-2A
568-2A
569-2A
569-2B
570-2A
571-2A
571-2B
572-2A
573-2A
575-2A
576-2A
576-28
577-2A
578-2A
579-2A
58Q-2A
581-2A
582-2A
563-2A
583-2B
564-2A
585-2A
586-2A
5B7-2A
588-2A
589-2A
590-2A
590-2B
591-2A
592-2A
593-2A
594-2A
601-2A
602-2A
603-2A
604-2A
605-2A
606-2A
EFFLU TCA LOW PH
RES TANK flES
TIME TIME
WIN WIN.
12.0
12.0
12.0
12.0
14.4
14.4
14.4
14. 4
10.8
10.8
10.8
10.8
10. 8
10.8
14.4
14. 4
14.4
14.4
14.4
14. 4
10.8
10.3
12.0
12. 0
3.9
3.0
4.
4.
4.
4.
4.
4.
4.
4.
4.
4.
4.1
4. 1
4. 1
4. 1
4. 1
4, 1
4. 1
4. 1
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
OXID EDUCTOR BLEED BLEED
AIR CIRCUL TO OX OXID H2S04
RATE RATE TANK TANK RATE
SCFM GPM GPM PH GPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
RUN
NO.
5S2-2A
562-2B
563-2A
564-2A
565-2A
566-2A
567-2A
568-2A
569-2A
569-2B
570-2A
571-2A
571-2B
572-2A
573-2A
575-2A
576-2A
576-2B
577-2A
578-2A
579-2A
530- 2 A
581-2A
582-2A
583-2A
583-2B
584-2A
585-2A
586-2A
587-2A
588-2A
589-2A
590-2A
590-2B
591-2A
592-2A
593-2A
594-2A
601-2A
602-2A
603-2A
604-2A
605-2A
606-2A
B-67
-------
TCA OPERATING CONDITIONS
03
i
en
CO
RUN
NO.
607-2A
608-2A
608-2B
609-2A
610-2A
611-2A
612-2A
613-2A
614-2A
615-2A
616-2A
S17-2A
618-2A
618-2B
619-2A
620-2A
621 -2A
622-2A
622-2B
623-2A
624-2A
625-2A
701-2A
702-2A
703-2A
704-2A
705-2A
706-2A
707-2A
708-2A
709-2A
710-2A
711-2A
712-2A
713-2A
714-2A
714-2B
715-2A
716-2A
717-2A
718-2A
7 19-2 A
801-2A
801-2B
ALK
TYPE
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
L
LS
LS
LS
LS
LS
LS
SL
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
FLY
ASH
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
N
N
N
N
N
N
N
N
N
N
N
N
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
MGO
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
N
N
N
N
Y
Y
Y
Y
Y
Y
Y
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
PH
CONTR
POINT
8.00
8.00
8.00
7.00
8.00
8.00
8.00
7.00
8.00
7.00
8.00
8.00
7.00
7. 00
7.00
7.00
7.00
7.00
7.00
7.00
7.00
8.00
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
5.80
5.75
N/A
N/A
N/A
N/A
N/A
GAS
RATE
ACFM
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
N/A
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
N/A
30000
27000
N/A
30000
18000
30000
30000
GAS
VEL
FPS
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
N/A
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
N/A
12.5
11 .3
N/A
12.5
7.5
12.5
12.5
TCA
LIO
RATE
GPM
900
900
900
900
900
900
900
1200
900
1200
1200
1200
1200
1200
1200
900
1200
900
900
1200
900
1450
1200
1200
1200
1200
1200
1200
1200
1200
1200
1200
1200
1200
1200
1200
1200
1000
1000
1000
1200
1200
1200
1200
TCA
L/G
GAL/
MACF
37.4
37.4
37.4
37.4
37.4
37.4
37.4
49.8
37.4
49.8
49.8
49.8
49.8
49.8
49.8
37.4
49.8
37.4
37.4
49.8
37.4
N/A
49.8
49.8
49.8
49.8
49.8
49.8
49.8
49.8
49.8
49.8
49.8
49.8
49.8
49.8
N/A
41 .5
46.1
N/A
49.8
83.1
49.8
49.8
SOLID
RECIRC
NOW X
8.0
15.0
15.0
8.0
8.0
8.0
8.0
8.0
8.0
8.0
8.0
15.0
7.8
7.5
8.0
8.1
8.1
8.6
8.0
8.2
8.0
8.1
8.0
15.0
8.0
8.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
5.0
4.9
5.2
N/A
5.0
4.4
14.7
14.4
14.8
14.6
14.6
SOLIDS
DISCH
RANGE
X
53-59
55-60
52-56
55-63
53-67
55-65
57-61
58-61
55-61
59-67
50-63
54-60
60-65
55-63
49-62
52-60
48-62
37-58
37-61
53-65
35-49
28-63
31-43
33-42
41-55
40-46
N/A
N/A
38-42
37-43
37-41
38-48
35-40
36-43
38-42
32-40
N/A
30-42
33-41
31-45
36-40
35-41
34-45
34-45
TCA
D.P.
IN.
H20
6.4
7.2
6.3
6.0
5.8
6.6
7.2
7.7
6.0
7.8
7.4
8.6
11.0
13.3
9.4
8.2
10.8
6.6
6.7
7.0
6.5
N/A
8.4
7.7
7.4
8.0
8.0
N/A
6.6
7.0
6.4
6.4
6.6
6.7
8.2
8.4
N/A
11.2
14.4
9.6
7.4
3.3
7.1
7.1
M.E. SYSTEM
D.P. RANGE
IN.H20
0.45-0.47
0.49-0.54
0.48-0.53
0.48-0.53
0.47-0.53
0.48-0.53
0.53-0.57
0.57-0.61
0.45-0.60
0.46-0.56
0.42-0.51
0.42-0.49
0.40-0.52
0.46-0.58
0.28-0.56
0.46-0.62
o, ' :-:.64
0.50-0.59
0.51-0.60
0.54-0.68
0.63-0.78
0. 1 1-0.57
0.42-0.56
0.45-0.50
0.43-0.49
0.40-0.54
0.43-0.52
0.44-0.59
0.45-0.57
0.44-0.49
0.44-0.49
0.47-0.55
0.50-0.62
0.48-0.61
0.44-0.50
0.33-0.46
N/A
0.44-0.55
0.34-0.44
0.17-0.52
0.40-0.50
0. 13-0.20
0.47-0.51
0.47-0.51
RUN
NO.
607-2A
608-2A
608-26
609-2A
610-2A
61 1-2A
612-2A
613-2A
614-2A
615-2A
616-2A
617-2A
618-2A
618-2B
619-2A
620-2A
621-2A
622-2A
622-2B
623-2A
624-2A
625-2A
701-2A
702-2A
703-2A
704-2A
705-2A
706-2A
707-2A
708-2A
709-2A
710-2A
71 1-2A
712-2A
713-2A
714-2A
714-2B
715-2A
716-2A
717-2A
718-2A
719-2A
801-2A
801-2B
-------
TCA OPERATING CONDITIONS (CONTINUED)
EFFLU TCA LOW PH OXID EDUCTOR BLEED BLEED
RES TANK RES AIR CIRCUL TO OX OXID H2S04
RUN
NO.
607-2A
608-2A
608-28
609-2A
610-2A
611-2A
612-2A
613-2A
614-2A
615-2A
616-2A
617-2A
618-2A
618-28
619-2A
620-2A
621-2A
622-2A
622-28
623-2A
624-2A
625-2A
701-2A
702-2A
703-2A
704-2A
705-2A
706-2A
707-2A
708-2A
709-2A
710-2A
711-2A
712-2A
713-2A
714-2A
714-2B
715-2A
716-2A
717-2A
718-2A
719-2A
B01-2A
801-2B
TIME
MIN
4. 1
4. 1
5.4
5.4
5.4
4. 1
3.0
3.0
16.0
12.0
12.0
12.0
4. 1
4. 1
4. 1
4. 1
3.0
4. 1
4. 1
3.0
3.0
3.4
4. 1
4. 1
4. 1
12. 0
12.0
12.0
4. 1
4.1
4.1
12.0
12.0
12.0
12.0
4. 1
4. 1
14.4
14.4
14.4
12.0
12.0
12.0
15.4
TIME
MIN.
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
RATE
SCFM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
600
530
RATE
GPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
1 N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
1590
1590
TANK
GPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
TANK I
PH
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
RATE
GPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
RUN
NO.
607-2A
608-2A
608-2B
609-2A
610-2A
611-2A
612-2A
613-2A
614-2A
615-2A
616-2A
617-2A
618-2A
618-2B
619-2A
620-2A
621-2A
622-2A
622-2B
623-2A
624-2A
625-2A
701-2A
702-2A
703-2A
704-2A
705-2A
706-2A
707-2A
708-2A
709-2A
710-2A
711-2A
712-2A
713-2A
714-2A
714-28
715-2A
716-2A
717-2A
718-2A
719-2A
801-2A
801-2B
B-69
-------
TCA OPERATING CONDITIONS
RUN
NO.
802-2A
803-2A
804-2A
805-2A
806-2A
807-2A
808-2A
809-2A
310-2A
8t 1-2A
812-2A
813-2A
814-2A
815-2A
816-2A
817-2A
818-2A
818-28
8 19-2 A
820-2A
821-2A
A UK
TYPE
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
FLY
ASH
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
MGO
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
N
Y
PH
CONTR
POINT
N/A
5.00
5.00
5.30
5.30
5.40
N/A
N/A
5.40
N/A
N/A
5.30
5.30
N/A
N/A
N/A
N/A
N/A
N/A
5.90
N/A
GAS
RATE
ACFM
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
20000
250O
25000
20000
20000
30000
GAS
VEL
FPS
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
12.5
8.4
10.4
10.4
8.4
8.4
12.5
TCA
LIO
RATE
GPM
1200
1200
1200
1200
1200
1200
1200
1200
1200
1200
1200
1200
1200
1000
1000
1000
10.00
1000
1000
1000
1200
TCA
L/C SOLID
GAL/ RECIRC
MACF MOM %
49.8 15.3
49.8 14.9
49.8 15.0
49.8 15.0
49.8
49.8
49.8
49.8
49.8
49.8
49.8
49.8
49.8
41 .5
41 .5
62.3
49.8
49.8
62.3
62.3
49.8
4.4
4.9
4.8
4.1
5.0
4.6
5.0
5.0
4.6
4.9
5.2
4.4
4.8
4.3
2.9
3.8
4.9
SO L I DS
DISCH
RANGE
%
32-38
33-48
30-50
26-39
32-44
28-44
24-64
80-89
84-91
35-50
32-44
35-44
33-42
35-41
38-42
31-48
38-42
35-42
32-42
32-42
78-80
TCA
D.P.
IN.
H20
8.4
8.4
8.3
8.2
8.2
8.5
8.2
8.4
8.6
8.1
8.0
9.6
9.6
11 .9
13.0
6.8
8.5
8.2
7.4
6.9
7.8
M.L. SYSTEM
D.P. RANGE
IN.H20
0.47-0.56
0.40-0.52
0.40-0.46
0.37-0.46
0.31-0.40
0.34-0.44
0.44-0.50
0.35-0.43
0.35-0.45
0.30-0.47
0.30-0.50
0.47-0.58
0.47-0.55
0.44-0.54
0.40-0.48
0. 15-0.26
0.26-0.36
0.24-0.35
0. 1 1-0.26
0.11-0.21
0.54-0.62
RUN
NO.
802-2A
803-2A
804-2A
805-2A
806-2A
807-2A
808-2A
809-2A
810-2A
81 1-2A
812-2A
813-2A
814-2A
815-2A
816-2A
817-2A
818-2A
818-2B
819-2A
820-2A
821-2A
-------
TCA OPERATING CONDITIONS (CONTINUED)
RUN
NO.
802-2A
803-2A
804-2A
805-2A
806-2A
807-2A
808-2A
809-2A
810-2A
811-2A
812-2A
813-2A
814-2A
B15-2A
816-2A
817-2A
818-2A
B18-2B
819-2A
820-2A
821-2A
EFFLU TCA LOW PH
RES TANK RES
TIME TIME
MIN MIN.
23.5
23.5
23.5
23.5
23.5
23.5
23.5
15.7
15. 7
23.5
15.7
23.5
15.7
14.4-
14.4
14.4
14.4
14.4
N/A
N/A
4. 1
N/A
N/A
N/A
N/A
N/A
2.9
2.9
1 .9
1 .9
2.9
1 .9
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
4.1
OXID EDUCTOR BLEED
AIR CIRCUL TO OX
RATE RATE TANK
SCFM GPM GPM-
485
465
410
470
290
475
200
300
300
270
350
310
145
N/A
N/A
N/A
N/A
N/A
N/A
N/A
170
1600
1600
1600
1600
1200
1600
1600
1600
1600
1600
1600
1600
1200
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
BLEED
OXID H2S04
TANK RATE
PH GPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
5.35
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
RUN
NO.
802-2A
803-2A
804-2A
805-2A
806-2A
807-2A
808-2A
809-2A
810-2A
811-2A
812-2A
813-2A
814-2A
815-2A
816-2A
817-2A
818-2A
818-2B
819-2A
820-2A
821-2A
B-71
-------
TCA ANALYTICAL RUN SUMMARY (GASES)
AVG
S02
RUN IN
NO. PPM
TFG-2A 3084
TFG-2B 3274
TFG-2C 3260
TFG-2D 3778
TFG-2E 3296
TFG-2F 3000
525-2A 2852
526-2A 3134
527-2A 3179
528-2A 3432
529-2A 3575
530-2A 3350
531-2A 3284
532-2A 3742
533-2A 3225
534-2A 2616
535-2A 3206
535-2B 3013
536-2A 3C69
i 537-2A 2780
^ 538-2A 3152
1X3 539-2A 3234
540-2A 3235
541-2A 3690
542-2A 3494
543-2A 2906
544-2A 3246
545-2A 3155
546-2A 2948
547-2A 3128
548-2A 2611
549-2A 2610
550-2A 2630
551-2A 3080
552-2A 3035
553-2A 2426
554-2A 2822
555-2A 2430
556-2A 2296
557-2A 2695
558-2A 2603
559-2A 3226
560-2A 3357
561 -2A 3043
M.IN MAX
502 S02
IN IN
PPM PPM
2640 3440
2560 3600
2760 4080
3160 4340
1180 4300
2520 3840
2520 3200
2800 3880
2060 4800
2800 4420
3000 4000
2480 4000
2400 3380
3480 4040
2280 3920
1200 3360
1360 4700
1480 4840
1240 4320
2200 3680
1960 4030
1920 4060
2520 3850
3520 3840
3080 4000
2440 3440
2480 3860
2440 3640
1380 3680
2400 3680
2240 2960
2080 3160
2080 3240
3040 3120
2640 3400
2080 2680
1880 3120
2000 2880
1480 3840
1360 3800
1040 3820
1520 4020
3000 4290
1920 3800
AVG
S02
OUT
PPM
312
409
570
767
1525
724
234
341
452
873
688
781
461
632
133
462
539
554
577
335
340
412
449
630
661
495
458
605
578
534
451
583
574
673
445
446
551
500
442
624
543
701
715
675
WIN MAX
S02 S02
OUT OUT
PPM PPM
70 1340
120 700
360 1040
580 900
1240 1940
500 1080
40 460
120 440
140 1200
540 1400
440 1000
360 1140
110 760
340 860
30 320
60 720
100 1210
125 1300
80 1150
170 500
120 610
100 900
170 950
560 700
450 920
340 675
230 670
200 910
220 1250
300 680
300 680
400 780
400 840
640 700
360 560
280 620
260 760
290 720
160 940
180 1120
110 1040
180 1160
520 1190
280 1020
AVG MIN
S02 502
REM REM
% %
89 56
86 76
80 72
77 75
41 -81
73 68
90 84
87 84
85 72
72 65
78 72
74 68
84 78
81 76
95 89
81 76
81 70
80 66
80 68
86 82
88 82
86 73
84 73
81 79
79 74
81 78
84 74
79 72
78 62
81 76
80 74
75 73
76 71
75 75
83 81
80 73
78 73
77 72
80 72
75 66
78 68
76 68
76 69
75 70
MAX
S02
REM
%
97
95
86
80
55
78
98
96
94
79
84
84
96
90
99
94
92
91
93
92
94
97
93
82
84
85
90
92
90
86
87
79
81
77
86
85
85
84
89
85
88
88
82 1
84 1
AVG MIN MAX
VIAKE MAKE MAKE AVG MIN MAX
PER PER PER AVG MIN MAX AVG MIN MAX BOIL BOIL BOIL
PASS PASS PASS , 02 02 02 N02 N02 N02 LOAD LOAD LOAD
WMOL MMOL MMOL IN IN IN IN IN IN MEGA MEGA MEGA
/L /L /L % % % PPM PPM PPM WATT WATT WATT
14.5 10.1 16.3 9.1 7.9 10.2 N/A N/A N/A 145 124 150
15.0 12.9 16.9 8.1 5.8 9.5 N/A N/A N/A 126 93 150
13.9 12.1 16.2 8.2 6.3 9.2 N/A N/A N/A 141 102 149
**** **** **** 7.8 6.7 9.2 N/A N/A N/A 138 92 153
17.0 -10. '3 22.8 7.4 4.5 8.5 N/A N/A N/A 147 125 151
11.6 10.2 14.0 7.2 5.7 9.2 N/A N/A N/A 142 100 160
13.7 11.9 15.9 N/A N/A N/A N/A N/A N/A N/A N/A N/A
14.6 12.7 18.2 N/A N/A N/A N/A N/A N/A N/A N/A N/A
14.2 9.7 18.4 N/A N/A N/A N/A N/A N/A N/A N/A N/A
17.4 15.6 20.3 N/A N/A N/A N/A N/A N/A N/A N/A N/A
10.2 9.1 11.4 N/A N/A N/A N/A N/A N/A N/A N/A N/A
17.5 14.7 20.1 N/A N/A N/A N/A N/A N/A N/A N/A N/A
19.6 14.4 22.5 N/A N/A N/A N/A N/A N/A N/A N/A N/A
21.5 20.5 23.2 N/A N/A N/A N/A N/A N/A N/A N/A N/A
21.7 14.4 26.9 N/A N/A N/A N/A N/A N/A N/A N/A N/A
7.6 4.1 9.3 N/A N/A N/A 0 N/A N/A N/A N/A N/A
9.4 4.5 3.2 N/A N/A N/A 0 N/A N/A N/A N/A N/A
8.7 4.8 2.7 N/A N/A N/A 0 N/A N/A N/A N/A N/A
10.3 4.8 4.0 N/A N/A N/A 0 N/A N/A N/A N/A N/A
8.7 7.0 1.4 N/A N/A N/A 0 N/A N/A N/A N/A N/A
0.1 6.6 2.2 N/A N/A N/A 0 N/A N/A N/A N/A N/A
7.0 10.8 21.5 N/A N/A N/A 0 N/A N/A N/A N/A N/A
6.7 14.2 18.9 N/A N/A N/A 0 N/A N/A N/A N/A N/A
8.3 17.7 19.0 N/A N/A N/A 0 N/A N/A N/A N/A N/A
6.9 15.3 8.2 N/A N/A N/A 0 N/A N/A 35 35 35
4.4 12.6 6.4 N/A N/A N/A 0 N/A N/A N/A N/A N/A
9.9 6.6 1.9 N/A N/A N/A 0 N/A N/A N/A N/A N/A
5.2 11.7 6.8 N/A N/A N/A 0 N/A N/A N/A N/A N/A
4.7 9.2 8.9 N/A N/A N/A 0 N/A N/A N/A N/A N/A
6.1 12.7 9.2 N/A N/A N/A 0 N/A N/A N/A N/A N/A
3.4 11.3 5.4 N/A N/A N/A 0 N/A N/A N/A N/A N/A
2.5 10.4 5.0 N/A N/A N/A 0 N/A N/A N/A N/A N/A
2.7 10.1 5.2 N/A N/A N/A 0 N/A N/A N/A N/A N/A
4.8 14.8 4.9 N/A N/A N/A 0 N/A N/A N/A N/A N/A
3.5 11.6 5.0 N/A N/A N/A 0 N/A N/A N/A N/A N/A
0.2 9.4 1.6 N/A N/A N/A 0 N/A N/A N/A N/A N/A
8.8 6.3 9.9 N/A N/A N/A 0 N/A N/A N/A N/A N/A
7.5 6.7 8.3 N/A N/A N/A 0 N/A N/A N/A N/A N/A
7.2 5.1 1.1 N/A N/A N/A 0 N/A N/A N/A N/A N/A
0.6 6.1 5.3 N/A N/A N/A 0 N/A N/A N/A N/A N/A
0.6 4.9 4.8 N/A N/A N/A 0 N/A N/A N/A N/A N/A
3.0 6.9 15.0 N/A N/A N/A 0 N/A N/A N/A N/A N/A
3.6 12.3 15.7 N/A N/A N/A 0 N/A N/A N/A N/A N/A
2.2 8.5 14.6 N/A N/A N/A 0 N/A N/A N/A N/A N/A
-------
TCA ANALYTICAL RUN SUMMARY (GASES)
RUN
NO.
562-2A
562-28
563-2A
564-2A
565-2A
566-2A
567-2A
568-2A
569-2A
569-2B
570-2A
571-2A
571-28
572-2A
573-2A
575-2A
576-2A
576-28
577-2A
CO 578-2A
' 579-2A
U> 580-2A
581-2A
582-2A
583-2A
583-28
584-2A
585-2A
586-2A
587-2A
588-2A
589-2A
590-2A
590-2B
591-2A
592-2A
593-2A
594-:2A
601-2A
602-2A
603-2A
604-2A
605-2A
606-2A
AVG
S02
IN
PPM
3085
3078
3216
3238
3627
3108
3272
3294
3112
3066
2958
2759
2574
3181
2720
2958
3247
3200
3205
3063
3090
3033
2814
2900
3040
2954
3016
2948
2877
3059
2476
3314
2066
2442
2386
2885
2810
2871
2852
3134
3179
3432
3575
3350
WIN
S02
IN
PPM,
2120
2440
2720
2520
2760
2520
2280
2720
2240
2440
2320
2120
2440
2440
2720
2600
2400
3040
2460
2840
2760
2660
2040
2620
2200
2100
2080
2400
2120
2400
1780
2200
1960
2000
1240
2280
2400
2080
2520
2800
2060
2800
3000
2480
MAX
S02
IN
PPM
4060
3920
4000
4040
4320
3920
4200
3800
4000
3840
3840
3380
2800
3840
2720
3200
4000
3360
3920
3160
3660
3440
3660
3040
3800
3600
4000
3880
3960
3800
3320
4360
2200
2920
3400
3640
3480
3480
3200
3880
4800
4420
4000
4000
AVG
S02
OUT
PPM
523
582
435
1288
1405
532
488
1089
940
1034
775
661
744
1254
760
820
813
1110
553
538
1130
626
421
381
602
370
171
399
538
194
159
301
620
516
181
120
208
213
234
341
452
873
688
781
MIN
S02
OUT
PPM
200
300
240
940
960
240
240
480
540
800
500
370
480
920
760
540
500
1020
340
220
840
280
120
90
340
60
40
180
280
50
60
110
460
400
40
60
120
80
40
120
140
540
440
360
MAX
S02
OUT
PPM
1260
1020
890
1670
2000
1 140
800
1500
1500
1500
1340
1040
1120
1640
760
1040
1320
1200
860
1110
1530
1000
860
1 100
1000
900
400
700
1020
540
260
640
700
740
420
280
480
320
460
440
1200
1400
1000
1140
AVG
502
REM
%
81
79
85
55
57
81
83
63
67
62
71
73
67
56
69
69
72
61
81
80
59
78
83
85
78
86
93
85
79
93
92
90
66
76
92
95
91
91
90
87
85
72
78
74
MIN
S02
REM
%
65
71
73
46
49
58
78
55
56
57
61
66
50
50
69
63
61
56
74
61
54
68
74
60
66
68
84
79
71
82
87
83
60
69
85
91
84
87
84
84
72
65
72
68
MAX
502
REM
%
92
86
91
.68
66
91
89
81
74
68
78
81
81
66
69
77
80
66
87
91
66
88
94
96
85
97
98
93
87
98
96
95
75
83
96
98
95
96
98
96
94
79
84
84
AVG
MAKE
PER
PASS
MMOL
/L
13.3
12.9
14.5
9.6
13.1
16.0
17.4
13.3
13.1
12.2
13.3
12.9
11.1
1 1 .4
1 1 ..9
13.0
14.9
12.6
16.5
15.7
1 1 .7
14.8
11.6
12.3
12.6
13.5
15.0
17.7
12.1
15. 1
8.3
15.8
7.3
9.9
11 .6
14.6
18.2
14.0
13.7
14.6
14.2
17.4
10.2
17.5
MIN
MAKE
PER
PASS
MMOL
/L
9.5
10.9
12.4
7.0
10.6
11 .0
12.8
10.9
10.4
9.7
10.8
10.9
7.9
7.9
11 .9
11 .3
11 .2
10.9
13.2
12.1
10.0
14.8
9.3
9.0
9.3
9.8
10.2
14.9
8.4
12.1
6.0
10.7
6.3
8.2
6.2
11 .4
15.2
10.4
11.9
12.7
9.7
15.6
9.1
14.7
MAX
MAKE
PER
PASS
MMOL
/L
16.9
15.7
17.3
13.5
16.9
19.8
21 . 1
15.8
5.8
5.4
5.5
4.7
4.2
4.0
1 .9
14.3
18.4
14.2
19.6
17.1
13.5
14.9
13.5
13.9
15.9
16.1
19.1
21 .9
16.9
18.6
11.1
20.8
8.1
11.4
15.9
18.8
22.7
16.9
15.9
18.2
18.4
20.3
11 .4
20.1
AVG
O2
IN
%
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
8.9
N/A
N/A
7.6
6.3
8.2
N/A
N/A
N/A
6.4
6.0
6.8
MIN
02
IN
%
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
8.0
N/A
N/A
6.0
5.6
5.4
N/A
N/A
N/A
6.0
5.2
4.4
MAX
02
IN
%
N/A
N/A
N/A
N/A
N/A
N/A
. N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
9.8
N/A
N/A
10.0
7.5
10.0
N/A
N/A
N/A
7.0
6.8
8.5
AVG
N02
IN
PPM
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
f>
«>
0
0
0
0
0
0
0
N/A
N/A
N/A
N/A
N/A
N/A
0
0
0
0
0
0
MIN
N02
IN
PPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
MAX
NO2
IN
PPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
AVG
BOIL
LOAD
MEGA
WATT
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
99
99
142
137
148
146
N/A
N/A
N/A
134
143
142
MIN
BOIL
LOAD
MEGA
WATT
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
77
44
124
96
111
96
N/A
N/A
N/A
113
128
110
MAX
BOIL
LOAD
MEGA
WATT
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
114
142
155
155
158
158
N/A
N/A
N/A
144
148
150
-------
TCA ANALYTICAL RUN SUMMARY (GASES)
RUN
NO.
607-2A
608-2A
608-28
609-2A
610-2A
61 1-2A
612-2A
613-2A
614-2A
615-2A
616-2A
617-2A
618-2A
618-28
51 9-2 A
G20-2A
621-2A
622-2A
03 G22-2B
^j 623-2A
-P> 624-2A
625-2A
701-2A
702-2A
703-2A
704-2A
705-2A
706-2A
707-2A
708-2A
709-2A
710-2A
711-2A
712-2A
713-2A
714-2A
714-2B
715-2A
716-2A
717-2A
718-2A
719-2A
801-2A
801-2B
AVG
S02
IN
PPM
3295
3742
3225
3130
2987
2912
3092
3280
3556
3141
3341
3107
2138
1763
1 813
1692
2035
2606
2554
2563
2841
2323
2775
2998
3009
2778
2812
2772
3007
3092
3314
3431
3284
3028
2678
2675
3130
2978
2684
2660
3234
3061
2782
2810
MIN
SO2
. IN
PPM
2400
3480
2280
2480
2240
2400
2800
2080
3000
2500
2680
2200
1520
1240
320
640
560
2360
2240
2080
2060
1320
2000
2-00
2560
1960
2400
2200
2720
2760
2800
2520
2840
2400
2200
2040
2720
2480
2060
1800
2760
2740
1920
2600
MAX
502
IN
PPM
3880
4040
3920
3860
3720
3520
3760
3920
4240
3960
4000
3600
3040
2840
3460
3660
3080
3000
2840
2880
3320
3360
3680
3680
3480
3520
3320
3600
3680
3760
3720
3920
o380
3320
3040
3960
3460
3580
3200
3740
3520
3400
3520
2920
AVG
S02
OUT
PPM
440
632
133
619
426
510
539
511
758
375
785
586
251
69
107
166
83
208
380
212
462
158
359
514
695
555
394
466
759
1449
1362
1436
1 1 14
836
452
321
320
404
213
362
703
390
744
825
MIN
S02
OUT
PPM
110
340
30
120
180
340
440
180
240
220
440
260
120
20
5
20
10
70
220
60
90
20
140
240
480
320
200
280
600
1080
920
860
800
540
320
120
180
260
1 10
100
620
320
260
680
MAX
S02
OUT
PPM
760
860
320
920
660
740
700
780
1080
680
1260
780
520
180
510
740
200
360
560
400
680
460
800
780
1080
1060
540
760
1140
2020
1630
1840
1360
1050
700
860
440
600
330
650
860
480
1140
900
AVG
502
REM
%
85
81
95
77
84
80
80
83
76
86
73
79
87
96
94
91
96
91
83
90
82
92
86
81
74
77
84
81
72
48
54
53
62
69
81
87
89
84
91
86
75
85
71
67
MIN
S02
REM
%
78
76
89
69
78
76
77
78
72
81
63
75
81
93
84
78
93
87
77
83
77
79
76
71
66
61
79
73
66
40
47
47
58
64
74
76
86
81
88
81
72
83
64
66
MAX
S02
REM
%
96
90
99
96
93
85
83
90
93
91
86
87
92
98
99
97
99
97
89
97
95
99
93
89
82
88
91
88
77
58
64
64
69
76
87
94
93
89
95
95
78
88
85
71
AVG
MAKE
PER
PASS
MMOL
/L
19.8
21.5
21 .7
17.3
17.8
6.6
7.6
4.4
9.2
4.4
13.1
13.0
9.9
9.0
9.0
0.7
0.3
6.8
5.1
2.3
6.4
N/A
• 2.6
2.9
1 .9
1 .5
2.6
1 .9
1 .5
7.9
9.6
9.7
0.9
1 .1
1 .5
2.3
N/A
6.1
4.0
N/A
13.0
8.4
10.4
10.0
MIN
MAKE
PER
PASS
MMOL
/L
14.4
20.5
14.4
13.1
13.0
14.3
15.9
10.0
15.8
11 .8
9.7
10.1
7.4
6.5
1 .6
4.4
2.9
14.6
14.1
10.7
13.9
N/A
9.4
10.2
10.5
8.2
10.8
9.7
10.1
7. 1
8.5
8.3
10.3
9.0
9.8
10.0
N/A
13.2
11.1
N/A
11 .0
7.6
8.3
9.8
MAX
MAKE
PER
PASS
MMOL
/L
24.6
23.2
26.9
23.7
21 .1
19.1
21 .1
16.2
23.3
17.0
16.8
15.0
13.2
4.0
5.3
20.1
5. 1
9.2
6.6
14.0
18.6
N/A
16.0
16.0
14.6
14.7
15.4
15.0
12.8
8.9
11.2
10.8
11 .5
12.3
13.5
16.5
N/A
18.5
16.2
N/A
14.2
9.3
11.9
10.2
AVG
02
IN
X
6.1
5.9
6.6
7.0
7.2
6.3
6.3
8.2
6.7
7.4
6.4
6.6
N/A
7.9
9.3
8.0
8.8
8.0
7.3
8.1
7.1
6.2
8.5
9.3
8.4
9.2
10.3
10.2
8.4
7.0
9.0
6.8
7.0
6.5
7.9
7.6
6.3
8.6
7.5
7.0
7.8
7.6
9.7
N/A
MIN
02
IN
%
4.5
5.0
4.7
5.0
4.9
5.2
5.0
6.1
5.2
5.7
5.0
4.5
N/A
6.0
8.1
5. 1
7.0
6.0
4.2
6.2
2.5
3.0
5.7
6.5
7.5
6.8
9.1
7.0
6.0
5.8
8.0
5.3
7.0
5.7
6.4
6.0
6.0
7.4
5.8
5.5
4.8
3.0
9.6
N/A
MAX
02
IN
X
9.8
7.6
9.0
11 .2
9.5
8.0
8.1
10.3
9.0
12.5
10.5
9.1
N/A
10.0
10.0
9.8
10.0
10.0
10.0
10.0
8.5
10.0
11 .0
10.4
9.7
10.8
12.0
12.5
11 .4
8.2
11 .8
10.5
7.0
8.4
10.4
11 .5
6.6
9.4
9.2
9.9
10.0
10.0
9.8
N/A
AVG
N02
IN
PPM
0
0
0
0
0
0
0
0
0
0
0
0
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
0
0
0
0
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
MIN
N02
IN
PPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
MAX
N02
IN
PPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
AVG
BOIL
LOAD
MEGA
WATT
142
131
131
141
140
133
146
143
141
142
146
146
83
69
73
113
85
128
133
123
140
127
142
146
141
133
144
143
141
144
130
136
148
133
137
136
150
138
136
141
141
146
109
133
MIN
BOIL
LOAD
MEGA
WATT
103
54
100
112
115
100
141
136
1 14
94
80
101
20
52
58
70
68
98
96
96
94
48
90
138
105
66
106
100
1 12
129
93
59
145
50
100
95
148
99
1 05
82
103
1 15
95
1 15
MAX
BOIL
LOAD
MEGA
WATT
148
145
150
163
148
148
150
147
149
156
156
157
154
123
1 16
146
149
156
156
154
157
156
151
152
150
150
162
152
152
152
159
156
150
150
152
154
152
1 54
153
156
152
154
149
148
-------
TCA ANALYTICAL RUN SUMMARY (GASES)
RUN
NO.
802-2A
803-2A
B04-2A
805-2A
806-2A
807-2A
B08-2A
809-2A
810-2A
811-2A
DO 812-2A
' 813-2A
tn 8 14-2 A
815-2A
816-2A
817-2A
818-2A
818-28
8 19-2 A
820-2A
821-2A
AVG
S02
IN
PPM
2888
2820
3033
3105
2965
2643
2862
3151
2940
2747
2996
2898
2589
2897
2871
3050
2988
3320
2742
2438
2482
MIN
S02
IN
PPM
2520
1760
2440
2800
2680
2080
2440
2480
2680
2120
2220
2360
2100
2520
2640
2840
2880
2880
2160
1680
1560
MAX
S02
IN
PPM
3200
3080
3600
3520
3680
3320
3S20
3800
3200
3320
3840
3280
3080
3160
3000
3200
3080
4100
3060
3120
2800
AVG
S02
OUT
PPM
624
985
1016
806
807
416
773
682
463
334
513
536
616
263
251
580
421
547
573
445
403
MIN
S02
OUT
PPM
540
420
480
560
680
160
400
360
280
200
300
380
380
200
140
500
390
420
330
130
100
MAX
SO2
OUT
PPM
700
1500
1320
1280
1080
700
1480
1100
860
560
960
760
840
400
360
680
500
760
800
1000
600
AVG
S02
REM
75
61
62
71
69
83
70
76
82
86
81
79
73
90
90
78
84
81
76
80
82
MIN
S02
REM
73
46
54
60
67
76
53
60
70
81
71
74
68
86
87
76
82
79
69
64
76
MAX
S02
REM
80
74
80
SO
73
91
82
85
88
90
87
83
82
92
94
82
86
84
86
91
93
AVG
MAKE
PER
PASS
MMOL
A
1 1 ,6
9.2
10.1
1 1 .7
11.0
1 1 .6
10.6
12.7
12.9
12.6
12.9
1 2.2
1 0.1
16.6
16.5
10.2
13.4
14.4
8.9
8.2
10.8
MIN
MAKE
PER
PASS
MMOL
A
9.9
6.9
8.5
9.9
10.1
8.8
9.0
8.2
11 .7
10.0
10.0
9.4
8.3
14.6
15.8
9.7
12.7
12.6
7.6
6.5
7.7
MAX
MAKE
PER
PASS
MMOL
A
13.0
10.8
12.8
13.7
13.2
13.5
1 1 .7
14.0
•14.0
14.3
15.3
13.6
12.3
17.5
17.1
10.8
14.0
17.3
10.1
9.3
1 1.9
AVG
02
IN
7.5
8.7
6.9
7.7
9.3
7.6
8.9
6.7
8.2
7. 1
8.2
7.5
9.5
7.4
7.2
6.7
6.7
7.2
9.3
N/A
7.7
MIN
02
IN
6.0
7.0
5.2
6.2
7.5
6.2
6.0
5.5
6.5
5.5
7.5
5.6
8.5
6.5
6.6
2.8
3.0
3.0
6.5
N/A
6.0
MAX
02
IN
X
8.5
13.0
8.5
9.0
12.5
8.5
14.5
8.0
11 .0
8.5
9.5
8.6
12.5
8.5
8.0
10.0
10.0
9.9
12.2
N/A
10.0
AVG
NQ2
IN
PPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
MIN
NQ2
IN
PPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
MAX
N02
IN
PPM
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
N/A
AVG
BOIL
LOAD
MEGA
WATT
126
138
138
125
127
133
136
1 19
138
126
142
145
135
151
131
131
144
148
119
116
139
MIN
BOIL
LOAD
MEGA
WATT
84
102
97
86
97
96
88
94
94
92
95
1 16
95
140
106
92
120
132
8
60
93
MAX
BOIL
LOAD
MEGA
WATT
149
154
154
153
150
153
154
152
155
154
154
155
154
155
151
154
156
155
152
152
154
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA
CONCENTRATIONS IN LIQUID, PPM
DO
I
-•J
ANALY
RUN TICAL
NO. POINT
TFQ-2A 2816
2825
TFG-2B 2816
2825
TFG-2C 2816
2825
TFG-2D 2816
2825
TFG-2E 2816
2825
TFG-2F 2816
2825
525-2A 2816
2825
526-2 A 2816
2825
527-2A 2816
2825
528-2A 2816
2825
529-2A 2816
2825
530-2A 2816
2825
531-2A 2816
2825
532-2 A 2816
2825
533-2 A 2816
2825
534-2 A 2816
2825
535-2A 2816
2825
535-2B 2816
2825
536-2A 2816
2825
537-2A 2816
2825
538-2A 2816
2825
539-2 A 2816
CA++
AVG MIN MAX
238 133 440
316 159 618
1835 T425 2175
1883 1590 2120
1622 1055 2270
1736 1185 2475
1394 1220 1710
1415 1255 1650
1146 885 1530
1183 932 1545
1633 1190 1990
1674 1160 2225
540 347 616
499 353 604
494 494 494
1382 1014 1632
1111 1052 1170
1883 1883 1883
1123 1123 1123
1581 1007 1915
1602 1170 2000
1121 1040 1165
1167 1167 1167
705 585 760
2222 2030 2370
2175 2175 2175
1550 800 2250
1250 828 1810
1104 910 1336
1031 807 1310
846 810 882
1450 1207 1755
1657 1500 1815
1370 654 1660
1308 574 1620
947 594 1585
AVG
10346
10284
696
702
573
573
466
470
470
487
563
608
130
126
103
107
120
334
141
306
277
766
319
11191
170
142
304
343
405
426
432
436
449
350
331
284
MG++
MIN
7639
80f9
631
633
345
333
330
318
322
431
465
459
77
102
103
0
92
334
141
140
53
349
319
9260
160
142
169
190
372
409
427
388
441
276
284
229
MAX
12139
12498
759
779
781
785
539
540
534
569
647
1089
187
154
103
265
148
334
141
443
387
1349
319
12780
180
142
410
536
451
462
437
480
457
466
360
335
AVG
7889
7653
115
149
143
177
89
164
107
236
80
163
14
21
23
125
106
26
272
111
136
213
456
2512
68
152
84
132
105
86
84
71
155
100
162
82
S03*
MIN
3844
4297
67
67
67
45
33
56
22
45
33
33
2
18
23
56
84
26
272
64
80
144
456
2017
48
152
16
16
56
24
56
38
150
0
48
24
MAX
12213
10856
203
271
203
237
158
294
294
644
158
441
25
27
23
272
128
26
272
232
216
264
456
3370
104
152
184
408
184
120
112
128
160
280
256
160
AVG
27818
28651
1909
2026
1371
1752
1797
1925
1153
1388
1868
1923
198
18Q
248
1471
767
2046
908
1721
1536
2735
2284
32767
1732
1414
1870
1955
2575
2466
2271
2222
2064
1965
1814
741
504-
MIN
20544
21314
962
927
617
1098
1306
1531
554
776
1121
1103
181
163
248
972
307
2046
908
1147
1140
2630
2284
23063
1498
1414
775
1047
1797
1897
1722
2158
2037
1010
848
296
MAX
34713
37075
2454
2388
2256
2702
2486
2697
2066
2269
2307
2346
225
206
248
1949
1227
2046
908
2098
1912
2797
2284
32767
1920
1414
2990
2757
2906
31 1 1
2821
2325
2092
2995
2475
1647
AVG
3284
3374
3769
3790
3421
3436
2546
2539
2536
2536
3317
3502
960
888
960
1666
161 1
3261
1682
2534
2505
1872
1170
2970
3536
3049
2373
1962
1421
1297
1169
2455
2579
2082
1847
1898
CL-
MIN
2570
2614
3190
3323
2215
2304
1905
1772
2189
2233
2836
2969
650
665
860
1346
1524
3261
1682
1489
1347
1240
1170
1914
3368
3049
1489
871
998
1009
850
1914
2375
1276
1311
1453
MAX
4121
4431
4343
4387
4631
4609
3080
3057
2969
2925
3944
5983
1200
1080
860
2269
1699
3261
1682
3332
3190
2783
1170
4183
3687
3049
3758
3120
1778
1524
1489
31 1 1
2783
2765
2552
2694
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA (CONTINUED)
RUN
NO.
TFG-2A
TFG-2B
TFG-2C
TFG-2D
TFG-2E
TFG-2F
52S-2A
526-2A
527-2A
528-2A
529-2A
530-2A
531 -2A
532-2A
533-2A
534-2A
535-2A
535-2B
536-2A
537-2A
538-2A
539-2A
ANALY
TICAL
POINT
2816
2825
2816
2825
2616
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
AVG
5.41
5.23
5.75
5.19
5.85
5.30
5.83
5.38
5.72
5.07
5.70
5.19
5.86
5.32
5.30
S.78
5.23
5.75
5.30
5.83
5.37
6.00
5.60
5.25
6.12
5.53
5.90
5.96
5.70
5.90
5.45
5.94
5.61
5.99
PH
MIN
5.21
4.90
5.62
4.77
5.71
5.08
5.70
5.16
5.65
4.95
5.57
5.00
5.75
5.25
5.30
5.70
5.20
5.75
5.30
5.75
5.15
5.60
5.60
5.25
5.85
5.25
5.85
5.90
5.60
5.90
5.40
5.85
5.55
5.80
MAX
5.67
5.62
5.83
5.45
6.11
5.75
5.91
5.53
5.81
5.27
5.90
5.44
6.00
5.40
5.30
5.85
5.25
5.75
5.30
6.00
5.85
6.10
5.60
5.25
8.60
5.95
6.00
6.00
5.80
5.90
5.50
6.00
5.70
6.15
TOTAL
AVG
49720
50425
8414
8642
7219
7763
6394
6614
5536
5956
7609
8017
1846
1718
1730
4893
3800
8189
4263
6405
6203
6793
5449
32767
7923
7109
6299
5751
5716
5399
4897
6741
7382
5949
5553
4028
IONS, PPM
MIN MAX
39540
40606
7281
7476
4492
5250
5746
6101
4332
4895
5953
6277
1307
1323
173O
3654
3361
8189
4263
4049
3969
5746
5449
32767
7773
7109
3984
4471
4505
4379
4740
5895
6942
3445
3336
2847
55236
58890
9826
9688
10118
10885
7422
7493
6923
7136
8719
12260
22T1
2066
1730
6432
4240
8189
4263
8035
7446
8274
5449
32767
8021
7109
7932
7061
6457
6434
5054
7650
7623
7278
6665
5940
PERCENT
GYPSUM
SATURATION
AVG MIN MAX
37
51
102
109
76
99
98
105
59
71
102
104
12
11
16
106
56
134
64
110
102
111
124
125
132
112
114
107
125
115
94
122
120
113
106
43
17 77
22 1 10
51 141
49 130
35 128
64 156
67 148
80 162
26 1 15
39 127
55 133
54 135
11 16
10 13
16 16
81 134
22 90
134 134
64 64
72 129
72 118
78 143
124 124
101 150
118 143*
112 112
41 164
64 155
86 150
83 155
78 111
114 130
117 124
48 170
42 146
18 97
PERCENT
IONIC
IMBALANCE
AVG MIN
-0.6 -9.8
-2.7 -13.4
1.9 -5.1
1.3 -7.8
2.3 -3.3
-0.6 -5.2
-0.2 -4.8
-2.9 -10.3
1.6 -7.5
-2.9 -8.1
-1.1 -13.6
-2.9 -14.9
16.1 11.8
16.6 12.1
9.6 9.6
2.8 -4.8
5.6 -3.9
3.4 3.4
-0.4 -0.4
-1.6 -9.6
1.1 -4.3
2.0 -9.4
-6.6 -6.6
7.3 -5.7
-5.7 -13.7
4.9 4.9
-2.5 -16.3
-5.4 -16.7
-4.7 -15.9
-0.1 -8.4
-1.9 -6.4
-5.0 -7.0
14.1 13.2
-2.0 -17.5
1.4 -6.6
3.0 -8.3
MAX
6.4
8.0
7.5
4.9
8.3
2.5
4.8
0.4
8.9
7.5
5.5
6.0
17.7
19.9
9.6
11.9
15.1
3.4
-0.4
6.1
8.2
18.7
-6.6
16.6
3.0
4.9
18.8
12.1
7.9
7.8
2.6
-3.2
14.9
12.4
14.1
17.1
B-77
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA
CONCENTRATIONS IN LIQUID, PPM
CO
CO
ANALY
RUN TICAL
NO. POINT
539-2A 2825
540-2A 2816
2825
541-2A 2816
2825
542-2A 2816
2825
543-2A 2816
2825
544-2A 2816
2825
545-2 A 2816
2825
546-2 A 2816
2825
547-2A 2816
2825
548-2A 2816
2825
549-2A 2816
2825
550-2A 2816
2825
551-2A 2816
2825
552-2A 2816
2825
553-2A 2816
2825
554-2A 2816
2825
555-2A 2816
2825
556-2 A 2816
2825
557-2A 2816
2825
558-2A 2816
2825
559-2A 2816
2825
560-2A 2816
2825
CA++
AVQ MIN MAX
1077 566 1648
757 480 1240
608 455 740
961 738 1185
760 587 1075
1417 1405 1430
1116 1116 1116
1277 775 1745
1240 1040 1705
1408 1100 1790
1080 1080 1080
1450 1005 2250
1388 1025 1875
1023 782 1475
1038 698 1565
961 507 1495
1185 1025 1345
1582 1200 1975
1548 1205 1910
1958 1245 2845
1800 1405 2195
1070 1010 1160
1020 1013 1025
881 765 965
897 897 897
1479 1455 1503
1135 1070 1200
1327 1105 1535
1550 1550 1550
1450 1190 1580
1444 1299 1590
1016 725 1438
1137 902 1319
1060 640 1680
1141 762 1745
920 508 1570
745 530 1110
856 662 1030
AVQ
312
289
295
288
316
343
375
338
353
345
348
191
194
276
279
123
126
142
138
204
228
244
221
259
248
268
298
170
202
217
238
279
264
332
315
363
362
356
MG++
MIN
239
242
277
271
267
342
375
296
296
309
348
23
24
232
245
100
99
101
96
1MJ
224
232
180
249
248
265
267
162
202
139
219
231
216
211
223
288
291
306
MAX
523
385
322
305
361
345
375
378
469
374
348
282
310
328
312
142
153
167
166
245
233
251
262
269
248
272
330
191
202
260
258
318
312
434
384
449
428
424
AVQ
111
108
132
148
126
164
216
102
143
114
232
81
142
116
81
99
180
80
96
91
100
96
132
129
144
272
48
62
88
84
88
87
173
105
148
98
116
50
503-
MIN
24
40
32
128
48
136
216
40
88
8
232
4
40
36
24
48
144
24
24
40
80
40
96
92
144
176
32
48
88
8
48
8
136
16
48
8
32
24
MAX
272
168
192
168
216
192
216
200
184
208
232
208
344
304
120
152
216
144
144
176
120
176
168
184
144
368
64
88
88
120
128
144
216
216
272
336
304
136
AVQ
881
865
744
1355
1130
2332
2404
2035
1851
1458
1202
1346
1228
655
704
525
697
865
855
1001
829
398
331
288
363
1407
1011
1372
1011
1638
1574
1380
1644
1598
1741
1403
1170
927
504*
MIN
314
307
552
987
709
8233
2404
1428
1060
1025
1202
368
340
377
358
225
214
620
591
454
547
291
262
84
363
1402
861
1038
1011
1460
1411
700
1497
641
1282
573
693
479
MAX
1652
2416
1038
1724
1476
2432
2404
2349
2443
1893
1202
2247
1745
1138
1204
1008
1181
1120
1033
1644
1111
462
400
443
363
1412
1161
1890
1011
1969
1738
1920
1845
2603
2586
2714
2227
1355
AVQ
2029
1439
1269
1489
1439
1797
1240
1856
1945
2348
2020
2199
2155
2069
2180
1375
1754
2467
2460
3079
2765
2257
2020
2118
2091
2286
2057
1745
1914
2121
2251
1674
1737
1666
1622
1772
1506
1991
CL-
MIN
1418
1099
1170
1418
1170
1219
1240
815
1418
1985
2020
1560
1666
1595
1489
850
1737
1701
1595
2517
2481
2162
1843
1985
2091
2233
1915
1524
1914
1134
2127
1240
1630
1099
921
131 1
1276
1772
MAX
2517
2127
1382
1560
1808
2375
1240
2623
2552
2836
2020
3332
2836
2446
2659
1701
1772
3084
3084
3722
3049
2340
2198
2269
2091
2340
2199
2056
1914
2446
2375
2127
1808
2375
2304
2800
1737
2269
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA (CONTINUED)
RUN
NO.
539-2A
540-2A
54 1-2 A
542-2A
543-2A
544-2A
545-2A
546-2A
547-2A
548-2A
549-2A
550-2A
S51-2A
552-2A
553-2A
554-2A
555-2A
556-2A
557-2A
558-2A
S59-2A
560-2A
ANALY
TICAL
POINT
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
AVG
5.66
5.96
5.88
5.60
5.89
5.85
5.40
5.99
5.53
5.93
5.50
5.83
5.39
5.95
5.48
6.00
5.55
5.88
5.40
5.82
5.35
5.93
5.60
5.99
5.50
5.83
5.98
5.94
5.55
5.96
5.85
5.95
5.47
5.84
5.39
5.84
5.40
5.61
PH
MIN
5.40
5.. 55
5.85
5.60
5.85
5.80
5.40
5.90
5.40
5.85
5.50
5.60
5.25
5.85
5.45
5.90
5.45
5.80
5.35
5.55
5.35
5.85
5.60
5.95
5.50
5.75
5.95
5.85
5.55
5.85
5.10
5.85
5.29
5.60
4.95
5.35
5.20
5.20
MAX
5.90
6.50
5.90
5.60
5.95
5.90
5.40
6.15
5.85
6.00
5.50
6.10
5.55
6.00
5.50
6.10
5.65
6.00
5.45
5.95
5.35
6.00
5.60
6.05
5.50
5.90
6.00
6.10
5.55
6.15
6.60
6.05
5.65
6.10
5.90
6.30
5.75
6.20
TOTAL
AVG
4490
3531
3118
4318
3848
6145
5437
5695
5619
5763
4965
5363
5198
4240
4381
3138
4012
5205
5166
6432
5821
4149
3795
3739 .
3822
5818
4684
4741
4829
5596
5691
4535
5058
4870
5071
4664
4007
4296
IONS, PPM
MIN MAX
2719
2693
2937
3644
3484
5646
5437
3607
4675
4761
4965
3793
4043
3509
3398
1918
3390
4090
4014
4701
4833
3868
3676
3378
3822
5817
4654
4197
4829
4367
5572
3485
4582
3583
3416
3161
3261
3634
5965
5368
3551
4992
4710
6644
5437
6947
7276
6834
4965
7657
6604
5435
5882
4486
4634
6107
6197
8611
6810
4449
3914
4125
3822
5819
4714
5232
4829
6302
5810
5865
5470
6976
7152
6556
5059
4852
PERCENT
GYPSUM
SATURATION
AVG MIN MAX
52
45
35
75
55
134
122
114
103
88
67
94
85
40
42
38
52
65
65
76
62
26
22
17
22
92
60
94
73
109
104
79
97
87
97
71
55
47
15 97
14 122
22 53
49 102
37 79
129 140
122 122
70 137
63 153
58 118
67 67
24 162
21 133
22 78
21 83
14 78
16 89
46 82
44 80
31 133
39 85
19 30
17 28
5 27
22 22
92 93
52 69
73 132
73 73
95 129
89 119
38 122
78 118
31 153
61 160
22 150
27 122
25 70
PERCENT
IONIC
IMBALANCE
AVG MIN
4.6 -7.0
4.1 -1.9
4.0 -6.5
0.4 0.1
-1.4 -6.5
-1 .3 -16.3
-1.3 -1 .3
-2.7 -11 .4
-3.1 -11 .3
2.1 -2.1
-2.9 -2.9
-1.4 -16.6
-2.0 -15.3
2.6 -2.3
-0.1 -1 -8
12.7 7.9
5.3 -2.0
3.4 -0.9
1.8 -5.1
5.6 -4.8
12.3 9.7
2.7 -0.9
6.0 5.1
-2.4 -4.3
-3.4 -3.4
-1.3 -3.9
6.2 1.9
3.6 -4.1
19.7 19.7
-2.8 -10.3
-4.2 -11 .3
-1.4 -10.4
-7.0 -8.6
0.6 -12.1
-11 .9
-3.2 -13.7
0.6 -11 .7
-1.4 -11.1
MAX
17.8
9.1
11.3
0.6
3.0
13.7
-1.3
13.2
10.5
5.2
-2.9
10.6
15.8
16.1
1.3
17.2
12.5
9.9
7.9
15.0
14.9
6.8
6.8
1.7
-3.4
1.4
10.4
11.6
19.7
3.1
2.9
6.0
-4.5
17.6
16.7
9.7
13.0
10.4
B-79
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA
CONCENTRATIONS IN LIQUID, PPM
ANALY
RUN TICAL
NO. POINT
561-2A 2816
2825
562-2A 2816
2825
562-2B 2816
2825
563-2A 2816
2825
564-2A 2816
2825
565-2A 2816
2825
566-2 A 2816
2825
567-2A 2816
m 2825
i 568-2A 2816
g 2825
569-2A 2816
2825
569-2B 2816
2825
S70-2A 2816
2825
571-2A 2816
2825
571-28 2816
2825
572-2A 2816
2825
573-2A 2816
2825
575-2 A 2816
2825
576-2A 2816
2825
576-2B 2816
2825
577-2A 2816
2825
578-2A 2816
2825
579-2A 2816
CA-H-
AVG MIN MAX
1344 864 2250
1233 * 679 2700
1598 1305 2280
777 378 1295
1256 1017 1365
1170 910 1355
1245 784 1780
843 584 1140
846 677 1032
1271 960 1971
1331 1220 1460
1437 1140 1930
1680 1540 1930
1707 1320 2155
2215 1970 2375
2008 1690 2320
1971 1575 2300
1556 1200 2250
1549 1435 1665
AVG
363
364
403
373
404
382
490
415
447
522
451
492
486
484
616
568
537
512
529
MG++
MIN
328
319
345
317
372
320
327
307
418
410
425
429
417
407
577
517
471
429
471
MAX
417
451
445
416
491
461
598
501
496
712
502
576
559
540
647
616
609
586
591
AVG
74
74
112
120
128
581
119
73
120
120
148
69
113
224
106
106
116
76
403
503-
MIN
8
8
16
52
80
432
56
24
28
72
24
32
64
72
72
24
32
24
248
MAX
268
160
168
192
224
678
488
192
208
176
240
104
160
424
144
144
208
248
632
AVG
1040
775
1038
568
2363
1887
1311
812
1715
2251
2266
2216
2144
2031
1951
1759
1546
1290
2198
S04=
MIN
595
240
451
321
2169
1252
658
544
1267
2095
2087
2021
1788
1652
1725
1629
1025
1030
2059
MAX
1676
2534
1734
941
2663
2669
2097
1684
2244
2391
2448
2695
2575
2228
2168
1891
2078
1808
2364
AVG
2592
2624
2935
2002
2082
1706
2493
2005
1729
2269
1888
2400
2880
3051
3888
3589
3862
3488
2743
CL-
MIN
1950
1772
2481
1347
1772
1560
1879
1524
1595
1347
1545
1950
2552
2304
3616
3190
3403
3084
2446
MAX
3332
3545
3442
2783
2304
1808
3226
2410
1915
3124
2588
3226
3510
4077
4148
4006
4148
4219
3261
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA (CONTINUED)
RUN
NO.
56 1-2 A
562-2A
562-2B
563-2A
564-2A
565-2A
566-2A
567-2A
568-2A
569-2A
569-2B
570-2A
571 -2A
571-2B
572-2A
573-2A
575-2A
576-2A
576-2B
577-2A
578-2A
S79-2A
ANALY
TICAL
POINT
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
AVQ
5.90
5.91
5.72
5.96
5.26
5.24
5.82
5.96
5.59
5.50
5.50
5.77
5.79
5.23
5.S1
5.59
5.63
s.ae
5.22
PH
MIN
5.70
5.75
5.50
5.75
5.10
.
5.15
5.15
5.85
5.47
5.36
5.47
5.65
5.68
5.15
5.48
5.49
5.48
5.67
5.12
MAX
6.20
6.10
5.85
6.15
5.40
5.30
6.00
6.05
5.86
5.60
5.56
5.85
5.89
5.40
5.54
5.68
5.76
6.21
5.35
TOTAL
AVG
5520
5169
6208
3946
6342
5817
5761
4244
4953
6551
6182
6725
7413
7614
8913
8157
8166
7041
7530
PERCENT
GYPSUM
IONS, PPM SATURATION
MIN
4214
3556
5145
2592
5688
4772
4518
3217
4386
5279
5927
5913
6998
6302
8632
7396
6673
6213
6873
MAX AVG
7859 63
9237 46
8110 65
5401 27
6780 124
6778 100
7114 70
5219 38
5533 74
8122 109
6706 118
7857 117
8127 122
8920 117
9452 117
8874 105
9243 94
8957 73
8079 118
MIN MAX
33 113
15 173
29 113
14 56
112 145
64 142
29 126
23 84
54 104
91 132
114 128
101 150
110 140
94 127
107 131
95 118
56 136
55 116
112 126
PERCENT
IONIC
IMBALANCE
AVG
3.1
2.6
8.4
1.5
-12.1
-10.1
4.6
4.6
-6.8
-4.0
2.4
-0.1
-1.0
-4.1
7.3
7.1
2.0
-3.5
-7.1
MIN
-4.6
-11.9
2.4
-10.1
-16.9
-14.7
-11 .9
-3.5
-17.6
-11 .8
-4.5
-«.6
-6.2
-12.0
-1.9
3.6
-8.1
-10.6
-10.8
MAX
13.2
18.6
17.4
16.1
-0.3
0.7
15.2
17.0
6.2
6.9
10.7
10.3
3.1
1.1
19.6
14.8
9.5
15.9
-3.9
B-81
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA
CONCENTRATIONS IN LIQUID, PPM
ANALY
RUN TICAL
NO. POINT
579-2A 2825
580-2A 2816
2825
581-2A 2816
2825
582-2A 2816
2825
583-2A 2816
2825
583-2B 2816
2825
584-2A 2816
2825
585-2A 2816
2825
586-2A 28 16
°° 2825
00 587-2A 2816
ro 2825
588-2A 2816
2825
589-2A 2816
2825
590-2A 2816
2825
590-2B 2816
2825
59 1-2 A 2816
2825
592-2A 2816
2825
593-2A 2816
2825
594-2A 2816
2825
601-2A 2816
2825
602-2A 2816
2825
603-2A 2816
2825
604-2A 2816
2825
CA++
AVG MIN
1415 1415
1894 1025
2579 2579
1833 1228
765 644
362 142
644 435
497 222
662 218
775 624
676 584
1465 1350
1521 1390
1455 1220
1545 1315
620 582
674 588
605 419
660 435
556 400
619 408
557 352
650 384
420 130
351 140
623 307
723 624
MAX AVG
1415 509
2700 473
2579 549
2260 2637
1132 6829
730 10600
752 10569
798 9991
900 9885
916 11418
874 10534
1540 356
1650 316
1670 389
1800 392
726 5372
780 5300
762 9735
868 9645
734 10301
842 10126
664 10175
834 10006
688 2537
788 2898
840 3198
850 3103
MG++
MIN MAX
509 509
391 535
549 549
2079 3309
5239 11359
5799 13878
8599 13373
8199 11639
8279 11839
10139 13658
B7"9 13358
350 364
306 325
304 450
305 430
4199 6209
4399 5839
9199 10379
8819 10520
9480 11600
9000 11760
9400 10760
9060 10600
1011 3489
2529 3339
2534 3759
2874 3504
AVG
320
103
22
415
2838
7476
3996
6907
5848
3179
3658
768
942
251
497
2008
2773
4376
5095
4536
5595
5371
6420
438
425
395
279
S03
MIN
320
11
22
180
1040
452
1990
2442
2623
904
226
508
848
113
226
904
1379
3110
2827
2657
3449
1640
2714
90
171
203
180
m
MAX
320
316
22
904
7237
20807
5428
18545
11534
5428
6083
927
1017
395
870
3222
4127
5880
6729
7803
10404
7859
8255
1040
814
723
452
AVG
2595
2109
1840
5382
19588
27308
31523
25923
30885
31722
32767
1827
2160
1967
2014
19296
18974
31128
30477
31193
30179
30554
30109
7967
7731
8663
8308
S04>
MIN
2595
1626
184C
3815
14202
12692
27077
12212
23183
26604
28273
1311
1740
1733
1490
17036
17052
28443
24186
27359
25876
27392
26761
3506
6549
7599
7263
MAX
2595
2597
1840
7542
27958
32767
32767
32767
32767
32767
32767
2174
2389
2168
2290
21792
21810
34998
35670
36693
36445
33121
33422
9515
9272
10752
9257
AVG
2410
3428
3900
7090
4115
5012
4176
4368
2027
6337
3652
1875
1801
1858
1851
1400
1414
2526
2550
3819
3853
3574
3648
1506
2587
3106
3101
CL-
MIN MAX
2410 2410
1099 4786
3900 3900
5318 8863
2304 6381
2659 8154
3190 6913
3013 6027
1240 3190
4077 9484
1063 9661
1772 1950
1772 1861
1595 2038
1595 1994
1152 1905
1196 1950
2127 3589
2082 3816
3106 4482
3151 4748
3062 4571
3106 4659
709 2570
2304 3102
2659 3988
2304 3545
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA (CONTINUED)
RUN
NO.
579-2A
580-2A
581 -2A
582-2A
583-2A
583-2B
584-2A
585-2A
586-2A
5B7-2A
588-2A
589-2A
590-2A
590-28
591 -2A
592-2A
593-2A
594-2A
60 1-2 A
602-2A
603-2A
604-2A
ANALY
TICAL
POINT
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
AVG
5.86
5.49
5.35
5. 54
5.32
5.50
5.36
5.34
5.35
5.41
5.41
5.07
4. 87
5.28
5.07
5.47
5.30
5.40
5.18
5.45
5.24
5.36
5.14
7.09
6.92
6.92
6.89
PH
MIN
5.. 86
5.21
5.35
5.37
4.98
5.16
5.21
5.16
4.98
5.12
5. 25
4.94
4.73
5.02
4.82
5.23
5.07
5.10
4.92
5.20
5.00
5.10
4.90
6.04
6.58
6.04
6.61
MAX
5.86
5.62
5.35
5.75
5.70
5.98
5.54
5.54
5.90
5.78
5.70
5.16
4.95
5.48
5.33
5.75
5.67
5.64
5.41
5.70
5.80
5.60
5.40
7.71
7.39
„ . - — -
7.66
7.11
TOTAL
AVG
7351
8116
9010
17592
32767
32767
32767
32767
32767
32767
32767
6407
6861
6037
6414
28837
29276
48479
48534
50530
50500
50354
50954
12937
14061
16084
1 5633
IONS. PPM
MIN
7351
5390
9010
14786
26482
31944
32767
32767
32767
32767
32767
5824
6260
5411
5980
24037
24892
44846
43054
46318
45671
46326
46367
6075
12096
14151
14302
MAX
7351
10026
9010
21225
32767
32767
32767
32767
32767
32767
32767
6839
7267
6661
7310
32605
32592
52378
54977
57037
59078
54018
56372
15512
15562
18701
17408
PERCENT
GYPSUM
SATURATION
AVG
133
125
122
139
111
56
107
73
113
122
117
109
132
113
118
104
112
105
113
93
102
92
107
58
43
76
86
MIN MAX
133 133
100 145
122 122
111 187
95 175
13 1 18
72 124
26 129
30 149
104 159
101 153
79 129
106 148
104 127
94 130
92 123
89 126
73 138
64 158
68 129
66 143
59 1 12
68 136
17 97
19 93
38 109
75 103
PERCENT
IONIC
IMBALANCE
AVG MIN
-12.3 -12.3
-4.5 -12.6
16.3 16.3
-2.4 -6.9
1.6 -14.0
-0.3 -10.6
3.1 -10.2
2.0 -9.6
0.1 -13.8
6.9 -5.2
2.3 -11.2
-3.5 -6.8
-12.6 -15.0
7.9 -3.3
5.4 -9.9
-3.0 -8.8
-6.3 -13.1
0.7 -9.7
-0.5 -14.3
0.8 -8.9
-1.1 -11 .3
-0.2 -5.8
-3.5 -12.1
5.0 -10.6
4.9 -12.9
6.1 -10.2
9.3 3.3
MAX
-12.3
6.0
16.3
2.4
12.0
10.8
12.3
18.4
14.0
13.5
12.1
-0.4
-11.1
12.6
13-8
3.7
1.6
12.7
13.2
14.8
6.9
8.8
6.0
15.8
13.7
15.1
15.7
B-83
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA
CONCENTRATIONS IN LIQUID, PPM
DO
i
CO
ANALY
RUN TICAL
NO. POINT
605-2A 2816
2825
606-2A 2816
2825
607-2A 2816
2825
608-2A 2816
2825
608-2B 2816
2825
609-2A 2816
2825
610-2A 2816
2825
611-2A 2816
2825
612-2A 2816
2825
613-2A 2816
2825
614-2A 2816
2825
615-2A 2816
2825
616-2A 2816
2825
617-2A 2816
2825
618-2A 2816
2825
618-2B 2816
2825
619-2A 2816
2825
620-2A 2816
2825
621-2A 2816
2825
622-2A 2816
2825
622-2B 2816
2825
623-2A 2816
CA-M-
AV6 MIN MAX
371 207 592
71 6 ' 628 836
492 75 760
926 850 1034
593 80 944
805 652 1094
121 5 406
183 55 353
417 64 782
785 169 1212
339 106 878
659 282 1082
859 255 1254
1155 1048 1384
869 760 998
1124 1054 1166
834 628 930
1048 966 1156
749 107 926
783 600 966
1133 1025 1430
2701 1700 3255
3108 2775 3520
2735 2010 3860
3046 2600 4370
1620 1500 1915
1924 1665 2175
1551 1375 1905
1662 1350 2150
569 100 708
696 116 960
628 524 746
727 580 810
660 528 850
799 575 1090
622 220 1076
724 292 1070
707 636 844
970 826 1052
510 158 900
AVG
3063
2887
4859
5032
4818
4961
4928
4833
3536
3668
3379
3385
3873
3769
4056
4290
4101
3969
3470
3734
3690
219
229
521
521
361
373
382
378
3124
3113
2733
2725
2686
2694
5280
5274
2665
2674
2742
MG++
MIN
2429
2519
3629
4909
4389
4649
4059
4509
2809
2929
2869
3019
3333
3539
3419
3879
3499
3549
2719
3149
3129
80
91
353
355
319
337
347
342
2599
2579
2329
2349
2139
2229
3310
3120
2380
2230
2320
MAX
3454
3159
5979
5179
5219
5559
5899
5129
4630
4369
4069
3859
4319
4329
4629
4709
4539
4599
3900
4109
4059
342
375
643
678
429
414
444
424
3999
4229
3289
3139
3124
3049
8160
7780
2960
3030
3400
AVG
394
278
771
2701
632
2538
2779
4712
700
2588
668
2105
300
1628
302
2117
278
1808
392
305
1679
136
1278
124
994
83
861
83
424
407
1103
330
914
312
1025
938
2092
465
1301
411
S03=
MIN
135
45
271
2668
280
1899
384
2917
226
1809
271
1311
113
1334
90
1809
226
1221
248
113
1176
45
361
0
90
22
271
11
11
158
214
248
237
147
294
565
1018
113
498
181
MAX
678
407
2058
2723
2284
3075
6083
6468
2691
4161
1176
2849
520
1967
542
2736
361
2193
1357
497
2353
339
1854
226
1402
135
1323
169
1017
1492
1956
418
1922
452
2148
1470
2601
1153
1922
746
AVG
8126
8721
15002
16316
14725
16362
11530
11488
9482
10067
8276
8625
9445
9667
9638
10233
9812
9955
8891
9718
9933
1498
1989
1560
2170
1985
2435
1993
2161
10778
10842
9861
10057
10185
10084
17207
16801
8852
9137
9022
S04*
MIN
6828
7046
9953
15026
10905
13368
9438
8160
7290
7677
7141
6815
8127
9037
6964
9919
9286
9440
8047
8017
8242
580
1147
827
631
1786
1930
1787
1994
9210
9054
8865
8308
8051
8052
12019
11584
8034
8250
7740
MAX
9362
9525
17594
17543
16438
21964
13840
13852
11796
11966
9684
10269
10360
10797
10913
10742
10668
10307
9791
11173
11053
2200
3252
1923
3279
2214
2650
2191
2622
12778
13642
11719
12461
11437
11814
26052
25066
10044
10158
11918
AVG
2694
2499
2581
2540
2312
2175
2974
3332
3510
3496
3515
3567
5186
5282
5598
5908
5554
5140
4236
4482
4595
4056
4106
4588
4653
2327
2350
2400
2381
2155
2159
1883
1882
1600
1600
2236
2285
1491
1526
1616
CL-
MIN
2393
1861
2304
2481
1950
1861
1879
3013
2840
2481
2659
2747
4609
5052
4786
5672
4609
4857
2127
3900
4148
2481
2659
3651
3634
1861
2171
2215
2127
1728
1772
1329
1506
1285
1240
1598
1598
1331
1287
1021
MAX
3013
2836
3013
2659
2659
2659
4431
4077
4609
4875
5052
4343
6204
5584
6027
6204
6293
5672
5229
5140
5495
5140
5229
6115
6115
2659
2605
2659
2659
2481
2481
2393
2393
2082
2082
3239
3417
1731
1775
2130
-------
RUM SUMMAKY
LIQUID ANALYTICAL DATA (CONTINUED)
ANALY
RUN TICAL
NO. POINT
605-2 A 2816
2825
606-2 A 2816
2825
607-2A 2816
2825
608-2A 2816
2825
608-2B 2816
2825
609-2A 2816
2825
610-2A 2816
2825
611-2A 2816
2825
612-2A 2816
2825
613-2A 2816
2825
6 14-2 A 2816
2825
61S-2A 2816
2825
616-2A 2816
2825
6 17-2 A 2816
2825
6 18-2 A 2816
2825
618-28 2816
2825
619-2A 2816
2825
620-2 A 2816
2825
621-2A 2816
2825
622-2A 2816
2825
622-28 2816
2825
B23-2A 2816
AVG
6.95
7.95
7.94
5.15
7.94
5.03
7.96
5.84
7.01
4.96
7.96
5.44
7.96
5.07
7.96
4.91
6.88
4.87
8.12
7.07
4.95
7.92
4.38
7.99
4.67
6.97
4.97
6.97
5.76
6.94
5.77
7.19
5.84
7.04
5.62
6.95
5.54
6.85
5.48
7.04
PH
MIN
6.79
7.83
7.67
5.06
7.75
5.02
7.83
5.48
6.82
4.83
7.73
5.06
7.78
4.87
7.81
4.58
6.74
4.68
7.83
6.86
4.77
5.74
4.12
7.70
4.32
6.40
4.75
5.73
5.16
5.21
5.14
6.68
4.79
6.65
5.15
6.50
5.20
5.90
5.20
6.45
MAX
7.10
8.21
8.20
5.24
8.20
5.06
8.10
6.19
8.11
5.08
8.17
7.97
8.11
5.17
8.15
5.24
7.10
5.02
8.56
7.50
5.07
8.32
4.73
8.14
7.95
7.67
5.50
7.37
8.20
8.08
7.00
8.16
7.36
7.75
6.41
7.20
6.70
7.10
6.00
7.90
TOTAL
AVG
14754
15192
23789
27606
23170
26934
22421
24632
17744
20701
16285
18447 .
19802
2*630
20620
23836
20719
22063
17849
19162
21169
8763
10867
9690
11566
6497
8064
6537
7139
17162
16050
15559
16433
15578
16338
26374
27269
14263
15693
14391
IONS, PPM
MIN MAX
13271
13506
17497
26067
20830
24075
18206
23061
14409
17934
14290
16072
18179
20334
17653
22790
18779
20233
14411
17489
19578
6041
8963
7637
8389
6204
7464
6262
6224
14711
15700
13874
14966
12698
14344
18634
19354
13162
13854
12085
16274
16247
27537
29046
24731
32767
26570
26409
21745
23155
19501
21309
20907
23237
22636
24688
22187
23893
19482
20428
22707
10208
12165
12317
14478
6974
8691
7083
8390
20696
21972
17797
18443
1 7498
18036
39655
39455
15290
16566
17876
PERCENT
GYPSUM
SATURATION
AVG MIN MAX
46
93
73
138
87
125
15
21
52
96
40
77
96
130
96
123
93
119
86
92
133
117
157
107
150
121
154
118
130
85
102
94
109
103
120
97
109
98
132
72
24 79
82 112
11111
127 160
9 135
89 194
1 51
7 35
8 96
22 157
12 105
29 134
30 138
120 155
76 109
114 139
77 108
116 122
15 104
77 100
112 154
50 171
94 259
52 123
48 233
110 136
133 170
102 133
115 163
15 114
17 143
82 116
94 122
74 128
86 149
36 170
47 170
88 114
116 149
23 130
PERCENT
IONIC
IMBALANCE
AVG MIN
6.7
6.1
5.0
-3.4
9.3
-2.6
5.0
-10.1
0.2
-8.4
3.1
-5.9
4.0
-5.3
4.1
-4.7
3.8
-4.2
3.2
3.9
-4.0
5.1
-5.9
10.2
-0.6
4.6
-6.4
1.3
-3.9
-2.1
-6.6
-2.9
-8.1
-2.8
-5.7
4.4
0.6
7.3
1.7
3.8
-3.4
-2.4
-11.6
-5.8
-2.0
-14.7
-6.3
-14.5
-11 .7
-14.8
-13.5
-12.2
-11.5
-11 .9
-1 .1
-9.9
-4.0
-11.6
-13.2
-7.3
-14.1
-5.4
-17.0
-0.9
-14.6
-5.9
-14.5
-5.1
-11.7
-15.1
-14.9
-10.6
-14.5
-12.9
-14.4
-3.9
-12.1
-2.5
-11.6
-6.6
MAX
12.3
9.8
15.6
0.4
17.4
4.1
14.9
-€.8
12.9
0.2
11.7
-1.3
10.7
-0.5
13.3
3.1
10.2
3.6
10.9
10.6
5.2
14.0
9.5
1S.1
16.7
14.0
5.2
13.7
7.2
5.9
3.6
9.2
8.7
11.3
6.6
11.7
13.4
12.0
9.0
14.9
B-85
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA
CONCENTRATIONS IN LIQUID. PPM
03
I
CO
en
RUN
NO.
623-2A
624-2A
625-2A
701-2A
702-2A
703-2A
704-2A
705-2A
706-2A
707-2A
708-2A
709-2A
710-2A
711-2A
712-2A
713-2A
714-2A
714-2B
715-2A
716-2A
7 17-2 A
7 18-2 A
ANALY
TICAL
POINT
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
28*5
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
CA-M-
AVQ MIN MAX
670 356 1000
522 206 962
861 330 1332
1497 838 2380
1698 1130 2475
171 1 979 3419
1670 1025 2240
1074 612 1455
1081 590 1557
1197 700 1790
1246 712 1755
1499 1035 2195
1570 1055 2385
1244 677 1875
1277 689 1910
1719 1320 2310
1798 1305 2330
1406 1125 2155
1426 1150 2070
1368 1190 1545
1534 1370 1790
1229 1050 1405
1317 1055 1535
1325 1060 1677
1459 1215 1700
1243 1020 1570
1587 1485 1690
991 618 1390
1003 618 1445
965 782 1300
980 795 1252
988 264 1540
1007 258 1685
306 260 374
317 204 391
1402 1095 1670
1414 1035 1717
1391 1180 1725
1424 1240 1755
1238 452 1905
1260 459 1930
1494 1165 1880
AVG
2671
2641
2587
360
371
291
289
599
614
545
551
557
552
633
639
687
703
551
548
453
470
411
402
443
441
486
472
436
427
372
375
493
481
254
294
427
415
414
414
441
437
453
MG++
MIN
2230
2140
2100
136
51
69
72
413
414
473
467
203
217
524
539
542
556
475
479
325
331
345
346
360
285
452
467
290
299
307
306
288
258
189
214
371
365
366
357
329
329
384
MAX
3370
3180
3160
560
578
511
495
839
879
619
622
629
664
714
738
837
831
637
655
559
575
449
477
519
524
551
478
542
561
416
440
642
699
392
380
565
499
481
496
696
688
506
AVG
1414
478
1777
153
850
132
117
64
101
142
354
144
386
139
236
125
234
100
121
403
829
311
625
305
725
93,
158
93
134
133
149
164
166
120
116
123
192
142
211
135
173
124
S03*
MIN
633
204
1221
23
204
22
22
22
22
33
90
22
113
45
67
22'
45
11
11
248
463
45
260
56
350
45
158
33
56
22
33
56
45
22
79
33
67
56
113
45
45
56
MAX
4071
882
2330
588
1447
1198
271
203
452
361
723
407
995
384
497
350
859
192
226
680
1337
633
1121
667
995
147
158
147
271
452
260
407
316
178
147
203
357
214
452
260
395
180
AVG
8972
7963
8205
1806
1970
726
712
458
509
459
584
1261
1393
1280
1304
2301
2450
1904
1913
2222
2380
2089
2154
2087
2252
1524
1989
1273
1299
1995
2066
1638
1720
551
662
1800
1892
1963
2109
1689
1758
2001
S04*
MIN
5848
6799
6996
863
806
213
213
67
269
218
165
326
368
420
284
1944
1867
1404
1470
1604
1834
1821
1836
1710
1569
1170
1979
741
738
1610
1604
536
560
359
622
1464
1532
1711
1831
688
713
1795
MAX
11641
9113
9595
2724
2737
2898
2417
1238
1247
845
989
2579
3045
3029
3045
2754
3170
2421
2193
2805
3333
2680
2606
2659
2720
1979
1999
2249
2156
2580
2705
2775
2747
722
695
2085
2378
2114
2621
2661
2793
2324
AVG
1616
2014
• 2014
2165
2140
3127
3079
3040
3089
3178
3220
3169
3195
2856
2902
3230
3323
2825
2854
1971
2013
1671
1700
1729
1686
2184
2270
1990
1980
1146
1152
1757
1741
761
930
2307
2223
2107
2099
2125
2095
2366
CL-
MIN
932
1S98
1598
1154
1154
2127
1950
1772
1701
2149
2171
1418
1462
1861
1994
1728
2526
2082
2105
1598
1644
1506
1506
1063
1107
2038
2215
1506
1373
866
797
753
753
531
531
1595
1595
1595
1551
1347
1329
1905
MAX
2130
2840
2884
3728
3550
4254
4077
3944
4254
3988
4033
4143
4121
3678
3722
4653
4431
4099
3855
2304
2393
1905
1950
2260
2149
2348
2326
2304
2504
1772
1772
2623
2597
1373
1418
3279
2836
2659
2535
3235
2969
3013
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA (CONTINUED)
RUN
NO.
623-2A
624-2A
625-2A
701 -2A
702-2A
703-2A
704-2A
705-2A
706-2A
707-2A
708-2A
709-2A
710-2A
711-2A
712-2A
713-2A
714-2A
714-28
715-2A
716-2A
717-2A
718-2A
ANALY
TICAL
POINT
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2829
AVG
5.37
7.03
5.16
7.98
5.15
5.80
5.20
5.85
5.28
5.67
5.08
5.67
4.99
5.85
5.20
5.55
5.07
5.59
5.21
5.21
4.92
5.34
4.97
5.41
4.93
5.65
5.02
5.85
5.16
5.73
5.26
5.76
5.31
6.13
5.77
5.74
5.22
5.72
5.24
5.90
5.39
5.79
PH
MIN
4.70
6.70
4.90
5.70-
4.50
5.00
4.96
5.54
4.91
5.40
4.79
5.20
4.50
5.66
4.92
5.17
4.65
5.43
5.00
5.02
4.68
4.89
4.63
5.16
4.57
5.43
4.96
5.64
5.00
5.60
5.14
5.46
3.62
6.03
5.70
5.52
5.00
5.53
5.03
5.58
4.70
5.62
MAX
5.79
7.30
5.60
9.00
6.10
7.98
5.78
6.08
5.50
5.91
5.36
6.10
5.45
5.95
5.43
6.00
5.58
5.79
5.45
5.40
5.33
5.54
5.12
5.77
5.28
5.83
5.07
6.04
5.40
5.92
5.40
6.04
5.79
6.19
5.87
5.98
5.58
5.95
5.49
6.12
5.87
5.95
TOTAL
AVG
15432
13717
15547
6078
7127
6090
5968
5308
5469
5580
6015
6679
7146
6200
6406
8125
8572
6848
6926
6515
7325
5813
6305
5994
6667
5636
6576
4890
4949
4664
4777
5209
5284
2075
2415
6175
6257
6128
6368
5744
5838
6565
IONS. PPM
MIN MAX
12510
11883
13782
3653
4941
4065
4262
3219
3209
3820
4043
4882
5029
4246
4349
6102
7216
5604
5729
5508
6529
5142
5187
4836
5132
5002
6435
3414
3249
3960
4041
2016
1933
1585
1710
5015
5071
5474
5850
3976
3866
6019
18705
16332
17746
8696
9740
10787
8347
6642
7090
6985
7054
9149
10367
8537
8892
9996
10049
9417
8862
6951
6225
6519
7530
6894
7601
6369
6718
6362
6889
5689
5816
6849
7538
3011
3082
7436
7313
6906
6992
7423
7720
7441
PERCENT
GYPSUM
SATURATION
AVG MIN MAX
94
68
112
108
122
50
48
21
23
24
30
70
79
62
64
118
126
98
99
118
130
109
117
110
124
79
113
62
64
96
100
75
80
19
21
100
106
109
117
89
93
111
52 148
28 127
44 181
52 170
51 161
17 235
17 171
3 64
12 65
11 41
8 49
16 151
19 187
16 162
11 166
97 153
99 155
66 147
70 134
86 143
103 177
88 143
90 142
84 131
89 149
57 107
110 116
33 118
36 110
73 136
75 141
17 124
18 141
13 27
18 26
75 118
80 133
101 121
105 136
18 145
18 170
101 132
PERCENT
IONIC
IMBALANCE
AVG MIN
-4.8 -14.2
4.5 -10.9
-5.4 -16.8
4.4 -9.6
-3.8 -13.4
4.8 -12.5
5.0 -8.6
8.0 -11 .1
6.1 -15.0
3.4 -12.1
-2.3 -14.5
2.9 -11 .4
-2.3 -13.9
4.5 -4.7
2.6 -8.1
1.6 -12.9
-0.7 -13.8
-3.4 -12.3
-4.1 -11.6
-3.0 -12.0
-7.3 -14.2
-0.3 -10.4
-6.3 -14.9
5.9 -7.1
0.1 -6.6
9.2 2.4
9.9 7.5
4.0 -10.7
2.8 -9.5
4.2 -5.0
3.0 -10.0
8.0 -12.5
6.5 -10.4
9.0 0.5
1.2 -6.4
3.1 -2.9
1.8 -5.8
3.1 -2.3
0.3 -11.4
3.4 -8.2
2.4 -14.4
3.6 -11.5
MAX
9.2
12.4
7.5
15.3
15.2
14.1
14.5
14.7
14.4
10.5
6.1
13.8
9.7
14.9
14.1
15.0
10.4
2.5
1.7
3.4
-1.8
14.0
10.1
19.2
12.1
13.0
12.2
16.4
16.0
11.3
11.8
14.2
13.7
17.2
10.0
13.7
14.4
12.5
10.6
14.2
14.9
11.6
B-87
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA
CONCENTRATIONS IN LIQUID, PPM
TO
i
CO
CO
ANALY
RUN TICAL
NO. POINT
719-2A 2816
2B25
801-2A 2816
2825
801-28 2816
2825
802-2A 2816
2825
803-2A 2816
2825
804-2A 2816
2825
805-2A 2816
2825
2831
806-2A 2816
2825
2831
807-2A 2816
2825
2831
808-2A 2816
2825
2831
809-2A 2816
2825
2831
810-2A 2816
2825
2831
811-2A 2816
2825
2831
812-2A 2816
2825
2831
813-2A 2816
2825
2831
814-2A 2816
2825
2831
8 15-2 A 2816
AVG
1130
1187
953
1002
987
1150
1068
1153
1159
1252
1344
1469
1122
1297
1340
1461
1282
1479
1832
2026
1725
1921
1585
1780
966
1129
1155
1354
1085
1229
1226
1308
1227
CA++
MIN
1015
1012
866
874
930
1070
1010
1068
1030
1087
920
1067
940
1017
1105
1175
957
1250
1570
1740
1400
1535
1395
1445
777
900
897
1085
927
1085
1060
1125
1050
MAX
1260
1470
1080
1106
1065
1260
1200
1255
1355
1470
1930
2190
1470
1687
1565
1732
1605
1900 .
2105
2250
1945
2165
1785
2195
1 152
1325
1387
1592
1395
1577
1352
1490
1470
AVG
415
414
372
368
378
361
382
382
478
477
553
556
539
551
519
543
510
496
513
524
646
631
754
750
393
392
406
416
394
351
411
402
458
MG++
MIN
369
322
277
306
357
307
332
321
409
413
459
423
372
452
439
471
470
340
416
452
549
499
562
629
288
254
335
307
178
201
372
381
395
MAX
519
549
448
435
420
392
490
486
555
561
630
639
639
650
610
594
591
560
594
620
733
754
904
882
562
452
499
528
637
439
517
442
529
AVG
166
272
109
319
180
595
101
331
141
510
64
351
188
647
433
872
123
462
622
1104
447
970
95
567
62
427
155
637
91
530
432
737
126
503 =
MIN
79
79
45
79
102
362
34
204
33
180
11
79
11
294
192
576
0
11
22
316
33
350
5
248
11
101
33
158
22
316
180
327
90
MAX
260
429
237
678
351
1074
158
452
463
1085
158
678
474
1062
701
1 153
361
1017
1967
2046
949
1583
531
1402
169
893
723
1605
452
1130
904
1187
158
AVG
2080
2177
2299
2457
2133
2326
1987
2207
2164
2267
2079
2347
2334
2676
2186
2244
1948
2327
21 11
2263
2194
2427
2283
2531
2166
2563
2015
2209
1807
1898
2218
2133
2128
S04*
MIN
1933
1822
2133
2149
1959
2223
1880
1805
1867
1919
1685
1760
2078
2182
1966
1984
1669
1784
1689
1623
1696
1391
2017
1942
1722
1783
1763
1068
1295
634
1792
1678
1962
MAX
2210
2380
2457
2665
2400
2446
2285
2541
2665
2522
2467
2828
2606
3090
2353
2732
2452
2974
2859
2797
2692
2891
2614
2958
2778
3262
2549
2707
2026
2581
2858
2663
2239
AVG
1524
1501
966
932
1137
1132
1469
1454
1850
1840
2319
2353
1581
1574
1961
1905
2116
2089
2922
2919
2957
2988
3052
3013
1303
1268
1712
1694
1657
1495
1655
1635
1564
CL-
MIN
1123
1196
799
799
1063
975
1321
1331
1750
1684
1573
1595
1307
1307
1506
1462
1506
1462
2260
2260
2659
2792
2747
2792
952
842
1196
1240
1063
1107
1418
1240
1285
MAX
2127
1950
1462
1119
1287
1287
1677
1598
1994
2038
3368
3722
2087
2127
2393
2393
2880
2925
3456
3589
3235
3279
3323
3213
1861
1905
2348
2260
2614
2082
1950
1905
1950
-------
RUM SUMMARY
LIQUID ANALYTICAL DATA (CONTINUED)
RUN
NO.
719-2A
80 1-2 A
801-2B
802-2A
803-2A
804-2A
805-2A
806-2A
807-2A
808-2A
8O9-2A
810-2A
811-2A
812-2A
8 13-2 A
8 14-2 A
8 15-2 A
ANALY
TICAL
POINT
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2816
2825
2831
2816
2825
2831
2816
2825
2831
2816
2825
2831
2816
2825
2831
2816
2825
2831
2816
2825
2831
2816
2825
2831
2816
2825
2831
2»16
2825
2831
2816
AVG
5.76
5.24
5.87
5.21
5.74
5.09
5.78
5.07
5.05
3.79
5.06
3.86
5.30
4.59
5.35
4.82
5.47
4.80
5.11
4.71
5.24
4.73
5.44
4.83
5.83
5.16
5.57
5.09
5.34
4.59
5.36
4.98
6.26
PH
MIN
5.54
5.02
5.63
4.89
5.46
4.95
5.71
4.95
4.71
3.29
4.85
3.29
4.74
4.03
5.25
4.70
5.16
3.78
4.91
4.45
5.02
4.52
4.83
4.07
5.60
4.86
5.33
4.86
5.19
4.24
5.16
4.70
6.00
TOTAL IONS, PPM
MAX
6.04
5.49
5.97
5.66
5.90
5.29
5.97
5.29
5.29
4.33
5.33
4.65
5.57
4.98
5.49
4.92
5.81
5.04
5.27
4.96
5.81
5.04
5.71
5.25
6.06
5.69
5.87
5.67
5.45
4.73
-.
5.75
5.40
6.41
AVG
5412
5650
4795
5179
4908
5657
5098
S623
5899
6455
6503
7219
5931
6907
6580
7161
6137
7010
8167
9005
8173
9141
7975
8851
5016
5904
5547
6412
5145
5613
6067
6334
5608
MIN
5002
5088
4517
4790
4654
5375
4800
4865
5501
5983
5377
5816
5420
6323
5650
6343
5594
6158
7729
8389
7234
8004
7440
8117
4591
5380
5029
5312
4063
4285
5307
5662
5227
MAX
6120
6448
5373
5844
5335
6327
5685
6263
6543
7039
7711
8533
6909
7891
7334
BO 63
6857
8044
8991
9819
9448
10408
8474
9433
5485
6424
7082
7302
6536
6772
6610
7200
6203
PERCENT
GYPSUM
SATURATION
AVG
104
111
108
118
103
121
100
114
104
113
101
118
104
126
110
115
97
123
123
135
116
134
109
127
102
127
103
119
92
103
115
115
107
MIN MAX
96 115
93 129
95 120
102 136
98 114
116 127
94 107
94 134
87 126
93 129
96 112
95 137
90 1 24
104 142
93 127
104 132
90 114
101 149
98 152
106 161
94 144
85 166
93 127
99 161
90 139
93 158
89 130
66 140
76 119
41 139
99 148
100 138
99 116
PERCENT
IONIC
IMBALANCE
AVG MIN
3.2 -14.7
1.9 -14.4
3.9 -12.8
-2.5 -14.7
•2.8 -4.0
-5.7 -11 .6
2.6 -2.9
-3.3 -10.9
-0.1 -10.5
-6.2 -12.0
5.4 -6.5
-0.8 -14.8
7.6 0.7
-0.6 -6.0
2.7 -8.9
0.3 -7.6
7.1 -6.0
0.8 -6.5
-1.9 -13.5
-4.7 -14.1
4.2 -9.4
-2.8 -13.2
8.1 -8.6
3.4 -13.3
1.3 -10.0
-7.7 -14.5
2.0 -7.5
-3.5 -13.8
3.6 -13.8
-0.7 -12.1
-4.2 -14.5
-8.2 -14.3
10.4 2.5
MAX
14.5
11.7
12.9
4.8
11.2
-1.2
10.6
6.9
7.5
4.1
13.7
13.8
11.3
3.6
13.4
7.7
14.6
11.4
4.7
5.8
13.6
14.8
14.8
14.0
12.2
2.7
9.8
14.9
11.6
11.5
8.9
6.4
ii.9
B-89
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA
CONCENTRATIONS IN LIQUID, PPM
03
I
10
o
ANALY
RUN TICAL
NO. POINT
815-2A 2825
8 16-2 A 2816
2825
2832
817-2A 2816
2825
2832
818-2A 2816
2825
2832
818-28 2816
2825
819-2A 2816
2825
820-2A 2816
2825
82 1-2 A 2816
2825
AVG
1254
1026
1068
1053
1209
1115
1150
1180
1189
1300
1433
1411
1548
640
684
CA++
MIN MAX
1040 1530
980 1120
1035 1120
945 1260
1090 1385
1035 1200
1070 1290
1035 1475
1050 1525
1080 1530
1130 1725
1200 1725
1335 1900
488 874
530 924
AVG
439
415
433
406
388
453
437
464
449
379
380
369
363
5852
5928
MG++
MIN
389
379
389
367
324
360
363
403
333
326
324
320
31j
4820
4650
MAX
524
.472
469
441
454
543
490
612
590
430
425
617
406
6360
6470
AVG
222
90
272
155
470
111
211
112
223
329
669
260
597
1496
2030
503-
MIN
135
11
22
67
119
67
101
56
99
11
45
22
204
90
656
MAX
395
158
568
350
802
203
361
180
373
1153
1673
915
1277
2695
3573
AVG
2231
2084
2133
2096
2311
1994
2039
2211
2164
2055
2195
2006
2129
20731
20482
S04 =
MIN
2128
1902
1953
1909
1921
1797
1810
2015
2008
1777
1626
1550
1585
17395
17099
MAX
2414
2217
2307
2270
2719
2141
2281
2341
2336
2728
2866
2474
2632
24153
24080
AVG
1442
1233
1211
1311
1294
1545
1491
1556
1528
1628
1596
1808
1772
2605
2615
CL-
MIN
1152
1107
1063
1107
1152
1373
1373
1373
1373
1376
1331
1595
1551
1819
1775
MAX
1950
1373
1329
1506
1506
1728
1684
1772
1861
1950
1905
2969
2171
3905
3861
-------
RUN SUMMARY
LIQUID ANALYTICAL DATA (CONTINUED)
RUN
NO.
815-2A
816-2A
817-2A
818-2A
818-2B
819-2A
B20-2A
821-2A
ANALY
TICAL
POINT
2825
2816
2825
2832
2816
2825
2832
2816
2825
2832
2816
2825
2816
2825
2816
2825
2816
2825
AVG
5.33
6.26
5.36
5.84
5.23
6.17
5.43
6.14
5.43
5.57
5.17
5.68
5.33
5.34
S.12
PH
MIN
5.19
6.04
5.16
5.79
4.99
5.99
5.25
5.50
5.23
5.07
4.36
5.29
5.00
5.10
4.90
MAX
5.46
6.42
S.61
5.89
5.54
6.35
5.61
6.40
5.67
6.07
5.48
6.06
5.60
5.90
5.50
TOTAL
AVG
5692
4947
5214
5123
5775
5323
5436
5634
5658
5794
6380
5967
6519
31465
31881
IONS, PPM
MIN
5317
4874
5054
4807
5232
4898
5160
5296
5425
5027
5356
5100
5647
25298
25238
MAX
6475
5095
5414
5463
6363
5643
5789
6123
5851
6744
7624
7691
7621
33673
34807
PERCENT
GYPSUM
SATURATION
AVG MIN
114 101
100 91
103 95
102 94
120 109
97 83
102 93
109 99
108 95
113 97
124. 85
115 89
126 104
108 92
113 91
MAX
27
07
15
15
35
105
115
124
134
131
159
146
155
156
158
PERCENT
IONIC
IMBALANCE
AVG
9.0
9.1
7.2
5.2
-1.0
8.8
7.3
7.7
5.8
2.5
-1.2
S.2
1.5
-4.8
-4.7
MIN
1 .2
2.5
1 .2
0.0
-9.8
3.1
3.3
2.3
-4.9
-13.0
-11.2
-5.5
-14.7
-14.1
-10.4
MAX
12.7
14.4
13.8
12.8
8.8
12.2
14.9
14.6
14.0
14.0
14.7
13.8
14.8
4.6
2.9
B-91
-------
RUN SUMMARY - SOLIDS ANALYTICAL DATA
CONCENTRATIONS IN SOLIDS, WT X
ACID INSOLUBLES SOLIDS
ANALY C02 502 S03 CAO WT % IN SLURRY WT % IN SLURRY
RUN TICAL
N0^_ POINT AVQ WIN MAX AVG MIN .MAX AVQ MIN MAX AVG MIN MAX AVG MIN MAX AVG MIN MAX
* * — ~ — ™ ••••••••••••••••*»"« »^—••^ •• —— •«W«*^,M ••••M»«BWMB«H»«M«M« v •••HA •••»•«.•.••••••• •»• •»*_v«^«»*w — — — • — ••••».• — — ••..•• —
TFG-2A 2816 S.52 3.11 9.02 24.10 19.54 28.99 4.67 0.98 8.11 31.79 29.42 35.49 3.04 2.63 3.53 15.8 13.5 18.9
2825
TFG-2B 2816 T.91 1.74 14.55 20.53 14.69 27.65 4.38 0.65 8.84 31.93 24.66 37.29 4.09 3.47 4.76 15.4 14.4 16.7
2825
TFff-2C 2816 3.93 2.51 6.58 23.88 15.92 27.69 3.71 1.50 5.92 28.96 21 .95 32.27 5.50 4.98 6.25 15.4 14.5 16.7
2825
TFG-2D 2816 3.83 2.80 6.49 23.95 19.54 26.42 3.67 0.19 5.72 29.33 26.30 31.17 3.88 3.72 3.99 14.0 12.8 19.5
2825
TFG-2E 2816 3.71 2.72 5.47 21.64 18.09 24.31 3.65 0.46 7.74 27.30 25.24 29.27 5.18 4.19 6.08 14.5 12.6 15.1
2825
TFG-2F 2816 3.93 2.82 4.78 23.14 19.54 29.31 5.60 2.26 10.18 29.72 25.56 33.20 4.37 3.37 5.37 15.1 12.9 16.2
2825
525-2A 2816 6.27 6.27 6.27 16.02 16.02 16.02 5.92 5.92 5.92 25.05 25.05 25.05 14.9 14.9 14.9
2825
526-2A 2816 6.62 2.58 11.17 14.56 11.02 17.87 7.15 4.48 11.2825.21 19.73 30.85 14.7 13.8 15.9
2825
DO 527-2A 2816 10.32 6.88 12.04 14.65 12.49 17.36 6.06 4.33 8.97 29.46 26.37 30.99 14.7 10.7 16.0
i 2825
ro 528-2A 2816 4.74 2.42 6.88 19.18 15.70 22.36 5.63 2.37 8.91 26.14 23.96 28.60 14.8 10.7 T6.6
2825
529-2A 2816 5.51 4.40 6.34 15.71 14.67 16.72 6.98 4.81 8.2824.20 23.47 25.80 15.1 14.5 15.5
2825
530-2A 2816 6.79 3.90 10.75 17.91 13.20 21.20 5.65 3.23 8.48 27.05 23.99 30.33 14.8 12.8 16.0
2825
531-2A 2816 5.94 1.01 13.41 16.81 10.91 22.23 6.65 2.79 13.59 28.30 17.49 35.50 8.1 7.1 10.0
2825
532-2A 2816 5.41 2.71 9.22 17.95 15.70 21.52 5.44 3.29 7.47 27.64 24.21 31.40 8.7 7.8 9.9
2825
533-2A 2816 6.26 2.88 9.33 20.11 12.89 24.62 5.61 1.77 8.52 30.12 25.54 32.36 14.8 12.2 17.6
2825
534-2A 2816 4.40 1.42 6.06 20.65 19.40 22.00 6.33 3.55 11.39 27.29 25.70 29.50 5.13 4.20 6.42 12.0 10.1 14.6
2825
535-2A 2816 7.68 3.76 11.60 18.78 13.20 23.96 4.73 1.10 9.82 29.32 25.40 32.87 5.18 3.38 7.10 13.5 9.0 16.7
2825
535-28 2816 4.97 1.30 7.40 19.75 14.60 24.20 5.41 2.34 9.16 26.87 23.91 30.54 5.10 4.00 6.58 12.3 8.9 15.0
2825
536-2A 2816 5.87 1.61 9.11 18.51 14.50 21.90 5.22 1.54 9.53 26.78 23.57 28.85 5.88 4.62 7.00 13.8 11.2 16.4
2825
537-2A 2816 5.85 2.61 8.55 18.24 12.50 21.91 4.36 3.18 8.90 27.13 24.72 29.87 6.05 5.00 7.35 13.9 12.7 16.8
2825
S38-2A 2816 8.03 5.09 12.30 18.29 13.40 22.30 5.02 1.95 9.36 29.21 26.06 33.96 5.73 3.01 6.81 15.1 12.5 17.1
2825
539-2A 2816 10.39 6.09 13.91 19.17 15.30 23.90 3.94 0.70 7.6631.59 28.36 34.42 4.87 4.16 6.22 14.3 12.7 16.7
-------
RUM SUMMARY - SOLIDS ANALYTICAL DATA (CONTINUED)
PERCENT PERCENT
SULFfTE STOICHIOMETRIC IONIC
ANALY OXIDATION RATIO IMBALANCE
RUN TICAL
NO. POINT AVG MIN MAX AVG MIN MAX AVQ MIN MAX
TFG-2A 2816 13.2 3.4 22.0 1.31 1.15 1.59 1.2 -4.4 5.0
2825
TFG-2B 2816 14.2 3.0 25.51.561.082.20 2.5 -2.9 8.3
2825
TFG-2C 2816 11.1 4.2 16.4 1.22 1.12 1.50 1.3 -8.5 7.3
2825
TFG-2D 2816 10.9 0.7 19.0 1.21 1.14 1.37 3.1 -1.7 6.4
2825
TFG-2E 2816 11.8 1.7 24.6 1.22 1.15 1.31 4.0 -1.3 7.5
2825
TFG-2F 2816 16.2 7.9 27.9 1.21 1.15 1.25 1.8 -3.2 8.2
2825
S25-2A 2816 22.8 22.8 22.8 1.44 1.44 1.44 -4.4 -4.4 -4.4
2825
526-2A 2816 28.2 17.3 44.3 1.48 1.19 1.87 -3.7 -7.9 4.5
2825
527-2A 2816 24.8 19.0 36.5 1.78 1.45 1.96 -2.6 -6.7 3.7
2825
528-2A 2816 19.1 8.3 26.3 t.30 1.14 1.49 -2.4 -8.4 6.8
2825
529-2A 2816 26.2 18.7 30.2 1.38 1.29 1.44 -6.1 -8.2 -4.7
2825
530-2A 2816 20.3 11.6 34.0 1.45 1.23 1.72 -4.6 -8.4 5.3
2825
531-2A 2816 24.2 12.0 48.81.41 1.062.25 4.7 -7.7 8.5
2825
532-2A 2816 19.5 13.2 25.9 1.36 1.17 1.69 4.5 -1.9 8.4
2825
533-2A 2816 18.4 6.4 32.1 1.38 1.17 1.63 2.1 -5.7 7.5
2825
534-2A 2816 19.3 12.2 31.1 1.25 1.07 1.35 -3.0 -7.1 -0.6
2825
535-2A 2816 16.9 3.7 32.81.501.211.83 -0.8 -8.4 8.5
2825
535-28 2816 18.1 7.9 28.8 1.31 1.07 1.45 -2.1 -8.4 8.4
2825
538-2A 2816 18.4 6.6 33.1 1.381.091.69 -2.1 -8.0 6.4
2825
537-2A 2816 16.3 10.4 36.3 1.40 1.16 1.59 2.4 -1.5 7.0
2825
538-2A 2816 18.2 7.0 35.01.531.331.89 -2.0 -8.2 6.8
2825
539-2A 2816 14.3 2.8 28.6 1.70 1.33 2.08 -3.9 -8.1 5.6
B-93
-------
RUN SUMMARY - SOLIDS ANALYTICAL DATA
CONCENTRATIONS IN SOLIDS, MT *
ACID INSOLUBLES
RUN
NO.
ANALY
TICAL
POINT
AVQ
C02
MIN
MAX
AVG
«V A V ArJiJWUWB kb^ «XJI» A fc/^
S02 S03 CAO WT % IN SLURRY NT % IN SLURRY
MIN MAX AVG MIN MAX AVQ MIN MAX AVG MIN MAX AVG MIN MAX
539-2A 2825
540-2A 2816 9.63 5.34 13.47 20.56 17.90 22.40 3.45 0.56 6.15 30.96 27.60 33.73 4.76 4.17 5.48 14.2 13.3 14.9
2825
541-2A 2816 10.94 9.85 12.25 17.73 16.20 19.70 5.68 5.34 5.99 32.88 31.09 34.03 4.52 3.68 5.75 14.8 13.9 16.5
2825
542-2A 2816 6.64 5.65 10.21 17.98 15.30 22.70 4.58 3.33 5.21 2*;«0 28.60 30.84 5.56 5.04 6.10 14.7 13.7 15.8
2825
543-2A 2S16 6.73 6.02 7.27 19.23 19.00 19.50 5.53 4.37 6.61 28.40 27.97 29.03 5.03 4.94 5.14 13.1 12.9 13.5
2825
544-2A 2816 7.89 4.90 11.72 18.04 14.20 20.70 5.34 3.00 7.53 29.37 27.16 32.84 4.89 1.51 6.07 15.4 12.3 40.4
2825
545-2A 2816 7.11 4.29 10.90 19.57 14.70 22.80 5.14 3.07 8.81 29.40 27.35 32.34 5.10 4.04 5.72 13.6 13.0 14.7
2825
546-2A 2816 4.98 2.05 9.55 20.84 17.50 23.20 5.05 3.96 6.01 27.15 23.44 32.44 6.03 4.70 7.67 15.0 11.5 16.3
2825
547-2A 2816 7.15 5.34 8.48 22.88 21.10 24.70 3.10 2.27 4.30 30.13 28.48 30.90 5.31 4.72 5.84 14.9 13.7 15.9
2825
548-2A 2816 9.38 6.89 11.49 19.75 18.40 21.10 3.34 2.67 4-30 31.04 28.65 33.89 4.53 3.69 5.27 12.8 11.4 14.5
2825
549-2A 2816 7.83 6.43 8.90 19.26 18.20 21.40 3.35 2.03 4.95 29.96 29.14 33.51 5.80 4.77 6.73 14.6 12.8 15.7
2825
550-2A 2816 8.39 7.53 9.60 19.67 16.40 23.00 4.52 2.37 9.11 31.36 28.71 33.06 5.09 3.26 5.74 14.7 12.5 15.7
2825
551-2A 2816 8.75 7.80 9.44 22.05 20.20 24.80 2.69 1.80 3.45 32.69 30.15 34.32 4.75 4.58 4.90 14.4 14.0 14.8
2825
552-2A 2816 7.29 5.90 9.24 22.09 18.40 25.20 3.40 0.53 6.37 31.04 29.36 32.91 5.36 4.92 5.76 15.2 14.6 15.7
2825
553-2A 2816 7.27 5.86 8.53 16.30 13.30 17.90 5.36 4.47 6.17 28.15 25.28 29.80 6.75 5.57 7.92 15.1 14.2 16.0
2825
554-2A 2816 8.74 7,50 9.80 17.42 15.60 18.30 4.10 0.73 8.20 29.00 26.40 30.50 15.1 14.9 15.3
2825
555-2A 2816 8.97 8.77 9.31 16.83 15.80 17.90 3.56 3.26 3.83 29.70 29.60 29.84 5.99 5.86 6.20 14.6 13.9 15.0
2825
5S6-2A 2816 8.77 5.00 12.50 15.80 13.60 17.20 5.66 3.13 9.30 28.31 25.47 31.40 5.34 4.58 5.90 12.6 10.8 14.5
2825 v
557-2A 2816 5.90 2.89 11.23 19.85 14.80 23.90 4.00 2.00 6.59 26.94 22.66 30.80 6.22 5.47 7.11 14.9 13.5 16.2
2825
558-2A 2816 5.39 2.07 9.08 19.41 14.20 23.30 4.28 2.36 7.7626.71 20.4430.52 6.34 5.47 7.79 14.5 11.3 16.5
2825
559-2A 2816 6.32 2.23 8.89 19.90 15.00 25.20 4.02 1.63 7.0728.13 23.92 30.09 6.15 5.40 6.85 15.0 13.1 16.3
2825
560-2A 2816 7.68 4.99 10.78 20.35 16.00 23.20 3.40 2.16 4.39 30.07 28.02 32.74 5.93 3.45 7.19 14.8 9.4 16.4
2825
-------
RUM SUMMARY - SOLIDS ANALYTICAL DATA (CONTINUED)
PERCENT PERCENT
SULFITE STOICNIOMETRIC IONIC
ANALY OXIDATION RATIO IMBALANCE
RUN TICAL
NO. POINT AVQ MIN MAX AVG MIN MAX AVG MIN MAX
539-2A 2825
540-2A 2816 11.8 2.0 21.6 1.61 1.31 1.92 -5.6 -8.5 -2.3
2825
541-2A 2816 20.5 19.6- 22.0 1.72 1.64 1.86 -1.7 -3.1 -0.8
2825
542-2A 2816 17.4 10.5 21.4 1.60 1.32 1.76 -0.6 -2.8 0.9
2825
543-2A 2816 18.6 15.6 21.3 1.41 1.35 1.47 -3.2 -5.0 0.2
2825
544-2A 2816 19.2 11.8 27.6 1.53 1.28 1.94 -0.8 -6.3 5.9
2825
545-2A 2816 17.5 10.1 32.41.451.241.73 -1.4 -6.2 2.5
2825
546-2A 2816 18.3 12.0 20.8 1.29 1.13 1.61 -3.6 -7.9 2.5
2825
547-2A 2816 9.8 7.5 12.9 1.41 1.28 1.50 -4.0 -8.5 1.8
2825
548-2A 2816 11.9 10.2 14.1 1.621.421.80 -1.9 -8.3 2.7
2825
549-2A 2816 12.2 7.5 17.9 1.51 1.43 1.58 3.4 -4.9 8.1
2825
550-2A 2816 15.5 7.6 28.4 1.53 1.44 1.67 0.8 -3.2 6.7
2825
551-2A 2816 9.0 5.5 12.01.531.431.59 0.8 -7.8 5.7
2825
552-2A 2816 11.0 1.6 21.7 1.43 1.33 1.57 -5.0 5 9
2825
563-2A 2816 21.1 16.8 27.1 1.51 1.47 1.58 3.3 -0.4 7.3
2825
554-2A 2816 15.5 3.2 29.61.621.491.70 -0.9 -4.9 2.2
2825
555-2A 2816 14.5 12.7 16.31.661.651.68 3.5 0.1 6.4
2825
5S6-2A 2816 22.1 13.3 35.4 1.63 1.36 1.90 -2.3 -6.4 6.3
2825
557-2A 2816 14.2 7.3 23.4 1.38 1.17 1.76 -2.6 -8.0 8.4
2825
558-2A 2816 15.2 8.2 29.6 1.35 1.12 1.63 -0.7 -7.8 7.7
2825
559-2A 2816 14.0 5.3 25.» 1.40 1.12 1.65 -0.6 -7.5 8.4
2825
560-2A 2816 11.9 7.6 15.4 1.49 1.31 1.83 0.4 -6.8 7.4
2825
B-95
-------
RUN SUMMARY - SOLIDS ANALYTICAL DATA
CONCENTRATIONS IN SOLIDS, NT X
ACID INSOLUBLES SOLIDS
ANALY C02 S02 803 CAO NT X IN SLURRY HT % IN SLURRY
RUN TICAL
NO. POINT AVQ MIN MAX AVQ MIN MAX AVQ MIN MAX AVQ MIN MAX AVG MIN MAX AVQ MIN MAX
561-2A 2818 6.47 3.96 0.09 22.36 19.70 25.00 2.98 1.T7 8.60 29.09 27.69 31.67 5.77 5.48 6.28 14.7 14.1 15.7
2825
562-2A 2816 9.15 4.99 15.24 20.18 12.60 25.10 3.56 1.10 9.0631.95 27.82 38.80 5.13 3.25 7.20 15.1 11.1 17.5
2825
562-28 2816 7.57 5.14 10.55 19.05 13.10 23.50 5.25 2.33 7.64 99.44 27.94 33.32 5.46 4.65 6.17 14.8 14.1 16.2
2825
S63-2A 2816 11.21 7.95 14.11 20.66 17.4O 23.90 1.79 -0.87 4.89 34.63 31.15 37.43 4.77 4.02 5.50 15.1 13.3 15.8
2825
B64-2A 2816 0.87 0.33 1.49 21.36 19.40 25.80 6.08 5.18 6.9632.75 20.49 27.70 6.71 5.55 7.48 13.9 12.1 15.0
2825
565-2A 2818 0.91 0.66 1.16 20.93 17.60 24.30 4.69 2.82 8.6421.62 20.45 24.22 7.44 6.94 7.81 14.4 14.0 15.1
2825
S66-2A 2816 4.62 0.66 9.78 22.77 18.80 26.50 3.37 0.98 7.92 26.97 20.79 32.86 6.22 4.62 7.74 15.0 13.8 15.7
2825
567-2A 2816 7.58 4.41 9.57 21.62 16.90 24.90 3.45 2.06 6.7829.10 26.47 30.40 5.67 5.23 6.10 15.2 14.3 15.8
2825
568-2A 2816 1.11 0.44 1.72 23.54 16.24 26.80 5.28 1.96 9.1624.90 22.75 29.50 7.02 5.89 7.71 15.0 14.0 15.8
2825
OT 569-2A 2816 1.43 0.78 1.79 20.03 16.10 22.90 5.93 5.18 7.13 23.10 21.45 24.40 7.25 7.23 7.27 14.5 14.2 T4.9
i 2825
cr> 569-28 2816 1.36 0.65 1 .85 21 .06 17.60 24.00 5.03 3.26 7.1722.80 21.23 25.00 7.43 6.60 8.07 15.0 14.0 16.1
2625
570-2A 2816 2.94 1.62 4.95 20.73 18.20 23.70 4.87 2.34 8.98 24.86 22.52 28.30 6.91 5.70 7.87 14.8 13.3 15.7
2825
571-2A 2816 3.99 1.96 5.67 18.95 15.90 23.00 3.95 1.46 6.08 24.04 22.46 25.74 7.41 6.77 8.42 15.0 14.0 15.9
2825
571-28 2816 5.28 1.22 7.61 19.70 18.70 20.20 5.37 3.17 6.8627.64 22.28 31.58 5.53 4.75 6.05 13.7 12.7 14.7
2825
572-2A 2816 1.39 0.23 2.09 18.38 13.70 21.40 5.37 2.60 7.SO 21.78 19.61 24.30 7.81 6.67 8.88 14.4 12.9 15.8
2825
573-2A 2816 1.37 1.02 2.20 19.58*16.24 24.45 5.85 2.63 9.1622.41 21.75 23.05 7.39 6.62 7.97 14.8 13.6 15.8
2825
575-2A 2816 2.96 9.69 3.43 21.53 20.30 22.80 3.63 3.06 4.90 93.53 22.43 24.63 7.21 6.05 7.73 14.8 13.6 15.8
2825
576-2A 2816 3.37 2.07 6.16 21.31 16.90 23.20 4.14 1.08 9.6494.44 22.52 28.20 7.02 5.54 7.86 15.1 14.2 15.8
2825
576-26 2816 2.69 1.10 4.07 20.42 18.00 21.80 5.12 3.65 6.62 23.93 23.40 24.70 6.85 6.85 6.85 15.0 15.0 15.0
2825
577-2A 2816 4.43 1.87 5.88 22.55 17.70 25.40 3.63 1.44 6.05 27.02 21.22 32.00 6.32 4.94 8.54 15.1 13.5 18.0
2825
578-2A 2816 8.34 3.83 8.08 22.90 21.70 25.00 2.58 0.85 3.66 28.93 27.10 31.40
2825
579-2A 2816 0.96 0.66 1.38 21.11 16.70 25.00 6.22 4.05 6.6323.65 21.30 26.10 7.12 6.33 7.93 15.0 14.0 16.3
-------
MM SUMMARY - SOLIDS ANALYTICAL DATA (CONTINUED)
PERCENT PERCENT
SULF*TE STOICHIOMETRIC IONIC
ANALT OXIDATION RATIO IMBALANCE
RUN TICAL
NO. POINT AVQ MIN MAX AV6 MIN MAX AVG MIN MAX
561-2A 2816 9.7 5.5 17.7 1.39 1.23 1.59 -2.8 -7.8 6.1
2825
562-2A 2816 12.5 4.5 35.5 1.59 1.27 2.14 0.2 -8.5 8.4
2825
562-2B 2816 18.3 8.0 32.4 1.46 1.28 1.78 -2.0 -8.5 6.5
2825
563-2A 2816 6.5 -2.6 15.41.751.472.02 2.8 -6.2 6.4
2825
564-2A 2816 18.6 17.0 22.2 1.OS 1.02 1.09 -5.9 -8.0 -4.0
2825
S65-2A 2816 15.3 7.7 28.2 1.OS 1.04 1.06 -S.5 -7.7 -1.2
2825
566-2A 2816 10.6 3.0 22.9 1.27 1.04 1.62 -4.6 -7.7 -0.1
2625
56T-2A 2816 11.4 6.2 21.7 1.4* 1.25 1.65 -6.5 -8.5 -1.7
2825
566-2A 2816 15.3 5.6 31.1 1.0*1.021.09 -3.4 -8.5 3.1
2825
569-2A 2816 19.3 15.3 24.0 1.W 1.04 1.11 -1.9 -7.1 3.3
2825
569-292816 16.1 10.2 24.6 1.M 1.04 1.12 -3.9 -6.1 4.4
2825
S7*-2A 2816 15.9 7.7 27.9 1.17 1.10 1.33 -4.4 -6.5 3.5
2825
571-2A 2816 14.8 5.3 23.4 1.27 1.12 1.40 -1.7 -«.1 5.9
2825
571-292816 17.7 11.4 21.41.931.071.50 -1.1 -7.9 7.4
2825
B72-2A 2816 19.1 9.4 30.6 1.O9 1.01 1.15 0.7 -9.4 8.0
2825
573-2A 2816 19.6 7.9 31.1 1.68 1.06 1.14 -2.6 -9.1 7.0
2825
575-2A 2816 11.9 9.9 13.8 1.18 1.16 1.21 -6.9 -9.5 -6.0
2825
570-2A 2816 13.4 3.6 28.0 1.20 1.11 1.42 -5.8 -6.3 2.9
2825
576-25 2816 16.8 11.8 22.7 1.16 1.06 1.25 -4.0 -6.4 -«.1
2825
577-2A 2816 11.5 4.8 -20.2-t.25 1.11 1.34 -3.5 -9.5 7.1
2625
578-2A 2816 8.2 2.9 11.4 1.39 1.20 1.48 -3.6 -6.2 2.3
2825
579-2A 2910 19.1 12.9 29.2 1.05 1.03 1.09 -1.7 -3.5 0.5
B-97
-------
RUN SUMMARY - SOLIDS ANALYTICAL DATA
CONCENTRATIONS IN SOLIDS, NT X
ACID INSOLU8LES SOLIDS
RUN
NO.
ANALY
TICAL
POINT AVQ
C02
MIN
MAX
AVO
S02
MIN
MAX
AVQ
S03
MIN
MAX
AVQ
CAO
MIN MAX
MT % IN SLURRY MT X IN SLURRY
AVG MIN
MAX AVQ
MIN MAX
579-2A 2B25
5BO-2A 2816 2.67 0.61 4.57 20.00 18.20 21.90 9.07 4.35 6.13 24.18 22.60 29.80 7.37 7.37 7.37 19.4 19.4 19.4
2625
581-2A 2816 3.02 0.81 6.23 19.61 15.60 24.80 9.03 3.33 14.80 27.08 21.60 31.20 5.94 4.72 8.09 IS.2 13.9 20.4
2825
582-2A 2816 7.67 1.54 13.81 18.87 14.70 21.50 10.19 8.38 13.18 32.49 27.70 38.80 4.11 3.83 4.39 16.1 18.2 17.0
2829
5B3-2A 2816 3.93 1.18 6.32 18.21 13.80 22.60 9.98 6.99 14.80 88.48 25.55 30.80 8.48 3.89 6.34 14.7 13.2 16.6
2825
583-28 2B16 5.33 2.67 10.17 16.82 10.90 22.80 10.23 6.98 15.33 28.78 25.10 34.39 8.37 2.73 7.57 14.8 7.7 17.7
2B25
564-2A 2816 7.46 2.39 13.44 20.60 14.50 27.40 5.51 0.83 9.88 31.88 28.00 34.70 5.38 4.30 7.68 IS.4 13.0 17.9
2825
585-2A 2816 7.27 4.41 9.64 17.71 13.80 21.30 7.B3 3.18 11.43 30.47 27.90 33.40 5.23 4.13 6.52 14.6 13.1 16,3
2825
5B6-2A 2816 8.39 5.17 9.79 18.58 14.50 21.30 7.42 0.98 11.60 29.61 24.50 31.70 5.38 3.83 7.19 14.8 12.8 15.8
2825
587-2A 2816 6.20 5.12 12.29 16.44 12.10 21.10 7.19 3.08 12*68 30.29 25.60 33.80 3.40 2.29 5.13 9.2 6.9 12.7
2825
58B-2A 2816 11.75 8.63 15.40 11.50 7.20 15.30 6.47 4.10 9.SS 30.99 29.00 34.80 5.28 4.64 5.78 14.2 12.9 15.1
2825
589-2A 2816 6.19 2.33 14.59 19.03 12.30 21.50 5.54 1.39 6.50 29.10 25.80 37.20 5.93 4.22 7.67 14.9 13.4 16.8
2825
590-2A 2816 1.58 1.19 1.98 10.09 9.04 11.68 9.95 7.99 12.63 17.76 17.32 18*32 6.86 6.56 7.12 13.6 13.9 14.5
2825
590-28 2816 2.68 1.24 4.51 14.58 12.55 17.01 8.32 7.05 11.67 22.03 19.25 23.89 5.59 4.73 6.86 14.5 13.5 15.9
2825
591-2A 2816 4.40 2.29 7.92 12.35 4.47 18.42 11.69 6.99 20.30 24.02 18.74 27.77 5.33 4.20 6.21 14.4 13.1 15.9
2825
592-2A 2816 7.50 4.45 10.69 16.31 12.90 23.68 6.56 0.01 12.75 27.63 24.20 30.92 9.43 4.52 7.19 19.1 14.0 17.0
2825
593-2A 2816 9.72 5.20 13.30 14.92 11.10 20.20 6.15 3.25 8.33 28.92 22.10 31.90 5.14 4.30 6.40 19.0 13.2 17.B
2825
594-2A 2816 5.58 3.90 8.60 19.07 14.80 22.80 8.31 3.20 7.68 26.80 23.70 29.60 5.59 5.20 6.70 15.1 13.9 16.2
2625
601-2A 2816 0.76 0.16 1.98 22.87 20.00 26.80 5.70 2.39 9.78 25.69 20.70 30.80 3.75 2.72 4.71 8.3 7.3 9.0
2825
602-2A 2816 0.73 0.29 1.46 24.45 21.30 27.20 4.79 0.02 9.65 23.91 23.30 28.30 6.67 3.24 8.18 14.7 8.7 16.3
2825
603-2A 2816 0.55 0.05 3.82 21.44 17.90 24.40 6.24 2.68 10.95 23.64 18.60 26.90 3.88 3.17 5.13 8.1 7.2 9.3
2825
604-2A 2816 0.30 0.05 1.10 IB.59 15.2021.30 10.00 6.98 13.6324.2221.6026.71 3.43 2.58 4.15 7.7 7.1 8.3
2825
-------
RUN SUMMARY - SOLIDS ANALYTICAL DATA (CONTINUED)
PERCENT PERCENT
SULFITE STOICHIOMETRIC IONIC
ANALY OXIDATION RATIO IMBALANCE
RUN TICAL
NO. POINT AVG MIN MAX AVG MIN MAX AVG MIN MAX
579-2A 2825
580-2A 2816 16.9 14.2 20.1 1.16 1.03 1.31 -0.7 -3.6 1.4
2825
581-2A 2816 26.6 10.4' 41.2 1.17 1.04 1.39 -1.8 -7.7 6.8
2825
S82-2A 2816 30.3 24.6 36.2 1.43 1.07 1.85 -3.1 -8.3 5.1
2825
583-2A 2816 30.6 20.9 41.2 1.22 1.06 1.39 2.0 -3.9 7.2
2825
583-2B 2816 33.8 26.0 43.5 1.32 1.14 1.70 0.4 -8.3 8.5
2825
584-2A 2816 17.4 3.2 28.7 1.46 1.13 2.09 1.5 -7.4 7.4
2825
585-2* 2816 25.4 13.1 35.4 1.45 1.24 1.60 1.5 -3.5 7.1
2825
586-2A 2816 23.0 5.1 35.1 1.40 1.29 1.93 0.1 -4.3 7.7
2825
S87-2A 2816 25.5 14.7 45.6 1.56 1.30 1.99 1.3 -7.0 8.5
2825
588-2A 2816 31.3 22.7 47.42.071.682.53 4.5 -1.4 8.5
2825
5B9-2A 2816 16.8 5.3 34.9 1.42 1.12 2.12 2.2 -3.0 7.9
2825
590-2A 2816 43.9 35.6 52.6 1.13 1.09 1.17 -0.1 -0.8 0.4
2825
590-28 2816 31.3 24.9 37.8 1.18 1.09 1.35 0.6 -4.6 7.4
2825
591-2A 2816 43.8 25.3 75.2 1.30 1.18 1.61 -2.8 -6.6 2.7
2825
592-2A 2816 23.1 0.0 44.0 1.55 1.24 2.16 -3.8 -7.9 3.5
2825
593-2A 2816 25.2 13.9 37.5 1.74 1.39 2.16 -2.9 -8.4 7.8
2825
594-2A 2816 18.4 11.0 25.8 1.35 1.23 1.46 -3.6 -7.9 5.1
2825
601-2A 2816 16.3 7.8 25.1 1.04 1.01 1,10 2.5 -7.9 7.2
2325
602-2A 2816 13.1 0.1 24.8 1.04 1.01 1.08 1.0 -6.3 8.2
2825
603-2A 2816 16.6 9.5 31.0 1.03 1.00 1.25 -0.9 -8.3 8.3
2825
604-2A 2816 30.0 20.8 37.3 1.02 1.00 1.06 2.3 -7.3 8.1
2825
B-99
-------
RUN SUMMARY - SOLIDS ANALYTICAL DATA
CONCENTRATIONS IN SOLIDS, WT X
ACID INSOLUBLES SOLIDS
ANALY C02 S02 S03 CAO WT X IN SLURRY WT X IN SLURRY
RUN TICAL
NO. POINT AVG MIN MAX AVQ MIN MAX AVG MIN MAX AVQ MIN MAX AVG MIN MAX AVG MIN MAX
605-2A 2816 0.56 0.19 0.93 24.49 19.72 2B.23 7.36 4.64 11.62 27.61 23.26 30.80 2.15 1.37 2.89 7.8 7.0 8.8
2825
606-2A 2816 0.91 0.33 2.27 20.47 16.75 25.33 7.78 3.20 17.35 24.11 20.33 31.57 2.66 2.23 3.42 8.0 7.4 9.3
2825
607-2A 2816 0.87 0.13 1.58 22.85 18.08 26.24 5.23 0.04 13.84 25.48 21.95 29.73 2.70 2.06 3.88 7.8 6.9 8.6
2825
608-2A 2816 1.17 0.82 1.55 24.61 20.81 28.84 7.33 5.23 10.01 27.80 25.24 29.86 4.36 3.99 4.59 14.7 13.4 15.7
2825
608-28 2816 1.44 1.02 1.84 26.01 21.17 28.67 4.70 2.22 9.39 27.79 25.73 30.14 4.51 4.05 5.08 14.8 14.0 15.6
2825
609-2A 2816 0.46 0.13 0.94 23.17 18.27 28.76 4.83 0.37 9.06 24.51 19.49 30.63 2.95 2.24 3.83 8.0 7.1 8.7
2825
610-2A 2816 0.74 0.35 1.08 22.79 17.96 28.95 2.64 0.25 5.51 23.63 19.19 28.55 2.58 1.84 2.95 7.9 7.2 8.7
2825
611-2A 2816 0.68 0.16 1.54 17.32 13.46 21.89 9.68 0.64 20.73 23.57 20.44 27.70 2.63 2.33 3.03 8.0 6.9 8.9
2825
612-2A 2816 0.33 0.11 0.66 18.04 15.53 20.26 9.99 7.08 12.33 24.54 21.00 27.10 2.75 2.32 3.31 8.0 7.0 9.2
2825
613-2A 2816 0.47 0.16 0.78 17.94 14.31 25.35 10.12 1.71 17.23 24.22 19.72 28.36 2.43 1.87 3.20 8.1 6.9 *8.7
2825
614-2A 2816 0.83 0.22 2.00 22.06 19.00 25.41 3.56 0.80 5.98 24.37 21.98 27.62 2.76 2.42 3.55 7.9 4.0 9.1
2825
615-2A 2616 0.55 0.15 1.65 19.49 15.5624.22 5.22 1.57 8.7B21.97 18.5425.29 3.03 2.48 3.42 8.1 7.5 8.8
2825
616-2A 2816 1.24 0.33 2.97 20.91 15.45 24.56 6.52 0.90 13.91 24.54 17.61 30.74 2.99 2.46 3.36 7.9 4.9 8.8
2825
617-2A 2816 1.16 0.71 1.70 22.59 19.18 25.46 3.50 1.68 6.78 24.95 22.62 27.79 5.10 3.11 6.01 14.3 8.1 15.5
2825
618-2A 2816 1.18 0.77 2.07 16.84 13.66 22.19 7.89 4.99 11.25 21.97 19.70 25.07 3.00 2.33 3.87 7.9 6.5 10.0
2825
618-2B 2816 0.96 0.44 1.42 16.06 12.2520.52 8.56 4.46 11.0422.00 18.8025.95 2.76 1.82 3.79 7.5 6.3 8.7
2825
619-2A 2816 0.78 0.27 1.98 20.12 14.96 25.33 7.43 2.73 14.34 24.48 19.02 29.31 2.72 1.76 4.07 8.0 6.9 9.5
2825
620-2A 2816 0.88 0.38 1.31 19.00 14.69 21.71 9.21 7.68 10.96 25.39 22.83 27.28 2.52 1.87 3.14 8.5 6.2 10.1
2825
621-2A 2816 0.82 0.10 4.16 17.21 12.3020.50 8.47 6.00 11.1622.26 18.81 27.98 3.29 1.88 4.21 8.1 6.3 9.2
2825
622-2A 2816 1.36 0.90 2.30 21.04 16.0025.30 7.45 4.85 11.5524.91 21.9027.80 3.14 2.80 3.60 8.6 7.7 10.1
2825
622-2B 2816 0.99 0.10 2.50 19.42 15.0021.30 3.81 1.35 5.5021.40 16.5024.20 3.56 2.90 5.30 8.0 7.3 9.2
2825
623-2A 2816 1.32 0.10 5.1022.51 18.4028.60 4.38 1.00 8.2023.9319.9026.90 3.21 2.50 4.20 8.2 7.4 9.3
-------
RUN SUMMARY - SOLIDS ANALYTICAL DATA (CONTINUED)
PERCENT PERCENT
SULFtTE STOICHIOMETRIC IONIC
RUN ?!JiI °*IO*TION RATIO IMBALANCE
NO. POINT AVC MIN MAX AVG MIN MAX AVG MIN MAX
805-2A 2816 19.3 13.3 27.7 1.03 1.01 1.04 1.0 -7 7 79
2825 .
606-2A 2816 23.0 9.2 40.8 1.05 1.02 1.12 -1.8 -84 79
2825
807-2A 2816 15.1 0.1 3t.8 1.05 1.01 1.09 2.8 -6.7 8 5
2825
608-2A 2816 19.3 12.7 26.2 1.06 1.04 1.07 -1.3 -5.6 1 6
2825
608-28 2816 12.6 6.5 23.1 1.07 1.05 1.09 -0.4 -4.3 4.1
2825
609-2A 2816 14.1 1.1 26.0 1.031.01 1.05 1.0 -6.2 8.0
2825
610-2A 2816 B.5 0.9 19.6 1.05 1.02 1.07 3.8 -3.9 8.2
2825
611-2A 2816 29.6 2.5 54.1 1.04 1.01 1.10 3.4 -4.6 8.5
2825
612-2A 2816 30.6 25.0 37.9 1.02 1.01 1.04 5.4 2.5 8.4
2825
813-2A 2816 3O.S 6.5 43.7 1.03 1.01 1.05 3.5 -0.6 8.0
282S
614-2A 2816 11.4 2.6 18.2 1.05 1.01 1.10 6.2 0.0 8.5
2825
615-2A 2816 17.7 5.3 27.6 1.03 1.01 1.09 2.6 -7.6 6.5
2825
616-2A 2816 18.6 4.3 33.8 1.07 1.01 1.17 0.4 -7.3 8.1
2825
617-2A 2816 11.0 5.6 22.01.071.041.11 5.0 0.0 8.4
2825
818-2A 2816 27.5 15.2 39.71.081.051.15 0.8 -4.9 7.3
2825
618-28 2816 30.1 1S.S 38.8 1.06 1.03 1.08 3.1 -4.7 8.5
2825
819-2A 2816 22.7 8.4 42.7 1.05 1.01 1.12 2.6 -5.8 7.7
2825
820-2A 2816 28.2 22.1 37.01.051.021.07 4.7 0.9 8.3
2825
621-2A 2816 28.3 20.0 41.3 1.05 1.01 1.26 0.8 -7.1 8.0
2825
622-2A 2816 22.3 13.8 3S;8~1.08 1.04 1.15 -1.8 -6.2 4.5
2825
622-28 2816 13.6 4.9 18.7 1.06 1.01 1.16 2.0 -7.3 8.4
2825
623-2A 2816 13.1 3.9 25.1 1.08 1.01 1.31 -2.2 -7.8 4.6
B-101
-------
RUN SUMMARY - SOLIDS ANALYTICAL DATA
CONCENTRATIONS IN SOLIDS, WT X
ACID INSOLUBLES SOLIDS
RUN
NO.
ANALY
TICAL
POINT
AV6
C02
MIN
MAX
AVG
502
MIN
MAX
AVG
503
MIN
CAO
MAX AVG MIN
WT X IN SLURRY WT X IN SLURRY
MAX AVG MIN MAX AVG MIN MAX
623-2A 2825
624-2A 2816 0.64 0..30 1.30 20.69 17.90 24.90 4.39 -0.70 8.2822.34 19.90 25.50 3.45 2.80 4.20 8.0 7.0 9.2
2825
625-2A 2816 2.43 1.20 5.40 20.73 12.90 25.70 4.79 1.55 12.8525.03 15.8031.00 2.99 1.50 4.50 8.1 5.3 10.5
2825
701-2A 2816 5.59 3.30 10.06 34.28 21.53 37.80 5.92 0.51 23.26 42.44 38.37 45.98 0.26 0.06 0.48 8.0 7.2 8.7
2825
702-2A 2816 4.15 1.92 6.93 37.10 31.29 41.21 3.26 0.05 11.11 40.30 37.96 42.56 0.38 0.29 0.50 14.9 9.9 16.3
2825
703-2A 2816 3.35 1.37 4.83 37.91 33.29 40.90 3.21 0.27 8.88 40.04 37.27 41.80 0.18 0.12 0.28 7.9 7.5 10.8
2825
704-2A 2816 2.92 0.71 14.08 36.29 10.13 42.34 7.36 0.41 23.93 42..03 37.31 44.78 0.23 0.12 0.49 6.0 5.8 8.9
2825
705-2A 2816 2.92 0.93 5.28 36.21 23.52 40.36 6.87 0.93 22.84 41.42 36.68 47.01 0.62 0.20 1.07 14.*7 9.6 15.9
2825
OT 706-2A 2816 3.67 1.26 7.93 33.33 27.14 36.91 9.61 1.44 19.60 40.53 35.44 44.59 1.09 0.19 7.05 14.6 13.5 16.0
i 2825
O 707-2A 2816 4.00 2.88 5.06 21.83 18.09 24.25 5.25 4.19 9.42 28.61 24.62 31.54 4.71 3.62 5.50 14.9 13.5 15.7
ru 2825
708-2A 2816 2.66 1.25 4.07 19.73 15.84 23.13 5.10 2.13 13.32 25.23 22.13 28.98 5.75 4.48 6.50 15.1 14.1 15.9
2825
709-2A 2816 3.00 1.48 4.75 20.22 17.30 23.52 6.74 1.90 12.82 27.34 25.00 30.71 4.70 4.32 5.08 14.1 13.1 14.9
2825
710-2A 2816 2.99 1.B2 5.67 21.45 16.32 27.73 4.40 0.07 10.74 26.62 23.09 30.58 5.17 4.82 5.46 14.7 13.0 15.6
2825
711-2A 2816 4.47 2.36 5.62 22.39 19.12 26.06 4.48 1.59 7.31 29.37 25.55 33.86 5.04 4.26 6.43 14.3 9.0 15.9
2825
712-2A 2816 4.01 2.66 5.34 22.99 IB.35 26.06 6.19 1.61 12.12 30.11 28.08 31.74 4.35 3.89 4.98 15.0 13.0 16.3
2825
713-2A 2816 5.05 3.61 6.93 21.50 18.50 24.61 6.10 3.91 9.17 28.88 25.97 30.99 4.58 4.12 4.86 14.9 13.9 16.5
2825
714-2A 2816 C.41 3.53 8.80 20.01 13.87 24.97 4.82 -0.54 14.35 29.91 23.17 36.16 4.37 0.44 6.24 15.2 14.1 16.5
2825
714-28 2816 9.58 8.74 10.41 21.08 20.23 22.74 1.11 0.21 1.73 32.59 31.20 34.78 3.78 3.78 3.78 15.3 14.2 17.0
2825
715-2A 2816 3.67 1.94 4.82 20.05 16.54 26.00 6.52 4.26 9.12 27.06 24.62 28.89 4.93 4.11 5.86 15.0 14.2 15.7
2825
716-2A 2816 2.88 0.20 6.29 20.59 16.48 23.96 8.40 5.19 12.43 27.28 25.25 29.41 4.66 3.98 5.57 14.4 13.0 15.5
2825 -
717-2A 2816 4.52 2.03 7.62 21.24 12.83 26.40 6.73 3.03 16.38 28.80 22.31 33.57 4.39 2.92 6.48 14.8 13.1 22.4
2825
718-2A 2816 5.37 2.97 8.16 18.76 14.24 23.88 6.43 3.10 8.95 27.34 24.98 29.10 4.70 3.69 5.54 14.3 13.1 15.3
2825
-------
RUN SUMMARY - SOLIDS ANALYTICAL DATA (CONTINUED)
PERCENT PERCENT
SULFITE STOICHIOMETRIC IONIC
ANALY OXIDATION RATIO IMBALANCE
RUN TICAL
NO. POINT AVG MIN MAX AVG WIN MAX AVG MIN MAX
623-2A 2625
624-2A 2816 14.4 -2.5 25.6 1.04 1.02 1.07 1.6 -6.7 8.2
2825
625-2A 2816, 15.5 5.6 33.7 1.15 1.07 1.37 1.7 -7.7 8.1
2825
701-2A 2816 11.9 1.1 46.4 1.21 1.13 1.42 2.7 -1.4 7.5
2825
702-2A 2816 6.3 0.1 19.6 1.16 1.07 1.28 0.5 -8.5 7.2
2825
703-2A 2816 6.3 0.-5 16.5 1.12 1.05 1.18 0.8 -4.2 5.0
2825
704-2A 2816 14.3 0.8 65.4 1.11 1.02 1.70 3.2 -79 a 4
2825
705-2A 2816 12.8 1.8 43.7 1.10 1.03 1.21 2.9 -8.1 7 9
2825
706-2A 2816 18.9 3.3 36.3 1.13 1.04 1.35 -0.5 -7.6 84
2825
707-2A 2816 16.2 12.8 28.6 1.23 1.16 1.31 3.1 -0.9 6.8
2825
708-2A 2816 IB.6 7.5 40.1 1.16 1.08 1.23 4.0 -1.2 8.2
2825
709-2A 2816 20.6 6.2 35.1 1.t8 1.06 1.32 4.0 0.2 7.1
2825
710-2A 2816 13,9 0.2 34.5 1.18 1.10 1.40 3.5 -7.6 8.3
2825
711-2A 2816 13.9 4.8 22.9 1.25 1.13 1.33 3.1 -1.5 7.9
2825
712-2A 2816 17.7 4.8 34.6 1.21 1.13 1.31 1.8 -3.4 8.3
2825
713-2A 2816 18.4 12.6 25.3 1.28 1.19 1.44 -2.3 -8.5 5.0
2825
714-2A 2816 *5.1 -1.9 33.2 1.41 1.15 1.65 2.9 -4.5 7.4
2825
714-282818 3.9 0.8 6.4 1.64 1.59 1.68 3.6 1.8 5.2
2825
715-2A 2816 20.7 13.2 29.1 1.22 1.09 1.30 1.0 -7.1 7.6
2825
716-2A 2816 24.5 16.0 34.3 1.16 1.01 1.41 -1.2 -8.5 7.0
2825
717-2A 2816 20.4 8.5 45.2 1.25 1.10 1.55 -1.0 -7.8 8.5
2825
718-2A 2816 21.6 11.1 31.8 1.34 1.16 1.53 -1.7 -8.3 8.1
2825
B-103
-------
RUN SUMMARY - SOLIDS ANALYTICAL DATA
CONCENTRATIONS IN SOLIDS, NT X
ACID INSOLUBLES SOLIDS
ANALY C02 S°2 S°3 CA° WT * 1N SLURRY WT * 1N
NO. POINT AVG WIN MAX AVG MIN MAX AVG MIN MAX AVG MIN MAX AVG MIN MAX AVG MIN MAX
719-2A 2816 2.68 0.55 4.98 20.85 18.13 24.25 6.36 4.16 10.06 26.36 24.62 28.49 4.76 4.04 5.37 14.8 13.5 16.7
2825
801-2A 2816 3.40 1.32 6.20 10.84 7.39 13.74 14.98 10.39 18.61 24.31 21.41 26.86 5.05 4.79 5.30 14.5 12.9 15.4
2825
801-2B 2816 3.42 2.03 4.60 7.44 4.82 11.94 15.32 11.72 19.09 21.88 19.47 24.69 5.06 4.77 5.35 14.7 12.3 16.0
2825
802-2A 2816 2.98 1.87 4.03 9.08 6.09 10.89 14.26 10.11 17.25 22.16 20.20 24.69 5.18 4.88 5.43 15.3 14.5 16.0
2825
803-2A 2816 0.48 0.15 0.87 1.29 0.59 2.12 15.24 4.99 25.84 12,65 5.80 20.27 7.54 4.94 10.83 15.1 14.1 16.4
2825 :
804-2A 2816 0.63 0.15 1.88 0.82 0.00 1.44 14.80 3.40 29.77 12.10 2.89 24.00 8.12 5.35 10.96 15.1 13.3 17.0
2825
805-2A 2816 1.80 0.24 5.33 1.16 0.15 6.81 17.64 6.70 28.01 16.07 9.76 24.60 6.55 5.25 9.69 15.1 13.8 16.7
2825
2831 1.03 0.07 3.16 1.11 0.18 2.61 19.48 5.96 27.92 16.22 8.52 24.09 15.4 14.1 16.9
806-2A 2816 1.52 0.48 3.36 8.30 4.70 13.60 14.37 9.84 21.67 19.67 16.58 22.74 6.15 5.88 6.30 14.4 13.5 15 0
co 2825
J_, 2831 1.45 0.77 3.10 8.80 5.33 14.64 13.02 9.93 23.88 19.08 15.27 23.29 14.9 14.1 16.1
0 807-2A 2816 2.56 0.83 4.40 0.68 0.00 1.80 19.60 13.75 25.43 17.47 11.18 23.97 5.55 4.14 7.22 14.8 13.5 16.0
-P» 2825
2831 2.70 0.37 5.48 0.69 0.00 2.17 20.31 15.52 26.95 18.34 12.60 24.90 5.05 5.05 5.05 15.5 13.0 17.1
808-2A 2816 5.72 3.37 7.46 1.07 0.17 2.53 16.46 6.73 28.25 19.78 13.11 30.10 5.00 3.86 5.57 14.9 12.6 16.1
2825
2831 5.73 4.12 7.29 1.16 0.16 3.13 14.67 3.63'24.88 18.58 11.7624.85 17.1 13.947.7
809-2A 2816 8.61 7.53 10.23 0.78 0.26 2.35 23.54 15.41 35.18 29.03 24.17 35.52 5.21 4.14 5.86 15.6 14.0 17.1
2825
2831 8.26 6.82 11.00 0.94 0.17 3.42 23.41 10.88 37.92 28.40 23.13 36.23 16.4 14.7 18.0
810-2A 2816 4.25 0.99 6.75 0.68 0.09 2.89 25.54 22.07 32.94 23.45 18.37 30.36 3.91 3.12 4.76 15.1 13.7 17.5
2825
2831 4.21 1.15 8.30 0.72 0.09 2.89 24.04 15.87 32.13 22.57 13.37 29.73 16.1 14.3 19.0
811-2A 2816 7.75 4.18 9.82 0.84 0.32 2.17 18.93 12.96 26.57 23.49 19.82 25.55 4.33 3.21 5.21 14.8 13.5 15.9
2825
2831 8.73 5.94 12.58 0.98 0.33 2.17 14.65 2.58 21.59 22.59 17.54 24.91 5.06 3.07 8.01 14.7 13.0 16.2
812-2A 2816 7.45 5.06 12.21 1.13 0.31 2.15 16.32 6.35 20.8922.29 15.0427.14 5.63 3.67 9.07 14.4 10.9 16.7
2825
2831 7.41 4.45 12.32 1.29 0.56 2.43 15.78 4.99 22.74 21.58 13.53 27.84 5.62 3.11 7.88 14.7 10.8 16.3
813-2A 2816 1.54 0.93 3.22 0.94 0.17 1.80 22.11 4.52 27.68 17.81 5.52 20.70 6.23 4.07 11.47 14.9 14.1 15.5
2825
2831 0.88 0.33 1.29 0.91 0.18 1.86 20.71 5.21 27.65 16.16 5.7521.68 6.64 3.94 11.00 15.0 14.0 16.0
814-2A 2816 1.92 0.73 4.16 7.31 2.62 11.03 14.97 10.53 17.95 18.54 15.67 20.36 6.49 5.73 7.84 14.7 14.3 15.0
2825
2831 1.85 0.74 3.90 7.28 4.91 9.08 15.84 11.75 20.54 19.31 16.51 21.61 6.32 5.19 7.68 15.0 13.3 15.7
815-2A 2816 3.86 2.53 5.79 14.82 11.93 17.39 12.09 7.79 15.7526.02 23.7927.72 4.84 4.07 5.31 14.9 14.2 15.6
-------
RUN SUMMARY - SOLIDS ANALYTICAL DATA (CONTINUED)
PERCENT PERCENT
SULFITE STOICHIOMETRIC IONIC
AMALY OXIDATION RATIO IMBALANCE
RUN TICAL
NO. POINT AVG MIN MAX AVG MIN MAX AVG MIN MAX
719-2A 2816 19.8 13.4 30.8 1.15 1.03 1.33 0.8 -5.1 7.5
2825
801-2A 2816 52.5 37.7 65.5 1.22 1.08 1.42 -0.1 -5.3 7.8
2825
801-2B 2816 62.8 48.1 72.3 1.27 1.13 1.47 1.2 -3.9 6.7
2825
802-2A 2816 55.6 42.9 68.7 1.22 1.12 1.30 1.9 -3.6 7.5
2825
803-2A 2816 88.7 65.6 96.6 1.06 1.01 1.21 1.7 -8.4 8.3
2825
804-2A 2816 93.0 79.5 100.0 1.07 1.03 1.15 1.5 -7.7 8.4
2825
805-2A 2816 92.0 69.3 98.8 1.23 1.02 2.20 2.5 -5.3 7.1
2825
2831 91.9 74.6 98.9 1.12 1.01 1.63 1.7 -6.2 8.0
906-2A 2816 58.0 36.7 78.7 1.12 1.03 1.26 2.0 -8.2 5.8
2825
2831 54.3 35.2 78.2 1.12 1.05 1.27 2.3 -7.1 7.5
807-2A 2816 96.1 91.3 100.0 1.23 1.09 1.37 -0,7 -8.2 4.6
2825
2831 96.1 89.6 100.0*1.24 1.04 1.51 0.3 -7.0 6.4
808-2A 2816 91.8 81.9 99.1 1.63 1.37 2.26 0.3 -8.1 7.5
2825
2831 88.6 48.1 99.1 1.74 1.422.76 -7.4 8.4
B09-2A 2816 96.1 86.8 98.5 1.68 1.44 2.08 3.1 -3.7 8.5
2825
2831 95.3 82.2 99.1 1.70 1.34 2.72 2.6 -4.0 8.1
810-2A 2816 96.9 90.1 99.5 1.31 1.06 1.49 -2.1 -7.8 6.5
2825
2831 96.5 89.9 99.6 1.31 1.09 1.66 -1.2 -8.0 7.2
B11-2A 2816 94.4 82.7 98.3 1.74 1.28 2.08 -1.8 -8.0 7.4
2825
2831 90.1 76.0 98.0 2.59 1.52 7.52 1.7 -7.8 8.2
812-2A 2816 92.2 85.1 97.5 1.89 1.44 3.32 1.4 -8.1 8.4
2825
2831 89.9 80.6 96.7 1.99 1.35 3.70 -0.5 -8.2 7.5
813-2A 2816 94.3 85.2 99.1 1.15 1.06 1.60 -2.9 -7.8 8.4
2825
2831 93.4 82.6 99.2 1/10 1.02 1.36 -1.8 -7.1 6.2
814-2A 2816 62.9 48.7 84.6 1.15 1.05 1.36 -4.3 -7.4 -0.9
2825
2831 63.5 55.8 74.7 1.15 1.05 1.37 -2.7 -7.1 2.4
815-2A 2816 39.3 29.8 49.8 1.23 1.14 1.35 -1.3 -7.6 4.5
B-105
-------
RUN SUMMARY - SOLIDS ANALYTICAL DATA
CONCENTRATIONS IN SOLIDS, WT X
ACID INSOLUBLES SOLIDS
ANALY C02 S02 SO3 CAO WT % IN SLURRY WT X IN SLURRY
RUN TICAL
NO. POINT AVG MIN MAX AVG MIN MAX AVG MIN MAX AVG MIN MAX AVG MIN MAX AVG MIN MAX
815-2A 2825
816-2A 2816 4.70 3.74 5.69 10.22 8.44 13.04 13.59 9.80 15.44 24.24 23.36 25.74 5.19 4.80 6.07 15.2 13.8 16.0
2825
2832 4.36 3.30' 5.31 11.15 8.86 13.41 13.09 9.82 16.36 24.09 23.50 25.29 5.57 4.79 6.80 16.3 14.8 17.9
817-2A 2816 2.93 1.87 3.74 1.18 0.28 3.44 22.31 13.25 24.83 20.14 13.64 22.59 5.25 3.97 8.08 14.6 13.2 17.7
TO 2825
i 2632 2.64 1.37 3.52 1.25 0.36 3.11 24.26 20.26 27.56 21.15 19.44 23.71 5.35 4.33 7.29 14.8 12.6 17.1
r" 818-2A 2816 4.30 3.19 5.58 7.21 4.70 9.23 17.91 14.39 21.0425.17 23.41 26.44 4.82 3.87 6.11 14.9 14.1 16.3
en 2825
2832 4.58 3.80 5.95 7.54 4.34 10.13 17.69 13.68 22.47 25.60 23.50 27.77 4.61 3.71 5.91 15.0 13.5 16.2
B18-2B 2816 4.26 2.19 5.87 19.80 17.01 22.86 7.71 5.35 10.87 28.42 25.53 31.34 4.16 3.57 4.68 14.3 13.4 15.3
2825
819-2A 2816 3.92 1.48 6.57 1.17 0.18 2.76 21.72 17.71 26.51 21.20 15.67 26.43 4.70 2.99 6.53 12.9 10.7 14.7
2825
820-2A 2816 6.96 3.4S 9.79 1.30 0.36 2.17 18.44 10.11 22.3623.34 13.20 26.86 4.77 2.97 7.02 13.8 11.7 15.6
2825
B21-2A 2816 3.66 1.00 9.60 0.86 0.20 2.10 20.89 10.48 27.23 19.53 14.50 24.20 6.76 5.20 11.50 14.9 13.4 16.1
2825
-------
RUN SUMMARY - SOLIDS ANALYTICAL DATA (CONTINUED)
PERCENT PERCENT
SULFtTE STOICHIOMETRIC IONIC
ANALY OXIDATION . RATIO IMBALANCE
RUN TICAL
NO. POINT AV6 MIN MAX AVG MIN MAX AVG MIN MAX
815-2A 2625
816-2A 2616 51.6 37.6 58.9 1.33 1.25 1.42 -0.9 -6.0 3.6
2825
2632 48.3 36.9 59.6 1.30 1.22 1.38 -1.6 -4.8 3.6
817-2A 2816 93.9 82.1 98.6 1.24 1.14 1.42 -1.3 -6.7 3.0
2625
2832 93.9 84.1 98.3 1.19 1.08 1.24 -1.5 -7.9 5.9
B18-2A 2816 66.5 55.5 78.2 1.29 1.22 1.38 3.4 0.1 6.5
2825
2832 65.2 53.8 60.6 1.31 1.24 1.40 3.0 -0.9 7.4
818-2B 2816 23.B 15.8 32.9 1.24 1.11 1.34 0.8 -2.8 4.5
2825
819-2A 2816 93.7 86.1 99.1 1.31 1.11 1.56 -0.2 -8.5 5.5
2825
820-2A 2816 91.7 84.6 98.0 1.64 1.32 1.97 1.9 -3.5 7.3
2825
B21-2A 2816 94.8 83.1 98.9 1.35 1.06 2.28 -2.6 -8.3 6.4
2825
B-107
-------
TECHNICAL REPORT DATA
(Please read Instructions on the reverse before completing)
1. REPORT NO.
EPA-600/7-80-115
2.
3. RECIPIENTS ACCESSION NO.
a. TITLE AND SUBTITLE EpA Alkali Scrubbing Test Facility:
Advanced Program—Final Report (October 1974-June
1978)
5. REPORT DATE
May 1980
6. PERFORMING ORGANIZATION CODE
7. AUTHOR(S)
D.A.Burbank and S.C.Wang
8. PERFORMING ORGANIZATION REPORT NO.
9. PERFORMING ORGANIZATION NAME AND ADDRESS
Bechtel National, Inc.
50 Beale Street
San Francisco, California 94105
10. PROGRAM ELEMENT NO.
EHE624
11. CONTRACT/GRANT NO.
68-02-1814
12. SPONSORING AGENCY NAME AND ADDRESS
EPA, Office of Research and Development
Industrial Environmental Research Laboratory
Research Triangle Park, NC 27711
13. TYPE OF REPORT AND PERIOD COVERED
Final: 10/74-6/78
14. SPONSORING AGENCY CODE
EPA/600/13
IB. SUPPLEMENTARY NOTES JERL-RTP project officer is John E. Williams, Mail Drop 61.
919/541-2483. EPA-600/2-75-050, 600/7-76-008, 600/7-77-105, and 600/7-79-244j
and -244b are related progress reports.
16. ABSTRACT
The report summarizes results of advanced testing (from October 1974
through June 1978) of 30,000-35,000 acfm (10 MW equivalent) lime/limestone wet
scrubbers for SO2 and particulate removal at TVA's Shawnee power station. Reliable
scrubber and mist eliminator operations were demonstrated. It was shown that the
mist eliminator is much easier to keep clean when the scrubber is operated under
conditions giving high alkali utilization. Mathematical models were developed for
predicting SO2 removal in limestone, lime, and magnesium-enhanced lime/lime-
stone scrubbers. Forced oxidation with two scrubber loops was developed on the
venturi/spray tower system with limestone, lime, and limestone/MgO slurry. Bleed
stream oxidation was successful only with limestone/MgO slurry. Forced oxidation
with a single scrubber loop was developed on the TCA system with limestone slurry.
Other test blocks included limestone type and grind, automatic limestone feed con-
trol, Ceilcote egg-crate packing in the TCA, and flue gas emission characterization.
17.
KEY WORDS AND DOCUMENT ANALYSIS
DESCRIPTORS
b.lDENTIFIERS/OPEN ENDED TERMS
COSATI Field/Group
Pollution
Flue Gases
Scrubbers
Calcium Oxides
Calcium Carbonates
Magnesium Oxides
Sulfur Oxides
Dust
Aerosols
Mist
Mathematical Models
Pollution Control
Stationary Sources
Alkali Scrubbing
Particulate
Mist Eliminators
13B
21B
07A,13I
07B
11G
07D
04B
12A
18. DISTRIBUTION STATEMENT
Release to Public
19. SECURITY CLASS (ThisReport)
Unclassified
21. NO. OF PAGES
382
20. SECURITY CLASS (Thispage)
Unclassified
22. PRICE
EPA Term 2220-1 (9-73)
B-108
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