f/EPA
United States
Environmental Protection
Agency
Industrial Environmental Research EPA-600/7-76-008
Laboratory September 1976
Research Triangle Park NC 27711
EPA Alkali Scrubbing
Test Facility:
Advanced Program
Second Progress Report
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 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-600/7-76-008
September 1976
EPA ALKALI SCRUBBING
TEST FACILITY:
ADVANCED PROGRAM
Second Progress Report
Harlan N. Head, Project Manager
Bechtel Corporation
50 Beale Street
San Francisco, California 94119
Contract No. 68-02-1814
Program Element No. EHE624
EPA Project Officer: John E. Williams
Industrial Environmental Research Laboratory
Office of Energy, Minerals, and Industry
Research Triangle Park, NC 27711
Prepared for
U.S. ENVIRONMENTAL PROTECTION AGENCY
Office of Research and Development
Washington, DC 20460
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ABSTRACT
This report presents the test results from June 1975 through mid-
February 1976 of an Advanced Test Program on a prototype lime/lime-
stone wet-scrubbing test facility for removing SO2 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 in lime and
limestone service and a Turbulent Contact Absorber (TCA) in lime-
stone service, each with a 30,000 acfm (10 MW equivalent) flue gas
capacity.
Single, three-pass, open-vane chevron mist eliminators were used in
both systems. Reliable operation of the mist eliminator was found to
be strongly dependent on the alkali utilization (moles SC>2 absorbed/
mole Ca added). Above about 85 percent utilization, an intermittent
topside and bottomside makeup water wash kept the mist eliminator
clean. Below 85 percent utilization, plugging occurred, but a con-
tinuous bottomside wash with diluted clarified liquor, coupled with an
intermittent topside wash with makeup water, stabilized the mist elim-
inator solids restriction below 10 percent. Tests were run at 9.4 and
12.5 ft/sec superficial velocity in the spray tower and TCA, respec-
tively, and at 8 to 1 5 percent slurry solids concentration.
An 1143-hour, variable-load test with lime slurry in the venturi/spray
tower system demonstrated that the system can be operated with good
control when following a typical daily boiler load cycle.
Limestone utilization tests were conducted to correlate utilization with
scrubber inlet liquor pH, hold tank residence time, and hold tank de-
sign. Utilization was unaffected by a change from 20 to 12 minutes
residence time, but utilization declined at 6 minutes residence time.
Three hold tanks in series improved utilization.
11
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CONTENTS
Section Page
1 SUMMARY 1 -1
1. 1 Venturi/Spray Tower Lime Reliability
Test Results 1-2
1.2 Venturi/Spray Tower Variable-Load
Test Results 1-3
1. 3 TCA Limestone Reliability Test Results , 1-4
1.4 Results of Limestone Utilization Tests in
the Venturi/Spray Tower and TCA Systems 1-6
1. 5 Laboratory Quality Assurance Program 1-9
1.6 Operating Experience During Lime/
Limestone Testing 1-9
2 INTRODUCTION 2-1
3 TEST FACILITY 3-1
3. 1 Scrubber Selection 3-1
3. 2 System Description 3-3
3. 3 EPA Pilot Plant Support 3-10
4 TEST PROGRAM 4-1
4. 1 Test Program Objectives and Schedule 4-1
4. 2 Closed-Liquor-Loop Operation 4-4
4. 3 Analytical Program 4-4
4.4 Data Acquisition and Processing 4-6
5 VENTURI/SPRAY TOWER LIME RELIABILITY
TEST RESULTS 5-1
5. 1 Performance Data and Test Evaluation 5-1
5.2 Conclusions . 5_7
111
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Section Page
VENTURI/SPRAY TOWER VARIABLE-LOAD
TEST RESULTS 6-1
6. 1 Performance Data and Test Evaluation 6-1
6. 2 Conclusions 6-7
TCA LIMESTONE RELIABILITY TEST RESULTS 7-1
7. 1 Testing with Two Chevron Mist Elim-
inators in Series 7-2
7. 2 Testing with a Single Chevron Mist
Eliminator 7-9
7. 3 Conclusions 7-16
LIMESTONE UTILIZATION TESTING IN THE
VENTURI/SPRAY TOWER AND TCA SYSTEMS 8-1
8. 1 Utilization Testing in the Venturi/Spray
Tower System with Variable Residence
Time 8-3
8. 2 Utilization Testing in the TCA System
with Three Hold Tanks in Series 8-12
8. 3 Utilization Data from Depletion Runs 8-20
8.4 Mist Eliminator Operability During
Limestone Utilization Testing 8-20
8. 5 Conclusions 8-29
LABORATORY QUALITY ASSURANCE
PROGRAM 9-1
9- 1 Quality Assurance Criteria 9_2
9. 2 Evaluation and Modifications of
Analytical Procedures 9_2
9. 3 Current Quality Assurance Measures 9-11
IV
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Section Page
10 OPERATING EXPERIENCE DURING LIME/
LIMESTONE TESTING 10-1
10.1 Scrubber Internals 10-1
10.2 Reheaters 10-6
10.3 Fans 10-7
10.4 Pumps 10-8
10. 5 Waste Solids Handling 10-9
10.6 Alkali Addition Systems 10-11
10.7 Instrument Operating Experience 10-13
10.8 Materials and Equipment Evaluation
Program 10-16
11 REFERENCES 11-1
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Appendices Page
A Converting Units of Measure A-l
B Scrubber Operating Periods B-l
C Properties of Raw Materials C-l
D Data Base Tables D-l
E Test Results Summary Tables for
the Venturi/Spray Tower E-l
F Graphical Operating Data from the
Venturi/Spray Tower Tests F-l
G Average Liquor Compositions for the
Venturi Spray Tower Tests G-l
H Test Results Summary Table for the TCA H-l
I Graphical Operating "Data from the
TCA Tests 1-1
J Average Liquor Compositions for the
TCA Tests J-l
K Analytical Precision and Accuracy
Procedures K-l
L Third TVA Interim Report of Corrosion
Studies ' L-l
VI
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ILLUSTRATIONS
Figure Page
3-1 Schematic of Venturi Scrubber and Spray Tower 3-4
3-2 Schematic of Three-Bed TCA Scrubber 3-5
3-3 Test Facility Mist Eliminator Configurations 3-6
3-4 Typical Process Flow Diagram for Venturi/
Spray Tower System 3-8
3-5 Typical Process Flow Diagram for TCA System 3-9
4-1 Shawnee Advanced Test Schedule . 4-3
8-1 Stoichiometric Ratio versus Scrubber Inlet Liquor
pH in the Venturi/Spray Tower Tower System with
a Single Hold Tank at 20 Minutes Residence Time 8-4
8-2 Stoichiometric Ratio versus Scrubber Inlet Liquor
pH in the Venturi/Spray Tower System with a Single
Hold Tank at 12 Minutes Residence Time 8-5
8-3 Stoichiometric Ratio versus Scrubber Inlet Liquor
pH in the Venturi/Spray Tower System with a Single
Hold Tank at 6 Minutes Residence Time 8-6
8-4 The Effect of Effluent Hold Tank Residence Time and
Scrubber Inlet Liquor pH on Stoichiometric Ratio in the
Venturi/ Spray Tower System 8-8
8-5 The Effect of Stoichiometric Ratio and Effluent Resi-
dence Time on Percent SO2 Removal in the Venturi/
Spray Tower System with a Single Hold Tank 8-9
8-6 The Effect of Scrubber Inlet Liquor pH on Percent
SC>2 Removal in the Venturi/Spray Tower System 8-10
8-7 The Effect of Scrubber Inlet Liquor pH and Inlet Gas
SC>2 Concentration on Percent SO2 Removal in the
Venturi/Spray Tower System 8-11
8-8 Stoichiometric Ratio versus Scrubber Inlet Liquor pH
in the TCA System with a Single Hold Tank at 12 Minutes
Residence Time 8-14
VII
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ILLUSTRATIONS
Figure Page
8-9 Stoichiometric Ratio versus Scrubber Inlet Liquor
pH in the TCA System with Three Hold Tanks in
Series at 14.4 Minutes Residence Time 8-15
8-10 Stoichiometric Ratio versus Scrubber Inlet Liquor
pH in the TCA System with Three Hold Tanks in
Series at 10.8 Minutes Residence Time 8-16
8-11 The Effect of Scrubber Inlet Liquor pH and Hold
Tank Configuration on Stoichiometric Ratio in the
TCA System 8-17
8-12 The Effect of Stoichiometric Ratio and Hold Tank
Configuration on Percent SC>2 Removal in the TCA
System 8-19
8-13 Stoichiometric Ratio versus Scrubber Inlet Liquor
pH for Depletion Test at 6 Minutes Residence Time
in the Venturi/Spray Tower System 8-21
8-14 Stoichiometric Ratio versus Scrubber Inlet Liquor
pH for Depletion Tests in the TCA System with
Three Hold Tanks in Series at 10. 8 Minutes
Residence Time 8-22
8-15 Stoichiometric Ratio versus Scrubber Inlet Liquor
pH for Depletion Tests in the TCA System with
Three Hold Tanks in Series at 14.4 Minutes
Residence Time 8-23
9-1 Results of Analysis for CaO by X-Ray Fluorescence
Spectrometry with Known Values for CaO in the
Prepared Samples q_4
9-2 Results of Analysis for SO3 by X-Ray Fluorescence
Spectrometry with Known Values for 803 in the
Prepared Samples 05
9-3 Results of Analysis for MgO by X-Ray Fluorescence
Spectrometry with Known Values for MgO in the
Prepared Sample o_£
10-1 Failure Rate of 6-Gram TPR Spheres in Limestone/
Fly Ash Slurry Service 10-3
Vlll
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TABLES
Table Page
4-1 Field Methods for Batch Chemical Analysis of
Slurry and Alkali Samples 4-5
8-1 Summary of Venturi/Spray Tower Limestone
Utilization and Mist Eliminator Tests 8-24
8-2 Summary of TCA Limestone Utilization and
Mist Eliminator Tests 8-25
10-1 Summary of Filter Cloths Tested at Shawnee 10-10
IX
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A CKNO WLEDGMENT
The following Bechtel personnel were the principal contributors to
the preparation of this report:
Dr. H. N. Head, Project Manager
Dr. M. Epstein, Project Manager to March 1976
A. H. Abduls attar R. G. Rhudy
D. A. Burbank R. W. Row
Dr. J. S. DeGuzman C. H. Rowland
R. T. Keen Dr. K. A. Strom
C. C. Leivo Dr. S. C. Wang
The authors wish to acknowledge the various personnel from the
Environmental Protection Agency and the Tennesse Valley Authority
who also contributed to the preparation of this report.
The authors also wish to acknowledge the contributions of the Bechtel
and TVA onsite personnel at the Shawnee Test Facility.
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Section 1
SUMMARY
This is the second progress report on an Advanced Test Program under
the direction of the Environmental Protection Agency (EPA) to test pro-
totype lime and limestone wet-scrubbing systems for removing sulfur
dioxide and particulate matter from coal-fired boiler flue gases. It
covers the period from June 1975 through mid-February 1976. Results
of earlier testing have been reported in EPA-650/2-75-047 and EPA-
600/2-75-050. The program is being conducted in a test facility inte-
grated into the flue gas ductwork of Boiler No. 10 at the Tennessee
Valley Authority (TVA) Shawnee Power Station, Paducah, Kentucky.
Bechtel Corporation of San Francisco is the major contractor and test
director, and TVA is the constructor and facility operator.
There are two parallel scrubbing systems being operated during the
Advanced Test Program:
• A venturi followed by a spray tower
• A Turbulent Contact Absorber (TCA)
1-1
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Each system is capable of treating approximately 10 MW equivalent
(30,000 acfm* @ 300°F) of flue gas containing 1500 to 4500 ppm sulfur
dioxide and 2 to 5 grains/scf of particulates.
The most significant result during this reporting period was the dis-
covery that mist eliminator reliability improves dramatically with in-
crease in alkali utilization (moles SO? absorbed/mole Ca added). Major
areas of testing included:
• Reliability testing of several mist eliminator configurations
with lime and limestone
• Variable load testing with lime on the venturi/spray tower
• Alkali utilization testing with limestone on both systems
1. 1 VENTURI/SPRAY TOWER LIME RELIABILITY TEST RESULTS
Lime reliability tests were continued from June through August 1975
on the adjustable-throat venturi followed by a four-header spray tower.
The spray tower had a three-pass, open-vane chevron mist eliminator
with provision for both underside and topside intermittent washing.
The mist eliminator was washed with makeup water. The underside
wash rate was 1.5 gpm/ft^ for 4 to 6 minutes every 4 hours. The
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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topside wash was accomplished by operating six nozzles in sequence.
Every 80 minutes, one nozzle was activated for 4 minutes at a rate
of 0. 5 gpm/ft . Since the previous report, superficial gas velocity was
increased to 9. 4 ft/sec (the system's maximum), mist eliminator wash
rate was reduced, solids concentration was increased to 15 percent,
and 1075 hours of operation were logged with essentially no fouling
of the mist eliminator (2 to 3 percent restriction at the end of the
period).
1. 2 VENTURI/SPRAY TOWER VARIABLE-LOAD TEST RESULTS
From August to October 1975, cycling gas load tests were conducted
on the venturi/spray tower with lime slurry. During these tests, the
gas rate was adjusted hourly to follow the daily boiler load cycle,
which ranged from 60 to 160 MW. The test series was divided into two
parts. The first part was a 717-hour test in which the venturi plug
position was adjusted according to the varying gas flow rate to main-
tain a constant 9-inch I^O pressure drop across the venturi. The
second part was a 426-hour test with the venturi plug fixed at a position
giving a 9-inch H^O pressure drop across the venturi at the maximum
gas flow rate of 35, 000 acfm.
Throughout the 1, 143 hours of operation, the system ran reliably with
good control and the mist eliminator remained clean.
1-3
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SO2 removal ranged from 70 to 98 percent at inlet SO2 concentrations
of 1500 to 4400 ppm; lime utilization (moles SO2 absorbed/mole Ca
added) averaged 90 percent; and total pressure drop was 7 to 1 5 inches
H2O, including the mist eliminator system and 4 to 9 inches H2O across
the venturi. Sulfate (gypsum) saturation* was 90 to 100 percent .
1. 3 TCA LIMESTONE RELIABILITY TEST RESULTS
1. 3. 1 Testing with Two Chevron Mist Eliminators in Series
During the boiler outage in May 1975, the old mist eliminator system in
the TCA (washtrayin series witha six-pass, closed-vane chevron mist
eliminator) was replaced with a new system. The new system con-
sisted of two identical three-pass, closed-vane, fiberglass-reinforced
plastic (FRP) chevron mist eliminators in series, with provision for
intermittent topside and bottomside wash of the lower mist eliminator.
A combination of intermittent topside wash with freshwater (2. 0 gpm/ft
for 30 seconds every 10 minutes) and continuous underside wash (up to
o
0.45 gpm/ft^1) using diluted clarified liquor on the lower stage did not
prevent solids accumulation in the mist eliminators during short runs.
Defined as (activity Ca++) x (activity SO4~)/(solubility product at
50°C). Estimated solubility product for CaSO4. 2H2O at 50°C is 2. 2
x 10~5 (Ref. Radian Corporation, "A Theoretical Description of the
Lime stone-Injection Wet Scrubbing Process," NAPCA Report, June
Q i Qvm
1-4
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At the end of an 89-hour run, the upper and lower mist eliminators
were 5 percent and 8 to 10 percent restricted, respectively. Alkali
utilization during these tests ranged from 65 to 85 percent. Long-
term reliability runs were not attempted with this two-stage system.
1.3.Z Testing with One Chevron Mist Eliminator
Because of the success of the single-stage 316L stainless-steel, three-
pass, open-vane chevron mist eliminator inlime service in the venturi/
spray tower, a similar mist eliminator was fabricated and installed
in the TCA. Testing of this system with limestone slurry began in July
1975 and continued through October.
In tests at both 12. 5 and 9-4 ft/sec scrubber gas velocity (8. 2 and 6. 1
ft/sec superficial gas velocity in the enlarged mist eliminator area),
plugging of the mist eliminator could not be prevented by a combina-
tion of intermittent topside and bottomside makeup -water wash. This
was unexpected because of the successful operation of the same mist
eliminator on lime service in the venturi/spray tower. Alkali utiliza-
tion ranged from 60 to 75 percent during these limestone tests. In
contrast, alkali utilization is normally above 95 percent in operation
with lime. Later testing revealed the strong effect of alkali utilization
on mist eliminator reliability.
1-5
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A combination of sequential topside wash with makeup water and contin-
uous underside wash with diluted clarified process liquor was found
to limit the buildup of solids in the mist eliminator to a steady-state
level of about 10 percent restriction. Solids accumulation occurred
mostly in the shadowed areas of the mist eliminator vanes and support
rails not directly impinged by the underside wash liquor.
1.4 RESULTS OF LIMESTONE UTILIZATION TESTS IN
THE VENTURI/SPRAY TOWER AND TCA SYSTEMS
From October 1975 through mid-February 1976, limestone tests were
conducted on both the venturi/spray tower and the TCA to explore for
methods of improving the utilization of the limestone feed (moles SO?
absorbed/mole Ca added). The results ofaTVA economic study showed
that improved limestone utilization would significantly improve the pro-
cess economics. Limestone utilization on both systems 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 the lower scrubber inlet liquor pH values, however, caused
a reduction in SO2 removal efficiency. For instance, at 2500 to 3500
ppm inlet SO2 concentration, SO2 removal in the venturi/spray tower
system was about 88 percent at a. scrubber inlet liquor pH of 6. 0 and
55 percent at a pH of 5. 2. But tests demonstrated that improved
1-6
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removal at high limestone utilization can be achieved by using three
hold tanks in series or by adding MgO to the scrubber slurry. These
tests will be described later.
1.4.1 Utilization Testing in the Venturi/Spray Tower
System with Variable Residence Time
In the venturi/spray tower system, limestone tests were conducted with
a single backmix effluent hold tank at residence times of 20, 12, and
6 minutes. Below a scrubber inlet liquor pH of about 5. 8, limestone
utilization tended to be higher at 12 to 20 minutes residence time than
at 6 minutes residence time. Above a pH of 5. 8, the scatter in the
data was too great to draw a conclusion.
1.4.2 Utilization Testing in the TCA System with
Three Hold Tanks in Series
In the TCA system, limestone tests were conducted-with a single stirred
hold tank and with three stirred tanks in series to approximate plug
flow reaction. Kinetic theory predicts that raw materials utilization
should improve •with the series hold tanks.
Within the range of total effluent residence times tested (10.8 to 14.4
minutes) and at scrubber inlet liquor pH values greater than about 5. 0,
higher limestone utilization was achieved with three hold tanks in se-
ries thanwitha singlehold tank. For example, ata pH of 5.7, limestone
1-7
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utilization increased from 79 percent with a single hold tank to 87
percent with three hold tanks in series.
1.4.3 Mist Eliminator Operability During Limestone
Utilization Testing
The most significant discovery during this reporting period was that
the reliability of the mist elimination system was a strong function of
alkali utilization. During the limestone utilization testing period, both
the venturi/spray tower and the TCA had single-stage, 316L stainless-
steel, three-pass, open-vane chevron mist eliminators.
For alkali utilization greater than about 85 percent, the mist elim-
inators were kept free of solids deposits by an intermittent top wash
with makeup water combined with either intermittent bottom wash with
makeup water or continuous bottom wash with diluted clarified liquor.
For alkali utilization less than about 85 percent, intermittent top and
bottomside wash with makeup water did not limit solids accumulation.
However, for these conditions, a. continuous bottom wash of diluted
clarified liquor used in combination with an intermittent topside wash
with makeup water limited the restriction within the mist eliminator
due to soft solids buildup to less than 10 percent. With this wash
1-8
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configuration, soft solids quickly accumulated to a maximum restric-
tion, which did not change for the duration of the run.
1. 5 LABORATORY QUALITY ASSURANCE PROGRAM
Because of the increased emphasis on chemical analysis during the
advanced test program, a laboratory quality assurance program was
initiated. Asaresultof this quality assurance program, several analyt-
ical methods have been modified or replaced. All methods have been
documented in the Shawnee Chemical Procedures Laboratory Manual,
•which is available on request.
Major areas in which revised analytical procedures have been intro-
duced are:
• X-ray spectrometry analysis for calcium, total sulfur, and
magnesium in solid samples
• Measurements of the pH of the scrubber slurry
• Amperometric titration of sulfite
1. 6 OPERATING EXPERIENCE DURING LIME/LIMESTONE
TESTING
Mist elimination systems have already been discussed. This sub-
section covers other aspects of scrubber system operations.
1-9
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1.6.1 Scrubber Internals
Beginning in June 1975, 6-gram thermoplastic rubber (TPR) spheres
were used in the TCA. Dimpling appeared to be about the same as with
the previously used 5-gram spheres. After 3800 hours of testing, about
11 percent of the 6-gram spheres had failed from splitting at the seams,
The average weight loss for the unsplit spheres was 10 percent.
In December 1975, the hollow TPR spheres were replaced with 6. 5-
gram nitrile solid foam spheres. After the initial 240 hours of oper-
ation, the spheres had shrunk to about 91 percent of their original
diameter but had lost only 1 percent of their original weight. No
additional change in weight or diameter was noted in an inspection
at 574 hours. A new batch of nitrile foam spheres made by a modi-
fied manufacturing procedure was installed in early February 1976.
These spheres did not experience an initial shrinkage. Quantitative
data will be given in the next progress report.
The 316 stainless-steel bar grids in the TCA have exhibited no erosion
after 16,000 hours of operation. The 316 stainless-steel slurry spray
nozzles, operating with 15 percent slurry solids at 5 psi pressure
drop, have shown no evidence of erosion after 9000 hours of operation.
1-10
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In the spray tower, stellite tips on the spray nozzles, operating with
8 to 15 percent slurry solids at 10 psi pressure drop, lost 40 percent
of their original weight during 11,700 hours of service. Wear was
greater during periods of operation with limestone than during periods
of operation with lime. The 316 stainless-steel reducers connecting
the nozzles to the headers have worn badly. Occasionally the reducers
have worn through and the nozzles have fallen off.
Both neoprene rubber and Flakeline 103 linings used on equipment in
contact with the scrubber slurry have continued to demonstrate excel-
lent resistance to erosion and deterioration. However, a Flakeline 103
test panel-mounted inside one of the TCA beds was significantly eroded.
1.6.2 Reheaters
The fuel-oil-fired external combustion reheaters have operated reliably
for over 13,700 hours on the venturi/spray tower system and 4400
hours on the TCA system.
1. 6. 3 Fans
There has been no system downtime due to fan problems during this
reporting period. A crack on the venturi/spray tower fan rotor shroud
was repaired during the May 1975 boiler outage.
1-11
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1 • 6. 4 Pumps
Pump seal failures have continued to be a problem. The frequency of
repacking on the 20 to 100 gpm pumps has been minimized by main-
taining the clearance between the shaft and the packing gland at 10
to 15 mils. Two mechanical seals have been tested on slurry bleed
pumps. One failed after 1500 hours of service, but the other was still
in operation at 4000 hours of service.
1.6.5 Waste Solids Handling
The rotary-drum vacuum filter has continued to suffer from short cloth
life: the longest cloth life during this reporting period was 642 hours
of service. Since the lastmajor resurfacing of internals, the centrifuge
has logged 3500 hours of satisfactory intermittent operation, and since
the feedwell was extended during the May 1975 boiler outage, the TCA
clarifier has had fewer upsets.
1.6.6 Alkali Addition Systems
The lime addition system has operated reliably for over 15,800 hours of
intermittent operation. The only significant problems have been occa-
sional slaker screen blinding and grit plugs in the feed pipe. The lime-
stone addition system has operated satisfactorily for the 4-year life of
1-12
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of the program. The alkali addition system pumps are Moyno posi-
tive displacement pumps. Typical operating life for a pump rotor
was 2000 hours and for a stator, 1000 hours.
1.6.7 Instruments
Scale formation on the submersible pH probes has occasionally caused
measurement error. This problem has been minimized by routinely
rinsing with water about twice a week and recalibrating when necessary.
Adiprene-L liner failures in the 1-1/2-inch magnetic flow meters were
caused by a tapered thickness near the meter exit. No more failures
have occurred since the meters were relined with Adiprene-L of uni-
form thickness.
Slurry tank level indication has continued to be a problem. Problems
with the Brooks Maglink level indicators have included jamming of the
float by floating materials, flush liquor depressing the float and causing
reading error, and uncoupling of the float from the magnet. However,
when properly maintained and calibrated, the Brooks level indicator
does measure effluent hold tank level to within _+ 6 inches.
The Du Pont UV SO2 analyzers have operated trouble-free.
1-13
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1.6.8 Mechanical Components Evaluation
Selected mechanical components have been continually evaluated at
the Shawnee Test Facility. These include plastic pipe, butterfly and
knife gate valves, line strainers, mechanical seals, an orifice plate,
and several Ceilcote lining materials.
1-14
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Section 2
INTRODUCTION
In June 1968, a program was initiated under the direction of the Envi-
ronmental Protection Agency (EPA)* to test a prototype lime and lime-
stone wet-scrubbing system for removing sulfur dioxide and particu-
lates from flue gases. The system was integrated into the flue gas
ductworkof a coal-fired boiler at the Tennessee Valley Authority (TVA)
Shawnee Power Station, Paducah, Kentucky. Bechtel Corporation
of San Francisco was the major contractor and test director, and TVA
was the constructor and facility operator.
The test facility consisted of three parallel scrubber systems: a venturi
followed by a spray tower, a Turbulent Contact Absorber (TCA), and
a Marble-Bed Absorber. Each system was capable of treating approx-
imately 10 MW equivalent (30,000 acfm @ 300°F)of flue gas containing
1500 to 4500 ppm sulfur dioxide and 2 to 5 grains/scf of particulates.
The National Air Pollution Control Administration prior to 1970
2-1
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The results of testing at the facility during the original program, -which
lasted fromMarch 1972 toOctober 1974, are presented in Reference 1.
The most significant reliability problem encountered during this testing
period was associated with scaling and/or plugging of mist elimination
surfaces. The TCA mist elimination system consisted of a washtray
in series with a chevron mist eliminator, both with underside washing.
Long-term operability of this system was demonstrated in limestone
service in an 1835-hour test at a scrubber gas velocity of 8. 6 ft/sec.*
The venturi/spray tower mist elimination system consisted of a chevron
rnist eliminator with underside washing. At the end of the original test-
ing program, long-term operability of the venturi/spray tower system
had not been demonstrated. Operation of the Marble-Bed Absorber was
discontinued in July 1973 (see Reference 1).
In June 1974, the EPA, through its Office of Research and Development
and Control Systems Laboratory, initiated a 3-year Advanced Test
Program at the Shawnee Facility. Bechtel Corporation continued as
the major contractor and test director, and TVAasthe constructor and
facility operator.
In this report, all gas velocities and liquid-to-gas ratios are at scrub-
ber operating conditions, i.e., saturated gas at scrubber tempera-
ture. With flue gas operations, the scrubber temperature is approx-
imately 125°F. The gas velocities are all superficial velocities.
2-2
-------
The major goals established for the advanced program were:
To continue long-term testing with emphasis on demonstrating
reliable operation of the mist elimination systems
To investigate advanced process and equipment design varia-
tions for improving system reliability and process economics
To perform long-term (2- to 5-month) reliability testing on
promising process and equipment design variations
The results of advanced testing from October 1974 through April 1975
at the Shawnee Facility are presented inReference 2. Successful opera-
tion of a chevron mist eliminator with intermittent top and bottom wash
was demonstrated in the venturi/spray tower system in lime service
at 8. 0 ft/sec. In the TCA in limestone service, plugging of the com-
bined washtray/mist eliminator system could not be prevented at veloc-
ities greater than 8.6 ft/sec. Tests were interrupted in May 1975
owing to a 6-week scheduled maintenance outage on Boiler No. 10.
This report presents the results of advanced testing at the Shawnee
Facility from June 1975 through mid-February 1976. During this period,
the TCA was operated on limestone. Mist eliminator testing was con-
tinued (see Reference 2), and the use of one- and two-stage systems,
different wash configurations, and different alkali utilization levels
was evaluated.
2-3
-------
The venturi/spray tower was operated on both lime and limestone.
Mist eliminator tests and variable-gas-load tests were run -with lime.
With limestone, mist eliminator tests and alkali utilization tests were
run.
2-4
-------
Section 3
TEST FACILITY
Two parallel scrubbing systems are being operated during the Advanced
Test Program. Scrubbers incorporated in these systems are:
• A venturi followed by a spray tower
• A Turbulent Contact Absorber (TCA)
Each system operates independently and is capable of treating approx-
imately 30,000 acfm of flue gas from the TVA Shawnee coal-fired
Boiler No. 10. This gas rate is equivalent to approximately 10 MW
of power plant capacity.
Boiler No. 10 normally burns a medium- to high-sulfur bituminous
coal which produces SC>2 concentrations of 1500 to 4500 ppm and inlet
particulate loadings of 2 to 5 grains/scf in the flue gas.
3. 1 SCRUBBER SELECTION
The major criterion for scrubber selection was the potential for remov-
ing both sulfur dioxide and particulates at high efficiencies (defined
3-1
-------
for the Shawnee Facility as sulfur dioxide removal greater than 80
percent and particulate removal greater than 99 percent). Other criteria
considered in the selection of the scrubbers were:
• Ability to handle slurries without plugging or excessive scaling
• Reasonable cost and maintenance
• Ease of control
• Reasonable pressure drop
The venturi/spray tower and the TCA were chosen to meet these cri-
teria.
The adjustable-throatventuri scrubber in the venturi/spray tower sys-
tem was manufactured by Chemical Construction Company. The ven-
turi scrubber removes the bulk of the particulates. But because the
residence time in a venturi scrubber is low, the scrubber with lime/
limestone slurry removes less than half of the SO->. The spray tower
that follows the venturi scrubber provides sufficient residence time for
the removal of most of the remaining SO?-
The TCA was manufactured by Universal Oil Products. It operates
with beds of nominal 1 -1 /2-inch-diameter low-density spheres that are
free to move between retaining grids. As the incoming flue gas contacts
the slurry in these beds, both SO.2 and particulates are removed.
3-2
-------
Figures 3-1 and 3-2 (drawn with major dimensions to scale) show the
two scrubber systems and the typical mist elimination systems se-
lected for deentraining slurry in the exit gas streams. The chevron
mist eliminators used during the testing on the two scrubber systems
are depicted, to scale, in Figure 3-3. The cross-sectional area of
2 7
the TCA scrubber is 32 ft in the scrubbing section and 49 ft in the
mist elimination section. The cross-sectional area of the spray tower
is 50 ft in both the scrubbing section and the mist elimination section.
3. 2 SYSTEM DESCRIPTION
The Shawnee Test Facility contains five major areas:
• The scrubber area (including tanks and pumps)
• The operations building area (including laboratory area, elec-
trical gear, centrifuge, and filter)
• The thickener area (including tanks and pumps)
• The utility area (including air compressors, air dryer, lime-
stone storage silos, mix tanks, gravimetric feeder, and pumps)
• The pond area
The test facility has been so designed that a number of different scrub-
ber internals and piping configurations can be used with each scrubber
system. For example, the TCA scrubber can be operated with one,
two, or three beds of spheres or with only the support grids. Waste
3-3
-------
GAS OUT
CHEVRON MIST
ELIMINATOR
SPRAY TOWER
INLET SLURRY
THROAT
ADJUSTABLE PLUG
VENTURI SCRUBBER
MIST ELIMINATOR
WASH WATER
iEST ELIMINATOR
WASH LIQUOR
EFFLUENT SLURRY
Figure 3-1. Schematic of Venturi Scrubber and Spray Tower
3-4
-------
GAS OUT
MIST ELIMINATOR
WASH WATER
" J
M
t
DN MIST / I
NATOR
GRIDS /
vHIWJ '">i
5 in jk,
A A A
XXX^XXX^XX-
T T
i
A /\ A
;-»?;-
Oo°o0°o°
o»p_o a. o
/BO
°oo o
s° 0 0 °0
~ o
OO o
2.°£L o3i_<£.
N /
MIST ELIMINA
-*£ _ HASH LIQU
4« — INI IT UlUBiY
/ MOBILE PACKING SPHER
5'
j |
APPROX. SCALE
EFFLUENT SLURRY
Figure 3-2. Schematic of Three-Bed TCA
3-5
-------
SPRAY TOWER AND TCA
TCA
THREE - PASS, OPEN - VANE, 316 S. S.
CHEVRON MIST ELIMINATOR
(HORIZONTAL CONFIGURATION)
TWO THREE - PASS, CLOSED - VANE,
FRP (fiberglass reinforced plastic)
CHEVRON MIST ELIMINATOR
(HORIZONTAL CONFIGURATION)
(only one shown)
OJ
I
GAS FLOW
GAS FLOW
6 in.
Figure 3-3. Test Facility Mist Eliminator Configurations
-------
solids separation can be achieved with a clarifier alone or with a clar-
ifier in combination with a filter or a. centrifuge. Either system can
be operated with a single backmix hold tank or with up to three tanks
in series.
Typical system configurations depicting lime testing with the venturi/
spray tower and limestone testing with the TCA scrubber are illus-
trated schematically in Figures 3-4 and 3-5, respectively. Such pro-
cess details as flue gas saturation (humidification) sprays are not shown.
For both systems, gas is withdrawn from the boiler ahead of the steam
plant particulate removal equipment so that all the entrained particulate
matter (fly ash) can be introduced into the scrubber. The gas flow rate
to each scrubber is measured by venturi flow meters and controlled
by dampers on the induced-draft fans. The concentration of sulfur diox-
ide in the inlet and outlet gas streams is monitored continuously by
Du Pont photometric analyzers.
The scrubbing systems are controlled from a central graphic panel-
board where all significant process variables are on digital display.
Important process control variables are continuously recorded. Trend
recorders are provided for periodic monitoring of selected data sources.
Chemical composition of major streams and scrubber inlet liquor pH
are determined several times a shift.
3-7
-------
i
00
SAMPLE POINTS
O Gas Composition
® Paniculate Composition & Loading
© Slurry or Solids Composition
SETTLING POND
Gas Stream
Liquor Stream
Figure 3-4. Typical Process Flow Diagram for Venturi/Spray Tower System
-------
I
NO
TCA
SCRUBBER
FLUE GAS J>- Q -Q -»
SAMPLE POINTS
O Gas Composition
tParticulate Composition 6 Loading
Slurry or Solids Composition
_ _ Gas Stream
____ Liquor Stream
I. D. FAN
I
I
L
/\ A A
,
i
STACK
SOILING POND
Figure 3-5. Typical Process Flow Diagram for TCA System
-------
3.3 EPA PILOT PLANT SUPPORT
There are two smaller scrubbing systems (300 acfm each) at the EPA
Industrial Environmental Research Laborabory in Research Triangle
Park, North Carolina. These small, pilot-scale scrubber systems
are capable of simulating the Shavmee scrubber systems with excel-
lent agreement in the lime/lime stone wet-scrubbing chemistry. Pre-
liminary data are generated on the pilot-scale system to verify and
guide the selection of those promising concepts that should logically
be investigated on the larger scale Shawnee units. Some of the results
from the support program have been presented in References 4 and 5.
3-10
-------
Section 4
TEST PROGRAM
This section contains a description of the Shawnee Advanced Test Pro-
gram, which is tentatively scheduled to run from June 1974 through
December 1977.
4. 1 TEST PROGRAM OBJECTIVES AND SCHEDULE
The objectives of the Advanced Test Program are:
To demonstrate process reliability with an emphasis on mist
elimination systems
To investigate advanced process and equipment design varia-
tions for improving system reliability and economics
To evaluate process variations for a substantial increase in
alkali utilization for limestone systems
To evaluate the effect of increased magnesium ion concentra-
tion on improving control, reducing gypsum saturation, and
increasing SO£ removal
To evaluate the efficiency and reliability of lime and limestone
scrubbers under conditions of widely varying flue gas flow rate
and inlet sulfur dioxide concentration
To evaluate system performance and reliability without fly ash
in the flue gas
4-1
-------
• To determine the effectiveness of forced oxidation for pro-
ducing an improved throwaway sludge product
• To determine the practical upper limits of sulfur dioxide
removal efficiency for both limestone and lime scrubbing
systems
• To evaluate the TCA performance with lime and the venturi/
spray tower performance with limestone
• To perform long-term (2- to 5-month) reliability demon-
stration runs on advanced process and equipment design var-
iations
• To characterize stack gas emissions, including outlet partic-
ulate mass loading and size distribution, slurry entrainment,
and total sulfate emissions
• To evaluate methods of automatic control
• To advise on the field evaluation of three commercially of-
fered sludge fixation processes. Aerospace Corporation is
the major contractor and test director for this effort
• To evaluate, under the direction of TVA, corrosion and wear
of alternative plant equipment components and materials
• To develop a. computer program, in conjunction with TVA,
for the design and cost comparison of full-scale lime and
limestone systems
The test program schedule based on the defined objectives is pre-
sented in Figure 4-1. The period covered by the Second Progress
Report extended from June 1975 through mid-February 1976. In the
TCA during this period, mist eliminator testing and alkali utilization
testing were conducted with limestone slurry. In the venturi/spray
tower, mist eliminator testing and variable-load testing were con-
ducted with lime slurry, and alkali utilization testing was conducted
with limestone slurry.
4-2
-------
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Figure 4-1. Shawnee Advanced Test Schedule
-------
4.2 CLOSED-LIQUOR-LOOP OPERATION
A closed liquor loop is achieved when the makeup-water input to the
system is equal to the water normally exiting the system in the set-
tled sludge and in the humidified flue gas. In this report, it was
assumed that a closed liquor loop is achieved when the solids concen-
tration of the purged sludge is 38 percent by weight or higher and no
separate liquor purge is taken. With few exceptions, the advanced
program tests are being conducted in closed-liquor-loop operation.;
The exceptions are typically short exploratory runs with limited objec-
tives. Such tests are noted when they occur.
\
4.3 ANALYTICAL PROGRAM
During the testing, samples of slurry, flue gas, limestone, lime,
and coal are taken periodically for chemical analyses, and samples
of flue gas ?"*e taken for particulate mass loading determinations.
The locations of slurry and gas sample points are shown on Figures
3-4 and 3-5. A summary of the analytical methods for determining
important species in the slurry solids and slurry liquor is presented
in Table 4-1. A laboratory procedures manual (Reference 6) was
issued in March 1976. A listing of the compositions of the raw ma-
terials used in the testing program is presented in Appendix B.
4-4
-------
Table 4-1
FIELD METHODS FOR BATCH CHEMICAL ANALYSIS
OF SLURRY AND ALKALI SAMPLES
SPECIES
Sodium
Potassium
Calcium
Magnesium
Sulfite
Total sulfur
Carbonate
Chloride
FIELD METHODS
SOLIDS
Primary Method
X-ray fluorescence
X-ray fluorescence
Amperometric titration
X-ray fluorescence
CC>2 evoloution
Backup Method
Atomic absorption
Atomic absorption
Ba(ClO4)2 titration
LIQUIDS
Primary Method
Atomic absorption
Atomic absorption
Atomic absorption
Atomic absorption
Amperometric titration
Ba(ClO4)z titration
Nondispersive infrared
Potentiometric titration
Backup Method
™*
Acid-base titration
Mercuric nitrate titration
-------
Four Du Pont photometric analyzers are used for continuous
analyzing at the inlets and outlets of both scrubbers. Values of pH
are monitored with Universal Interloc pH analyzers. Scrubber inlet
liquor pH is monitored continuously; scrubber outlet liquor pH is
monitored periodically by the laboratory. A modified EPA parti culate
train (manufactured by Aerotherm/Acurex Corporation) is used to
measure mass loading at scrubber inlets and outlets.
4. 4 DATA ACQUISITION AND PROCESSING
Data recorded by onsite personnel are sent to the Bechtel Corpora-
tion offices in San Francisco for processing. Data, received from
the test facility are entered into a computerized data base in San
Francisco. The data are sorted, further calculations made (e.g.,
percent sulfite oxidation, stoichiometric ratio), and reports prepared
that present the data covering a specified period for a given scrubber.
The data base reports for June 1975 through mid-February 1976
are presented in Appendix D.
4. 4. 1 Analytical Data
The analytical data acquisition system, which records the results of
laboratory analyses on printed summary sheets, was designed and
(in part) installed by Radian Corporation. A minicomputer is used
4-6
-------
to perform certain calculations and print the resultant data on a sum-
mary sheet, which is then transferred to San Francisco for inclusion
in the master data base.
4-7
-------
Section 5
VENTURI/SPRAY TOWER LIME RELIABILITY TEST RESULTS
Performance and analytical data from reliability testing with lime on
the venturi/spray tower system from June through August 1975 (Runs
625-1A through 627-1A) are presented in this section. An evaluation
of each test and the conclusions drawn to date are also presented.
Results of lime reliability tests conducted prior to June 1975 (Runs
601 -1A through 624-1A) have been reported in References 1 and 2.
5. 1 PERFORMANCE DATA AND TEST EVALUATION
Properties of lime and coal used during these tests can be found in
Appendix B. A log of the scrubber operating periods is given in Ap-
pendix C. Appendix D tabulates analytical data. Reliability test con-
ditions and results are summarized in Appendix E* (V/ST Summary
Tables for Runs 601-1A through 627-1A). Selected operating data are
graphically presented in Appendix F. Average scrubber and clarifier
overflow liquor compositions and the corresponding calculated percent
Lime reliability runs made prior to June 1975 have been included in
in this table.
5-1
-------
sulfate (gypsum) saturations are given in Appendix G.* An evaluation
and discussion of each test is presented below.
5.1.1 Venturi/Spray Tower Run 625-1A
Venturi/spray tower lime Run 625-lA was started on June 20, 1975,
to continue testing the 316L stainless-steel, three-pass, open-vane
chevron mist eliminator. This testing had been interrupted by a 6-week
scheduled maintenance outage on-Boiler No. 10.
The major test conditions selected were (see Appendix E):
Spray tower gas velocity 8.0 ft/sec
Venturi liquid-to-gas ratio 25 gal/Mcf
Spray tower liquid-to-gas ratio 50 gal/Mcf
Percent solids recirculated 8
Effluent residence time 12 min
Scrubber inlet slurry pH (controlled) 8
During the test, the topside of the mist eliminator was washed sequen-
tially with makeup water with six spray nozzles on a 4 minute "on " 76
minute "off" time cycle, with only one nozzle activated during each
"on" cycle. This arrangement resulted in an 8-hour total cycle time
for the six nozzles. The makeup water flow rate through one nozzle
The degree of liquor saturation with CaSO4.2H2O at 50°C was cal-
culated with the use of the Bechtel Modified Radian Equilibrium Com-
puter Program. See Reference 1 for a listing of this program.
5-2
-------
during the "on" cycle was set at 8 gpm. (at 13 psig), covering about a
15 ft2 area to give a specific spray rate of 0. 5 gpm/ft2.
In addition to the sequential topside wash, the entire underside of the
mist eliminator was washed intermittently withmakeup water at 75 gpm
*?
(1. 5 gpm/ft^) using 10 nozzles at 50 psig for 4.3 minutes every 4
hours.
The 75 gpm wash rate was only one-half of that used during the pre-
vious run (Run 624-1 A) in which the mist eliminator was entirely clean
after 823 hours of operation (see Appendix E). The combined makeup
water usage for the topside and bottomside mist eliminator wash during
Run 625-1A was only about half the makeup water available in closed-
liquor-loop operation.
Run 625-1A was ended on July 9, 1975, after 319 hours of operation
The mist eliminator was essentially clean (less than 2 percent re-
stricted, as estimated by a visual inspection), with only a lightly scat-
tered dust coating on the vanes.
Some scale was noticed on the spray tower wall below the top slurry
spray header and on the wall above the mist eliminator. However,
these scale deposits did not influence the spray tower operation.
5-3
-------
The venturi section operated without trouble. The only scale observed
was a. uniform coating whose thickness did not exceed 50 mils over
the rubber surface below the throat and in the flooded elbow section.
No large solids deposits accumulated in the flooded elbow.
The calculated average sulfate (gypsum) saturation was 115 percent
for the scrubber inlet liquor and 150 percent for the scrubber outlet
liquor. Alkali utilization averaged 89 percent. Over an inlet SO-,
concentration range of 2000 to 3350 ppm, SO? removal ranged from
67 to 90 percent.
5.1.2 Venturi/Spray Tower Run 626-1A
Run 626-1A began on July 9 and ended on August 4, 1975 after 569
operating hours. The scrubber system was not cleaned before the
start of the run. The purpose of the run -was to test the mist elim-
inator reliability at 9.4 ft/sec spray tower gas velocity (versus 8.0
ft/sec for Run 625-1A). The spray tower slurry rate was increased
to 1400 gpm (versus 1200 gpm for Run 625-1 A) to improve the SO?
removal efficiency. These changes resulted in liquid-to-gas ratios
of 21 and 50 gal/Mcf for the venturi and spray tower, respectively.
The "on" phase of the mist eliminator bottom wash cycle was increased
to 6 minutes every 4 hours (versus 4.3 minutes for Run 625-1A).
5-4
-------
The run ended as planned. The mist eliminator condition was almost
unchanged during the run (less than 2 percent restricted).
The spray tower wall below the top slurry spray header had acquired
more scale, which at the end of the run averaged about 100 mils in
thickness.
The wall area above the mist eliminator gained additional hard scale.
The venturi scrubber was generally clean.
The average calculated sulfate (gypsum) saturation was 100 percent for
the scrubber inlet liquor, compared with 115 percent for Run 625-1 A.
Alkali utilization averaged 85 percent. Over an inlet SCX concentration
range of 1750 to 3250 ppm, SOo removal was 68 to 88 percent.
5.1.3 Venturi/Spray Tower Run 627-1A
Run 627-1A was started on August 5 and ended on August 13, 1975,
after 187 hours of operation. The purpose of this run was to test the
mist eliminator operability at 9.4 ft/sec spray tower gas velocity with
the recirculated solids increased to 15 weight percent. The effluent
residence time was increased from 12 to 20 minutes, and the lime
slurry feed was added to the effluent hold tank (versus scrubber down-
comer) to observe the effect on the liquor sulfate (gypsum) saturation.
All other test conditions were the same as for Run 626-1 A.
5-5
-------
An inspection on August 8 revealed that some sulfite and carbonate
scale had formed on the scrubber walls and internals and the mist
eliminator vanes, probably because low-sulfur coal had been burned
from August 6 to 8. The inlet SO2 concentration decreased to about
1500 ppm, which resulted in unusually high scrubber outlet liquor pH
(6.0 to 6.25). The scale diminished by the end of run. At the end
of the run, the mist eliminator was about 2 to 3 percent restricted
by scale and solids. The mist eliminator had not been cleaned since
the beginning of Run 625-1A, a total of 1075 operating hours.
The spray tower wall below the mist eliminator generally lost scale,
and the bottom of the tower showed almost complete loss of old scale.
However, the tower walls above the mist eliminator and the outlet
duct gained hard scale. These areas were cleaned during the inspec-
tion. The venturi section appeared to be cleaner with continued loss
of old scale.
For this run, the average calculated sulfate (gypsum) saturation was
65 percent for the scrubber inlet liquor and 115 percent for the scrub-
ber outlet liquor. This is approximately 30 percent lower than for
Run 626-1 A. Alkali utilization averaged 82 percent. Over an inlet
SO2 concentration range of 1400 to 3500 ppm, SO2 removal was 69
to 93 percent.
5-6
-------
5. 2 CONCLUSIONS
Emphasis was placed on the reliable operation of the 316L stainless-
steel, three-pass, open-vane chevron mist eliminator during the ven-
turi/spray tower lime reliability testing from June through August
1975.
In earlier lime reliability testing (see Reference 2), a combination
of sequential topside and intermittent underside wash used all available
makeup water. It had been successful in keeping the mist eliminator
free of scale and solids accumulation for 823 hours of operation at
8.0 ft/sec spray tower gas velocity (Run 624-1A).
Further testing of this mist eliminator washing system was conducted
at a reduced underside wash rate, increased spray tower gas velocity,
and increased solids concentration in the recirculating slurry. The mist
eliminator was essentially clean after 1075 hours of operation without
cleaning. This included 319 hours at 8.0 ft/sec gas velocity and 8 per-
cent solids recirculated during Run 625-1A, 569 hours at maximum
gas velocity of 9-4 ft/sec and 8 percent solids during Run 626-1A,
and 187 hours at 9.4 ft/sec and 15 percent solids during Run 627-1A.
The combined makeup water requirement for the topside and bottom-
side mist eliminator wash during Runs 625-1A, 626-1A, and 627-1A
5-7
-------
•was only about one-half of the available makeup water in closed-liquor-
loop operation.
Alkali utilization during these runs averaged 82 to 89 percent, which is
typical of the high utilization inherent with lime systems. The relation-
ship between high utilization and reliable mist eliminator operation was
not known at the time of these runs. This relationship became apparent
during the utilization study (see Section 8).
5-8
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Section 6
VENTURI/SPRAY TOWER VARIABLE-LOAD TEST RESULTS
A 7-week, variable-load (cycling gas rate) test series with lime (Runs
628-1A and 628-1B) was conducted on the venturi/spray tower system
from August to October 1975. These tests were designed to evaluate
the ability of the scrubber system to handle the variable gas rate and
composition resulting from a daily boiler load cycle. This section
presents the performance and analytical data, along with the test run
evaluation and conclusions drawn from the tests.
6. 1 PERFORMANCE DATA AND TEST EVALUATION
Properties of lime and coal used during these tests can be found in
Appendix B. A log of scrubber operating periods is given in Appendix
C. Appendix D tabulates analytical data. Variable-load test conditions
and results are summarized in Appendix E. Selected operating data
are graphically presented in Appendix F. Average scrubber and clari-
fier overflow liquor compositions and the corresponding calculated per-
cent sulfate (gypsum) saturations are given in Appendix G. An evalua-
tion and discussion of each test is presented below.
6-1
-------
6.1.1 Venturj/Spray Tower Run 628-1A
Run 628-1A was started on August 16, 1975, after cleaning of the mist
eliminator and the spray tower areas above the mist eliminator, includ-
ing the outlet duct. The purpose of the run was to test the operability
and controllability of the venturi/spray tower system under cycling gas
load and a varying inlet gas SC>2 concentration. The gas flow rate for
this run (17,000 to 35,000 acfm) was varied so as to follow the actual
Boiler No. 10 load (about 60 to 160 MW).
The major test conditions at the start of run were (see Appendix E):
Spray tower gas velocity 4. 5 to 9-4 ft/sec
Venturi liquor rate (constant) 600 gpm
Spray tower liquor rate (constant) 1400 gpm
Percent solids recirculated 11
Effluent residence time 12 min
Venturi pressure drop (constant) 9 in. H2O
Scrubber outlet pH (controlled) 5. 0+^0. 5
Scrubber inlet pH ^8.0
The spray tower liquor rate was increased from 1400 to 1600 gpm on
August 26 to improve the SC>2 removal efficiency during periods of high
gas rate and high inlet SC>2 concentration. Because of changing gas
rate, the liquid-to-gas ratio ranges were 21 to 44 gal/Mcf and 50 to 117
gal/Mcf for the venturi and spray tower, respectively.
6-2
-------
The percent solids recirculated was initially specified as 11+3 percent
in anticipation of poor control due to the cyclically fluctuating gas rate.
However, no difficulty was encountered during the first. 10 days of
operation, and the percent solids recirculated was lowered to a more
desirable 9+2 percent.
The venturi pressure drop was maintained at 9 inches H^O by varying
the adjustable plug position with the gas rate.
The mist eliminator was washed sequentially on the topside and inter-
mittently on the underside using makeup water. The wash rate and
cycle were the same as for Runs 626-1A and 627-1A (see Subsection
5.1). The required wash water (2.3 gpm on a continuous basis) was
at all times less than the permissible makeup water in closed-liquor-
loop operation, even under the worst possible conditions (i.e., low
gas rate and high inlet SC>2 concentration).
To prevent sulfite and carbonate scaling during periods of low sulfur
coal, the scrubber outlet pH was maintained at 5. (HO. 5 and the inlet
pH equal to or less than 8. 0. Sulfite and carbonate scaling had been
experienced during Run 627-1A (see Subsection 5. 1. 3).
Run 628-lAended as planned on September 18 after 717 operating hours.
Inspections were made after 214, 401, and 510 hours of operation and
6-3
-------
at the end of the run. The system ran reliably and no significant con-
trol problems were encountered during the run.
Inspection at the end of the run showed the mist eliminator condition
to be stable, as in the previous inspections, with 2 percent restriction
by dust-like solids.
The spray tower walls remained generally unchanged throughout the
run, and there was a decrease in old scale in the -lower third of the
vessel. The bottom of the vessel was clean, with only 5 percent
of the surface covered by light scale. Scale on the wall above the
mist eliminator varied in coverage and thickness. The top of the vessel
was 95 percent covered by light scale, and the vessel outlet held the
usual scale collar averaging about 1 inch in thickness. The presence
of scale, however, did not hinder the normal operation of the spray
tower.
Solids deposits on the venturi section and flooded elbow were stable
during the entire run. Only minor scale was seen in the venturi scrub-
ber, and a few minor solid deposits were found at the top of the inlet
to the flooded elbow. No significant deposits were seen in the reheater
or in the outlet duct.
The average calculated sulfate (gypsum) saturations were 100 and 140
percent for the scrubber inlet and outlet liquors, respectively. Inlet
6-4
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SO2 concentration varied from 1500 to4400ppm and SO2 removal ranged
from 70 to 98 percent. Alkali utilization averaged 91 percent.
6.1.2 Venturi/Spray Tower Run 6 28-IB
Run 628-lBwas started on September 18, 1975 without system cleaning,
and was terminated on October 7 after 426 hours of trouble-free oper-
ation. The run was a continuation of Run628-lA except that the venturi
plug position was fixed to observe the effect of cycling gas rate on
particulate and SO- removal.
The venturi plug position was set to give a maximum pressure drop of
9 inches H7O at the maximum gas rate of 35, 000 acfm. During the
run, the gas rate varied between 19,000 and 35,000 acfm (5. 1 to 9.4
ft/sec spray tower gas velocity) and the venturi pressure drop varied
between 4 and 9 inches H-,O.
As in Run 628-1 A, no control problems due to the cycling gas rate
were encountered. At the end of the run, the mist eliminator condition
was the same (about 2 percent restricted by dust-like solids) as at
the end of Run 628-1 A.
The spray tower wall below the mist eliminator descaled slightly, but
scale increased somewhat in areas above the mist eliminator. This
6-5
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scale did not hinder spray tower operation. Light scale formed on
most surfaces of the outlet duct and the reheater.
The inlet gas duct to the venturi was clean, the venturi plug and the
inlet cone section had no significant deposits, and the flooded elbow was
clean. There was some loss of old scale in the area below the throat.
The stellite diffusers of the slurry spray nozzles (Bete No. ST48FCN)
showed no significant wear in approximately 9600 hours of service,
although minor pits were scattered along the diffuser spiral. Ero-
sion was observed in the bore of the 316 stainless-steel body of these
nozzles.
The average calculated sulfate (gypsum) saturation was 90 percent for
the scrubber inlet liquor and 130 percent for the scrubber outlet liquor.
These values are each lOpercent lower than those for Run 628-1A. Inlet
SC>2 concentration varied from 2000 to 4000 ppm while SC>2 removal
ranged from 72 to 96 percent. Alkali utilization averaged 90 percent.
The results of the particulate mass loading tests obtained during Runs
628-1A and 628-IB were questionable because of problems in sample
collection, anda direct comparison of the particulate removal efficien-
cies between the two runs could not be made. A stack-gas character-
ization program has been planned for the Shawnee Test Facility in
the fall of 1976 (see Section 4, Figure 4-1).
6-6
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6.2 CONCLUSIONS
A 7-week, variable-load test series with lime was conducted on the
venturi/spray tower from August to October 1975. A longer period had
been scheduled but, because of the excellent results, was not needed.
To follow the Boiler No. 10 load, which cycled between 60 and 160
MW, the gas flow rate was varied between 17,000 and 35,000 acfm.
Inlet SO2 concentration ranged from 1500 to 4400 ppm.
During the entire variable-load test sequence, the scrubber system
operated well. No problems due to the cycling gas rate and composition
were encountered in a total of 1143 hours of operation, including 717
hours at constant 9 inches f^O venturi pressure drop for Run 628-1A
and 426 hours at fixed venturi plug position (4 to 9 inches H^O pressure
drop) for Run 628-IB. The condition of the mist eliminator remained
almost unchanged throughout the variable-load tests, with a 2 percent
restriction of the total cross-sectional area by dust-like solids at
the conclusion of the tests.
6-7
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Section 7
TCA LIMESTONE RELIABILITY TEST RESULTS
Performance data from reliability testing with limestone on the TCA
system from early June through mid-October 1975 are presented in
this section. During this period, the major testing effort was con-
cerned with the performance of two different mist elimination configu-
rations. The first consisted of two closed-vane chevron mist elimina-
tors in series; the second was a single open-vane mist eliminator.
Properties of coal and limestone used during the tests can be found
in Appendix B. A log of the scrubber operating periods is given in
Appendix C. Analytical data are tabulated in Appendix D. Relia-
bility test conditions and results are summarized in Appendix H (see
References 1 and 2 for runs made prior to June 1975). Selected oper-
ating data for major tests are presented graphically in Appendix I.
Average scrubber and clarifier overflow liquor compositions and the
corresponding calculated percent sulfate (gypsum) saturations for major
runs are given in Appendix J.
7-1
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7. 1 TESTING WITH TWO CHEVRON MIST ELIMINATORS
IN SERIES
Prior to the 6-week boiler maintenance outage of Boiler No. 10, which
began in April 1975, a washtray (Koch Flexitray) was used in series
witha six-pass, closed-vane chevron mist eliminator in the TCA. Al-
though long-term reliability of this mist elimination system had been
demonstrated at an 8.6 ft/sec scrubber gas velocity in an 1835-hour
test (Run 535-2A), operation of this system at 10 and 12 ft/sec scrub-
ber gas velocity had not been successful (see Reference 2),
Consequently, during the 6-week boiler outage, a new mist elimination
system was installed in the TCA for testing at a 12. 5 ft/sec scrubber
gas velocity. The new mist elimination system, which was supplied
by the Air Correction Division of UOP, consisted of two identical three-
pass, closed-vane, fiberglass-reinforced plastic (FRP) chevron rnist
eliminators installed in series (see Figure 3-3), with provision for
washing the topside and underside of the lower mist eliminator. Air
Correction Division originally requested that a trapout tray be installed
below the lower mist eliminator belt. But because of successful oper-
ation in the spray tower in lime service of a mist eliminator without
trapout tray or washtray, the trapout tray was not installed.
7-2
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An evaluation and discussion of each test follows (Runs 546-2A through
552-2A). Unless otherwise specified, major operating conditions for
these tests were (see Appendix H):
Scrubber gas velocity 12. 5 ft/sec
Liquid-to-gas ratio 42 gal/Mcf
Percent solids recirculated 15
Effluent residence time 15 min
Scrubber outlet liquor pH (controlled) 5. 4+0. I
The scrubber gas velocity of 12.5 ft/sec corresponds to 8.2 ft/sec
superficial velocity in the mist eliminator area. The scrubber outlet
slurry pH was controlled at 5.4_+0.1 to avoid sulfite scaling on the
scrubber internals at high pH and high SC>2 make-per-pass (low liquid-
to-gas ratio of 42 gal/Mcf). The scrubber inlet liquor pH was not
allowed to exceed 6.0.
During these runs, SO2 inlet concentration ranged from 2000 to 3500
ppm and SO-> removal varied from 73 to 89 percent. Alkali utiliza-
tion ranged from 65 to 83 percent.
7.1.1 TCA Run 546-2A
Run 546-2A was started on June 8, 1975 with clean mist eliminators.
The topside of the lower stage mist eliminator was washed with makeup
water at 1. 5 gpm/ft (at 23 psig) for 10 minutes at 4-hour intervals.
7-3
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The underside was washed with the remaining makeup water at 1. 5 gpm/
ft2 (at 23 psig) for an average of 7. 1 minutes each hour. The upper
stage mist eliminator was not washed.
Run 546-2A ended on June 17, 1975, after 207 hours of operation,
because of an increasing pressure drop across the mist eliminators.
The upper stage mist eliminator was less than 5 percent restricted
by solids, but the lower stage was 30 to 35 percent restricted.
The flue gas leaving the lower stage mist eliminator appeared to chan-
nel toward the east side of the scrubber, causing heavy solids deposit
(up to 200 mils thick) on the east scrubber wall. This was the side
toward which the upper blades of the lower stage mist eliminator were
oriented.
The average calculated sulfate (gypsum) saturation was 90 percent
for both the scrubber inlet and outlet liquors.
7.1.2 TCA Run 547-2A
Run 547-2A was started on June 18 after the mist eliminators had
been cleaned.
Both the wash rate and the frequency for the lower stage mist eliminator
were increased for this run. The scrubber outlet liquor pH control
7-4
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point was increased from 5.4 to 5. 5. Other test conditions were un-
changed from Run 546-2A.
The lower stage mist eliminator was washed with makeup water at 2. 0
gpm/ft^ (45 psig) for 20 seconds every 10 minutes on the topside,
and for 1 minute every 10 minutes on the underside. Again, the upper
stage mist eliminator was not washed.
Because of the apparent flue gas channeling toward the east side of the
scrubber between the two mist eliminator stages during the previous
run, the east one-third section of the lower stage was horizontally
rotated 180 degrees before the test. By this rotation, all the channels
between the vanes on the topside of the lower stage mist eliminator
were directed towards the center of the scrubber.
The run ended on June 23, 1975, after 112 on-stream hours, because
of rapidly increasing pressure drop across the mist eliminators. The
restriction of mist eliminators by solids was about 5 percent in the
upper stage and 30 to 40 percent in the lower stage. The scrubber
walls between the mist eliminators were clean, which suggests that
gas channeling due to vane orientation is a factor in solids deposition
between mist eliminator stages.
The calculated average sulfate (gypsum) saturation was only 30 percent
for the scrubber inlet liquor. However, this may not be a represen-
7-5
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tative value under the conditions tested owing to the relatively short
duration of the test.
7.1.3 TCA Runs 548-2A and 549-2A
Runs 548-2A and 549-2 A were conducted from June 23 through July
2, 1975. The mist eliminators had been cleaned before the start of
Run 548-2A.
The principal objective of the runs was to observe whether the mist
eliminators could be kept free of solids deposit with a continuous make-
up water underwash for the lower stage. This mode of operation re-
sulted in an open-liquor-loop system. It -was planned to resort to con-
tinuous underwash with diluted clarified liquor if these runs proved
to be successful in keeping the mist eliminators clean.
The lower stage mist eliminator was washed continuously from the
ry
underside with makeup water at 26 gpm (0. 53 gpm/ft at 8 psig) during
Run 548-2A, and at 14 gpm (0. 29 gpm/ft2 at 10 psig) during Run 549-2A.
The topside of the lower stage was washed intermittently with makeup
water at 2.0 gpm/ft2 (45 psig) for 30 seconds every 10 minutes during
both runs. Other test conditions were unchanged from Run 547-2A.
At the end of Run 548-2A, after 71 hours of operation, the upper stage
mist eliminator was 5 percent restricted by solids and the lower stage
7-6
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was entirely clean. However, at the end of Run 549-2A after 112
operating hours (183 hours total), both stages were approximately 5
percent restricted. The solids accumulation appeared to be due to a
gap in the lower stage mist eliminator, which resulted when a one-third
section of the bottom stage had been inadvertently installed in the wrong
alignment.
As expected, because of the open-liquor-loop operation, the average
calculated sulfate (gypsum) saturation of the scrubber inlet liquor was
only 35 percent for Run 548-2A and 65 percent for Run 549-2A. The
latter was higher because less water was used for the lower stage
mist eliminator underwash during Run 549-2A.
7.1.4 TCA Runs 550-2A through 552-2A
Runs 550-2A, 551-2A, and 552-2A were conducted from July 2 through
July 14, 1975. Their on-stream times were 119, 39, and 86 hours,
respectively. The mist eliminators were cleaned before each run.
The purpose of these runs was to observe whether the two-stage mist
elimination system could be kept free of solids deposit with a continuous
underwash for the lower stage using a mixture of makeup water and
clarified process liquor.
7-7
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The wash scheme for the topside of the lower stage mist eliminator
during these runs was the same as in Runs 548-2A and 549-2A, i.e.,
2.0 gpm/ft2 for 30 seconds every 10 minutes using makeup water.
During Run 550-2A, the underside of the lower stage mist eliminator
was washed continuously with diluted (one-to-one ratio) clarified pro-
2
cess liquor at 16 gpm (0. 33 gpm/ft ), using four spray nozzles. Be-
cause of frequent plugging problems with these small nozzles, the un-
derwashpiping -was modified to use a larger single nozzle for the same
16 gpm flow rate during Run 551-2A. The underwash flow rate was
increased to 22 gpm (about 8 gpm water and 14 gpm clarified liquor)
during Run 552-1 A, using four spray nozzles.
Prior to Run 550-2A, the east one-third section of the lower stage
mist eliminator, -which had been rotated 180 degrees horizontally be-
fore Run547-2A, was inadvertently restored to the original vane orien-
tation.
Despite the short duration of each test, the operations of the mist
eliminators were generally not successful during the three runs. The
restrictions by solids of the upper stage were 5 to 8 percent, less
than 3 percent, and 5 percent for Runs 550-2A, 551-2A, and 552-2A,
respectively. For the lower stage, the restrictions were 15 percent,
10 to 15 percent, and 8 to 10 percent, respectively.
7-1
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Although with continued testing this mist elimination system might have
become workable, no further tests were conducted.
7. 2 TESTING WITH A SINGLE CHEVRON MIST ELIMINATOR
Because of the success with the spray tower mist eliminator operation
with lime (see Sections 5 and 6), a new mist elimination system of
similar design (single-stage, 316L stainless-steel, three-pass, open-
vane chevron mist eliminator with sequential topside and intermittent
bottomside freshwater wash) was installed in the TCA in July 1975
for testing •with limestone slurry. An evaluation and discussion of each
test (Runs 553-2A through 561-2A) is presented below.
7. 2. 1 TCA Run 553-2A
TCA limestone Run 553-2A was started on July 19, 1975, to test
the operability and reliability of the new single-stage, 316L stainless-
steel, three-pass, open-vane chevron mist eliminator.
The major test conditions selected were (see Appendix H):
Scrubber gas velocity 12.5 ft/sec
Liquid-to-gas ratio 50 gal/Mcf
Percent solids recirculated 15
Effluent residence time 15 min
Percent SO2 removal (controlled) 84
7-9
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The scrubber gas velocity of 12.5 ft/sec corresponds to a superficial
gas velocity of 8. 2 ft/sec in the mist eliminator area.
The topside of the mist eliminator was washed sequentially withmakeup
water,using six spray nozzles on a 4 minutes "on," 76 minutes "off"
time cycle, with only one nozzle activated during each "on" cycle. This
•wash sequence resulted in a total cycle time of 8 hours for the six noz-
zles. The makeup water flow rate through one nozzle during the "on"
o
cycle was set at 8 gpm (at 13 psig), covering about 14. 5 f t , to give
O
a specific spray rate of 0. 55 gpm/ft ...
The underside of the mist eliminator -was -washed intermittently with
makeup water, using nine spray nozzles, at 125 gpm (2. 5 gpm/ft~) and
40 psig for 5 minutes each hour.
Run 553-2A ended on July 21, 1975, after only 42 hours of operation,
•when an inspection revealed that the mist eliminator -was 15 percent
restricted by solids. This was unexpected since the mist eliminator
of similar design in the spray tower had worked reliably at 9.4 ft/sec
gas velocity using a similar wash scheme.
The average calculated sulfate (gypsum) saturation of the scrubber inlet
liquor was 90 percent. Inlet SO2 concentration varied from 2300 to
2500 ppm. Alkali utilization averaged 64 percent.
7-10
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7.2.2 TCA Runs 554-2A through 556-2A
The failure of the mist eliminator operation during TCA Run 553-2A,
as compared with the successful operation in the spray tower with lime
using a similar mist elimination design and washing scheme, was ini-
tially attributed to the differences in the physical design, gas flow
distribution, and mist generation pattern within the two scrubbers. *
The scrubber gas velocity was dropped to 9.4 ft/sec (6. 1 ft/sec super-
ficial gas velocity in the mist eliminator area) for Runs 554-2A through
556-2A. The liquor rate was maintained at 1200 gpm, giving a liquid-
to-gas ratio of 67 gal/Mcf for these runs. The mist eliminator was
cleaned before the start of each test.
Run 554-2A was conducted from July 25 to 28, 1975, for 60 operating
hours. The washing frequency for the topside of the mist eliminator
was doubled (4minutes "on," 36 minutes "off," at 8 gpm makeup water
during the "on" cycle). The frequency for the underside was changed
to 6 minutes (at 2. 5 gpm/ft2) every 2 hours. The mist eliminator
was 50 percent restricted by solids at the end of the run.
It was later discovered that mist eliminator reliability is a strong
function of the alkali utilization (see Subsection 8.4).
7-11
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Because of the failure with the intermittent makeup water mist elim-
inator underwash, Run 555-2A was tested with a continuous makeup
water underwash at 20 gpm (0.4 gpm/ft , 25 psig), using a single
spray nozzle. The topside wash -was unchanged from Run 554-2A. This
wash scheme resulted in an open-liquor-loop operation. The run was
ended as planned after 63 hours of operation (July 29 to August 1).
The mist eliminator was 5 percent restricted by solids at the end of the
run. It was thought that a corrosion specimen assembly under the
mist eliminator andaCeilcote panel (for corrosion and erosion testing)
under a slurry nozzle might have influenced the mist eliminator under-
spray pattern and the gas flow distribution. Both assembly and panel
were removed for subsequent tests.
Run 556-2A was tested under the same conditions as in Run 555-2A,
except that the underside of the mist eliminator was washed continu-
ously with 20 gpm of diluted clarified process liquor (all available
makeup water plus clarified liquor). After 89 hours of operation from
August 1 to 5, the mist eliminator was essentially clean, with only
2 percent restriction by solids.
The average calculated sulfate (gypsum) saturation of the scrubber inlet
liquor for these runs ranged from 55 to 105 percent. Inlet SO2 con-
centration ranged from 1500 to 3000 pprru Alkali utilization varied
from 58 to 68 percent.
7-12
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7.2.3 TCA Runs 557-2A through 561-2A
Runs 557-2A through 561-2A were conducted from August 5 through
October 6, 1975. Because of the encouraging result of mist elim-
inator operation during Run 556-2A, the scrubber gas velocity was
increased to 12.5 ft/sec (8.2 ft/sec superficial gas velocity in the
mist eliminator area) for Runs 557-2A through 561-2A. As in Run
556-2A, the underside of the mist eliminator was washed continuously
during these runs with 20 gpm (0.4 gpm/ft ) of diluted clarified liquor
(all makeup water plus clarified liquor) at 25 psig using a single noz-
zle. The mist eliminator was cleaned before each of these tests.
Run 557-2Awas tested under the same conditions as Run 556-2A except
that the scrubber gas velocity was increased to 12. 5 ft/sec (liquid-to-
gas ratio of 50 gal/Mcf). The wash scheme for the topside of the
mist eliminator was unchanged, i.e., sequential washusing six nozzles
with 4 minutes "on, " 36 minutes "off, " at 8 gpm flow rate to each
nozzle during the "on" cycle. The run ended after 181 operating hours
when an inspection revealed the mist eliminator was 5 percent re-
stricted by solids. The average calculated sulfate (gypsum) satura-
tions were 70 and 80 percent for the scrubber inlet and outlet liquors,
respectively.
During Run 558-2A, the time cycle for the mist eliminator sequential
topside wash was changed to 6 minutes "on" and 24 minutes "off, "
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with 8 gpm -water flow rate to each nozzle during the "on" cycle. ThJs
change resulted in a total cycle time of 3 hours for the s:'x nozzles.
The mist eliminator was inspected after 229 and 324 hours of opera-
tion and again at the end of the run after 398 hours of operation. The
mist eliminator restriction increased from 3 percent at 229 hours to
8 to 10 percent at 324 hours, and then to 12 to 14 percent at the
end of the run. The solids accumulation occur red mostly on the topside
of the northeast section of the mist eliminator vanes, possibly because
of uneven distribution of gas flow, and on shadow areas around the vane
supports where underside wash liquor did not impinge. The average
calculated sulfate (gypsum) saturation was 85 percent for the scrubber
inlet liquor and 100 percent for the scrubber outlet liquor.
Owing to the heavier solids deposit on the topside of the northeast
mist eliminator section during Run 558-2A, the water flow rate to the
northeast and north-center sequential top wash nozzles was increased
from 8 to 12 gpm during Run 559-2A. The flow rate to the remaining
four nozzles remained at 8 gpm. The sequential top wash cycle was
changed to 3 minutes "on" and 7 minutes "off," resulting in a total
cycle time of 1 hour for the six nozzles. In addition, the single noz-
zle for the continuous underwashwas moved 6 inches closer to the mist
eliminator. Prior to Run 559-2A, plywood plugs were placed flush with
the inside wall of the scrubber in the scrubber window ports to reduce
7-14
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gas turbulence. Inspections were made after 88 and 225 hours of oper-
ation and at the end of the run at 384 hours of operation. At the
time of these inspections, the mist eliminator restrictions were 1, 5,
and 7 percent, respectively, and the solids deposit had again formed
in shadow areas of the mist eliminator vane supports (three inverted
T-beams). The average calculated sulfate (gypsum) saturation for Run
559-2A was 70 percent for the scrubber inlet liquor and 65 percent
for the scrubber outlet liquor.
!
Run 560-2A was tested under the same operating conditions as Run
559-2A. Before the test, to reduce the shadows created by the T-beams,
the three inverted T-beams supporting the mist eliminator were re-
moved and the mist eliminator was supported from the topside. At
the end of the run, after 142 hours of operation, the mist eliminator
was 5 to 7 percent restricted by solids. The solids deposit was heavier
in the east half of the mist eliminator. For this run, the average cal-
culated sulfate (gypsum) saturation was 45 percent for both the scrubber
inlet and outlet liquors.
Prior to Run 561 -2A, all tests with the single-stage mist eliminator
had been made with all the upper blades of the mist eliminator oriented
toward the east wall of the scrubber. Run 561-2A was tested with
the east half of the mist eliminator rotated 180 degrees horizontally,
so that the gas flow exiting the mist eliminator was directed toward
7-15
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the center of the scrubber in a more symmetrical flow pattern. The
water flow to all six sequential top wash nozzles was adjusted to 8
gpm. These changes resulted in a slightly improved mist eliminator
operation. At the end of the run, after 135 on-stream hours, the
mist eliminator was 4 to 5 percent restricted by solids. Solids had
accumulated mostly in the shadow areas created by the supporting side
rails of the mist eliminator. The average calculated sulfate saturation
of the scrubber inlet liquor was 55 percent.
During Runs 557-2A through 561-2A, inlet SC>2 concentration ranged
from 1500 to 4100 ppm. Average alkali utilization varied from 65 to
74 percent.
7. 3 CONCLUSIONS
7. 3. 1 Testing with Two Chevron Mist Eliminators in Series
At a scrubber gas velocity of 12.5 ft/sec (8.2 ft/sec superficial gas
velocity in the mist eliminator area), the two-stage FRP chevron mist
elimination system became inoperable within a short time when the
lower stage was washed only intermittently with fresh water from both
the topside and the underside.
A combination of intermittent fresh water topwash and continuous un-
derwash with diluted clarified liquor for the lower stage significantly
7-16
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reduced solids accumulation in the two-stage mist elimination system.
However, long-term reliability of this system was not achieved.
During these tests, average alkali utilization ranged from 65 to 83 per-
cent.
7. 3. 2 Testing with One Chevron Mist Eliminator
The operation of the single-stage, 316L stainless-steel, three-pass,
open-vane chevron mist eliminator was not successful at either 12. 5 or
9.4 ft/sec scrubber gas velocity when the mist eliminator was washed
sequentially on the topside and intermittently on the underside with
fresh water (Runs 553-2A and 554-2A). Alkali utilization during these
runs averaged 64 and 63 percent.
A combination of sequential topside wash with fresh water and contin-
uous underside wash with diluted clarified process liquor increased
the reliability of this mist elimination system. At 12. 5 ft/sec scrub-
ber gas velocity, the mist eliminator restriction by solids appeared
to stabilize at less than 10 percent in about 380 hours of operation
(Runs 557-2A through 561-2A). Alkali utilization averaged 65 to 74
percent during these runs. Solids accumulation occurred mostly in
the shadowed areas of the mist eliminator vanes and support rails
not directly impinged upon by the underside wash liquor.
7-17
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The difficulty in maintaining the mist eliminator free of solids accu-
mulation in the TCA in limestone service was unexpected because of
the success in operating a similar mist eliminator in the spray tower
in lime service. It was later discovered that high alkali utilization
(inherentin a lime system) contributes significantly to the clean opera-
tion of a mist eliminator (see Subsection 8.4).
7-18
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Section 8
LIMESTONE UTILIZATION TESTING IN THE
VENTURI/SPRAY TOWER AND TCA SYSTEMS
During the period from October 1975 through mid-February 1976, lime-
stone utilization tests were conducted on both the venturi/spray tower
and the TCA systems. These tests were made as a result of a TVA
economic study which showed that a potential existed for significantly
improving the economics of limestone scrubbing by improving the util-
ization of the limestone feed (moles SO? absorbed/mole Ca added).
Improved limestone utilization not only results in a decrease in lime-
stone feed requirements but also a corresponding decrease in waste
sludge production.
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. For the venturi/spray
tower system, a single backmix effluent hold tank was evaluated. For
the TCA system, both a single backmix hold tank and three backmix
hold tanks in series (to simulate a plug flow reactor) were evaluated.
No attempt was made in this report to account for secondary variables
such as chloride concentration in the slurry liquor, which ranged from
8-1
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1500 to6500ppm during testing. Models that take such secondary vari-
ables into consideration are being developed and will be described in
later reports.
For each combination of hold tank residence time and hold tank design,
tests were conducted to cover a range of values of scrubber slurry li-
quor 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 recir-
culation slurry.
Both the venturi/spray tower system and the TCA system were oper-
ated during utilization testing with a single-stage, three-pass, open-
vane, 316L stainless-steel mist eliminator with top and bottom wash.
Details of the dramatic effect of alkali utilization on mist eliminator
operation are discussed in Subsection 8. 4.
Properties of raw materials and scrubber operating periods for the
utilization runs are given in Appendices B and C, respectively. Data
base tables, test result summary tables, graphical operating data, and
average liquor composition data for the utilization runs are presented
in Appendices D, E, F, and G, respectively, for the venturi/spray
tower runs and Appendices D, H, I, and J, respectively, for the TCA
runs.
8-2
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8. 1 UTILIZATION TESTING IN THE VENTURI/SPRAY TOWER
SYSTEM WITH VARIABLE RESIDENCE TIME
In the venturi/spray tower system, limestone tests were made with a
single backmix effluent hold tank to determine the effect of scrubber
inlet liquor pH and residence time on stoichiometric ratio. Runs were
made at residence times of 20, 12, and 6 minutes.
Major test conditions during this period were:
Spray tower gas velocity 9.4 ft/sec
Ve-nturi liquid-to-gas ratio 21 gal/Mcf
Spray tower liquid-to-gas ratio 50 to 57 gal/Mcf*
Venturi pressure drop 9 in. ^2®
Percent solids recirculated 15
Data showing the relationship between stoichiometric ratio and scrub-
ber inlet liquor pH for the venturi/spray tower system are plotted
in Figures 8-1, 8-2, and 8-3 for residence times of 20, 12, and 6
minutes, respectively. The stoichiometric ratio/pH relationship was
best defined at 12 minutes residence time. As expected, scatter in
the data was greatest at 6 minutes residence time, where pH recovery
time was limited and small variations in tank level resulted in signifi-
cant changes in residence time. At 20 minutes residence time, only
a limited number of data were obtained at higher pH values.
*
All but two tests were at 50 gal/Mcf.
8-3
-------
1.8
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VENTURI/SPRAY TOWER SYSTEM
SINGLE HOLD TANK
20 MINUTES RESIDENCE TIME
O RUN 701 - 1A
D RUN 702 - 1A
A RUN 703 - 1A
V RUN 704 - 1A
O RUN 705 - 1A
~I
4.8
5.0
5.2 5.4 5.6
SCRUBBER INLET LIQUOR pH
5.8
6.0
Figure 8-1. Stoichiometric Ratio versus Scrubber Inlet Liquor
pH in the Venturi/Spray Tower Tower System with
a Single Hold Tank at 20 minutes Residence Time
6.2
8-4
-------
5.4 5.6
SCRUBBER INLET LIQUOR pH
Figure 8-2. Stoichiometric Ratio versus Scrubber Inlet Slurry
pH in the Venturi/Spray Tower System with a Single
Hold Tank at 12 minutes Residence Time
8-5
-------
1.8
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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
D
A A
A A
AA
v-7
-------
Sight average curves drawn through the data in Figures 8-1 through
8-3 are compared in Figure 8-4. In Figure 8-4, a tendency for lower
stoichiometric ratio at a given pH can be seen as residence time in-
creases. However, above a pH of 5.8, the sight average curve for
20 minutes residence time fell between 6 and 12 minutes. This incon-
sistency is indicative of the broad scatter of the data.
Figure 8-5 shows, the general relationship between SO2 removal and
stoichiometric ratio for an inlet gas SC>2 concentration range between
2500 and 3500 ppm. Data points have been plotted for hold tank resi-
dence times of 20, 12, and 6 minutes, and a sight average line through
all the data has been drawn. Although a reduction in SO? removal
at low residence time might be expected, such a decrease could not
be discerned within the scatter of the data in Figure 8-5.
Figure 8-6 shows the relationship between SO- removal and scrubber
inlet liquor pH for an inlet gas SOo concentration range from 2500 to
3500 ppm and a 12-minute hold tank residence time. Averages from
Figure 8-6 and from similar plots for higher arid lower inlet gas SO_
Cj
concentration ranges at 12 minutes residence time are drawn in Figure
8-7, which shows the effect of inlet gas SO^ concentration and scrubber
inlet slurry pH on SOo removal. As expected, an increase in inlet SO?
8-7
-------
1.8
1.7 ••
1.6 ••
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VENTURI/SPRAY TOWER SYSTEM
6 MINUTES HOLD
TANK RESIDENCE TIME
4.8
5.0
5.2 5.4 5.6
SCRUBBER INLET LIQUOR pH
5.8
6.0
6.2
Figure 8-4. The Effect of Effluent Hold Tank Residence Time and
Scrubber Inlet Liquor pH on Stoichiometric Ratio in
the Venturi/Spray Tower System
8-8
-------
100
95 -
90 -
85 ••
80 • •
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70-
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55
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VENTUR I/SPRAY TOWER SYSTEM
INLET GAS SO2 CONCENTRATION BETWEEN 2500 & 3500 ppm
SYMBOL
O
O
A
SINGLE HOLD TANK
RESIDENCE TIME
20 minutes
12 minutes
6 minutes
4-
4-
1,0 1.2 1.4 1.6 1.8 . 2.0
STOICHIOMETRIC RATIO, moles Ca added/mole SO2 absorbed
2.2
Figure 8-5. The Effect of Stoichiometric Ratio and Effluent Resi-
dence Time on Percent SO2 Removal in the Venturi/
Spray Tower with a Single Hold Tank
8-9
-------
VENTURI/SPRAY TOWER SYSTEM
SINGLE HOLD TANK
12 MINUTES RESIDENCE TIME
INLET GAS SO2 CONCENTRATION
BETWEEN 2500 & 3500 ppm
O RUN 706-1A
RUN 707-1A
RUN 708 -1A
RUN 709 - 1A
RUN 710-1A
50
5.4 5.6
SCRUBBER INLET LIQUOR pH
Figure 8-6. The Effect of Scrubber Inlet Liquor pH on Percent
Removal in the Venturi/Spray Tower System
8-10
-------
100
95 •
90-
85
80- •
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VENTUR I/SPRAY TOWER SYSTEM
SINGLE HOLD TANK
12 MINUTES RESIDENCE TIME
4-
4.8
5.0
5.2 5.4 5.6
SCRUBBER INLET LIQUOR pH
5.8
6.0
6.2
Figure 8-7. The Effect of Scrubber Inlet Liquor pH and Inlet Gas
SO? Concentration on Percent SO^ Removal in the
Venturi/Spray Tower System
8-11
-------
concentration results in a decrease in percentage SO2 removal at con-
stant inlet pH. *
I. 2 UTILIZATION TESTING IN THE TCA SYSTEM WITH
THREE HOLD TANKS IN SERIES
Kinetic theory shows that for a continuous system -where the reac-
tion order is greater than zero, raw materials are more completely
converted in a plug flow reactor than in a backmixed reactor with
the same residence time. This concept for improving utilization was
successfully tested by Borgwardt (Reference 4) in a 0. 1 MW limestone
scrubber with both a plug flow reactor and with three stirred tanks
in series to approximate plug flow. The concept has now been tested
with limestone in the TCA system at the Shawnee Test Facility. Major
conditions for these tests were:
TCA superficial gas velocity 12.5 ft/sec
Liquid-to-gas ratio 42 to 50 gal/Mcf
Number of TCA beds 3
Static sphere height per bed** 5 in.
Percent solids recirculated 15
See Equation 14-7 in Reference 1.
.1,
Initially, 6-gram, hollow TPR (thermoplastic rubber) spheres were
used. These were subsequently replaced with 6.5-gram, nitrile solid
foam spheres.
5-12
-------
Hold tank configurations tested were:
• Single hold tank at 12 minutes residence time
• Three hold tanks in series at 14. 4 minutes total residence
time (5.2, 2.6, and 6.6 minutes, respectively)
• Threehold tanks in series at 10. 8 minutes total residence
time (4. 6, 2. 3, and 3. 9 minutes, respectively)
The total residence times for the runs with three hold tanks in series
•were intended to be 12 and 9 minutes, but because of a flow meter
error (lOOOgpm actual circulating slurry flow rate at a indicated meter
reading of 1200 gpm), the total residence times were actually 14.4
and 10.8 minutes.
Results of the utilization testing for these three configurations are plot-
ted as stoichiometric ratio versus scrubber inlet liquor pH in Figures
8-8, 8-9, and 8-10, respectively. Sight drawn averages from Figures
8-8 through 8-10 are compared in Figure 8-11. 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 dis-
tinct difference between operation with a single tank and 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
8-13
-------
1.8 -
1.7 -
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2* 1.3-
6.
SCRUBBER INLET LIQUOR pH
Figure 8-8. Stoichiometric Ratio versus Scrubber Inlet Liquor pH
in the TCA System with a Single Hold Tank at 12 minutes
Residence Time
8-14
-------
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TCA SYSTEM
THREE HOLD TANKS IN SERIES
14.4 MINUTES RESIDENCE TIME
O RUN 565 -2A
O RUN 566-2A
A RUN 567 -2A
V RUN 568-2A
• RUN 573 -2A
O RUN 575-2A
O RUN 576-2A
• RUN 577-2A
• •
• • f
o 6
4-
5.0
5.2 5.4 5.6
SCRUBBER INLET LIQUOR pH
5.8.
6.0
6.2
Figure 8-9. Stoichiometric Ratio versus Scrubber Inlet Liquor
pH in the TCA System with Three Hold Tanks in
Series at 14.4 minutes Residence Time
8-15
-------
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1.7 -
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1 1 1 1
4.8
5.0
5.2 5.4 5.6
SCRUBBER INLET LIQUOR pH
5.8
6.0
6.2
Figure 8-10.
Stoichiometric Ratio versus Scrubber Inlet Liquor
pH in the TCA System with Three Hold Tanks in
Series at 10.8 minutes Residence Time
8-16
-------
1.8
1.7 -•
1.6 •-
1.5 -•
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TCA SYSTEM
1 TANK, 12 minutes
3 TANKS, 10.8 minutes
3 TANKS, 14.4 minutes
4.8
5.0
5.2 5.4 5.6
SCRUBBER INLET LIQUOR pH
5.8
6.0
6.2
Figure 8-11.
The Effect of Scrubber Inlet Liquor pH and Hold
Tank Configuration on Stoichiometric Ratio in the
TCA System
8-17
-------
in series. The latter is a 7 percent improvement in limestone util-
ization. At higher pH, the improvement was greater; e. g. , at pH 5. 8,
the improvement in utilization was 14 percent.
The improvement in utilization with three tanks in series can also be
seen in Figure 8-12, where SC>2 removal is plotted against stoichio-
metric ratio for an inlet gas SC>2 concentration range of 2500 to 3500
ppm. At 85 percent SC>2 removal, the stoichiometric ratio •with three
tanks in series averaged about 15 percent lower than with a single
tank. This comparison is valid even though the residence times and
the liquid-to-gas ratios are different for the data shown. Residence
time does not significantly affect stoichiometric ratio for three tanks
in series (see Figure 8-11). Increase in liquid-to-gas ratio increases
SC>2 removal. Thus, the improvement of utilization with three tanks
would have been even greater than shown in Figure 8-12 if the data
for three tanks in series had been taken at the same liquid-to-gas
ratio as for the single tank data.
Data for three tanks in series at 10. 8 minutes residence time were
not included in Figure 8-12 because the TPR spheres in the TCA were
replaced withnitrile solid foam spheres during the 10.8 minute testing.
Unfortunately, the effectof lO.Sminutes residence time onSCU removal
LJ
could not be separated from the effect of the new bed of spheres on
SC>2 removal.
-------
100
95 • •
90 •
3TANKS
14.4 MIN. RESIDENCE TIME
L/G - 42
85
80 - •
ui
cc
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70
65
60
55
50
1TANK
12 MIN. RESIDENCE TIME
L/G = 50
TCA SYSTEM
INLET GAS SO2 CONCENTRATION
BETWEEN 2500 & 3500 ppm
SYMBOL
O
HOLD TANKS
4.
1.0 1.2 1.4 1.6 1.8
STOICHIOMETRIC RATIO, moles Ca added/mole SO2 absorbed
2.0
2.2
Figure 8-12.
The Effect of Stoichiometric Ratio and Hold Tank
Configuration on Percent SC>2 Removal in the TCA
System
8-19
-------
8. 3 UTILIZATION DATA FROM DEPLETION RUNS
/
During January and early February 1976, several limestone depletion
runs* were conducted on both the venturi/spray tower and TCA systems
to determine if valid utilization data could be produced by this method.
The results of these tests are plotted in Figures 8-13, 8-14, and 8-15,
along with the corresponding sight average line from the normal utili-
zation tests. Most of the data fell within the scatter band of the normal
utilization test data, but did not define the same average line. In
general, the depletion data defined a lower utilization than indicated
by longer term runs. Since the methods did not give the same result,
data from depletion runs were not included in the plots of Subsections
8. 1 and 8. 2.
5.4 MIST ELIMINATOR OPERABILITY DURING LIMESTONE
UTILIZATION TESTING
Tables 8-1 and 8-2 summarize the results of mist eliminator oper-
ability during the limestone utilization testing. These tables list the
average scrubber inlet liquor pH, average limestone utilization and
stoichiometric ratio, mist eliminator wash scheme, and percent of
the mist eliminator passage restricted by solids deposit at the end
of each run. Mist eliminator restriction was estimated visually by
*
Limestone depletion runs were conducted without limestone addition
during SO2 absorption. The scrubber inlet liquor pH was allowed to
drop from about 5. 9 to 4. 8.
8-20
-------
1.8
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VENTURI/SPRAY TOWER SYSTEM
SINGLE HOLD TANK
6 MINUTES RESIDENCE TIME
A RUN 712-IB
AVERAGE FROM
UTILIZATION DATA
4.8
5.0
5.2 5.4 5.6
SCRUBBER INLET LIQUOR pH
5.8.
6.0
6.2
Figure 8-13.
Stoichiometric Ratio versus Scrubber Inlet Liquor
pH for Depletion Test at 6 minutes Residence Time
in the Venturi/Spray Tower System
8-21
-------
1.8
1.7 -
1.6 -
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TCA SYSTEM
THREE HOLD TANKS IN SERIES
14.4 MINUTES RESIDENCE TIME
A RUN 573 - 2B
O RUN 576 - 2B
O RUN 578 - 2A
A
D
AVERAGE FROM
UTILIZATION DATA
4.8
5.0
5.2
5.8
6.0
Figure 8-15.
5.4 5.6
SCRUBBER INLET LIQUOR pH
Stoichiometric Ratio versus Scrubber Inlet Liquor
pH for Depletion Tests in the TCA System with
Three Hold Tanks in Series at 14.4 minutes
Residence Time
6.2
8-23
-------
Table 8-1
SUMMARY OF VENTURI/SPRAY TOWER LIMESTONE
UTILIZATION AND MIST ELIMINATOR TESTS
oo
i
Run
No.
701-1A
702- 1A
703-1A
704-1A
705- 1A
706- 1A
707- IA
708- 1A
709-1A
710-1A
711-1A
711-1B
712-1A
712-1B
Single Tank
Res. Time,
min.
20
20
20
20
20
12
12
12
12
12
6
6
6
6
713-1A 6
714-lA(h) 6
715-1A
716- 1A
717-1A
20
20
6
Avg. Av
Scrubber Stoi
Inlet Liquor pH Rat
j. ' Avg. Percent
ch. Limestone
io Utilization
5.90 1.45 69
5.80 1.45 69
5.20 1.07 93
5.75 1.45 69
5.65 1.25 80
5.30 1.06 94
5.75 1.30 77
5.65 1.20 83
5.85 1.35 74
6.00 1.50 67
5.70 1.30 77
5.55 1.40 71
5.80 1.50 67
Depletion' '
-
5.25 1.10 91
5.55 1.25 80
5.30 1.43 70
Avg. Percent
SO, Removal'8'
88
87
58
86
84
58
83
77
83
91
81
82
87
-
69
90m
25
4.80 1.98 51 13lu
5.45 1.18 85
88
Mist Eliminator
Wash Scheme
Top | Bottom
Intermittent Intermittent
1
Intermittent10' Intermittent1.1!!
i
Intermittent.
Continuous
Intermittent Intermittent
1 !
1 i
" ?
Run
Hours
73
60
319
66
136
180
118
138
134
234
144
71
119
18
52
157
23
18
181
Hours Since
Cleaning Mist
Eliminator
73
60
319
385
136
180
298
436
134
368
512
583
702
720
772
157
180
198
379
Percent Mist
Eliminator
Restriction
50-60
45-50
1
45-50
17-20
1
10-15
15-20
5-7
_
5-7
10-15
10
2
_
.
8
Note: AH runs made with a 316 stainless steel, 3-pass, open-vane, chevron mist eliminator. Run
conditions: 15 wt % solids in recirculated slurry, 9.4 ft/sec spray tower superficial gas
velocity, 21 gal/mcf liquid-to-gas ratio in venturi, 50-57 gal/mcf Hquid-to-gas ratio in spray
tower (except Runs 7I5-1A and 716- IA had no slurry flow to spray tower).
(a)
(b)
(c)
(d)
(e)
(f)
(h)
(i)
Intermittent, sequential top wash with makeup water at 0. 53 gpm/sqft for 4 min/8 hr/section,
Intermittent, full face bottom wash with makeup water at 1. 5 gpm/sqft for 6 min/4 hr.
Intermittent, sequential top wash with makeup water at 0. 53 gprn/sqft for 3 min/hr/section.
Intermittent, full face bottom wash with makeup water at 1. 5 gpm/sqft for 4 min/hr,
Continuous, full face bottom wash with diluted clarified liquor at 0, 4 gpm/gqft,
A limestone depletion run is conducted without limestone addition during SCK absorption,
The scrubber inlet liquor pH is allowed to drop from about 5. 9 to 4. 8.
T removals are for 2500 to 3500 ppm inlet gag SO?
concentration.
A liquor Mg ion concentration of 5000 ppm was maintained during Runs 714- IA through 717-1A
by addition of MgO in the effluent hold tank. The limestone stoichiometric ratios and utilizations
for these runs have been corrected to account for sulfur in liquid phase, which is normally negligible
-when no MgO is added.
Venturi only operation (no slurry flow to spray tower).
-------
Table 8-2
SUMMARY OF TCA LIMESTONE UTILIZATION AND MIST ELIMINATOR TESTS
Run No
No. Tan
56Z-ZA
562-2B
563-2A
564-2A
Total
ks Ret. Time,
mlnlO
12
12
12
1 12
565-2A 3 14.4
566-2A 3 14.4
567- ZA 3 14.4
568-2A 3 14.4
S69-2A 3 10.8
569-2B 3 10.8
570-2A 3 10.8
571-2A 3 10.8
571-2B 3 10.8
572-2A 3 10.8
573-2A 3 14.4
573-2B 3 14.4
574-2A 3 10.8
575-2A 3 14.4
576-2A 3 14.4
.576-28 3 14.4
577-2A 3 14.4
578-2A 3 14.4
579-2A 3 10.8
580-2A 3 10.8
581 -2A
582-2A
14.4
14.4
Avg.
Scrubber
Inlet pH
5.90
5.65
5.85
5.15
5.25
5.85
5.95
5.55
5.50
5.50
5.80
Avg.
Stoich,
Ratio
1.6
1.4
1.7
1.06
1.05
1.25
1.4
1.06
1.08
l.OB
1.18
5.80 1.25
Avg. Percent
Limestone
Utilization
63
1
71
59
94
95
80
71
94
93
93
85
80
Avg. Percent
SO2 Removal1 '
83
81
86
58
58
83
84
63
69
64
72
73
Mlit Eliminator Run
Wash Scheme Hours
Top | Bottom
Intermittent Continuous 495
Depletion1 ' - - ,
5.25
5.55
Depletion
Depletion
5.55
5.70
Depletion
5.80
Depletion
5.25
Depletion
5.45
Depletion
1.09
1.08
.
-
1.15
1.17
.
1.25
.
1.05
-
1.15
-
92
93
.
.
87
85
_
80
_
95
.
87
-
57
66
.
_
69
73
.
83
.
61
,
80
•
134
182
113
109
166
. . 138
Intermittent'6' 162
No wash
1
Intermittent1*'
1
i
66
97
144
96
11
154
45
28
12
47
112
3
159
9
62
12
, 164
18
Houri Since
Cleaning Mlit
Eliminator
155
332
495
629
811
924
109
275
413
575
641
738
882
978
989
1143
1188
1216
1228
47
159
162
159
168
230
242
406
424
Percent Mlit
Eliminator
Restriction
2
5-7
7-9
7
7
3
0
0
2
1
<1
<1
<1
<1
.
.
-------
onsite personnel during inspections. All of the available makeup water
was used for tests with continuous mist eliminator bottom -wash, while
only about one-half of the available makeup -water was used for tests
with intermittent bottom wash.
During venturi/spray tower limestone Runs 701-1A and 702-1A (see
Table 8-1) with intermittent topside and bottomside makeup water wash,
the mist eliminator was heavily restricted by soft solids within 2 to 3
days. This was unexpected because earlier operation with lime slurry
under nearly identical operating conditions was successful (see Run
627-1 A, Section 5). The limestone utilization for Runs 701-1A and
702-lAwas only 68 percent, as compared with 90 percent normally
obtained with lime operation. Subsequently, during Run 703-1A, the
limestone utilization -was increased to 93 percent by dropping the aver-
age scrubber inlet liquor pH to 5.2. The mist eliminator was found
to be essentially clean (1 percent restricted) after 319 operating hours
with intermittent underside and topside raw water wash. The average
SO removal for Run 703-1A was only 58 percent, as compared with
87 percent for the previous tests.
Subsequent venturi/spray tower Runs 704-1A through 708-1A confirmed
the observation that reliable mist elimination operation could be ob-
tained only at high alkali utilization (greater than about 85 percent),
with intermittent under side and topside wash using makeup water. Runs
709-1A through 711-IB also showed that for utilization less than about
8-26
-------
85 percent, continuous bottomside wash with diluted clarified liquor
could reduce or limit the amount of soft solids deposition on the mist
eliminator vanes.
Testing with the TCA system similarly confirmed the strong effect of
limestone utilization on mist eliminator reliability. Runs 56Z-ZA,
562-2B, and 563-2A (see Table 8-2) were conducted at average scrub-
ber inlet liquor pH values of 5. 7 to 5. 9, with limestone utilizations
from 59 to 71 percent. The mist eliminator was washed intermittently
with fresh water on the topside, and continuously with diluted clarified
liquor on the bottomside. The mist eliminator restriction increased
to 7 to 9 percent during the first 500 hours of operation and appeared
to level out at 7 percent restriction after 811 hours at the end of Run
563-2A. Folio-wing these tests, the scrubber inlet liquor pHwas dropped
to 5. 2 (Run 564-2A) and the operation continued for an additional 113
hours. At the end of Run 564-2A, the mist eliminator restriction
decreased to 3 percent from the 7 percent at the start of the run.
The limestone utilization during Run 564-2A averaged 94 percent.
This decrease in mist eliminator restriction indicates that in some
cases an already fouled mist eliminator can be cleaned by increasing
the alkali utilization.
As was discussed in Subsections 8. 1 and 8. 2, operation at reduced
scrubber inlet liquor pH to achieve high utilization causes a reduction
8-27
-------
in SO2 removal efficiency. SO- removal efficiency at high utilization
can be increased in a number of ways, including increasing the slurry
flow to the absorber, increasing the TCA packing height and gas phase
pressure drop, or adding MgO to the scrubber slurry. Furthermore,
SO removal efficiency can be increased -while maintaining high lime-
L*
stone utilization by operating with three hold tanks in series.
Venturi/spray tower limestone Runs 714-1A through 717-1A (see Table
E-2 and Figures F-17 through F-19) were conducted to obtain scrubber
liquor pHand SO_ removal data at a specified limestone stoichiometry
o
and a steady-state liquor Mg concentration of 5000 ppm. Table 8-1
shows that the mist eliminator was only 2 percent restricted after 157
hours of operation during Run 714-1A, at an average limestone utili-
zation of 80 percent and -with an intermittent topside and underside
freshwater -wash. During Runs 715-1A and 716-1A, the slurry flow
to the spray tower was turned off with only the venturi in operation.
The scrubber inlet liquor pH dropped steadily during these two runs,
even at an increased limestone addition rate, resulting in SO_ gas
£t
evolution from the effluent hold tank and centrifuge. The mist elim-
inator restriction increased to 8 percent at the end of Run 717-1A
after a total of 379 operating hours. This increase was probably due
to the low limestone utilization during Runs 71 5-1A and 716-1 A.
TCA Runs 565-2A through 580-2A were operated with three hold tanks
in series (see Table 8-2). As with the venturi/spray tower system,
8-28
-------
continuous bottomside wash with diluted clarified liquor and intermit-
tent topside wash with makeup water limited the amount of soft solids
deposition at low utilization (Run 567-2A), Also, the mist eliminator
was kept completely free of solids with continuous bottomside wash
at high utilization (Runs 565-2A and 566-2A). As expected, with inter-
mittent bottomside and topside wash at high alkali utilization (Runs
568-2A through 573-2A), the chevron mist eliminator remained nearly
free of solids. After a total of 1188 operating hours with continuous
and intermittent bottomside wash and intermittent topside wash, the
chevron mist eliminator in the TCA was less than 1 percent restricted
with soft solids (see Run 573-2A in Table 8-2).
A further example of a mist eliminator that had become less restricted
during operation at high utilization can be seen in Runs 577-2A through
582-2A. At the conclusion of Run 571-2A (run at 80 percent limestone
utilization), the mist eliminator was 20 percent restricted by soft solids,
and after an additional 226 hours of operation at 97 and 87 percent util-
ization (Runs 579-2A and 581-2A), the mist eliminator restriction de-
creased to 2 percent.
8. 5 CONCLUSIONS
• Limestone utilization in the venturi/spray tower and TCA sys-
tems 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
8-29
-------
pH, however, caused a reduction in SO2 removal efficiency
•when other test conditions were held constant.
• For the venturi/spray tower system with a single effluent hold
tank, limestone utilization tended to be higher at 1 2 to 20 min-
utes residence time than at 6 minutes residence time.
• For the TCA system within the range of total effluent residence
times tested (10,8 to 14.4 minutes) and at scrubber inlet li-
quor pH values greater than about 5.0, higher limestone utili-
zation can be achieved with three hold tanks in series than
with a single hold tank.
• The reliability of the mist elimination system is a strongfunc-
tion of alkali utilization.
* For high alkali utilization (greater than about 85 percent),
the mist eliminator can be kept free of solids deposits by an
intermittent makeup water top wash combined with either inter-
mittent bottom wash with makeup water or continuous bottom
wash with diluted clarified liquor. Intermittent wash may be
required in closed-liquor-loop operation owing to restrictions
in the allowable makeup -water to the scrubber system.
» For alkali utilization less than about 85 percent, intermit-
tent top and bottomside wash with makeup water does not limit
solids accumulation. However, for these conditions, a con-
tinuous bottom wash with diluted clarified liquor used in com-
bination with an intermittent topside wash with makeup water
can limit soft solids buildup to a stable condition of less than
10 percent restriction -within the mist eliminator.
» Operation for a period of time at high alkali utilization (greater
than about 90 percent) may, in certain instances, clean up an
already fouled mist eliminator.
8-30
-------
Section 9
LABORATORY QUALITY ASSURANCE PROGRAM
The Shawnee Advanced Test Program has put an increasingly heavy an-
alytical load on the test facility chemical laboratory. At the same
time, the analytical results have never been more important for the
control of system parameters and for the development of advanced
theoretical models by which lime/lime stone SO2 scrubbing systems
may be described.
To achieve the objectives of the Advanced Test Program, it was nec-
essary to perform some of the analytical procedures more rapidly and
with greater precision and accuracy than was the case in previous long-
term reliability tests. Therefore, a quality assurance program was
initiated at the test facility to identify procedures that did not sat-
isfy the needs of the Advanced Test Program. The goals of the lab-
oratory quality assurance program included the following:
• To establish the precision and accuracy of the analytical meth-
ods used at Shawnee
• To provide continuous surveillance of the quality of the analyt-
ical data
• To develop new analytical procedures as required to supplant
or augment existing procedures
9-1
-------
9. 1 QUALITY ASSURANCE CRITERIA
Precision and accuracy provide criteria for evaluating test data. Pre-
cision refers to the reproducibility among repeated observations of
the same sample. Accuracy refers to the degree of difference between
observed and known, or actual, values. When precision and accuracy
criteria are established, systematic checks to assess test data validity
are possible. Procedures used for establishing precision and accuracy
for the Shawnee analytical methods are given in Appendix K. These
procedures follow EPA guidelines set forth in Reference 7.
9. 2 EVALUATION AND MODIFICATIONS OF ANALYTICAL
PROCEDURES
The first step in the quality assurance program was a comprehensive
review of the analytical methods and equipment used at Shawnee. The
available precision and accuracy data were used to identify problem
areas. The methods judged to require improvement for the Advanced
Test Program were the following:
Liquids
e pH
• Sulfite by titration
• Sulfate by titration
Solids
• Total sulfur, magnesium, and calcium by X-ray
• Total sulfur by the backup method (titration)
• Carbonate by CO? evolution
9-2
-------
These methods are described in the Shawnee Chemical Procedures
Laboratory Manual (Reference 6). The problem areas that have been
identified are described in more detail below.
9- 2. 1 X-Ray Fluorescence Spectrometric Analysis
The precision of the X-ray fluorescence spectrometry method (Method
16, Reference 6) used to analyze for calcium, total sulfur, and mag-
nesium in solid samples was excellent. Precision control limits are
discussed in Appendix K.
The accuracy of the X-ray fluorescence method was less satisfactory.
Several known samples were analyzed at the test facility for calcium,
sulfur, and magnesium, and the results of the analyses are compared
with the known values in Figures 9-1, 9-2, and 9-3. The accuracy
of Method 16 was found to be a function of the composition of the solid
and thus not amenable to the control chart techniques described in Ap-
pendix K.
On January 29, 1976, a new pellet preparation method (Method 17 in
the Shawnee laboratory manual) was initiated with the objective of im-
proving the accuracy of the calcium and sulfur analysis. This method
uses lithium carbonate (Li2CC>3) to dilute the solids, thereby reducing
interferences from other species. The accuracy of the new procedure
is being monitored.
9-3
-------
36
35
34
33
32
31
30
a?
| 29
IB
| 28
S
c 27
o
£ 26
3 25
24
23
22
21
20
X RAY
STANDARD NO. 3
25.4 % CaO
I
I
20 21 22 23 24 25 26 27 28 29 30 31
CaO (by*X-ray method), wt. %
32 33 34 35 36
Figure 9-1.
Results of Analysis for CaO by X-Ray Fluorescence
Spectrometry with Known Values for CaO in the
Prepared Samples
9-4
-------
X-RAY
STANDARD NO. 3
28.4 % S03
22
22 24 26 28 30 32 34 36
SO3 (by X-ray method), wt. %
38
40
42
44
Figure 9-2. Results of Analysis for SO3 by X-Ray Fluorescence
Spectrometry with Known Values for SO3 in the
Prepared Samples
9-5
-------
1.0 -
0.8
a
2 0.6
1
e
0.4
0.2
X-RAY
STANDARD NO. 3
0.31 % MgO
0.0
0.0
0.4 0.6 0.8
MgO (by X-ray method), wt. %
1.0
Figure 9-3.
Results of Analysis for MgO by X-Ray Fluorescence
Spectrometry with Known Values for MgO in the
Prepared Sample
9-6
-------
Equations to improve the accuracy of the older data by correcting for
compositional interferences were developed from the analyses (Figures
9-1 and 9-2) pf known samples. These equations will be applied to
solids data collected prior to January 19, 1976. The equations are:
1.521 0.209
% CaO (corrected) = 0.083 x (%CaO) x (% fly ash)
X-ray
0.985 0.153
% SOS (corrected) = 0.639 x (%SO3) x (% fly ash)
X-ray
where (%CaO)
X-ray
(%S03)
X-ray
(% fly ash)
weight percent calcium (as CaO) in the dry
slurry solids found by Method 16 of Refer-
ence 6.
weight percent sulfur (as 803) in the dry
slurry solids found by Method 16 of Refer-
ence 6.
weight percent acid insolubles in the dry slurry
solids found by Method 4 of Reference 6.
The multiple correlation coefficients of 0.95 and 0. 99 for these equa-
tions indicate a good fit of the data.
Routine X-ray analysis of solids samples for magnesium was discon-
tinued. The low atomic number of this element and its low concen-
tration in the solids (less than 0. 5 percent) made the results of such
analysis doubtful (shown in Figure 9-3).
9-7
-------
9. 2. 2 pH
A study of pH data-taking procedures was conducted in November and
December 1975 to determine how to improve them. Several pH meters
in use were experiencing difficulty. The glass electrodes required long
periods (up to 20 minutes for some electrodes) to reach thermal equi-
librium when transferred from buffer at ambient temperatures to slur-
ries at scrubber temperature (125°F). The sample shack used for
housing pH measuring equipment was crowded and inadequately heated.
As a result of the study, a formal procedure was adopted for measure-
ment with the pH meters and electrodes. The revised pH procedure
includes a4-minute period to allowthe glass electrodeto reach thermal
equilibrium at slurry temperature and a monthly equipment check to
ensure correct pH values at slurry temperature as well as ambient
temperature.
A new field laboratory was constructed to replace the sample shack.
Slurry pH readings in the field lab were to be made only with a new
Fisher Accumet Model 520 pH meter. This meter has an internal cir-
cuitry check that is useful for troubleshooting.
Tests were initiated to further improve the pH measurement process.
This included testing of electrodes to see if electrode life expectancy
9-8
-------
can be increased by the use of hot baths for electrode storage between
readings and use of hot buffers.
Preliminary results have shown that buffering the pH meter at scrub-
ber temperature will improve the pH data. There are indications that
storing the glass electrodes at scrubber temperature in a pH 4 buffer
saturated with potassium chloride can increase the life expectancy
of the glass electrodes. Combination glass electrodes with glass-to-
glass seals between the electrodes and the sample solution are more
suitable for slurry service at Shawnee than other types, such as those
with rubber-to-glass seals.
The results of the pH study are detailed in a report entitled, pH Study
at the Shawnee Test Facility -- Phase II, September 1976.
9.2.3 Sulfite
The sulfite analysis procedure (Method 7, Reference 6) was found to
have a precision upper control limit of about 0. 5 (see Appendix K).
This means that the results of the analysis of a sample and its replicate
could differ by a factor of 2 to 3 without exceeding the upper control
limit. The amperometric cell and ammeter used in the amperometric
titration procedure (discussed in the laboratory manual) were consid-
ered to have been major causes of error.
9-9
-------
On February 5, 1976, the sulfite procedure was changed. A commer-
cial amperometric titrator (Wallace and Tiernan Series A-790) re-
placed the cell and ammeter in use prior to that date. The new procedure
is Method 8 in Reference 6. The instrument appears to be performing
well, although accuracy and precision data for this new method are
not yet available.
9.2.4 Sulfate
The ion exchange/titration procedure used at the test facility for sulfate
analysis was investigated. Although the precision of this analysis
(Method 9 in Reference 6) is acceptable (see Appendix K, Figure K-l),
the results of the accuracy samples analyses (shown in Appendix K)
indicated that this procedure produces unsatisfactory values. The av-
erage error [(Found-Actual)/(Actual) ] for 15 analyses was +28 percent.
A turbidimetric method (such as described in Reference 7) that would
not require ion exchange and would be relatively free of interferences is
being investigated to replace the titrimetric method currently in use.
9. 2. 5 Carbonate
Accuracy data for the solid carbonate analysis procedure (Method 5 in
Reference 6) were not available. However, the precision data available
9-10
-------
(Appendix K, Figure K-2) suggested that this method needed to be
improved or replaced.
Development of a new carbonate procedure was initiated at the site
employing the nondispersive infrared (NDIR) equipment described in
Method 6 of Reference 6. If this method proves to have acceptable pre-
cision and accuracy, it will replace the CC^ evolution method (Method
5 in Reference 6).
9. 3 CURRENT QUALITY ASSURANCE MEASURES
The ongoing laboratory quality assurance program at Shawnee includes
the following:
Daily review of analytical data to determine whether expected
trends are followed
Replicates of regular samples (providing data for precision
control charts)
Analysis of accuracy samples (providing data for accuracy
control charts)
Improvements in old procedures and the development of new
procedures on the basis of precision and accuracy data as
they become available
The program also includes documentation of equipment status, includ-
ing equipment inventories, equipment checkout results, and equipment
operating histories.
9-11
-------
Section 10
OPERATING EXPERIENCE DURING LIME/LIMESTONE TESTING
This section summarizes the operating experience during lime/lime-
stone testing at the Shawnee Facility from June 1975 through mid-
February 1976. Summaries ofprior operating experience are presented
in References 1 and 2.
10.1 SCRUBBER INTERNALS
10.1.1 Mist Eliminators
Reliable mist eliminator performance has been linked to percent alkali
utilization, with better reliability occurring at higher alkali utiliza-
tions. A review of mist eliminator performance during utilization
testing is presented in Subsection 8.4.
10.1.2 TCA Grid Supports
The 3/8-inch-diameter, 316 stainless-steel bar-grids, installed on
1-1/4-inch centers in October 1973, have been in slurry service for
approximately 16,000 hours with no evidence of significant erosion.
10-1
-------
10.1.3 TCA Spheres
In June 1975, three beds of 6-gram thermoplastic rubber (TPR) hol-
low spheres, each containing 10,000 spheres, were installed in the
TCA. Although these spheres were expected to reduce the dimpling
previously experienced with 5-gram spheres, a significant reduction
in dimpling did not occur. The failure rate for these spheres is plotted
in Figure 10-1. 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 recirculated. As indicated in Figure 10-1, 1500
TPR spheres were added to each of the top and middle beds inNovember
1975 to make up for previous sphere losses.
All the TPR spheres were replaced by new 6. 5-gram nitrile solid foam
spheres in December 1975, and 7500 of these new spheres were instal-
led in each of the three 5-inch beds. After 240 hours of operation, a
sample of the spheres 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 roughened, open
pores were visible under a microscope, and mold seams were still
apparent. The spheres did not look wet, nor could water be squeezed
10-2
-------
cc
D
UJ
cc
UJ
Q.
to
Ul
m
D
Z
i,500 •
,000 •
,500 •
,000
,500
,000 •
500 •
0
0
1 9 4 ft/sec SCRUBBER GAS VELOCITY
L, 12.5 ft/sac ,j, ^ 12.5 ft/sec f
CO
O
-rP
°?
cP )
O 1,500 SPHERES/BED
ADDED TO TOP 2 BEDS
O
o
o
o
o
o
o
°
o
00
o
0
3 BEDS
Q 10,000 SPHERES/BED
(-0D SLURRY SOLIDS PERCENT =15
O
' cou
0°°
° 1 1 1 1 1 1 1
• 11
• 10
• 9
• 8
7
' 6
5
4
3
2
1
n
500 1,000 1,500 2,000 2,500 3,000 3,500 4,000
UJ
QC
D
u.
UJ
cc
UJ
QC
Ul
a.
TOTAL TIME.Hr
Figure 10-1. Failure Rate of 6-Gram TPR Spheres in Limestone/
Fly Ash Slurry Service
-------
from them, but prior to drying they weighed approximately 9 percent
more than new, unused spheres. After drying for 3 days at 45°Cto
60°C, comparison of the new and used spheres showed for the used
spheres:
Weight loss = 1%
Diameter loss = 9%
Volume loss = 25%
Since the mold seams were still visible and since there was little
weight loss after drying, it is presumed that the spheres merely shrunk.
After 574 hours of operation, the spheres -were again sampled and after
acid washing and drying, they-were unchanged from their condition after
240 operating hours.
In early February 1976, the old spheres were replaced with new 6.3-
gram nitrilefoam spheres. These new spheres are being closely moni-
tored to better document the apparent shrinkage. Results will be pre-
sented in a later report.
10.1.4 Spray Tower Nozzles
The nozzles being tested in the venturi/spray tower system are Bete
No. ST48FCN stellite-tipped nozzles installed in March 1974. The
stellite tips have decreased approximately 40 percent in weight during
11,700 hours of service. Wear rate was greater in limestone service
than in lime service.
10-4
-------
Wear on the inside of the 316 stainless-steel base has been significant,
occasionally causing detachment of the nozzles. Making the base out
of stellite should eliminate this problem. The nozzles have operated
at 10 psi pressure drop for 9450 hours with 8 percent solids slurry
(lime), and for 2250 hours with 15 percent solids slurry (limestone)
10.1.5 TCA Nozzles
The four TCA slurry feed nozzles were installed in September 1974.
These were Spraco No. 1969F full-cone, open-type nozzles, made of
316 stainless steel. No significant wear has been observed after 9000
hours of operation at a 5 psi pressure drop with slurry containing
15 percent suspended solids. The low wear rate is probably due to
the low pressure drop across the nozzles.
10.1.6 Venturi Internals
The venturi at Shawnee is a variable-throat, 316L stainless-steel type
manufactured by Chemical Construction Corporation (Chemico). During
the current operating period, both erosion and minor corrosion have
continued, as indicated in the following discussion of specific internal
components.
As noted in Reference 2, inspection after shutdown for the May 1975
boiler outage revealed stress cracking on the portion of the inlet duct
10-5
-------
that extends into the venturi. Since then, two more pieces of the 40-
inch duct extension at the venturi inlet have failed. Because the fail-
ures do not significantly affect system operability, repair has been
delayed until a shutdown of sufficient length can be scheduled.
Erosion of the bull nozzle, plug guide vanes, and plug shaft sleeve
flanges has continued. To prolong the life of the guide vanes and
to test materials of construction, the vanes have been covered with
expendable materials or rubber shields. A discussion of the mate-
rials used through April 1975 can be found in TVA's Third Interim
Report on Corrosion Studies, Appendix L of this report. Materials
tested after April 1975 will be covered in a Fourth Interim R eport
on Corrosion Studies.
The only corrosion experienced in the venturi has been minor pitting
(see Appendix L).
It should be emphasized that solids buildup at the hot-gas/liquid inter-
face in the venturi entrance has never been significant, contrary to
the experience at some installations.
10.2 REHEATERS
Flue gas from the scrubber is reheated to prevent condensation and
corrosion in the exhaust system, to facilitate isokinetic and analytical
10-6
-------
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. )
have both been modified to incorporate a fuel-oil-fired external com-
bustion chamber {manufactured by Bloom Engineering Co. ). Reasons
for the changes are discussed in Reference 1. Both of the units have
operated reliably with minimum flameout and equipment problems
for over 13,700 hours on the venturi/spray tower system and 4400
hours on the TCA system. A major repair of the refractory in the
Bloom reheater on the venturi/spray tower system was made during
the May 1975 boiler outage. Repairs were made by using a mixture
of 15 percent Kaocrete and 85 percent Kruzite castable #32 refractory
(A.P, Green Co. , Mexico, Missouri).
10.3 FANS
The 316L stainless-steel fans at theShawnee Test Facility are induced-
draft, centrifugal fans manufactured by Zurn Industries. Reliability
has been good during the current operating period, with no system
downtime due to fan problems.
During the May 1975 boiler outage, a 4-inch hairline crack was dis-
covered in the fan rotor shroud of the venturi/spray tower fan. The
10-7
-------
crack was repaired by welding with a Type 347 stainless-steel rod
and grinding the weld smooth.
Ease of cleaning the fans, fan dampers, and ductwork between the
dampers and reheaters has been greatly increased by the use of a
new portable steam generator. The unit has also been useful in thawing
frozen lines during winter.
10.4 PUMPS
The major pump problem during the current operating period (see Ref-
erence 1 for a report on prior operation) has been pump seal failure.
The seals on the rubber-lined centrifugal pumps (manufactured by Allen-
Sherman-Hoff) are air-flushed packings. The frequency of repacking
of the 20 to 100 gpm pumps has been minimized by maintaining the
clearance between the shaft and the pump casing at 10 to 15 mils.
In another attempt to solve seal problems at Shawnee, mechanical seals
have been tested on various centrifugal pumps. These tests are part
of the equipment components testing program, and the results are cov-
ered in detail in Subsection 10. 8. 2,
10-8
-------
10. 5 WASTE SOLIDS HANDLING
10.5.1 Filter
Because of frequent cloth failure and cake discharge difficulties, the
Maxibelt rotary-drum vacuum filter was converted from a roll dis-
charge type to a snap-blowback discharge type in February 1975. The
filter cloth life has been extended by this change but is still con-
sidered too short. The major reasons for cloth failures have been tear-
ing and blinding. Table 10-1 summarizes details of the cloths tested at
Shawnee. A program will be initiated to determine both the reason for
the continuing short cloth life and the steps necessary for improvement.
10. 5. 2 Centrifuge
The centrifuge being used at Shawnee is a solid-bowl continuous type
manufactured by Bird Machine Co. Owing to severe erosion, the
surface of the original unit required rehardening after 1400 hours of
operation. Since repair, a total of 3500 hours of satisfactory inter-
mittent operation has been achieved.
10.5.3 Clarifiers
The 6-foot feedwell extension on the TCA clarifier (8 feet total), in-
stalled during the May 1975 boiler outage, has proved successful in
10-9
-------
Table 10-1
SUMMARY OF FILTER CLOTHS TESTED AT SHAWNEE
Cloth
Ametek STE-F908-HJO
Lamports S/4048-SHS
Lamports 7512-SHS
Material
100% olefin
Polyester (Dacron)
Multifilament polypropylene
Number Tested
6
4
8
Longest
Cloth Life, hr
603
203
642
o
I
-------
reducing clarifier upsets and subsequent high solids content in the
clarifier overflow.
10. 6 ALKALI ADDITION SYSTEMS
10.6.1 Lime
The lime addition system consists of a storage silo, a screw feeder, a
lime slaker (manufactured by Portec-Cahaba), a slaked-lime holding
tank, and associated feed pumps. An analysis of the lime used can
be found in Appendix C. Fresh water slakes the lime to approxi-
mately 20 to 25 weight percent solids. The system has given excellent
reliability in over 15,800 hours of intermittent operation. Plugging
of the lime addition lines by gradual buildup of grit that gets through the
slaker screen has been reduced by placing a screen over the entrance
to the slaked lime slurry hold tank.
10- 6. 2 Limestone
The limestone addition system consists of a drying-grinding system,
a dry storage tank, a belt feeder, a slurry tank, and associated feed
pumps.
The drying-grinding system was installed during an earlier EPA-spon-
sored dry-limestone injection program at the Shawnee Power Station.
10-11
-------
The only major repair during the current reporting period was the
relining of the dryer fire box. Generally, it has given s£ tisfactory
performance with low maintenance during the 4 years of the alkali
\vet-scrubber test program.
The slurry addition system was modified to provide 60 weight percent
limestone slurry in November 1972 and was further modified to incor-
porate clarified process liquor for slurrying the limestone in March
1974. Since March 1974, the system has continued to operate satisfac-
torily for an additional 11,400 hours of intermittent operation with little
maintenance.
The alkali addition system pumps are positive displacement pumps man-
ufactured by Moyno Pump Division of Robbins & Myer Co. They were
installed in November 1972 when the limestone system -was converted
to provide a 60 -weight percent limestone slurry. The pumps are over-
sized by a factor of 2. They are allowed to wear until the required
flow can no longer be maintained. Typical operating life for a rotor
is 2000 hours and for a stator, 1000 hours.
A composition and size distribution analysis of the ground limestone
can be found in Appendix C.
10-12
-------
10.7 • INSTRUMENT OPERATING EXPERIENCE
10.7.1 pH Meters
The main problem associated with the Uniloc Model 321 submersible
pH meters (Universal Interloc, Inc. , Santa Ana, Calif. ) used to mea-
sure scrubber liquor pH has been occasional scale formation on the
probes. This scale causes measurement error and is removed by
rinsing with hydrochloric acid. All probes are routinely rinsed with
water about twice a week and calibrated when necessary.
In April 1975, a short period of testing was conducted using a contin-
uous ultrasonic cleaner (a Uniloc add-on) to aid in the prevention of
scale buildup. The cleaner was effective at preventing heavy scale
buildup when operating in a highly scaling mode.
Current operating experience with lab pH meters is covered in Sub-
section 9. 2. 2.
10.7.2 FlowJMeters
In Reference 1, it was reported that the Adiprene L-liner in the 1-1/2-
inch Foxboro magnetic flow meters deteriorated. Subsequently, it was
noted that these liners were tapered in thickness near the meter exit
10-13
-------
while all the other meter sizes had a uniform lining thickness. As
a result, the meters were relined with Adiprene-L of uniform thick-
ness, and since that time no liner failures have been experienced.
Satisfactory meter accuracy can be en maintained by electrical purging
once per shift and flow checks approximately once every 3 months.
10.7.3 Level Measurement
Three Brooks Maglink 5300 Series level indicators were installed
in scrubber effluent hold tanks D-101, D-201, and D-208 for eval-
uation at the Shawnee Test Facility. The Brooks indicator consists
of a verticallymounted standpipe or stilling chamber fastened exter-
nally 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, and eventual immobiliza-
tion of, the float. A liquor flush stream was installed to eliminate the
problem, but the following difficulties are occasionally encountered.
10-14
-------
• Floating material still causes occasional immobilization of
the float.
• The flush system liquor stream impinges on the float, causing
float depression and reading error. The magnitude of the error
is variable and dependent on the distance the purge stream
free falls prior to impingement on the float.
• Dislodging an immobilized float can uncouple the magnet. Reac-
tivating the system can take several manhours.
• Modifying the measurement range requires the installation
of a new gear drive.
However, when properly maintained and calibrated and when a constant
flush of about 2 gpm of slurry or clarified liquor is used, the Brooks
indicator will measure the slurry level in the effluent hold tank to within
6 inches. A dipstick level measurement is used routinely to check
the Brooks indicator.
10.7.4 SO2 Meters
Operation with the Du Pont Model 400 UV SO2 analyzers has been
essentially trouble-free during the current operating period. The units
are calibrated on Monday, Wednesday, and Friday of each week using
a set of calibrated filters.
10.7.5 Density Meter
The Dynatrol density meter continues to give trouble-free operation.
10-15
-------
10.8 MATERIALS AND EQUIPMENT EVALUATION PROGRAM
10. 8. 1 Materials
Lining or coating materials for equipment at the Shawnee Facility gen-
erally consist of neoprene rubber (pipes, pumps, scrubber internal
walls, and small tanks) or Flakeline 103 (effluent hold tanks and clar-
ifiers). Flakeline 103 is a bisphenol-A type of polyester resin filled
25 to 35 percent with glass flake. It is manufactured by Ceilcote
Company.
Both rubber and Flakeline coatings have shown very little erosion or
other deterioration. However, a Flakeline 103 test panel-mounted in-
side one of the TCA beds did exhibit significant wear. Successful re-
pairs have been made using Epoxylite-203 (Epoxylite Corp, Anaheim,
California), an epoxy resin formulated with selected fillers, making
a paste material. The resin is cured with Epoxylite's No. 301 amine
hardener. Apatchon the venturi/spray tower effluent hold tank agitator
blade has shown little wear after over 13, 500 hours.
The Third Interim Report of Corrosion Studies at the test facility,
written by TVA, is presented in Appendix L. The report covers
the operating periods from October 1973 through April 1975 and dis-
cusses corrosion and erosion of the test facility equipment and the
10-16
-------
results of the materials of construction evaluation carried out simul-
taneously. Results for the current operating period will be presented
in the Fourth Interim Report.
10.8.2 Equipment
A program to evaluate selected mechanical components has been ini-
tiated at the Shawnee Test Facility. Plastic pipe, butterfly and knife
gate valves, Hay ward line-strainers, mechanical seals, an orifice plate,
and several Ceilcote lining materials are currently being evaluated.
Results are summarized in this section.
Plastic Pipe. High-impact polyvinyl chloride pipe was installed on
the suction line of the TCA slurry recycle pump (G-201) during the
current operating period. The piping consists of one Tee, one 90°
elbow, a 120° "S", and 2 feet of straight pipe. After 3163 hours car-
rying a 15 percent slurry at 10 ft/sec velocity, the pipe was removed.
Inspection revealed essentially no occurrence of erosion. A section
of Bonstrand Series 4000 fiberglass-reinforced plastic pipe was then
installed in the same spot and is currently being tested.
Butterfly Valves^ A 6-inch Durco manual block valve (throat and disc
coated with abrasion-resistant polyethylene) and a Valtek 6-inch butter-
fly control valve are being evaluated.
10-17
-------
The Durco valve is located in the pump G-204 discharge line (G-204
feeds two of the spray tower headers). A total of 3700 hours of service
in 8 percent slurry at approximately 9 ft/sec slurry velocity through
the valve (in full-open position) resulted in a 4. 5-mil loss of the disc
coating thickness. This represents about 10 percent of the total coating
thickness. The throat liner was in good condition, and there was no
leakage through the valve when it was leak-tested at 55 psig.
The Valtek valve is also located in the G-204 pump discharge line.
After approximately 3000 hours of service, hairline cracks appeared
in the valve body and the disc experienced some slight erosion. Use
of the valve for control has been attempted only at 700 to 800 gpm,
and at that flow rate control has been good.
Knife Gate Valves. The knife gate valves being tested at Shawnee are
Fabri-Valve 316 stainless-steel valves. Two 8-inch Figure 45 and
two 8-inch Figure 37 valves are installed as block valves at the inlet
and outlet of the parallel Hayward basket strainers in the discharge
of pump G-201 (TCA slurry recycle pump). Four 6-inch Figure 37
valves are installed on the inlet and outlet of the Hayward strainers
on the discharge of pump G-204.
Initial experience with the valves was poor. A hard scale formed
on the surface of the gate, causing abrasion, flattening, and displace-
ment of the neopreneO-rings in the valve seat. Often a displaced O-ring
10-18
-------
lodged between the gate and seat, causing the valve to leak. Experience
has shown that without the O-rings, the valve seats without leaking,
but the valves become difficult to open and close. Erosion has been
negligible after more than 4000 hours of operation,
Line Strainers. Two Hayward single-basket line-strainers were in-
stalled in parallel at the discharge lines of both pump G-204 and
pump G-201 as replacements for the failed Elliot line-strainers. After
approximately 3700 hours of service, the iron body of the strainer
was severely eroded in several areas. The 316 stainless-steel baskets
(30-mil thick with 3/8-inch-diameter perforations) have not eroded sig-
nificantly.
Mechanical Seals. Durametallic type "CRO" mechanical seals were
installed on pumps G-105 (venturi/spray tower system bleed) and G-205
(TCA system bleed). The seal on G-105 failed after approximately
1500 hours of service; however, one of its carbon inserts was broken
when it was installed. The seal on G-205 is still performing well
after more than 4000 hours of service.
Orifice Plate. A 316 stainless-steel orifice plate equipped with a
diaphragm DP cell for flow measurement is being tested in the line
downstream from pump G-204. After 12, 000 hours of operation, the
plate is still in good condition with very little erosion or corrosion.
10-19
-------
Chemical scale, however, deposits on the diaphragms, resulting in
a measurement inaccuracy of about 1 5 percent after 2 weeks of service.
Frequent cleaning of the diaphragms is necessary to keep the orifice
meter calibrated.
Ceilcote Lining Materials. Plates of 316 stainless-steel were coated
with Ceilcote materials by the Ceilcote Company and mounted at several
locations inside the TCA scrubber to test these materials as scrubber
liner materials. Flakeline 103, Coroline 505AR, and Flakeline 151 are
being tested. After approximately 4000 hours, except for mechanical
damage which was done by workers in the scrubber, the only panel
that has undergone significant erosion or chemical attack is the panel
mounted inside a TCA mobile bed. The panels will be returned to
Ceilcote Company in June 1976 for final evaluation.
Future Evaluations. Scheduled for future testing and evaluation are
both Metritape and sonic tank level sensors, a Moyno positive dis-
placement pump for long distance pumping, a cone-diaphragm check
valve in clarified liquor service, and both polybutylene and PVC pipe
for slurry circulation.
10-20
-------
Section 11
REFERENCES
1. Bechtel Corporation, EPA Alkali Scrubbing Test Facility; Sum-
mary of Testing through October 1974, EPA Report 650/2-75-047,
June 1975.
2. Bechtel Corporation, EPA Alkali Scrubbing Test Facility; First
Progress Report, EPA Report 600/2-75-050, September 1975.
3. Universal Oil Products, Air Correction Division, Bulletin No. 608,
"UOP Wet Scrubbers," 1971.
4. R. H, Borgwardt, "Increasing Limestone Utilization in FGD Scrub-
bers, " presented at the 68th A.I. Ch. E. Annual Meeting, Los Angeles
November 16-20, 1975.
5. R. H. Borgwardt, "IERL-RTP Scrubber Studies Related to Forced
Oxidation, " Proceedings; Symposium on Flue Gas Desulfurization,
New Orleans, March 1976, Volume 1, EPA Report 600/2-76-136a,
pp 117-144, May 1976.
6. Bechtel Corporation, Shawnee Chemical Procedures Laboratory
Manual, March 1976.
7. National Environmental Research Center, Methods for Chemical
Analysis of Water and Wastes, EPA Report 625/6-74-003, 1974.
11-1
-------
Appendix A
CONVERTING UNITS OF MEASURE
Environmental Protection Agency policy is to express all measure-
ments in Agency documents in metric units. When implementing this
practice will resultin undue costs or lack of clarity, conversion factors
are provided for the non-metric units used in the report. Generally,
this report uses British units of measure. For conversion to the
metric system, use the following conversions:
To Convert From
scfm (60°F)
cfm
OF
ft
ft/hr
ft/sec
ft2
ft2/tons per day
gal/mcf
To
gpm/ft*
gr/scf
in.
in. H2O
Ib
Ib-moles
Ib-moles/hr
Ib-moles/hr ft2
Ib -mole s /min
psia
nm3/hr (0°C)
m3/hr
°C
m
m/hr
m/sec
m2
m2/metric tons
per day
1/m3
1/min
1/min/m*
gm/m*
cm
mm Hg
gm-moles
gm -mole s /min
gm-moles/min/m2
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-l
-------
Appendix B
SCRUBBER OPERATING PERIODS
B-l
-------
SCRUBBERS OPERATING PERIODS
W
-------
SCRUBBERS OPERATING PERIODS
-------
SCRUBBERS OPERATING PERIODS
W
-------
SCRUBBERS OPERATING PERIODS
-------
SCRUBBERS OPERATING PERIODS
tri
i
2. I 0/3 ! -8Af
-------
SCRUBBERS OPERATING PERIODS
bd
i
00
-------
SCRUBBERS OPERATING PERIODS
tfl
l
vO
-------
SCRUBBERS OPERATING PERIODS
O I ID/// 110/12. ifO/13
-------
SCRUBBERS OPERATING PERIODS
-------
SCRUBBERS OPERATING PERIODS
td
i
h-«
ts)
-------
SCRUBBER OPERATING PERIODS
I /Z3 111/24 I 11/2.5
-------
SCRUBBER OPERATING PERIODS
::.i.:..l....l !
i j i
•
....!.
' .' r i
|
1
EMD
iijli' -
i .:
i
n|, |;H
j
j
j •
1 ' i i
• 1 j :
> 1
2/i/- M2./5 |l2/6l27
/2/8 1/2/9
-------
SCRUBBER OPERATING PERIODS
-------
SCRUBBER OPERATING PERIODS
1/4 i >/5 | 1/6
j 12/23
-------
SCRUBBER OPERATING PERIODS
-------
SCRUBBER OPERATING PERIODS
.'. <8'/--hr5lDEPLETV(j»N)
I 1/27 ! 1/281 !/2«H l/3o I i/3/ I 2/1 I 2/2 I 2/3
2/6 I 2/7 | V8 I 2 A? J2//0
-------
SCRUBBER OPERATING PERIODS
2/21 I 2/22 | 2/23
2/1112/12 | 2/13 I JM 12/15 \2/\l>\2j)l |2/l8
1974
-------
Appendix C
PROPERTIES OF RAW MATERIALS
C-l
-------
The following is a summary of the properties of the raw materials used
from June 1975 through mid-February 1976.
C.I COAL
Supplier: Several
Type: Eastern (Southern Illinois) high sulfur.
Analysis: 9.4 to 12.4 wt % total moisture
2. 3 to 5. 5 wt % sulfur
0. 03 to 0. 27 wt % chloride
14.7 to 27.9 wt % ash
Approximate Ash Analysis:
54 wt % SiO2
23 wt % A12O3
12 wt % Fe^Os
3 wt % CaO
1 wt % MgO
1 wt % 803
3 wt % KzO
1 wt % Na2O
3 wt % Ignition loss
C-2
-------
Note: During isolated instances, Shawnee Unit No. 10 has burned low
sulfur western coal of the following composition:
C.2
C.3
Supplier:
Type:
Analysis(a):
Western Energy Company, Cow Creek, Montana
Col strip seam
26. 8 wt % total moisture
0. 95 wt % sulfur
0.1 wt % chloride
10.7 wt % ash
Approximate Ash Analysis: (None made)
LIMESTONE
Supplier:
Type:
Analysis:
Grind:
LIME
Supplier:
Type:
Analysis:
Fredonia Quarries, Fredonia, Kentucky
Fredonia Valley White
95 wt % CaCO3
1 wt % MgCC>3
4 wt % Inerts
91 wt % less than 325 mesh
87 wt % less than 30 microns
86 wt % less than 27 microns
53 wt % less than 6 microns
Linwood Stone Co. , Davenport, Iowa (through 9/75)
Mississippi Lime Co., Alton, Illinois (after 9/75)
Pebble lime, unslaked
97.0 wt % CaO total
95. 5 wt % CaO available
0. 28 wt % MgO
0.47 wt % Inerts
(a)
Average values, from only two analyses.
C-3
-------
C. 4 MAGNESIUM OXIDE
Supplier: Basic Chemicals, Ft. St. Joe, Florida
Type: MAGOX PG (pollution grade)
Analysis: 97.6 wt % MgO
1.5 wt % CaO
0. 5 wt % SiC>2
0.4 wt %
C-4
-------
Appendix D
DATA BASE TABLES
D-l
-------
PAGE
SUMMARY OF VENTURI/SPRAY TOWER RUNS FROM JUNE 1975 TO MID-FEBRUARY 1976
o
I
IN)
RUN START END
NUMBER DATE DATE
625-1A 06/20/75 07/09/75
626-1A 07/09/75 08/04/75
627-1A 08/05/75 08/13/75
628-1A 08/16/75 09/18/75
628-1B 09/18/75 10/07/75
701-1A 10/09/75 10/12/75
702-1A 10/14/75 10/17/75
703-1A 10/19/75 11/01/75
704-1A 11/03/75 11/06/75
705-1A 11/07/75 11/13/75
706-1A 11/13/75 11/19/75
707-1A 11/21/75 11/26/75
708-1A 11/26/75 12/02/75
709-1A 12/06/75 12/12/75
710-1A 12/12/75 12/22/75
711-1A 12/24/75 12/30/75
711-16 12/30/75 01/02/76
712-1A 01/02/76 01/87/76
712-1B 01/07/76 01/08/76
713-1A 01/08/76 01/10/76
714-1A 01/19/76 01/26/76
715-1A 01/26/76 01/27/76
716-1A 01/27/76 01/28/76
717-1A 01/28/76 02/05/76
HRS
ON
STRM
319
569
187
717
426
73
60
319
66
136
180
118
138
134
234
144
71
119
18
52
157
23
18
181
LIME ALK GAS
OR ADDN FLY RATE
LS PT. MGO ASH ACFM
L
L
L
L
L
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
LS
DNC
DNC
EHT
DNC
DNC
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
EHT
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
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
30000
35000
35000
*
*
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
35000
VEN VEN
LIQ L/G
RATE GAL/
GPM MACF
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
600
25
21
21
*
*
21
21
21
21
21
21
21
21
21
21
21
21
21
21
21
21
21
21
21
S.T. S.T.
LIQ L/G
RATE GAL/
GPM MACF
1200
1400
1400
*
1600
1600
1400
1400
1400
1500
1400
1400
1400
1400
1400
1400
1400
1400
1400
1400
1400
0
0
1400
50
50
50
#
*
57
50
50
50
53
50
50
50
50
50
50
50
50
50
50
50
0
0
50
S.T. NO. OF
HEADER HOLD
CONFIG TANKS
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1234
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
EFFLU
RES SOLID
TIME RECIRC
MIN WT.%
12.0
12.0
20.0
12.0
12.0
20.0
20.0
20.0
20.0
20.0
12.0
12.0
12.0
12.0
6.0
6.0
6.0
6.0
6.0
6.0
6.0
20.0
20.0
6.0
6.0
8.0
15.0
10.0
9.0
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
SOLIDS
DISCH
RANGE
%
55-60
52-60
52-56
51-55
52-56
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
59-60
57-62
56-66
70-73
53-59
M.E.
SYSTEM
CONFIG
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
1-3P/0V
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
C/I
C/I
C/I
C/I
C/I
C/I
C/I
I/I
I/I
I/I
I/I
M.E.
DE- SYSTEM
WATER D. P. RANGE
SYSTEM IN. WATER
CL/F
CL/F
CL/F
CL/F
CL/F
CL/F
CE
CE
CE
CL/F
CL/F
CL/F
CL/F
CE
CL/CE
CE
CE
CE
CE
CE
CE
CE
CE
CE
0.15-0
0.37-0
0.37-0
0.08-0
0.10-0
0.35-0
0.35-0
0.30-0
0.35-0
0.35-0
0.30-0
0.25-0
0.43-0
0.33-0
0.33-0
0.35-0
0.33-0
0.36-0
0.38-0
0.33-0
0.35-0
0.35-0
0.25-0
.30
.40
.42
.45
.40
.70
.60
.40
.76
.43
.40
.43
.55
.40
.40
.40
.38
.40
.40
.40
.40
.40
.50
VEN
D.P.
IN.
H20
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
9.0
Note; Runs 628-1A and 628-IB were variable gas-load tests. See Appendices E and F for more operating details.
-------
PAGE
O
I
DIM
N!JP?tn CATE
6?5-lft 06/20/75
n6/21/75
Oft/21/75
rf /2?/75
r^/22/75
C6/23/75
"6/23/75
f 6/24/75
-S./25/75
C6/25/75
~C/3rl/75
T6/30/75
"7/01/75
07/01/75
P7/02/75
07/02/75
07/03/75
r7/e*/75
"7/04/75
07/04/75
P7/05/75
?7/05/75
07/06/75
07/Pf/75
C7/07/75
n?/C8/75
^T/98/75
626-1A 07/09/75
C7/09/75
07/10/75
C7/10/75
"7/11/75
T7/11/75
"7/11/75
"7/11/75
G7/12/75
07/12/75
07/13/75
r-7/1^/75
C7/14/75
C7/14/75
"•7/15/75
"7/15/75
07/15/75
C7/1S/75
C7/16/75
07/16/75
07/17/75
C7/17/75
r7/17/75
PM AT
SCRU3U£°
TIMF I«JLET
2300
1500
2300
1500
2305
150C
23 OC
1500
1500
2300
16CC
2300
1500
2300
1500
2300
1500
23PO
1500
2300
1500
2300
1500
2300
23CO
1500
2300
1500
2300
1500
2300
1500
1501
1502
2300
1500
2300
1500
2300
1500
2300
0700
1*00
2300
0700
1500
2300
0700
1500
2300
8.2=5
7.50
7.90
7.45
P. TO
«.*fl
8.60
7.7Q
8.00
«.10
R.25
7.90
fi.20
ft. 00
9.15
8.45
B.45
P. 00
8.15
R.25
9.10
R.1Q
B.10
R.10
R .75
9.00
fi.OC
8.10
8.15
7.20
7.55
8.19
•'.90
°. .00
8.00
P. ID
7.90
8.05
7.90
e.oo
8.20
8.20
3.15
3.30
B.30
R.OO
6.15
3.10
CA + »
POM
1215
1660
1955
3795
2599
2930
27?4
?879
2975
?«14
3260
3339
34PO
4109
42PO
3769
3550
3455
3469
3?4C
3179
27PO
2719
3^14
2724
2510
2425
?5(,
63
55
55
55
54
54
47
63
49
53
48
4S
48
45
52
48
L TiLS »
K +
PPM
48
7S
80
160
117
157
131
108
120
127
127
132
133
141
143
144
135
141
132
114
118
115
115
122
106
lie
151
126
119
119
123
12C
117
117
122
1 ;> u n u L'
503 —
PP*
120
104
60
8
24
40
PC
40
24
72
120
72
72
KB
88
96
144
16
48
128
32
168
RC
16
64
24
152
32
h8
40
32
88
48
72
80
K LK 1 Pti. I
S04 —
PPM
1225
1150
1354
1030
2258
1432
1179
1523
996
1067
1460
1619
1625
lo'H
1342
1442
1205
1420
1171
917
1196
542
1271
1457
891
1077
633
1150
812
1028
966
896
1109
1573
1226
CL-
PPM
1311
21'*8
2659
4396
3793
4254
4041
4077
4538
4573
4821
4892
5211
6209
5779
5530
6098
5690
5956
5429
5282
4892
4963
5016
4928
4715
4715
4768
4609
4431
4396
4467
4254
4573
4360
TOTAL SULFATE
IONS SAT. AT
PP*i 50 C
4001
5301
6235
9026
8931
8967
8335
8815
8815
8945
9996
10277
10664
12394
11881
11262
11409
11005
11009
10017
10060
8720
9389
9790
8958
8709
8341
8931
8186
8270
8300
8288
8311
9152
8556
93
91
110
90
181
120
98
125
?6
90
123
135
136
139
117
122
101
118
100
80
99
46
103
117
73
85
51
91
65
80
76
71
88
122
96
LIQUID
ICNIC MAKE PER
IMBAL. PASS
i M.MOL/L
3.6
4.7
2.0
18.4
-8.2
6.8
7.9
7.9
8.4
5.9
6.5
6.9
3.5
6.5
17.8
11.2
0.0
3.2
-0.3
1.3
3.1
2.8
-7.S
-2.4
-1.6
-5.2
-4.0
-4.5
-9.0
-3.6
3.0
-1.2
2.7
-8.9
-1.5
7.5
7.1
7.6
7.5
7.8
7.5
6.6
7.0
8.0
6.8
9.2
8.5
7.7
7.9
7.0
6.3
7.1
6.1
7.5
8.4
6.8
6.0
7.3
a. 3
8.9
9.4
8.8
9.3
9.2
8.9
9.7
8.6
8.7
6. 8
9.9
9.7
5.3
9.4
8.8
9.4
9.5
10.0
8.9
9.0
8.5
9.1
9.5
8.1
8.4
-------
PAGE
a
RUN
NUMPES CATE
626-1A 07/18/75
' 7/18/75
C7/18/75
r7/19/75
07/19/75
07/19/75
~7/20/75
P7/20 /75
C7/21/75
07/21/75
r7/?2/75
"7/23/75
C7/23/75
07/21/75
r. 7/24/75
^7/24/75
r.7/25/75
07/25/75
C7/25/75
t'7/26/75
T7/26/75
^7/26/75
07/27/75
'7/27/75
07/27/75
"7/28/75
07/28/75
07/29/75
07/29/75
T7/3G/75
P7/30/75
07/31/75
C7/31/75
07/31/75
08/01/75
OW/C1/75
" P/C2/75
OS/02/75
CS/02/75
Oft/02/75
OR/03/75
OP/03/75
0!/07/75
£H AT
SCRUBBED
TIMF INLET
0700
1500
2300
0700
1500
2300
1500
2300
1500
2300
0500
1700
2300
0500
1500
2300
0700
1500
2300
0700
1502
2300
0700
150C
2300
1500
2300
0700
1500
1500
2300
1502
2300
23C2
1500
2313
0700
1500
2300
2302
0700
1500
23 "0
0700
1500
230C
1500
230C
1500
2ntOO
8.05
8.10
1.15
7.95
«.15
f .15
8.05
7.90
ft. 10
7.75
7.85
7.95
8.00
8.25
8.15
8.00
7.90
8.00
7.95
8.35
7.95
o.2C
7.80
8.10
8.25
7.75
7.25
8.00
7.95
8.15
*.05
7.85
7.95
7.90
8.25
P. 05
8.05
7.90
7.70
T.95
7.90
7.80
7.10
7.30
fi.10
8.05
8.25
CA + +
PPM
2150
2640
1965
2630
2640
2&«9
2555
267S
2673
2<*75
2750
2513
?525
2605
26»0
2261
?540
2595
2345
2525
2950
26°5
2<»70
3879
3570
3285
41 19
3315
3919
3300
3479
4000
3445
3: '& 5
3940
2934
2989
3186
LIU
M6 + +
PPW
201
?t4
212
238
241
2»B
255
251
258
270
260
216
217
231
264
224
191
165
189
18?
23H
193
211
?21
215
221
2fi5
243
246
229
253
264
255
246
248
ino
99
51
U 1 U « N A
NA +
PPM
50
51
50
43
49
55
48
56
119
5."
110
110
•52
110
54
101
56
53
55
53
56
61
65
69
69
66
75
74
78
81
82
21
86
81
78
74
74
S3
L TSt ?> C
K*
PPM
114
130
117
119
119
125
ioe
128
250
130
250
250
48
250
123
250
IIP
124
115
122
131
139
142
132
132
135
138
133
142
145
147
147
158
159
156
132
140
148
I £(^r< u K
S03 —
PPM
200
200
176
312
1P4
216
128
46
32
=>&
48
24
48
32
PO
40
45
16
72
40
32
72
104
112
4C
16
32
88
112
24
88
16
32
24
56
16
24
24
DLK I nIL!
S04 —
PPM
933
682
707
1296
1278
1249
1382
1411
1316
1374
1603
1411
1315
1633
1297
1210
2072
1888
951
1268
1878
1529
1425
1443
1263
1477
1458
1343
1316
1456
1312
1533
1615
1526
1094
1057
1199
1094
CL-
PPM
4219
4290
4041
4360
4644
4396
4047
4432
4574
4503
4609
4325
4184
4134
3936
4006
4224
4068
36S7
4113
4290
4222
4892
5070
5105
5779
6062
5672
6275
6346
6417
6452
6523
6204
6311
4716
4680
4963
TOTAL SULFATE
IOMS SAT. AT
PPK 50 C
7867
8257
7268
9003
9155
8978
8523
9001
9222
9266
9630
8849
8389
8995
8434
8092
9246
8909
7414
8303
9575
8911
9809
10926
10394
109B1
12149
10868
12088
11581
11778
12483
12114
11507
11883
9120
9205
9549
73
54
54
101
100
98
106
110
102
108
124
110
103
126
101
93
159
149
76
101
147
122
115
122
106
121
123
110
111
119
108
132
131
123
93
87
103
97
LIQUID
IONIC MAKE PER
IMBAL. PASS
X M.MOL/L
-11.3
11. fl
-10.3
-1.2
-3.5
3.0
4.7
2.7
5.4
8.5
3.1
1.5
0.5
5.5
13.0
2.0
-10.5
-*.o
8.9
2.0
6.8
2.5
1.0
19.4
15.3
-3.0
13.7
1.0
7.0
-10.0
-4.3
4.7
-8.8
-8.6
9.9
7.9
4.0
4.2
8.9
8.7
8.8
8.9
8.2
6.4
7.4
7.7
8.4
8.6
8.6
8.7
9.8
6.3
5.1
7.5
8.7
9.2
8.4
9.0
9.2
9.6
6.3
5.4
4.6
7.2
7.5
8.0
7.6
8.5
7.7
6.7
5.8
5.5
6.8
7.8
4.9
5.1
6.1
9.3
9.8
5.7
5.8
5.8
5.3
-------
PAGE
I
Ul
BUN
627-1A 08/08/75
08/08/75
Oft/08/75
OS/09/75
OH/09/75
"'P./C9/75
rs/io/75
rr./10/7^
CH/10/75
C8/11/75
rg/11 /75
rf /12/75
"8/12/75
08/13/75
Oft/13/75
6?3-lA 06/16/75
"3/16/75
OB/ 17/75
OP/ 17/75
T8/17/75
P8/1B/75
r>8/18/75
OS/18/75
OS/19/75
08/19/75
08/19/75
08/20/75
''S/20/75
r 8/23/75
0^/21/75
"8/21/75
r'B/22/75
"fi/22/75
f 3/2^/75
08/23/75
T8/23/75
G8/24/75
rp/?4/75
"R/24/75
nR/25/75
08/25/75
Hg/26/75
C8/26/75
DS/26/75
C3/27/75
f/27/75
Cfi/27/75
OR/28/75
OP/28/75
T8/29/75
PH AT
SCRUBaER
0700
1215
2300
0700
1500
2300
0700
1EDD
2300
1500
23PQ
1500
23CO
0700
1100
1500
23CO
0700
1500
2300
0700
1500
2300
0700
1500
2300
0700
1500
2300
1500
2300
070C
2300
0700
1500
230C
0700
1500
2300
0700
2300
0700
1500
23nO
0700
1500
23 00
150C
2300
070C
fi.15
7.35
H.25
P. 15
8.05
8. 1C
8.15
8.20
8.10
8.00
8.10
7.75
8.05
7.80
8.00
6.95
7.10
6.90
6.30
6.65
7.85
7.65
7.15
7.50
7.35
7.30
7.95
8.10
7.80
7.75
7.80
7.65
7.80
7.75
7.75
8.05
7.90
8.25
7. 70
7.80
7.60
CA + *
r-pff
3051
3660
2468
2480
21&4
2121
2065
?140
2190
2076
2056
26;5
3515
2445
2761
2255
3859
2070
2250
25?.0
2100
25R9
3115
2390
2435
2310
?060
2125
2215
2000
2075
2010
1940
LI'J
PPI«
54
59
75
77
«3
8"
F.9
103
110
102
121
122
127
115
157
135
171
170
173
203
177
241
252
268
254
296
289
211
305
301
312
312
308
UIU «U«fl
MA*
74
7L>
7B
63
74
71
7?
Th
80
138
117
55
73
70
72
72
78
69
&7
74
72
75
68
70
68
68
72
34
66
62
7?
63
57
L TM.5 fl
Kt
PFH
175
19
160
31
188
164
191
183
195
360
391
155
16S
175
163
164
184
159
174
159
157
163
154
153
143
147
144
130
149
155
156
125
118
1 i L h L L'
SOI —
PPK
46
72
72
96
8
2C8
56
104
24
48
40
56
1D4
56
72
328
80
80
104
72
24
24
8
24
16
96
t-8
40
112
192
&
112
72
S04 —
1007
610
403
318
451
181
557
887
718
537
1758
1644
1395
1420
1589
1215
1451
1236
1361
1189
1486
1672
1086
1097
1856
1031
771
1360
1341
994
1404
1444
1736
. i
CL-
PPM
5318
5140
4609
4325
4290
3545
3935
3368
3722
351C
3446
3793
3829
3758
3616
3758
3793
3793
4077
4254
3970
4201
3864
4254
3900
4006
4006
3935
3510
1455
3580
3510
3332
TOTAL SULFATE
IONS SAT. AT
PPM 50 C
9730
9630
7885
7590
7258
6381
6986
6861
7039
6771
7962
8480
8202
8083
8433
792;
8616
757?
8206
8481
7986
8965
7547
8256
8672
7954
7430
7835
7698
5159
7607
7576
7563
89
56
35
45
39
16
47
74
60
45
136
135
114
116
129
98
118
96
106
94
114
128
81
83
138
77
57
103
97
71
99
101
118
tiauia
IONIC t«
IWBAL.
X H
-4.6
16.5
-2.1
-1.2
-6.3
9.5
-3.8
5.8
4.9
12.4
-4.3
4.2
2.3
0.8
13.5
-6.5
15.6
-8.3
-9.0
2.5
-13.5
1.6
1.0
3.3
0.0
6-.S
1.6
-9.4
8.9
49.3
4.3
0.0
-3.3
AK^ PE"
PASS
.POL/L
5.4
9.7
11.6
9.3
9.2
6.8
8.5
7.8
8.7
4.1
-------
PAGE;
d
i
CH AT
<*lt\ ^CRUBDE1?
NUHprR niTE TIMf INLET
6P8-1A OS/P9/75
OP/30/75
Oft/30/75
O.F,/ 30/75
08/31/75
•"•P/71/75
C9/01/75
09/02/75
"9/02/75
09/02/75
'"9/03/75
09/04/76
V9/05/75
^9/05/75
r9/C6/75
"9/06/75
"5/06/75
09/07/75
"9/07/75
C9/07/75
09/08/75
"9/08/75
C9/08/75
f 9/09/75
09/09/75
"9/10/75
"9/1C/75
C9/10/75
"9/11/75
09/11/75
"9/12/75
r,Q/l?/75
09/13/75
05/1 * /75
r9/l*,/75
09/14/75
09/14/75
09/14/75
C9/lr./75
09/15/75
^9/16/75
"9/16/75
C9/16/75
09/16/75
09/17/75
"9/17/75
"9/17/75
6?8-lE 09/18/75
C9/18/75
"9/19/75
2310
0700
1500
2300
0700
1500
2300
0730
1500
2300
0700
2300
0700
2300
0700
1500
230,0
0700
1500
2300
070C
150 C
2300
0700
23C&
0700
15CC
2300
1500
2300
07-V)
23 ?0
0700
150C
2300
0700
1500
2300
1500
23C3
0700
12C*
1500
2300
07 OC
150C
23CO
15C3
23 OC
07CC
7.75
7.85
7.15
f-.eo
6.70
6.70
7.25
7.65
7.85
7.85
7.15
7.95
7.65
7.45
7.70
7.95
7.30
7.45
7.75
7.45
7.95
7.95
7. in
P. 55
7.75
7.95
7.15
7.75
7.60
7.95
7.90
7.95
7.95
7.90
S.OO
7.75
7.50
P .30
7.95
7.70
7.75
6.45
6. =10
CA + *
PPM
17?5
1895
1700
?150
1870
1830
2000
1775
16«0
1935
1520
1 '•? 3 0
1115
1610
1595
llfi?.
I7f 0
1475
1250
1405
22 S5
1805
1^15
2255
1695
1375
1855
1510
1650
1755
1730
2105
LiUUiU SNA
M G + * N A +
286
327
289
349
331
312
364
3U9
314
31ft
281
313
319
2t9
337
272
341
292
329
304
253
312
311
302
330
274
364
273
249
311
211
315
59
68
53
66
65
61
67
66
64
64
60
56
52
5S
56
54
52
53
51
49
65
53
5S
57
56
54
57
53
53
51
5D
63
L lit.^ «
K*
PPM
121
155
113
148
154
140
154
154
160
150
158
132
120
136
133
130
129
122
129
125
118
127
122
115
132
123
148
114
130
115
124
126
1 iCKUf
SC3--
PPM
168
24
104
32
16
24
56
304
48
48
80
72
16
88
4
168
36
56
16
72
48
56
48
72
48
h4
48
60
136
64
48
16
RC.R i«U!
$04 —
PPM
1333
1662
1666
1646
1661
1645
1624
1488
1527
2073
1317
2189
2284
1634
1347
8h3
1166
886
749
934
2330
1306
1513
2350
1192
813
1069
1265
1680
1352
1948
1671
-_ , ______
CL-
PPM
3191!
3332
3403
3403
3297
3190
3261
3053
2943
2871
3084
3049
1595
3155
2875
2871
2694
2694
2694
2588
3084
3261
3084
3049
2836
3013
2942
2907
3049
3120
3U13
3442
TOTAL SULFATE
IONS SAT. AT
PPM 50 C
6882
7463
7328
7794
7394
7202
7526
7149
6736
7509
6500
7741
5501
6947
6347
5563
5778
5578
5218
5477
8181
6920
7051
8200
6289
5716
6483
6202
6947
6768
7124
773«
91
112
111
114
111
111
109
100
100
139
87
145
122
109
37
56
71
59
46
60
167
89
104
164
79
54
72
84
114
91
135
117
LIQUID
IONIC MAKE PER
IMBAL. PASS
% f.MOL/L
-5.8
-0.6
-17.1
8.1
-0.5
-1.3
6.9
-3.2
0.5
4.9
-10.2
-4.3
-6.6
-15.6
3.5
-18.8
0.3
7.0
3.1
6.2
2.8
0.6
5.6
4.3
9.8
-7.1
17.3
-7.1
-14.7
0.5
-16.2
3.4
-------
PAGE
O
I
<»u\
NUfpf CATE
628-1* 09/19/75
rg/20/75
"9/20/75
"0/20/75
OS/21/75
"9/21/75
09/21/75
?9/?2/75
C9/22/75
P9/23/75
"9/2?/75
09/23/75
^3/24/75
n»
123
125
126
125
121
134
122
111
125
14C
124
109
125
lie
130
134
131
132
131
106
133
12S
122
120
125
12B
125
125
115
113
116
8
56
24
72
72
40
48
56
as
72
8
16
64
96
72
40
40
3?
32
24
32
24
48
48
0
16
40
32
24
56
24
atK inn-i
S04--
RDM
1075
973
1200
938
1444
1561
1217
1181
1613
1707
1619
1210
1133
908
1078
1222
1940
1652
1488
1260
1094
1072
944
965
1116
1076
1530
1570
954
978
1005
: i -----.
CL-
PPM
3439
3403
3350
3403
3297
3226
3226
3226
336H
3474
3442
3616
3794
3722
3829
3970
5070
4609
4609
4502
4892
4892
4750
4715
4715
4750
5548
5530
4857
4431
4857
TOTAL SULFATE
IONS SAT. AT
PPM 50 C
6847
6663
6954
6692
7219
7201
6775
6703
7449
7806
7650
7112
7689
7165
8078
7990
10260
9616
9363
8997
9586
9663
8724
8688
9017
9106
11050
11081
8747
8527
8974
74
68
84
65
100
107
86
-------
PAGE
O
CO
N'jyPER TATE
62fl-IR 10/P5/75
10/05/75
10/06/75
10/06/75
1C/06/75
1P/P6/75
10/06/75
10/06/75
10/06/75
1P/P7/75
10/07/75
701-1A 10/P9/75
10/09/75
10/09/75
10/10/75
1G/10/75
10/10/75
10/10/75
10/10/75
10/11/75
10/11/75
in/11/75
11/11/75
10/11/75
10/11/75
10/12/75
10/12/75
10/12/75
10/12/75
10/12/75
10/12/75
7C2-1A 10/14/75
IP/14/75
IP/15/75
10/15/75
10/15/75
10/15/75
IP/15/75
ir/15/75
10/15/75
1C/16/75
10/16/75
10/16/75
10/16/75
1-/16/75
10/17/75
703-ia 10/19/75
10/19/75
K/19/75
lr/19/75
FH AT
^CRUBBCR
TIT INLET
23PO
2301
0709
1500
1501
23?0
2306
23P8
2311
070C
0701
23PD
2301
2306
0700
0706
23^0
2301
2308
0700
0701
1500
1501
2300
2301
0700
0701
1500
1501
1511
2311
2300
2301
^709
1500
1501
2300
2301
2311
2312
1500
1501
1508
2370
23P1
0500
1100
1500
1°OC
23^0
R.OO
8.00
7.75
7.75
7.85
7.35
7.35
5.70
5.70
5.95
5.85
5.85
5.80
5.80
5.85
5.85
5.90
5.90
5.85
5.85
5.90
5.90
5.60
5.60
5.75
5.95
5.95
5.80
5.80
5.85
5.85
5.80
5.30
5.10
5.25
5.10
CA* +
2270
2125
2460
2445
2200
2210
2'>40
2604
2230
2283
2579
25C-4
2135
2150
19R5
1940
1710
1630
2015
2P35
2110
2080
2025
3044
Liuuiu »rj«
M6+* NA*
PPM PPM
292
279
361
3b5
330
365
371
365
3 '16
392
465
457
448
451
436
454
447
484
619
634
469
451
600
841
64
59
66
65
63
64
64
68
73
70
67
67
74
75
70
63
54
55
54
54
53
54
82
57
L ' ati »
K*
PPM
119
117
127
131
122
118
115
99
110
108
109
108
115
116
113
107
104
105
74
76
7b
75
106
127
1 iLKUB
S03--
PPM
144
144
40
56
BO
16
32
24
64
56
72
64
16
fc
16
32
80
88
32
32
88
60
32
192
BL* iNl_>
SCJ4 —
PPM
850
850
833
793
835
828
798
1419
585
596
467
455
329
348
370
371
278
296
451
441
490
520
4Q3
1928
CL-
PPM
4538
4753
4786
4786
4006
4431
4467
4821
4892
4857
4928
4928
4921
4921
5034
4999
4360
4396
4502
4487
5140
5176
5105
5247
TOTAL SULFATE
IONS SAT. AT
PPM 50 C
8277
8324
8673
8631
7636
8032
8087
9400
8350
8359
8687
8643
8038
8069
8024
7971
7033
7054
7747
7739
8426
8436
8353
11436
64
63
62
59
61
59
57
104
42
43
34
33
23
24
25
25
18
18
28
27
33
35
25
121
LIQUID
IONIC HAKE PER
IM8AL. PASS
X M.MOL/L
-4.3
-15.4
3.3
2.9
7.3
2.4
3.1
-0.4
-1.3
0.7
12.8
12.4
2.3
2.9
-6.5
-6.9
-2.9
-4.9
11.9
13.9
-6.3
-9.4
2.2
14.9
9.8
9.8
7.5
7.5
7.5
9.0
9.0
8.4
8.4
9.0
9.0
9.4
9.4
9.2
9.2
9.4
9.4
9.2
9.2
11.7
9.7
9.7
9.5
9.5
9.4
9.4
10.1
6.0
5.5
6.8
7.5
-------
PAGE
o
I
sO
"UN
NUMCf-R DATE
703-lft 10/20/75
10/20/75
10/21/75
10/21/75
10/21/75
10/22/75
10/22/75
10/22/75
10/22/75
10/22/75
10/23/75
1C/73/75
10/23/75
10/23/75
10/23/75
10/23/75
10/24/75
10/24/75
10/24/75
10/24/75
10/24/75
10/24/75
10/25/75
10/25/75
10/25/75
10/25/75
10/25/75
10/25/75
IP/26/75
10/26/75
1C/26/75
10/26/75
10/26/75
10/26/75
10/27/75
10/27/75
10/27/75
10/27/75
10/27/75
10/27/75
10/28/75
10/26/75
10/28/75
10/28/75
10/28/75
in/28/75
10/29/75
10/29/75
10/29/75
10/29/75
LIQUID
*=H AT Cft»+ MG»+ NA» K* S03-- S04-- CL- TOTAL SULFATE IONIC MAKE PER
SCRUBBER IONS SAT. AT IMBAL. PASS
TI"*E INLET PP« PPM PPM PPM PPM PP1 PPM PP* 50 C * M.MOL/L
03PO
1500
1500
1900
2300
0300
Oft DO
1500
1900
2300
0300
0700
1100
15CO
1900
23CO
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0302
0700
1100
1500
1900
2300
0300
0700
11CO
1500
1900
2300
0300
0700
1100
1500
1900
23CO
0300
G700
1130
1500
5.10
??30 623 84 106 216 2084 5353 11296 137 -0.5
5.30 285<» 819 95 170 96 1667 570S 11414 104 9.3
5.30
5.10
5.25
5.20
b.05
5.25
5.20
5.15
5.20
5.20
5.25 2665 695 45 96 112 1532 5353 10498 98 4.6
5.15
5.20
5.35
5.15
5.15
5.30 2BP9 454 82 93 112 1623 5743 10996 117 -5.9
5.20
5.15
5.32 ?739 536 77 90 104 1574 6027 11147 108 -X0.2
5.19
5.12 2920 535 93 106 320 1450 5991 11415 102 -5.4
5.16
5.30
5.30
5.25 295C 539 90 110 £.4 1459 6736 11948 103 -11.9
5.28
5.21 SOS1* 544 100 113 120 1383 6878 12177 98 -10.9
5.24
5.30
5.32
5.32 3419 673 104 113 16 1346 6771 12442 95 6.0
5.22
5.23 3100 600 104 109 f.4 988 6594 11559 70 1.5
5.35
5.25
5.13
5.31 3149 697 113 121 48 1030 6700 11858 71 4.9
5.20
5.12 29*15 623 117 122 104 1017 6523 11501 71 0.6
5.25
5.03
5.07
5.13 3609 614 105 128 56 1542 6633 12687 112 7.5
5.12
5.27
7.4
4.5
5.8
6.0
7.9
8.1
7.4
7.0
7.0
6.9
7.6
6.c<
5.7
5.0
5.4
5.8
5.4
5.2
5.2
5.4
5.7
6.3
6.2
5.5
4.8
4.7
6.2
6.8
6.9
6.7
6.8
7.3
8.5
8.4
8.6
7.6
7.3
7.0
6.6
6.5
8.3
7.3
6.5
6.3
5.4
6.0
6.7
6.8
7.4
-------
PAGE
O
I
PL)',
NUwntR DATE:
703-18 10/29/75
10/29/75
10/30/75
10/50/75
10/30/75
10/30/75
10/30/75
10/30/75
10/31/75
10/31/75
11/01/75
11/01/75
11/01/75
11/01/75
11/01/75
704-1* 11/03/75
11/04/75
11/04/75
11/04/75
11/04/75
11/04/75
11/04/75
11/04/75
11/05/75
11/05/75
11/05/75
11/05/75
11/05/75
11/05/75
11/06/75
11/06/75
11/06/75
11/C6/75
11/06/75
ll/Ofe/?1)
11/06/75
11/07/75
705-14 11/07/75
11/07/75
11/08/75
11/08/75
11/08/75
11/08/75
ll/OB/75
11/03/75
11/09/75
11/09/75
11/09/75
11/09/75
11/09/75
PH *T
SCRimE"
lift INLET
1900
2300
030T
0700
1100
15 D1?
1900
2 SCO
0700
1500
C300
0700
1100
1500
1900
2300
0300
0700
1100
15CQ
1900
2300
2337
0300
0700
1100
1500
1900
2330
0300
0700
HOG
1500
1533
1900
2300
0500
1900
2300
0300
0700
HOC
1500
1900
2300
0300
C71P
1100
15CD
1900
5.13
5.25
5.07
5.17
5.32
5.15
5.24
5.24
5.10
5.18
5.32
5.08
5.13
5.55
5.55
5.58
5.60
5.66
5.69
5.82
5.84
5.77
5.86
5.94
5.89
5.74
5.95
5.99
5.91
5.86
5.79
5.65
5.81
5.39
5.42
5.46
5.67
5.71
5.79
=..70
5.71
5.71
5.64
5.63
5.78
5.75
CA + +
Ppiw
2869
3314
3349
3135
2970
3039
3310
3395
3215
"410
1935
20?5
1860
5185
1915
2165
16P5
LIU
HG* +
PP^
608
666
429
662
669
697
698
759
617
737
1053
773
527
4T1
623
497
551
U1U a "is
N» +
PPM
100
92
94
102
97
103
105
114
113
102
108
91
97
S3
81
85
7-1
L T ^C.0 «
K*
PPM
118
117
141
125
115
127
125
127
121
116
112
112
118
103
107
101
105
i i^nur;
S07--
PPM
104
216
48
64
56
164
88
112
104
72
160
104
56
96
96
48
72
D L H 1 ft 1_ 1
S04 —
PPM
1146
1133
1965
1753
1407
1258
1535
1375
479
298
240
422
787
1085
972
882
826
CL-
PPM
5850
6062
6559
6452
6552
6417
6736
6594
6381
5850
5389
5070
4928
4538
4077
4077
4041
TOTAL SULFATE
IONS SAT. AT
PPH 50 C
10795
11600
12585
12293
11866
11825
12597
12476
11030
9585
8997
8597
8393
8581
7871
7855
7359
79
er
147
119
95
85
106
94
35
19
12
24
49
72
58
59
49
LIQUID
IONIC MAKE PE"
IHBAL. PASS
X M.MOL/L
4.5
12.0
-8.1
-0.7
-2.4
2.3
2.7
9.4
12.2
8.1
15.6
10.0
-9.6
1.7
10.1
13.3
1.9
6.9
7.0
7.0
7.5
7.7
6.1
6.5
6.6
8.2
7.5
7.0
6.3
5.6
8.1
7.8
8.6
9'. 2
9.3
9.5
10.7
13.1
12.8
12.0
12.3
11.6
12.6
14.2
13.0
12.5
12.1
9.9
8.7
9.7
7.5
7.7
8.1
6.8
9.0
8.6
9.4
8.5
8.5
9.2
9.D
8.S
8.8
-------
PAGE
SUN
NUKRER GATE
705-1* 11/09/75
11/10/75
11/10/75
11/10/75
11/10/75
11/10/75
11/10/75
11/11/75
11/11/75
11/11/75
11/11/75
11/11/75
11/11/75
11/12/75
11/12/75
11/12/75
11/12/75
11/12/75
11/12/75
11/15/75
11/13/75
706-1A 11/13/75
11/14/75
11/14/75
11/14/75
11/14/75
11/14/75
11/14/75
11/15/75
11/15/75
11/15/75
11/15/75
11/15 '75
H/l'5/75
11/15/75
11/15/75
11/16/75
11/16/75
11/16/75
11/16/75
11/16/75
11/16/75
11/16/75
11/17/75
11/17/75
11/17/75
11/17/75
11/17/75
11/17/75
11/18/75
Ll'JUIU O^ALTbt a Al &LKUK?tK 1N1-I
PH AT CA» + M6++ NA+ K» S03 — S04--
SCRUBBER
TIKE INLET PPM PPM PPM PPI"! FP*1 PPM
2300
0300
0700
1100
1500
1900
2300
03PO
0700
1100
1500
1900
2300
0300
0700
1100
15 on
1500
2300
0300
0700
2300
0300
076-0
1100
1500
1900
2300
0300
0700
0707
0710
1100
1500
1
-------
PAGE 10
d
RUf*.
NUWPf DATE
706-1A 11/18/75
11/18/75
11/18/75
11/18/75
11/18/75
11/19/75
11/19/75
11/19/75
11/19/75
11/19/75
11/19/75
11/19/75
11/19/75
11/19/75
11/20/75
11/20/75
11/20/75
11/20/75
11/20/75
11/20/75
11/20/75
11/20/75
11/20/75
11/21/75
11/21/75
11/21/75
11/21/75
707-1A 11/21/75
11/21/75
11/22/75
11/22/75
11/22/75
11/22/75
11/22/75
11/22/75
11/25/75
11/27/75
11/23/75
11/23/75
11/23/75
11/23/75
11/24/75
11/24/75
11/24/75
11/24/75
11/24/75
11/24/75
11/25/75
11/25/75
11/25/75
LI5UI1J ANALTbtb PI at-NUCDtK iFMUtl----'
LIQUID
PH AT CA + + MG++ NA* ** S03-- SO*-- CL- TOTAL SULFATE IONIC MAKE P£°
SCRUBBER IONS SAT. AT I1BAL. PASS
TI!^ INLET PPM PPM PPM PPM PPM PPM PPM PPM 50 C % M.MOL/L
0700
1100
I5or
1900
2300
030C
0700
1100
1500
1900
2300
2307
2310
2311
0300
0700
1100
1500
1510
1900
2300
2307
2310
0300
0700
0707
0710
1900
2300
0300
0700
HOC
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
23CO
0300
0700
1100
5.30 1725 643 67 108 272 2472 3758 9045
5.40
5.30 1710 699 57 121 320 2622 3580 9109
5.15
5.20
5.20
5.25 1465 704 69 108 48 2363 3651 8408
5.25
5.20 1885 757 63 106 272 2572 3829 9484
5.25
5.25
5.10
5.15 1^65 732 79 119 72 2745 3616 9328
5.25
5.10 22°5 752 84 115 200 2290 3829 9565
5.20
5.10
5.10
5.15 2390 774 91 117 224 1786 3864 9246
b.50
5.55
5.60
5.60 2015 821 74 121 184 1533 4467 9215
5.65
5.75 1635 777 R7 115 264 791 4644 8313
5.75
5.75
5.80
5.80 2010 919 77 139 200 836 4538 8719
5.70
5.80 1?70 882 83 113 88 840 4502 7873
5.80
5.75
5.80
5.85 1385 922 75 135 50 728 4495 7790
5.85
5. 75 1P70 874 73 104 168 421 4077 6737
5.80
5.80
5.80
5.75 1425 1011 71 106 136 882 4041 7672
5.70
130 -13.5 6.4
6.4
132 -10.2 5.7
5.9
6.9
7.2
111 -12.1 8.3
7.9
133 -4.0 6.2
6.3
6.0
5.Q
145 2.3 5.?
5.7
131 12.2 5.6
5.9
6.8
7.6
105 20.1 8.4
9."
10.7
10.5
83 6.8 11.0
11.4
41 -1.2 11.5
11.1
10.4
10.4
44 17.7 9.9
10.2
37 0.5 10.3
11,4
12.3
12.3
32 5.6 17.0
13.0
17 -0.7 12.8
11.7
10.9
10.9
37 15.2 9.8
8.8
-------
O
i
t—i
OJ
PUN
NUMQER DATE
707-1A 11/25/75
11/25/1*
11/25/75
11/26/75
11/26/75
11/26/75
708-1A 11/26/75
11/26/75
11/26/75
11/27/75
11/27/75
11/27/75
11/27/75
11/27/75
11/27/75
11/28/75
11/28/75
11/28/75
11/28/75
11/28/75
11/26/75
11/29/75
11/29/75
11/29/75
11/29/75
11/29/75
11/29/75
11/30/75
11/30/75
11/10/75
11/30/75
11/30/75
11/30/75
12/01/75
12/01/75
12/01/75
12/01/75
12/01/75
12/01/75
12/01/75
12/02/75
12/02/75
709-1A 12/06/75
12/06/75
12/07/75
12/07/75
12/07/75
12/07/75
12/07/75
12/07/75
-LJ'JUIU AN«LT5,t_5 Al SINU!' B LK i HI- t. 1 -----------
LIQUID
PH AT CA++ MG«* NA+ K+ S03-- SO*-- CL- TOTAL SULFATE IONIC MAKE Pt°
SCRURBER IONS SAT. AT IHBAL. PASS
TIME INLET PPM PPM PPM PPM PPM PPM PPM PPM 50 C % M.MOL/L
1500
1900
2300
030D
0700
1100
1500
1900
2300
0300
0700
1100
1500
190C
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
0701
1100
1500
1900
2300
0300
0700
19CO
2300
0300
C700
11CO
1500
1900
2300
5.70 1480 1082 82 120 68 1*51 4467 877i
5.60
5.70
5.70
5.80 1790 914 53 127 96 1026 4467 8473
5.70
5.85 1305 734 103 120 64 913 40T7 7366
5.96
5.80
5.80
5.B5 1850 924 88 129 88 1131 4538 8748
5.80
5.70 1755 85U 80 110 112 1480 4680 9067
5.70
5.55
5.80
5.70 2140 529 82 118 32 1330 4824 9055
5.65
5.65 1990 795 S3 105 120 1386 5347 9826
5.60
5.60
5.60
5.55 2090 815 90 111 112 1568 4831 9617
5.60
5.60 1635 819 81 114 104 1381 4750 8884
5.65
5.60
5.45
5.50 1675 891 79 111 88 1240 4715 8799
5.60
5.50 15PO 879 79 114 120 1061 4609 8442
5.55
5.65
5.60
5.60 1220 829 80 103 240 810 4006 7288
5.70
5.90
5.65 1248 881 70 112 112 695 4006 7124
5.65
5.70
5.70
5.75
5.46
5.66
5. SO
5.71 1452 875 74 112 40 1288 4254 8095
5.69
5.65 2045 737 79 126 64 1246 4538 8835
5.70
5.92
59 6.5 8.2
8.7
8.9
9.1
51 12.0 S.4
9.5
41 1.1 9.6
9.0
9.0
9.2
57 12.4 8.8
8. 6
74 -1.1 7.3
7.0
9.1
10.0
85 -4.9 10.0
8.7
75 -6.8 7.6
7.2
7.3
7.6
86 3.6 7.6
7.2
68 -6.4 7.3
7.3
8.5
8.8
60 1.3 9.4
9.1
50 1.5 9.4
10.0
10.1
11.5
35 -0.5 11.3
11.3
11.0
29 7.4 10.1
10.2
10.0
9.5
9.5
8.6
9.4
9.8
58 1.8 9.7
9.5
71 8.1 9.9
11.2
11.8
-------
PAGE 12
RIA
NUHPER DATE
709-1A 12/08/75
12/08/75
12/08/75
12/08/75
12/08/75
12/08/75
12/09/75
12/09/75
12/09/75
12/09/75
12/09/75
12/09/75
12/10/75
12/10/75
12/10/75
12/10/75
12/10/75
12/10/75
12/11/75
12/11/75
12/11/75
12/11/75
12/11/75
12/11/75
12/11/75
12/11/75
12/11/75
12/12/75
12/12/75
12/l?/75
12/12/75
710-10 12/12/75
12/12/75
12/l?/75
12/12/75
12/13/75
12/13/75
12/13/75
12/13/75
12/13/75
12/13/75
12/13/75
12/13/75
12/13/75
12/14/75
12/14/75
12/14/75
12/14/75
12/14/75
12/14/75
LIQUID
PH AT CAt + MG»+ NA* * + SC3 — S04 — CL- TOTAL SULFATE IONIC MAKE PE*
SCRUBBER IONS SAT. AT IMBAL. PASS
TIM*" INLET PP» PPM PPM PPM PPM PPM PPM PPM 50 C % M.MOL/L
03CO
0700
1100
1500
1900
2300
0300
0700
1100
IfrOO
1900
2300
0300
0700
1100
1500
1900
2300
0300
070.0
1100
1500
1537
1900
2300
2301
2307
0300
0700
0707
1600
1500
1601
1900
2300
0303
070D
1100
1500
1501
1502
1900
2300
2301
0300
07CO
1100
1500
1501
1902
5.85
5.84 1045 759 7? 109 24 530 4006 6545
5.85
5.87 1285 837 71 116 80 529 3651 6569
5.90
5.99
5.90
5.86 967 833 66 101 72 980 3439 645S
5.91
5.95 1185 763 70 109 16 1326 3404 6873
5.92
5.95
5.90
5.84 R42 77fi 64 117 104 739 3156 5800
5.93
5.97 693 508 69 109 80 576 3368 5403
5.98
6.01
6.06
5.99 -565 768 60 102 22 634 3261 5412
6.00
5.94 607 791 74 119 112 576 3155 5434
5.91
6.03
6.03
5.99
5.86 968 785 75 10S 64 978 3651 6629
5.90 1048
1048 949 3? 115 184 1146 3126 6600
5.90
5.86
5.86
5.96
5.94 ^24 867 7b 11? 96 434 3474 5990
1022 803 69 120 40 652 3900 6606
6.08
6.04
6.07
6.06
6.03 812 ft37 73 115 120 448 3687 6092
6.03
750 H17 71 119 80 b77 3332 5746
12.0
22 -3.4 12.4
13.2
24 16.6 12.5
12.2
11.5
11.2
36 2.5 9.8
9.6
57 2.9 9.2
9.4
10.8
11.1
26 4.3 10.3
10.6
23 -32.6 10.3
10.3
10.5
10.5
17 -9.4 11.9
11.3
16 -2.1 10.6
10.6
9.9
10.0
9.?
37 -5.1 8.8
10.?
41 13.4
10. •»
10.6
10.8
11.4
16 11.6 11. =1
11.4
26 -1.2
10.6
10.7
10.9
10.7
11.0
10.?
15 -0.7 11.5
10.1
19 2.5 10.4
10.4
9.5
-------
PACT 13
RUN
MUMPER DATE
710-1A 12/14/75
12/15/75
12/15/75
12/15/75
12/15/75
12/15/75
12/15/75
12/15/75
12/15/75
12/16/75
12/16/75
12/16/75
12/16/75
12/16/75
12/16/75
12/16/75
12/16/75
12/16/75
12/17/75
12/17/75
12/17/75
12/17/75
12/17/75
12/17/75
12/17/75
12/17/75
12/18/75
12/18/75
12/18/75
12/18/75
12/13/75
12/18/75
12/15/75
12/15/75
12/19/75
12/19/75
12/15/75
12/19/75
12/15/75
12/19/75
12/20/75
12/20/75
12/20/75
12/2C/75
12/20/75
12/20/75
12/20/75
12/21/75
12/21/75
12/21/75
TI!*E
2300
0300
07CO
1100
1500
15C1
1900
2300
2301
03CO
070D
07P1
1100
1500
1501
1900
2 3 0 C
23? 1
03CO
C700
lino
1500
1501
1900
23CO
2301
C2PO
0700
11CO
1500
1900
23CO
0300
0301
0700
C7C1
1100
1500
1900
2300
0300
07CO
07C1
1100
1500
1900
23CC
03"0
0700
0701
--------Li'-J'JlU flNHL.TS.Li «l Sl,nUReC.X I NUt. 1 ------
PH AT CA*+ MG + + NA» K* S03-- S04-- CL-
INLET PP" PPM PPM PPM PPM PPM PPM
^.12
6.05
f.06 1127 841 79 127 t4 752 3651
6.11
6.16 667 797 74 Ufa 72 529 3084
£ .16
6.10
6.14
6.14
6.16
6.15
6.15
6.10
6.19 5»4 761 69 118 64 465 3049
6.16
6.11 624 7S5 7U 109 48 684 3088
6.11
6.11
6.15 504 713 64 117 136 410 3013
6.07
1108 769 73 141 64 558 2942
6.13
5.62
6.03
6.02 745 7&0 69 105 88 8&4 3155
5.92
5.86 1175 842 70 14f. 72 1379 3585
5.86
5.86
5.83
5.49
5.84 1543 415 50 62 112 1229 4219
5.49
5.85
5.93 9SO 809 63 109 32 827 3687
5.91
5.58
5.58
5.86 ?277 1P9 35 150 32 1455 3613
5.86
5.94
5.97 20f,0 791 68 104 48 1461 3120
5.93
5.90
5.92
5.9P 19R4 797 55 106 120 513 3403
5.98
LIQUID
TOTAL SULF4TE IONIC
IONS SAT. AT 1MHAL.
PPM 50 C X
6641 31 9.0
5339 16 5.0
5110 13 0.5
5408 20 -1.0
4957 11 -8.2
5655 24 23.2
5810 28 -1.9
7269 56 2.3
7630 75 -26.3
6512 31 -0.7
7671 118 -3.9
7652 81 31.0
6978 29 35.4
MAKE PEP
PASS
H.*CL/L
9.5
9.4
11.1
10.fi
11.6
11.8
11.3
10.9
11.1
12.1
11.8
11.8
11.4
11.3
11.1
11.0
11.2
11.3
12.0
12.2
11.3
12.4
12.6
11.9
9.9
9.8
9.3
8.5
8.6
7.7
9.?
a.9
9.4
9.5
10.0
10.0
11.0
9.B
10.1
10.6
10.8
10.0
10.1
9.9
10.6
11.0
11.0
11.3
11.3
11.5
-------
PACT 11
°u\
M'J^ER DATE
710-1A 12/21/75
12/21/75
12'21/75
12/21/75
12/21/75
12/21/75
12/22/75
12/22/75
12/22/75
12/22/75
711-1A 15/21/75
12/21/75
12/21/75
12/25/75
12'25/75
12/25/75
12/25/75
12/25/75
12/25/75
12/26/75
12/26/75
12/26/75
12/26/75
12/26/75
12/26/75
12/27/75
12/27/75
12/27/75
12/27/75
12/27/75
12/27/75
12/28/75
12/28/75
12/28/75
12/28/75
12/28/75
12/28/75
12/29/75
12/25/75
12/29/75
12/29/75
12/29/75
12/29/75
12/30/75
12/^0/75
12/'0/75
12/30/75
17/31/75
711-1B 12/50/75
12/30/75
-----LiauIU ANALTM.S Al SLKUtCtK INLtl- ----
LIQUID
PH AT CA + * M6+* %A* K+ SC3 — SOI — CL- TOTAL SULFATE IONIC MAKE PER
SCRUBBER IONS SAT. AT IMBAL. PASS
TIM17 INLET PP" PPM PP1 PPM PPM PPM PPM PPM 50 C X M.MOL/L
1100
1500
1700
190D
2100
2300
0100
03CO
05CO
0700
1500
1900
2300
0300
!)7PO
1100
1500
1900
2300
0300
0700
11CO
1500
1900
23CC
0300
0700
HOC
1500
1900
23CO
0300
0700
nn-n
1500
1900
2300
0300
0700
1100
1500
1900
23 CO
0300
0700
0701
1100
1237
1500
1900
5.81
5.86 ?RO 739 59 110 80 776 3019 5693
5.55
5.61
5. BO
5.83
5.65
5.89
5.83 2251 135 32 117 16 3397 2902 8853
5.65 1778 658 56 102 136 1710 2612 7082
5.68
5.68
5.72
5.73 1772 819 5;J 115 61 1258 3793 7910
5.72
5.81 1035 713 63 105 56 1063 3297 6332
5.75
5.76 1781 10 2309 2783
5.79
5.88 1661 717 59 115 16 1912 2811 7381
5.90
5.99 1600 691 51 90 3? 767 2116 5667
5.96
5.80
5.61
5.60 1915 297 10 117 381 905 2978 6666
5.75
5.58 1780 661 60 85 32 1686 2836 7110
5.17
5.16
5.51
5.57 1510 651 61 87 6C 1730 1396 8595
5.19
5.16 2155 739 71 99 101 1691 1821 9686
5.51
5.63
5.59
5.59 1505 337 39 112 32 2039 2623 6687
5.62
5.66 1530 757 66 10P. 18 976 1396 7881
5.68
5.57 1825 727 61 103 80 1199 1396 8691
5.61
5.72 1977
5.72
5.10 2719 673 60 97 1-8 2122 2907 8656
5.61
10. 0
29 5.1 10.1
9.8
10.2
10.8
11.7
11.7
12.0
11.8
217 -19.5 11.8
93 23.3 8.9
8.6
8.3
8.2
61 17.7 8.1
8.6
11 -0.7 8.7
10.0
11.5
11.1
97 19.1 11.0
11.1
11 38.9 11.7
11.1
9.5
8.7
65 10.9 6.9
8.9
92 21.7 8.0
7.6
8.1
8.2
90 -17.6 8.1
8.0
97 0.1 8.3
8.9
10.1
10.1
123 -9.2 9.9
9.8
49 -0.9 9.0
8.7
81 -0.7 8.5
9.5
9.7
9.7
9.6
135 35.5 8.1
9.2
-------
PAGF 15
d
I
"UN
NUK?ER SATE
711-1B 12/30/75
12/31/75
12/31/75
12/31/75
12/31/75
12/31/75
12/31/75
01/01/76
Hl/01/76
01/01/76
fU/01/76
01/01/76
01/01/76
ni/0?/76
01/02/76
01/02/76
712-1A 01/02/76
01/02/76
01/02/76
01/03/76
Pl/03/76
01/03/76
01/03/76
01/03/76
01/03/76
IU/04/76
01/04/76
01/04/76
01/04/76
01/04/76
Cl/04/76
ni/05/76
01/05/76
01/05/76
01/05/76
01/05/76
01/05/76
01/06/76
01/06/76
01/06/76
01/06/76
01/06/76
01/06/76
01/06/76
01/07/76
01/07/76
01/07/76
712-16 01/07/76
"1/07/76
"1/07/76
PH AT
SCRUBBER
TIPE INLET
2330
0300
0700
1100
1500
1960
2300
0300
0700
HOC
1500
1900
2300
0300
07CC
1100
1500
1900
2300
03CO
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
070C
0701
1100
1500
1900
2300
0300
0700
1100
2200
2230
2300
5.55
5.65
5.60
5.52
5.58
5.58
5.55
5.56
5.57
5.58
5.61
5.65
5.58
5.58
5.58
5.86
5.69
5.68
5.55
5.67
5.56
5.67
5.66
5.73
5.71
5.63
5.07
5.74
5.78
5.79
5.76
5.80
5.79
5.86
5.93
5.96
5.89
6.00
6.00
6.03
6.10
5.92
5.81
5.86
5.74
5.98
6.04
5.98
5.89
LIQUID ANALT'JtS «
CA + + MG+* NA+ K+
PPP PPM PPM PPM
1875
1735 355
190P 834
?835 713
3059 771
2265 761
2749 731
2385 767
2149 789
1575 699
1560 784
1451 800
1163 754
1060 789
1090 719
1065 784
46 118
76 134
81 US
78 115
94 112
74 106
70 100
74 120
67 114
61 127
55 117
61 118
59 110
55 113
55 109
I bCKUH
303 —
PPP!
72
64
96
144
112
56
104
40
72
72
136
40
176
56
96
titR 1NLI
S04 —
PPM
1838
1555
1400
1971
440
549
464
589
471
360
500
509
399
538
825
L 1 ------
CL-
PPM
2978
2907
5637
6559
6133
6594
6169
6027
5247
4824
4290
4113
4041
3900
4148
LIQUID
TOTAL SULFATE IONIC WAKE PER
IONS SAT. AT IMBAL. PASS
PPH 50 C X M.WOL/L
7142
7470
10877
12697
9917
10859
9959
9779
8245
7788
7349
6758
6634
6471
7082
9.1
9.5
117 -2.7 9.1
9.1
31 31.8 7.7
7.8
7.6
9.0
91 7.8
8.9
127 -3.2
8.8
8.9
10.1
27 -1.3
9.4
8.3
8.1
8.?
8.7
36 2.2
10.4
28 -1.9
10.3
10.5
10.5
34 -3.0
11.7
25 -12.4
11.9
12.0
10.7
18 2.0
11.1
24 6.1
11.2
23 -1.5
9.9
10.8
10.8
10.6
16 -2.8
10.0
24 -3.2
12.0
34 -11.2
11.2
9.6
9.2
-------
16
O
i
i—i
oo
RUN
NUHFER DATE
712-18 01/07/76
01/08/76
01/08/76
01/08/76
01/08/76
01/08/76
01/08/76
01/08/76
01/08/76
01/08/76
"1/08/76
ri/08/76
PI/08/76
713-1A 01/08/76
01/08/76
01/08/76
01/08/76
01/09/76
"1/09/76
01/09/76
Cl/09/76
01/09/76
Cl/09/76
01/10/76
01/10/76
01/10/76
714-1A 01/19/76
01/19/76
01/20/76
01/20/76
ni/?0/76
01/?0/76
01/20/76
01/20/76
01/20/76
01/21/76
01/21/76
91/21/76
01/21/76
01/21/76
01/21/76
01/22/76
01/22/76
Cl/22/76
01/22/76
11/22/76
ni/22/76
51/22/76
fl/23/76
"1/23/76
PH AT
SCRUBBER
TIMF INLET
2330
0000
0030
0100
0130
0200
0230
0300
0330
0400
0430
0500
0530
1100
1500
1900
2300
0300
0700
1130
1500
1900
2300
0300
0700
1100
1900
2300
0300
0700
0701
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0301
0700
1100
1500
1900
2300
0300
0700
5.73
5.73
5.76
5.99
5.84
5.78
5.71
5.58
5.42
5.32
5.13
4.95
4.73
5.40
5.36
5.29
5.21
5.17
5.14
5.24
5.24
5.26
5.32
5.19
5.23
5.28
5.26
5.59
5.79
5.85
5.85
5.66
5.54
5.64
5.81
5.59
5.57
5.73
5.69
5.61
5.63
5.58
5.43
5.55
5.60
5.53
5.38
5.44
5.43
5.41
CA + *
PRM
2140
2530
3230
2879
370
270
283
708
366
556
670
667
854
746
624
HUU1U ftNA
M6*» NA*
PPM PPM
899
783
999
94?
4129
4269
4519
4859
5859
4519
4469
4799
5469
6509
4979
48
67
70
93
73
64
66
69
63
68
58
71
55
57
4'J
LI ~>ti I
K +
PPM
105
118
122
128
92
88
60
62
64
67
54
148
56
54
124
» i acnui
SC3--
PPH
104
88
96
96
616
1425
3210
3634
1345
904
1032
864
1377
1785
8PO
?Bt_K J.WL
S04--
PPH
2644
1970
1814
1951
9584
9773
10911
12493
18053
14810
15669
17415
16881
15240
.. _.
14497
CL-
PPM
4609
5530
5708
6452
4538
3829
3900
3651
4467
4892
4609
4360
5566
6133
5920
TOTAL SULFATE
IONS SAT. AT
PPM 50 C
10549
11086
12039
12546
19402
19718
22949
24976
30217
25816
26561
28324
30253
30524
27073
136
117
112
116
42
31
34
27
56
85
107
111
125
90
fl7
LIQUID
IONIC 1AKF PER
IMBAL. PASS
% M.MOL/L
-1.1
-1.3
19.4
1.7
5.7
6.1
-6.9
-9.4
-6.1
-16.0
-19.0
-16.6
-9.4
7.2
-10.0
9.7
10.2
10.5
10.8
11.0
10.6
10.9
8.4
8.2
7.3
8.0
9.2
S.O
7.6
8.0
7.9
7.6
8.2
8.0
9.P
9.9
10.3
10.2
10.1
11.7
13.2
13.3
13. S
12.9
10.1
8.2
7.7
10.4
10.6
10.5
10.4
10.1
9.3
8.4
8.7
9.3
1C. 6
10.7
-------
17
RUN
NU«PER DATE
714-1A 01/23/76
01/23/76
01/23/76
11/23/76
01/24/76
Ql/24/76
i11/24/76
01/24/76
01/24/76
01/24/76
(51/25/76
11/25/76
01/25/76
01/25/76
01/25/76
01/25/76
01/26/76
?U/26/76
O 715-1A 01/26/76
1 01/26/76
^ 01/27/76
ni/27/76
01/27/76
01/27/76
PI/27/76
716-1A 01/27/76
01/27/76
01/28/76
01/28/76
(11/28/76
717-IA 01/28/76
01/28/76
01/28/76
01/28/76
01/28/76
01/29/76
01/29/76
01/29/76
PI/29/76
01/29/76
ni/29/76
01/30/76
01/30/76
01/30/76
01/30/76
01/30/76
-------
PAGF
RUN
NUKPER CATE
717-1A 01/31/76
01/31/76
^1/31/76
02/01/76
02/01/76
02/01/76
02/01/76
02/01/76
r>2/02/76
02/02/76
02/02/76
02/02/76
02/02/76
C2/03/76
02/03/76
02/03/76
02/03/76
02/03/76
h-j 02/03/76
I 02/04/76
ts) 02/04/76
O 02/04/76
02/01/76
02/04/76
C2/04/76
02/05/76
^2/05/76
PH AT
SCRUBBER
TlP.r- INLET
1530
1900
2300
0300
0700
1100
153H
1900
0700
1100
1545
1900
2330
0300
0730
1130
1530
1930
2330
0330
0730
1130
153C
1930
2330
0330
0730
5.45
5.35
5.43
5.54
5.45
5.40
5.40
5.47
5.15
5.57
5.48
5.44
5.50
5.22
5.57
5.66
5.55
5.46
5.49
5.47
5.28
5.29
5.45
5.23
5.22
5.38
5.35
CA + +
PP*
572
655
654
688
396
569
507
622
559
451
667
541
634
608
LiUUIU ANA
"IG + + NA +
pt>M PPM
4589
4629
3839
4659
5059
4589
5699
5579
4619
5309
5649
4869
5179
4779
48
6.8
3?
41
3fi
46
51
32
36
38
38
43
41
37
I. Tit a i
K +
PPM
87
253
89
85
96
81
79
102
94
77
99
94
112
110
n I ainui
S03--
PPM
2674
1921
1985
2625
2369
1489
1505
1008
2001
2842
2201
2361
1601
968
-DL" irci-t
S04 —
PPM
15941
16268
14304
16893
16821
170&5
20144
18355
18436
20030
18236
16971
17645
16039
CL-
PPM
3013
2588
2446
2198
1914
1772
1595
1879
1843
2098
2269
2907
2800
2552
TOTAL SULFATE
IONS SAT. AT
PPM 50 C
26924
26382
23349
27189
26693
25611
29580
27577
27588
30845
29159
27786
28012
25093
92
105
107
113
63
96
86
98
100
80
104
88
102
95
LIQUID
IONIC MAKE PER
IHBAL. PASS
X M.MOL/L
-17.9
-a. 7
-18.2
-13.7
-5.3
-7.9
-0.7
6.8
-18.0
-18.2
0.7
-14.5
-5.2
-0.5
9.9
11.2
10.2
10.5
9.7
10.2
8.6
10.1
11.9
10.9
10.1
10.4
10.2
10.2
9.9
9.6
10.2
11.3
11.0
9.9
9.7
10.6
10.7
9.8
9.6
9.7
9.9
-------
-SOLID ANALYSES AT SCRUBBER 1NLET-
O
IN)
SUN
NUMBER D/STF
625-1* 06/20/75
C6/21/75
06/21/75
T6/22/75
"ft/25/75
06/23/75
r&/23/75
T6/24/75
r&/?5/75
De/25/75
06/30/75
T6/30/75
P7/01/7E
07/01/75
P7/02/7b
''7/03/75
P7/03/75
07/01/75
P7/04/75
<"7/!H/75
U7/05/75
P7/OE/75
C7/06/75
C7/06/75
07/07/75
C7/08/75
C7/08/7S
626-1A 07/09/75
r7/0«»/75
"7/10/75
"7/10/75
P7/11/75
•7/11/75
07/11 /7b
r7/ll/75
C7/12/75
P7/12/75
C7/lW7b
'7/13/75
fi7/14/75
P7/14/75
H7/15/75
C7/lt>/75
07/15/75
07/16/75
f.7/16/7^
07/l*/7r-
07/17/75
07/17/75
C7/17/7h
C 7 /1 6/75
TJMF
2300
1500
2300
150P
230C
1500
2300
1500
1500
2300
1600
2300
1500
2300
1500
2300
1500
2300
1500
3300
1500
2300
1500
230C
2300
1500
23CO
1500
2300
1500
2300
1500
1501
15C2
2300
15CO
2300
1500
2300
1500
2300
07^0
1600
2300
0700
1500
2300
0^00
1500
2300
07PO
SQ2 SO.? S02
INLET OUTLET REMOVAL
PP1 COM X
3160
?ean
320P
3090
3040
3120
2100
2600
2880
?320
3200
3200
?560
2720
2280
2POO
2030
2C40
2610
3120
2280
26 SO
2640
3160
2880
3120
3200
32RO
3320
3000
3240
29or
2920
2880
3520
7-320
3320
3420
3120
3560'
3600
3680
3200
3120
296C
3?4P
3320
2830
3040
344C
950
800
960
R80
760
920
500
560
56C
36!)
560
740
360
460
280
200
80
300
480
681
340
400
520
740
340
4? P.
64Q
700
76C
5f n
5fO
54P
540
463
730
640
740
820
6hC
940
9GO
90C
740
640
620
720
700
56C
700
94C
66.7
69.2
66.8
63.3
72.3
67.3
76.9
76.1
78.5
82.8
80.6
74.4
84.4
81.3
86.4
89.0
95.8
83.7
79.9
75.9
83.5
83.5
78.2
74.1
86.9
85.1
77.9
76.4
74.6
79.3
80.2
79.4
79.5
82.3
75.5
7H.7
75.3
73.4
75.9
70.7
70.5
72.9
74.4
77.3
76.8
75.4
76.6
77. s
74.5
69.7
CAO
UT X
24.20
20.50
23.60
23.10
24.80
26.20
24.90
23.40
25.50
25.90
27.30
30.90
29.40
25.90
27.90
27.60
27.40
2S.50
24.20
30.00
23.20
20.40
26.90
26.80
22.80
26.30
28.10
30.30
30.70
25.30
25.60
26.70
23.80
22.70
25.80
27.10
27.80
28.30
25.00
26.20
26.80
24.80
26.70
27.30
25.00
26.80
31.60
25.40
25.80
25.90
S02
yT %
18.30
15.40
19.40
17.60
20.00
23.10
20.70
17.30
21.90
22.30
19.50
23.50
17.70
18.70
22.60
16.60
16.00
16.10
17.40
21.40
20.20
ie.60
22.00
21.90
17.90
21.50
21.30
24.00
22.90
21.00
21.90
21.00
19.10
18.00
20.60
23.20
21.90
25.90
21.60
19.50
24.10
22.90
23.90
23.80
23.90
21.60
22.10
21.00
23.30
24.10
SC3
yT x
6.63
7.15
6.35
8.05
7.20
7.13
7.03
8.78
6.93
7.03
15.03
6.23
11.48
7.43
3.85
11.55
11.80
12.38
9.05
5.45
6.25
6.45
6.50
6.?3
7.53
4.13
6.28
7.30
3.58
5.45
6.13
9.75
8.83
4.50
5.75
4.40
5.73
1.33
6.71'
7.63
5.68
6.48
5.43
6.35
5.43
8. 1C
10.58
6.75
5.98
4.78
TOTAL S
AS S03
yT. x
29.50
26.40
30.60
30.30
32.20
36.00
32.90
30.40
34.30
34.90
39.40
35.60
33.60
30.80
32.10
32.30
31.80
32.50
30.80
32.20
31.50
29.70
34.00
33.60
29.90
31.00
32.90
37.30
32.20
31.70
33.50
36.00
32.70
27.00
31.50
33.40
33.10
33.70
33.70
32.00
35.80
35.10
3b.30
36.10
35.30
3o. 10
3ft. 20
33.00
3b.lO
34.90
C021 SLURRY X ACID MOLE X
SOLIDS INSQLS SULFUR
UT X yT. X IN SOLD OXIDIZED
2.15
1.30
1.S4
1.25
1.48
2.12
2.16
2.23
2.92
2.12
1.89
2.39
2.29
1.87
2.23
2.30
1.95
2.33
1.54
1.64
1.59
1.86
1.64
1.64
2.05
2.07
2.07
1.80
1.57
1.59
2.48
1.56
1.50
1.64
1.92
2.18
1.63
1.86
1.52
1.15
1.43
1.85
1.62
1.49
2.19
2.29
1.48
1.23
1.60
1.59
4.5
8.6
8.1
8.6
8.4
8.3
7.4
7.7
8.5
6.9
7.3
a. .7
8.6
8.9
9.4
8.0
8.7
8.3
8.2
8.5
8.4
8.5
8.2
8.0
9.2
7.5
7.6
8.8
8.7
8.4
8.0
8.5
8.2
8.7
d.e
8.5
8.1
8.4
8.7
8.6
9.1
8.7
8.4
8.3
8.2
8.2
a. 6
8.2
8.3
8.9
2.12
4.61
3.91
4.14
3.81
3.37
3.28
3.56
3.55
2.87
2.30
3.22
3.09
4.00
4.14
3.09
3.41
3.03
3.72
3.52
4.07
4.41
3.46
3.45
4.44
3.49
2.20
3.16
3.65
3.89
3.50
3.31
3.85
4.62
4.02
3.74
3.47
3.81
3.86
3.79
3.82
3.82
3.56
3.42
3.62
3.26
2.72
3.69
3.58
2.93
22.5
27.1
20.8
26.6
22.4
19.8
21.4
28.9
20.2
20.1
38.1
17.5
34.2
24.1
12.0
35.8
37.1
38.1
29.4
16.9
19.9
21.7
19.1
18.5
25.2
13.3
19.1
19.6
11.1
17.2
18.3
27.1
27.0
16.7
la. 3
13.2
17.3
3.9
19.9
23.8
15.9
18.5
15.4
17.6
15.4
23.1
27.7
20.5
17.0
13.7
STOICH
RATIO
1.13
1.12
1.09
1.08
1.08
1.11
1.12
1.13
1.15
1.11
1.09
1.12
1.12
1.11
1.13
1.13
1.11
1.13
1.09
1.09
1.09
1.11
1.09
1.09
1.12
1.12
1.11
1.09
1.09
1.09
1.13
l.OS
1.08
1.11
1.11
1.12
1.09
1.10
1.08
1.07
1.07
1.10
l.OB
1.09
1.11
1.12
1.07
1.07
1.08
1.08
SOLID
IONIC
IMBAL
3.T
-1.4
0.9
1.2
1.4
-6.6
-3.6
-3.1
-8.8
-4.8
-9.9
9.4
10.0
7.5
9.2
7.4
9.6
9.7
2.7
17. a
-3.8
-13.6
3.7
4.4
-3.3
7.4
8.6
6.2
20.0
4.2
-4.0
-1.9
-4.3
7.5
5.C
3.4
9.1
8.2
-2.2
8.9
-0.4
-8.6
-0.3
0.4
-10.1
-2.6
9.4
2.8
-S.2
-2.2
-------
PAGf
-SOLID ANALYSES AT SCRUBBER INLET-
d
I
fO
IV
PUN
NUMBER ~ATE
6?6-lft 07/18/75
C7/1P/75
'17/19/75
"7/19/75
07/19/75
^7/20/75
"7/20/75
•'7/21/75
-7/21/75
07/22/75
07/23/75
•"7/23/75
07/24/75
07/24/75
r>7/24/75
"7/25/75
G7/25/75
07/25/75
f-7/26/75
07/26/75
07/26/75
'7/27/75
C7/27/75
07/27/75
07/28/75
07/28/75
•17/29/75
"7/29/75
07/30/75
17/30/75
"7/31/75
C7/31/75
H7/31/75
CB/01/75
ne/oi/75
ri8/02/75
^8/02/75
QP/02/75
C<3/02/75
PP./03/75
06/03/75
OB/03/75
08/04/75
627-1A OP/05/75
rP/05/75
OP/06/75
OH/06/75
"P/07/75
C°/Q7/75
08/08/75
08/08/75
3f> SC2 S02
1'iLTT CUTLET REMOVAL
fjvr ppw PPM %
1=00
2300
07f 0
150C
2300
1500
2300
150C
7300
05CO
1700
2100
0500
1500
2300
0700
1500
23CO
07CC
1 5 p 2
2301
P7n C
1500
2300
1500
2300
07 CO
1500
15CO
2300
1502
2300
23C2
1500
2300
0700
15CO
23 GO
2302
0700
1500
2300
0700
1500
23PO
150C
2300
1500
2300
070C
121*
32 Of'
22 T,
3440
300C
20«0
24 BO
2600
3000
2960
3HOO
2^20
3320
2HOO
1440
2280
3120
3320
2720
oqfjp
31 2P
3240
1920
1560
1520
2280
2400
3200
2680
2800
2520
2040
1720
156C
2320
2720
1720
1520
1880
348T
'I4pr
1560
1600
1600
144C
1480
2800
7fi--<
fi?0
9«"
72P
320
44C
4fif
680
500
62 C
540
620
23:''
80
24P
700
7ht
420
50P
6 or
60D
220
110
260
31C
36 n
960
5P-0
4?0-
42G
220
160
80
440
360
5-30
360
140
?20
900
760
40
40
50
30
40
180
73.0
72.3
69.7
73.4
83.0
80.4
79.6
74.9
78.3
77.1
79.5
79.3
84.5
93.9
88.4
75.1
74.0
82.9
61.3
78.7
79.5
87.3
92.2
81.1
85.0
83.4
66.8
76.0
81.0
81.6
88.1
89.7
94.4
79.0
76.4
76.8
89.8
87.1
71.3
75.8
97.2
97.3
96.6
97.7
97.1
92.9
CAO
yT %
26.10
26.10
25.70
25.50
23.90
22.70
24.00
26.20
23.30
22.40
24.10
25.10
24.10
25.30
23.50
22.50
21.10
25.40
24.80
25.90
26.70
25.20
23. SC
22. 1C
22.80
22. 8U
24.20
24.30
24.70
21.60
22.10
21.30
20.40
19.50
23.50
19.90
20.20
23.40
19.90
19.20
22.70
22.90
23.80
24.60
24.00
24. 6C
24 .80
24.30
SO?
UT %
24.10
24.00
24.00
21.40
14.50
14.70
17.60
17.80
17.10
16.10
20. CO
2 G . 1 0
14.90
20.40
15.10
16.50
16.30
19.70
19.40
20.60
19.10
19. 70
16.00
14.80
16.50
16.90
lb.30
20.10
20.10
16.30
17.00
14.20
12.90
15.20
16.20
15.60
15.80
19.40
14.80
12.50
17.10
16.70
19.60
19.20
17.60
16.00
22.50
17.20
S03
yT •/.
5.£ 8
b.2C
6.00
H.25
10.08
7.13
7.50
7.95
8.13
7.18
5.40
6.88
11.78
6.5C
7.33
4.68
5.33
5.88
6.F.5
3.35
4.«3
3.68
9 .oO
8.50
6.28
5.36
9.88
5.06
6.08
6.63
9.05
11.75
12. °8
9.40
6.^5
10.10
8.55
5.55
9.90
11.78
6.63
H.03
4.10
4.30
5.00
3.90
3.78
5.20
TOTAL S
AS SOi
wT. X
35.80
35.20
36.00
35.00
28.20
25.50
29.50
30.20
29.50
27.30
30.40
32.00
30.40
32.00
26.20
25.50
25.70
30.50
31.10
29.10
28.70
28.30
29.50
27.00
26.90
26.50
29.00
30.20
31.20
27.00
30.30
29.50
29.10
28.40
27.10
29.60
28.30
29.80
28.40
27.40
28.20
2B.90
28.60
28.30
27.00
26.40
31.90.
26.70
C02
UT %
2.u3
1.67
1.59
1.97
2. 03
2.03
1.59
1.09
1.31
1.25
1.4S
1.69
1.96
1.86
2.41
2.51
1.97
1.88
1.44
0.75
2.11
1.66
1.30
2.04
2.12
1.73
2.35
1.29
1.54
1.24
1.93
1.86
1.44
1.94
2.28
0.60
1.68
1.38
1.68
1.72
0.90
1.20
2.58
2.38
3.19
3.27
2.26
3.72
SLURRY X ACID "OLE X
SOLIDS INSOLS SULFUR
WT. X IN SOLO OXIDIZED
ft. 7
8.4
h.3
8.4
7.6
8.5
a.i
8.7
9.(j
9.1
a. 1
8.6
8.6
7.5
8.5
P. 6
"?. 1
8.4
8.3
9.6
9.4
8.9
8.2
7.7
7.5
7.5
8.1
8.7
8.6
7.5
7.3
7.5
10.4
14.7
14.6
14.8
14.8
-16.0-
15.0
3.70
3.63
3.57
3.50
3. El
4.3S
4.23
4.26
5.06
4.29
4.37
3.B5
3.86
4.01
4.46
4.44
3.76
3.72
3.82
7.36
7.55
7.35
15.9
14.8
16.7
23.6
35.7
28.0
25.4
26.3
27.6
26.3
17.8
21.5
3
-------
PAGE
-SOLIO ANALYSES AT SCRUBBER INLET-
d
I
IN>
oo
RUN
NUfRER CdTE
627-1A OS/08/75
C8/09/7S
OP/09/75
08/09/75
08/10/75
rs/io/75
08/10/75
re /i 1/75
e«/ll/75
P8/12/75
fn/12/75
08/13/75
08/13/75
628-1A 03/16/75
PR/16/75
C°/17/7S
"<-/17/75
"3/17/75
05/18/75
rp/i8/7b
08/18/75
np/i"?/75
rp/19/75
Cfi/l<5/75
C8/20/75
CS/20/75
C8/20/75
RS/21/75
CS/,71/75
!>9/2?/75
CS/22/75
r*/23/75
n?/23/75
f 8/23/75
CS/24/75
no/24/75
OS/24/75
C<«/?5/75
18/25/75
CS/26/75
Hp/26/75
CS/26/7E
OS/27/75
06/27/75
"S/27/75
T8/P8/7K
n°/28/75
'.-'(• 1 2*) tl*
"?/59/75
C»/'«0/75
' -S.flO/Ts
TlHf
2300
0700
1500
2300
0700
1500
23PO
1500
2300
1500
2300
0700
1100
1500
2300
0700
150C
2300
0700
1500
23CC
0700
150C
2300
0700
1500
23no
1500
23CC
07PC
2300
0700
15 Ot
2?ro
0700
1500
23CC
070C
2302
0700
1*00
23?0
0700
150 C
23CC
icr?r
2300
U70U
23?C
07DC
1SOC
S02
INLET
PPM
3560
3280
3fi4n
220D
3200
24RO
3POO
1280
2610
1480
1120
1160
1120
1200
1960
32SO
2FQO
3000
3000
2520
22*0
1520
28 8f;
3320
276C
?POC
2300
3280
352^
2920
320C
35SP
3240
2960
?32P
2f °C
3240
3280
35 D ^
292"
S02
OUTLET F
PPM
400
720
1240
34T
840
360
600
160
360
40
20
20
CO
120
160
960
400
660
640
540
300
90
58S
760
bOO
530
130
800
950
500
680
900
820
530
24D
540
7UO
6 6 C
520
200
S02
-------
PAGr
U
I
CN)
NUMER 'ATE
62B-M Oh/30/75
r ': Vl/75
•t/31/75
."c/Cl/75
'•5/ 02/75
'r'/0?/75
r' ':• 1 0 ? / 7 5
9/0^/75
rr> /Pi/75
r 9/0 5/75
rs/05/75
:r/Of>/75
r?/C6/75
' WC6/75
i "•/ 07/75
'9/07/75
' 3/07/75
"r/C8/75
"/OS/75
"O/OP/75
r 5/09/75
°5/ 09/75
"9/10/75
09/10/75
05/10/75
r°/ll/75
Gc/ll/75
0^/12/75
CS/13/75
''9/17/7^.
Or'/l"5/75
r?/13/75
"9/14/75
Oc/14/75
r5/14/75
"9/15/75
C^/15/75
09/16/75
'9/16/75
fS/16/75
fl/16/75
09/17/75
OS/17/75
C^/17/75
^'P-IE 0°/18/75
"c / 18/75
" 5/19/75
r=>/l° /75
r "5/20 /75
C=/20/75
"5/20/75
2300
0700
15CC
23CC
P70C
1500
230C
07PO
2300
0700
2300
0700
150C
2310
0700
1500
2300
n7or
1500
2300
0700
?300
n70P
1500
230C
1500
23r r
0700
23 OC
070C
1500
2300
070C
1500
2300
1500
230C
07GO
120C
1500
2700
0700
1500
2? CO
1500
23CC
Q7CO
2300
C700
150D
2300
SO?
IMLTT
op *
2600
284C
264H
?32r
2280
1760
2800
2080
3360
16 KG
1720
3080
3080
288C
2320
3330
3680
3520
3920
36 PO
3960
4040
3600
3080
2160
3440
3460
3240
3160
3f«0
3480
32RO
3PPO
2880
2800
3240
I960
16HO
1800
356C
3600
2"36P
36U0
S02 SO?
OUTLET REMOVAL
23C
160
100
?4C
240
100
4«C
150
54 r
100
80
51C
540
Q f1
2«0
600
104"
800
1170
400
1000
950
700
52G
40
680
700
340
«80
96P
700
660
600
540
160
500
50
120
160
700
76C
460
5SO
90 .2
93.fi
95. %
88.6
88.4
93.7
81.0
92.0
8?.?
93.4
94. 9
81.7
80.6
97.0
86.7
80.3
68.7
74.3
66.9
87.7
72.0
73.9
73.5
81.3
98.0
78.1
77.7
88.4
83.2
72.6
77.7
77.7
77.9
79.2
93.7
82.9
97.2
• 91.7
90.2
78.2
76.6
82.°
82. b
-SOLID fl'vALY
c A : s n :•
*T X UT %
24.00
23.90
23.30
24.30
24.80
23.60
25.60
23.50
25.50
24.7?
24.7:
?4.50
24.10
25.60
26.30
24.30
25. CO
24.50
2 5 . 0 0
25.30
25.30
25.40
25.40
25.40
2 (-. . 6 0
24.50
25.40
24.90
24.80
24. 8C
25.50
26.80
JC.20
24.90
25.40
24.10
25.90
24.10
22.60
22.10
25.00
24.90
24.40
25.90
15.30
16.90
18.80
20.30
20.50
16.10
15.00
16.20
21.10
18.60
16.50
18.10
19.30
21.20
18.30
17.23
20.20
17.10
23.30
21.10
23.00
23.00
21.UO
22.60
19.70
20. 4C
22.10
20.40
20.70
21.20
18. 4D
19.40
21.70
?0.90
21.00
18.60
22.40
18.00
17.40
15.60
21.90
20.60
19.50
21.50
CE3 AT t
SO?
JT '/.
7.28
8.58
7.0C
6.73
6.28
3.68
8.55
8.55
6.13
7.6L
7.18
7.?6
7.18
6.40
4. £3
8.67
6.05
9.83
5.88
8.33
6.35
6.15
9.75
6.25
10.66
6.00
4.78
6.50
6.93
6.50
11.20
12.15
7.88
6.18
6.45
6.55
4.70
6.90
6.35
7.20
5.63
£.85
7.63
8.73
CRU3[
-------
PAGE
-SOLID ANALYSES AT SCRUBBER INLET-
U
tsJ
Ul
NL'PFF1; C«Tf
6?8-U< Oc/21/75
^•9/21/75
"9/21/75
Or/22/75
T 9/22/75
•"lcl/23/75
09/2^/75
fo/23/75
15/24/75
"9/24/75
r
10/01/75
10/01 /75
1C/H2/75
l?/?2/75
l"/??/75
10/02/75
10 '03/75
ir /oT/75
10/04/75
10/04/75
10/04/73
10/04/75
10/04/75
10/H5/75
10/Oc./75
10/H5/75
10/05/75
10/05/75
10/05/75
ir/C5/75
10/06/7*3
10/nt/7K
10/06/7*
S02 502 $02
INLET OUTLET REMOVAL
Tjwr ppw ppM j;
0700
1500
2300
1500
2300
0700
1500
2300
1500
23CO
2300
0700
1500
23 HO
2302
ono
1500
2300
1500
1502
23(50
2302
0700
150 0
2300
1500
1501
2350
23"!
1500
lc,01
23TO
23 01
2300
2301
0700
0701
15CO
1501
23 CO
[1700
1500
1EC1
1506
1511
2300
23?1
07" 9
1500
JCD1
3860
3440
32f>0
302
SLURRY 5! ACID MOLE X
SOLIDS INSOLS SULFUR
WT. X IN SOLO OXIDIZED
9.1
9.7
9.0
9.3
9.5
9.2
8.5
8.6
9.4
9.3
:».6
10.2
9.2
9.0
9.9
9.7
9.6
9.0
7.8
8.7
9.7
9.9
9.6
9.6
= .3
9.3
9.4
9.4
8.7
8.7
8.4
8.4
8.7
9.1
9.1
9.5
9.3
9.5
9.5
9.5
9.b
9.2
9.2
4.05
4.17
4.07
4.25
4.22
4.61
4.01
3.82
4.23
4.29
4.51
4.33
4.47
4.21
3.12
3.97
4.49
4.15
4.10
4.29
4.01
4.18
4.17
4.14
4.00
3.94
3.95
3.97
4.00
3.95
3.E8
4.89
4.22
3.91
2.91
4.15
4.23
3.84
3.83
17.7
17.8
22.6
21.9
23.6
17.5
25.8
24.3
25.6
21.6
16.3
25.5
19.1
21.3
13.0
19.7
18.1
20.1
29.7
20.5
19.4
27.3
17.4
15.3
26.1
16.9
16.3
17.0
21.2
21.1
21.2
19.1
23.3
22.5
20.5
21.5
11.7
15.1
17.4
17.3
14.2
12.3
16.9
17.4
STOICH
RATIO
1.10
1.14
1.03
1.10
1.08
1.09
1.07
1.13
1.10
1.13
1.09
1.11
1.06
1.17
1.24
1.16
1.11
1.13
1.12
1.17
1.1S
1.15
1.13
1.13
1.06
1.11
1.10
1.10
1.12
1.14
1.06
1.03
1.10
1.14
1.09
1.11
1.12
1.10
1.08
1.09
1.09
1.08
1.09
1.10
SOL 11
IONIC
IHBAL
-1.9
-8.0
1.3
-4.0
2.2
4.2
3.9
-0.3
0.4
-0.3
1.4
-0.9
0.2
-4.4
-11.7
-4.8
0.8
0.?
2.4
0.1
-1.4
-5.1
-3.2
-2.2
6.2
0.5
-3.2
-3.2
-4.6
-6.9
8.3
7.?
3.1
-O.B
-0.4
-1.6
-3.0
-5.8
-2.9
-3.0
-3.9
-2.8
-2.8
-3.6
-------
-SOLID ANALYSES AT SCRU3BER INLET-
PA6F
U
")l^
NUMBER
62S-1B
701-1 8
702-1A
7G3-1A
CSTE
10/06/75
IP/06/75
IP/06/75
in/06/75
1C/07/75
10/07/75
10/H9/75
10/P9/Y5
IP/09/75
10/10/75
10/10/75
If /10/75
1C/10/75
10/10/75
10/11/75
10/11 /75
10/11/75
ir/n/75
10/11/75
IP/11/75
10/12/75
1C/1P/75
10/l?/75
IP/12/75
l"/l?/75
10/12/75
10/14/75
IP/14/75
IP/15/75
TC/15/75
10/15/75
10/15/75
10/15/75
10/15/75
10/15/75
10/16/75
IP/16/75
10/16/75
10/16/75
IP/16/75
10/17/75
1C/19'75
IP/19/75
ir/19/75
10/19/75
10/20/75
10/20/75
10/21/75
10/21/75
lC/?l/75
1 P /22/75
TIVF"
2300
23f 6
23CP.
2311
P7PO
07C1
2300
2301
23P6
0700
0706
23CO
2301
23 "p
0700
C701
1500
1501
23PO
2301
0700
0701
1500
1501
1511
2311
2300
2301
0709
1500
1501
2300
2301
2311
2312
1500
1501
1508
23CO
23C1
0500
1100
1500.
190C
2300
Q3PO
15CO
1500
1900
23T.Q
P3PC
sc?
INLTT
PPM
3010
384"
3MO
260P
2600
2440
3000
3000
2120
29?0
•5080
308C
3160
3160
30PO
3COP
304P
3040
3120
3120
406"
30RO
3PRO
2R40
2840
2760
?76P
2920
2440
2430
292P
3120
2»80
2520
26CO
2400
34PO
GC2 S02
CUTLET REMOVAL
POM x
500
980
960
360
360
220
32P
320
400
4CO
3«C
380
34 P.
340
260
2£P
740
240
600
600
840
420
4?0
26P
260
220
220
200
760
900
98 C
1000
R20
1200
940
72n
1160
81 .h
71.7
71.7
84.7
84.7
90. P
88.2
8B.2
84.8
84.8
86.4
86.4
88.1
88.1
90.4
90."
91.3
91.3
76.7
78.7
77.1
84.9
84.9
89.9
89.9
91.2
91.2
92.4
65.5
59. B
62.8
64.5
6B.4
47.2
59.9
66.6
62.?
C40
«T %
25.70
25.40
25.60
2R.90
28.40
32.10
32.00
32.10
29.20
29.20
29.30
29.30
31.00
31.00
32.10
32.10
33.20
32.90
29 .50
29.60
29.40
31.00
31.00
33.10
33.10
34.70
34.40
35.20
25.20
25.10
25.20
24.70
24.80
23.20
20.80
21.90
23.90
SO?
«T X
22.30
22.90
22. 8C
19.80
19.50
17.30
18.10
18.30
21.10
21.00
21.50
21.60
21.40
21.90
19.90
20.20
23.10
22.30
25.00
24.80
27.00
26.00
25.80
23.80
23.90
20.00
20.10
20.20
25.90
27.20
27.30
25.90
26.00
22.50
17.50
20.20
21.50
S03
JT %
7.03
5.88
6.30
6.55
6.13
5.78
6.26
6.53
5.73
5.55
5.33
4.9C
4. £5
4.03
7.13
6.35
2.73
3.03
3.56
4.20
1.86
1.51
1.56
1.95
1.83
3.60
2.18
1.65
1.93
1.51
0.78
1.23
1.91
3.68
b.93
3.95
6.23
TOTAL S
AS S03
JT. X
34.90
34.50
34.80
31.30
30.50
27.40
28.90
29.40
32.10
31.80
32.20
31.90
31.40
31.40
32.00
31.60
51.60
30.90
34.80
35.20
35.60
34.00
33.80
31.70
31.70
28.60
27.30
26.90
34.30
35.50
34.90
33.60
34.40
31.80
27.80
29.20
33.10
C02
UT %
2.09
2.00
2.22
5.74
5.62
9.37
10.25
10.19
5.21
5.60
6.61
6.69
7.68
7.25
7.54
7.60
8.56
9.89
5.39
5.94
5.67
6.99
7.26
9.34
9.35
10.51
10.40
11.37
2.61
2.50
1.98
2.37
2.26
1.27
0.78
0.05
0.11
SLURRY % ACID MOLE X
SOLIDS INSOLS SULFUR
WT. % IN SOLD OXIDIZED
9.3
9.2
9.2
15.0
15.0
15.9
14.4
14.4
15.0
lb.0
15.6
15.6
16.7
16.7
1B.1
18.1
18.6
18.6
14.8
14.8
16.8
14.8
14.8
15.9
15.9
14.8
14.8
14.7
14.1
14.3
14.6
15. Z
15.2
14.4
14.4
14.8
14.9
3.93
4.01
3.93
5.70
5.94
b.48
4.67
4.60
5.78
5.73
5.81
5.85
5.92
6.07
5.84
5.98
6.23
6.10
5.56
5.36
6.44
5.44
5.39
5.32
5.35
4.67
5.03
4.87
6.58
6.58
6.95
7.28
7.19
7.22
7.79
3.03
7.10
20.1
17.0
1S.1
20.9
20.1
21.1
21.7
22.2
17.8
17.5
16.6
15.4
14.8
12.8
22.3
20.1
ft. 6
9.8
10.2
11.9
5.2
4.4
4.6
6.2
5.B
12.6
8.0
6.1
5.6
4.2
2.2
3.7
5.5
11. e
21.3
13.5
18.8
STOICH
RATIO
1.11
1.11
1.12
1.33
1.34
1.6?
1.65
1.63
1.30
1.32
1.37
1.38
1.44
1.42
1.43
1.44
1.49
1.58
1.2-*
1.31
1.29
1.37
1.39
1.54
1.54
1.67
1.69
1.77
1.14
1.13
1.10
1.13
1.12
1.07
1.05
1.00
1.01
SOLir
lONir
IHBAL
_<=,.*
-5.?
-6.'
-1.?
-0.4
3.D
-4.1
-4.6
0.3
-0.7
-5.7
-5.4
-2.5
-0.8
0.2
0.9
0.5
-4.1
-5.9
-8.9
-9.4
-5.6
-6.2
-3.0
-3.1
3.7
5.9
5.?
-8.5
-11.8
-7.0
-7.5
-8.8
-3.3
1.6
6.3
2.4
-------
PAGE
-SOLID ANALYSES AT SCRUrfBER INLET-
O
I
"UN
MUMPER DATE
703-1A 10/?2/75
10/22/75
10/22/75
1P/22/75
l"/23/75
l"/23/75
10/23/75
U>/23/75
10/23/75
10/23/75
10/24/75
10/21/75
1C/24/75
10/24/75
10/24/75
in/24/75
in/35/75
10/25/75
10/25/75
10/25/75
10/25/75
1C/25/75
19/26/75
!P/2f-/7I;
10/26/75
IP/26/75
10/26/7=
1C/26/75
in/27/75
10/27/75
1C/27/75
10/P7/75
10/27/75
10/27/75
10/28/75
10/?R/75
10/2B/75
10/28/75
10/28/75
10/28/75
10/29/75
10/29/75
10/21/75
10/29/75
1P./29/75
lC/29/7c,
10/30/75
10/30/75
10/30/75
1C/JO/75
lO/^C/75
TI,,r
0600
1530
1900
2300
0300
P700
1100
15PC
1SOO
2300
0300
0700
1100
15PO
1900
2300
0300
0700
1100
1500
1900
23CO
0302
070C
1100
1500
1900
2300
0300
07CC
1100
1500
1900
2300
0300
0700
1100
1500
1900
23" 0
030P
0700
11^0
1500
1900
23 nc
0300
0700
1100
l^OC
1900
SC2
INLET
PPM
34«D
392^
3600
364C
34Hf>
3880
3080
2720
2560
2600
2600
2410
2*00
2410
2&4H
2«ro
2800
2?00
24f>o
2200
2120
?520
3120
30SP
2ROO
3160
32P"
3600
3680
372"
3R.4
15.1
15.2
16.0
14.3
15.2
15.6
15.4
14.9
15.4
14.9
It ACID
[NSOLS
IN SOLD C
7.61
7.41
3.19
8,76
7.60
7.52
7.57
/.79
6.74
7.67
7.74
7.34
7.57
6.84
6.64
7.44
7.92
7.96
7.88
8.24
7.32
8.14
8.86
6.38
7.27
8.26
7.80
7.80
7.83
7.46
7.54
7.38
7.18
7.33
7.93
7.97
6.32
7.57
7.46
8.25
8.25
8. 05
7.92
8.54
7.23
7.37
9.42
9.21
3.05
7.89
7.69
MOLE X
SULFUR
IX10IZEO
17.4
15.9
27.2
16.3
7.5
14.0
14.5
17.8
11.0
5.5
8.1
7.6
28.2
18.2
18.3
15.7
13.3
32.3
33.1
10.5
20.7
13.9
30.0
47.4
21.3
24.0
13.1
9.8
12.0
7.6
13.1
15.5
11.1
6.0
11.3
7.8
10.1
10.7
9.4
8.3
7.4
8.7
8.9
11.1
28.3
33.8
6.6
10.4
15.5
11.5
STOICH
RATIO
1.12
1.06
1.07
1.03
1.06
1.05
1.06
1.02
1.12
1.07
1.09
1.07
1.11
1.15
1.13
1.20
1.06
1.14
1.13
1.06
1.08
1.13
1.06
1.15
1.13
1.01
1.09
1.10
1.11
1.11
1.05
1.09
1.14
1.07
1.14
1.13
1.01
1.01
1.01
1.06
1.03
1.04
1.06
1.13
1.05
1.05
1.03
l.OS
1.01
1.06
SOLID
IONIC
1WBAL
-5.7
-1.5
-0.1
3.1
-5.2
-2.4
-0.8
-2.3
-11.7
-0.4
-2.5
-2.0
-1.3
-10.2
-11.2
-11.2
0.8
-2.5
-2.9
-1.7
-2.4
-3.6
-0.2
-2.5
-2.1
8.*
4.1
2.1
-1.5
-5.1
0.6
-1.8
-8.5
0.2
-2.3
-3.4
4.1
3.6
5.4
2.4
4.5
3.6
8.1
-6.5
-9.4
12.1
5.6
2.7
2.R
0.4
-------
PAGE
-SOLID ANALYSES AT 5CRUB3ER INLET-
d
I
rs>
oo
B|J!,
NUfntP r/!TE
702-1A 10/20/75
10/31/75
10/M/75
11/01/75
11 /Cl/75
1 1/C1/75
11/01/75
11 /Cl/75
7C4-1A 11/03/75
11/04/75
11/04/75
11 /04/75
11 /C4/75
11/01/75
1 1/04/75
11 /04/75
11/05/75
11/05/75
11/05/75
11/05/75
11/C5/75
11 /05/75
11/06/75
11/06/75
11/OP./75
11/06/75
11/06/75
11/06/75
11/06/75
11/07/75
705-1A 11/07/75
11/07/75
11/08/75
11/08/75
11/06/75
ll/OS/75
11/08/75
11/08/75
11/09/75
11/05/75
11/09/75
11/09/75
11/09/75
11/09/75
11/10/75
11/10/75
11/10/75
11/10/75
11/10/75
11/10/75
3 1/11/75
TI'-'F
2300
H700
15 C 3
03CG
C7CO
1100
1500
19 no
2300
03CO
0700
1100
1500
1900
23PO
2307
6300
C7HO
1100
15CO
1900
2 3 n o
osno
0700
1.1 PP
150P
1530
1900
23PO
n^oo
1900
23P-0
03PO
07PO
1100
15CO
1900
2300
0300
0700
1100
1500
1900
2300
D303
0700
11 CO
1500
1900
2300
D30C
c n o
IMLET
ppv
30 SO
422P
388P
3230
2940
2600
2POO
2560
284C
29 2r
29?C
296C
33PT
4180
40CO
36 Tj
368P
3480
384"
4400
4120
3720
3660
3080
?840
3160
?pac
3000
3000
3040
304C
2940
3280
2960
2920
3C8Q
3160
'•080
3000
3040
312P
3120
2960
296P
332D
3520
"?64f>
c-o2 sor
CUTLET REMOVAL
cp« %
llhO
1*?0
l&P.O
1200
1120
ioon
560
420
4SC
42C
3PO
380
4f.O
600
500
T40
340
320
420
540
560
340
360
380
460
500
700
760
640
520
460
380
58 n
500
480
440
560
540
480
460
480
420
320
400
520
530
f>40
57.5
52.2
52.0
58.4
57.8
57."
77.9
81.<2
81.3
84.1
85.6
85. R
84.9
84.1
86.2
89.6
89.8
85.8
87.9
86.4
85.0
89.9
89.1
86.4
82.1
82.5
73.1
71.9
76.4
81.1
83.3
85.2
SO. 4
81.3
81 .8
84.2
80.4
80. f,
82.3
83.3
83.0
85.1
88.1
85.1
82.7
81. R
80.5
CAO
'*T X
C1.10
21.80
21. 9C
21.30
22.40
21.40
23.40
24.70
25.50
26.30
26.60
26.10
28.90
29.90
31. CD
32.00
32.60
32.30
32.90
32.80
33.50
33.70
33.30
30.20
27.50
28.10
27.60
31.50
31.30
30.50
31.30
33.00
29.70
32.20
31.10
30.20
29.50
32.10
33.60
3 2 . 2.0
32.40
28.10
28.70
28.80
27.80
28.80
31.60
SO?
WT X
17.00
18.60
19.70
17.90
' 21.90
19.00
20.80
20.20
20.50
18.50
18.00
IP. 20
14.70
14.70
16.60
16.30
17.90
17.00
14.50
14.00
20.90
20.80
22. CO
16.10
24.90
27.10
19.40
25.40
24.30
23.60
22.70
23.40
21.60
24.90
23.20
25.70
25.80
23.40
18.90
26.20
25.00
23.70
23.10
26.30
22.70
25.60
27.90
SO 3
yT %
5.85
5. 1C
4.28
b.53
2.83
4.2b
2.8P
3.45
2.78
4.18
5.50
3.35
5.93
6.73
b.CS
6.23
5.83
5.85
11.98
12.90
2.68
3.20
2.80
5.08
3.28
2.63
2.35
1.06
4.03
3.00
1.43
3.25
0.40
3.68
6."0
2.98
1.76
6.85
8.18
3.16
6.96
1.98
4.43
0.83
4.13
4.71
1.53
TOTAL S
AS ST i
JT-. X
27.10
28.60
28.30
27.90
30.20
28.00
28.80
28.70
28.40
27.30
26.00
26.10
24.30
25.10
26.80
26.60
28.20
27.10
30.10
30.40
28.80
29.20
30.30
25.20
34.40
36.50
26.60
32.80
34.40
32.50
29.80
32.50
27.40
34.80
35.20
35.10
34.00
36.10
31o80
35.90
38.20
31.60
33.30
33.70
32.50
36.70
36.40
C02
UT X
1.64
1.47
1 .27
1.60
1.83
1.13
2.18
3.10
3.87
4.83
5.50
5.54
11.15
8.37
10.10
10.04
8.87
8.89
10.45
10.08
9.31
9.65
10.40
10.46
4.47
2.31
5.02
1.77
2.69
2.86
4.21
4.46
4.91
3.94
3.88
3.08
3.19
4.91
5.93
3.09
2.97
4.55
6.09
4.74
6.32
4.22
3.96
SLURRY X ACID "OLE X
SOLUS INSCLS SULFUR
WT. X IN SOLD OXIDIZED
15.0
15.5
17.3
15.5
15.4
IS. 5
14.9
15.4
15.5
15.5
15.2
14.9
14.4
15.2
15.8
15.4
15.6
15.9
15.9
16.2
16.3
15.8
14.9
1J.8
13.8
15.5
14.2
14.3
15.0
16.1
15.8
15.6
15.3
14.9
14.4
14.7
14.5
14.6
15.0
15.0
15.3
13.9
15.4
15.2
15.0
15.3
15.3
6.02
8.15
9.18
8.19
8.04
8.45
7.73
7.56
7.47
7.20
7.08
7.02
5.49
5.87
5.54
5.30
5.33
5.56
4.17
4.17
5.65
5.30
4.88
5.17
5.65
6.41
6.63
6.08
5.82
6.68
6.67
5.79
7.02
5.46
5.09
5.82
6.08
4.70
4.78
5,49
4.95
6.02
S.89
6.38
5.97
5.71
5.73
21.6
17.8
14.8
19.8
9.4
15.2
9.7
12.0
9.8
15.3
13.5
12.8
24.4
26.8
22.6
23.4
20.7
21.6
39.8
42.4
9.3
11.0
9.3
20.2
9.5
7.2
8.8
3.2
11.7
9.2
4.8
10.0
1.5
10.6
17.6
8.5
5.2
19.8
25.7
8.8
18.2
6.3
13.3
2.5
12.7
12.8
4.2
STOICH
RATIO
1.11
1.09
1.08
1.10
1.11
1.07
1.14
l.?0
1.25
1.32
1.38
1.39
1.83
1.61
1.6"
1.6"
1.57
1.60
1.63
1.60
1.59
1.60
1.62
1.76
1.24
1.14
1.34
1.10
1.14
1.16
1.26
1.25
1.33
1.21
1.20
1.16
1.17
1.25
1.34
1.16
1.14
1.26
1.33
1.26
1.35
1.21
1.20
SCLin
IONIC
IMBAL
0.1
-0.5
0.2
-1.3
-4.8
1.6
1.9
2.6
2.6
2.8
5.2
2.9
-8.1
5.5
-2.1
1.8
4.7
6.2
-4.6
-4.1
4.4
2.8
-3.5
-2.6
-8.3
-3.7
9.3
19.9
12.1
13.4
16.2
13.8
14.3
8.7
4.8
5.6
5.5
1.7
11.2
9.7
5.7
0.6
-8.3
-2.9
-10.9
-7.9
3.3
-------
PAGE
-SOLID ANALYSES AT SCRU3BER 1NLET-
ti
I
C\>
sO
°v\
NUKnES DATE
705-1A 11/11/75
11/11/75
11/11/75
11/11/75
11/11/75
11/12/75
11/12/75
11/12/75
11/12/75
11/12/75
11/12/75
11/11/75
11/13/75
706-1A 11/13/75
11/14/75
11/14/75
11/14/75
11/14/75
11/14/75
11/14/75
11/15/75
11/15/75
11/15/75
11/15/75
11/15/75
11/15/75
11/15/75
11/15/75
11/16/75
11/1^/75
11/16/75
11/16/75
11/16/75
ll/lfc/75
11/16/75
11/17/75
11/17/7E
11/17/75
11/17/75
ll/17/7b
11/17/75
11/18/75
11/18/75
11/1H/75
11/18/75
11/18/75
11/18/75
11/19/75
11/1S/75
11/19/75
ll/n/75
TIME
0700
1100
1500
1900
2300
0300
07 CO
1100
1500
1SCO
2300
0300
0700
2300
0300
0700
1100
1500
1900
2300
0303
0700
0707
0710
1100
1500
1900
2300
0300
C7CO
07C7
1100
1500
1 9 r> o
2300
0300
C700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
?3T:0
0700
1100
15t)C
S02
INLET
PPH
392C
3R80
36«0
364f
3P40
396P
3R40
328C
28BP
2R4C
2840
2600
?480
2960
3080
3080
3200
3520
3600
3600
3280
3100
3100
2«40
?8Rfi
2840
292C
3000
34f)0
3440
3760
3720
3520
3360
364"
3080
3080
3000
2960
2ROO
?720
2560
2920
344n
3360
3R40
349D
2920
S02 S02
CUTLET REMOVAL
PPM %
780
72P
580
620
640
620
600
380
32T
360
340
260
260
740
720
640
620
940
680
660
560
500
480
643
100T
700
520
t;?n
860
14aO
1460
1480
1360
12?0
1489
1180
1200
1060
1100
930
900
940
1200
1440
12BO
1460
1240
1140
78.0
79.5
82.6
81.1
81.6
82.7
82.7
87.2
87.4
86.0
86.8
89.0
88.4
72.3
74.1
77.0
78. b
70.4
79.1
79.7
81.1
82.1
82.9
75.0
61.5
72.7
80.3
69.7
72. 0
52.3
56.9
5b.9
57.2
57. B
54.9
57.5
56.8
60. R
58.8
61.2
63. 7,
59.3
54.4
53.6
57. R
57. r-
60.5
56.7
CAO
WT X
23.40
28.90
29.00
27. SO
28.80
28.30
27.40
26.80
28.00
25.30
28.90
29.40
25.80
26.30
27.30
26.20
26.50
27.70
28.40
28.10
28.00
27.50
27. 3T
27.10
25.30
26.10
26.10
24.90
24.20
25.90
22. 70
23.50
53.70
24.10
24.50
23.00
22.30
23.40
23.30
24.30
24.70
24.50
24.20
22.80
23.30
24.00
21.10
23.40
S02
UT X
20.30
26.00
24.10
24.20
26.90
26.80
23.80
21.30
22. 1C
18.00
22.80
23.20
18.80
23.10
25.50
20.10
19.70
19.80
21.30
20.50
20.30
20.10
19.70
24.90
23.30
23.70
23.20
21.00
19.60
25.50
20.00
21.40
22.70
20.90
24.00
20.00
lfc.4u
20.70
21.00
24.40
25.50
22. ID
22.50
19.20
19.50
23.30
19.40
21.90
S03
UT %
2.23
2.81
1.68
0.95
2.18
1.01
1.55
1.48
1.58
o.eo
3.70
4.3C
8.50
5.53
2.93
5.08
5.88
10.25
7.78
6.18
7.63
6.28
6.28
5.06
6.68
6.18
7.20
7.25
6.30
5.B3
5.90
5.85
4.43
6.98
4.30
6.90
7.30
6.53
6.05
3.20
5.23
6.68
6.08
7.30
7.63
4.18
2.95
5.73
TOTAL S
AS 503
MT. X
27.60
35.30
31.80
31.20
35.80
34.50
31.30
28.10
29.20
23.30
32.20
33.30
32.00
34.40
34.80
30.20
30.50
35.00
34.40
31.80
33.80
31.40
30.90
36.20
35.80
35.60
36.20
33.50
30.80
37.70
30.90
32.60
32.80
33.10
34.30
31.90
30.30
32.40
32.30
33.70
34.60
34.30
34.20
31.30
32.00
33.30
23.20
33.10
CO!
yT x
3.88
4.60
6.15
6.94
5.50
4.81
7.47
8.67
8.06
10.72
3.98
6.45
6.71
3.20
2.84
5.45
5.30
3.57
4.72
4.77
3.98
3.54
5.27
1.52
1.37
2.92
2.58
2.04
3.19
0.83
1.08
1.05
0.83
1.13
0.85
1.25
1.31
1.27
1.21
1.58
1.04
0.47
0.74
1.14
1.83
1.47
1.93
0.92
SLURRY X ACID MOLE X
SOLIDS INSCLS SULFUR
UT. X IN SOLD OXIDIZED
15.6
15.2
15.3
14.7
15.1
15.2
15.1
14.7
15.1
14.3
14.2
14.3
14.7
12.9
12.9
14.7
14.2
14.5
15.0
14.2
14.4
14.7
14.1
13.9
13.2
13.3
13.7
14.7
15.5
14.5
14.1
14.6
15.0
15.5
14.6
14.5
15.2
15.0
14.8
14.7
14.2
13.4
13.7
14.6
14.2
14.9
14.6
14.9
6.52
6.02
6.26
6.21
5.85
6.33
6.28
6.38
6.23
6.65
5.88
5.33
5.68
5.37
3.56
6.32
5.97
5.25
5.51
5.64
5.56
6.14
5.76
5.86
5.68
5.45
5.51
6.42
7.13
6.10
7.03
7.02
7.30
7.13
6.88
6.96
7.50
7.09
7.14
7.05
6.50
6.14
6.33
7.07
6.56
7.15
7.90
7.11
8.1
7.9
5.3
3.1
6.1
2.9
5.0
5.3
5.4
3.4
11.5
12.9
26.6
16.1
8.4
16.8
19.3
29.3
22.6
19.4
23.1
20.0
20.3
14.0
18.7
17.3
19.9
21.7
20.5
15.5
19.1
18.0
13.5
21.1
12.6
21.6
24.1
20.2
18.7
9.5
15.1
19.5
17.8
23.3
23.8
12.6
14.0
17.3
STOICH
RATIO
1.26
1.24
1.35
1.40
1.28
1.25
1.43
1.56
1.50
1.84
1.22
1.35
1.3*
1.17
1.15
1.33
1.32
1.19
1.25
1.27
1.22
1.21
1.31
1.08
1.07
1.15
1.13
1.11
1.19
1.04
1.06
1.06
1.05
1.06
1.05
1.07
1.08
1.07
1.07
1.09
1.05
1.02
1.04
1.07
1.10
1.08
1.12
1.05
soLin
IONIC
IMBAL
-3.7
-5.8
-3.8
-10.4
-11.4
-7.1
-14.8
-14.7
-9.7
-18.5
4.4
-7.3
-20.0
-7.1
-2.5
-7.2
-6.1
-4.9
-6.0
-0.9
-0.7
3.6
-3.9
-0.7
-6.0
-10.3
-9.8
-4.7
-5.9
-6.0
-1.4
-2.9
-1.4
-2.2
-2.5
-4.1
-2.7
-3.9
-3.7
-5.4
-3.5
-0.5
-2.9
-2.5
-6.2
-5.0
-5.3
-4.1
-------
-SOLID ANALYCES AT SCRUHriER INLET-
PAGr 10
I
t_o
o
RU".
NUK^E? CATE
706-X 11/19/75
11 /19/75
11/19/70
11/19/75
11/19/75
11/20/75
11/20/75
11/20/75
11/20/75
11/20/75
11/30/75
11/20/75
11/20/75
11/20/75
11/21/75
11/21/75
11/21/75
11/21/75
7C7-1A 11/21/75
11/21/75
11/22/75
11/22/75
11/22/75
11/22/75
11/22/75
11/22/75
11/23/75
11/2^/75
11/23/75
11/23/75
11/23/75
11/23/75
11/24/75
11/24/75
11/24/75
ll/2*/75
11/24/75
11/24/75
11/25/75
11/25/75
11/25/75
11/25/75
11/25/75
11/25/75
11/26/75
11/26/75
11/26/75
708-1A 11/26/75
11/26/75
11/26/75
11/27/75
TIVE
1900
231C
23C7
2310
2311
0300
0700
HOC
150C
1510
1900
2300
2307
231C
3300
0700
0707
0710
1900
2300
H300
07"0
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
H3CO
SO?
INLTT
ppy
2960
2B8C
?4HO
2600
2600
264D
2760
32«0
3600
3800
390n
4040
3920
396<3
4040
3880
3640
34^0
3400
3200
332C
3360
3800
4170
4200
4340
4400
430D
3820
3520
3560
3120
2800
26SC
2960
2920
3000
3000
3080
3080
2840
2800
2880
ct>2 S02
C'JTLffT REMOVAL
~>PX %
1143
1140
1040
lC«n
960
1040
1060.
1320
1420
1400
1120
1060
1000
920
880
720
600
56 C
540
43U
520
540
660
780
820
760
«20
781
620
540
5^0
440
400
440
560
480
500
440
480
460
380
• 340
380
57.3
56.1
53.5
53.9
59.1
56.3
57.4
55.4
56.3
59.2
68.2
70.9
71.7
74.3
75.9
79.5
81.3
81.8
82.4
83.4
82.7
82.2
80.8
79.3
78.4
80.6
79.4
79.9
82.0
83.0
82.0
84.4
84.2
81.8
79.1
81.8
81.6
83.8
82.8
83.5
85.2
86.6
85.4
CAO
WT %
22.60
22.90
22.50
23.00
21. HO
21 .50
22.60
22.10
22.50
20.50
24.40
24.80
25.70
27.60
26.30
28.60
29.40
29.20
27.90
30.00
30.00
30.80
30.00
29.30
29. 6&
50.10
30.00
30.10
29.60
28.90
29.10
27.70
29.40
29.10
28.80
28.20
28.70
28.80
29.10
29.20
27.20
29.60
29.10
S02
WT X
19.20
19.30
18.00
21.30
18.30
17.90
19.50
20.20
20.50
19.50
22.40
21.60
21.80
24.00
22.60
22.70
21.00
22.80
24.10
23.70
20.10
24.30
23.20
21.20
20.80
26.00
24.80
25.00
24.00
18.00
22.60
23.10
23.80
23.50
23.40
22.80
23.90
23.20
23.30
23.90
24.20
22.40
20.20
SO 3
WT X
7.60
7.58
8.70
4.98
6.53
6.33
5.53
3.95
4.36
2.43
3.70
3.00
3.35
2.60
0.45
4.53
6.55
3.80
0.78
2.08
6.38
4.23
4.50
4.50
6.80
2.21
3.30
3.46
3.00
7.20
3.25
1.53
3.05
4.13
3.95
3.00
2.63
2.60
3.88
3.43
1.05
5.30
7.75
TOTAL S
AS S03
WT. X
31.60
31.70
31.20
31.60
29.40
28.70
29.90
29.20
30.00
26.80
31.70
30.00
30.60
32.60
28.70
32.90
32.80
32.30
30.90
31.70
31.50
34.60
33.50
31. OC
32.80
34.70
34. 3C
34.70
33.00
29.70
31.50
30.40
32.80
33.50
33.20
31.50
32.50
31.60
33.00
33.30
31.30
33.30
33.00
CQ2
JT X
1.03
1.03
1.13
1.32
1.60
1.31
1.31
0.54
0.38
1.16
2. 09
3.30
3.91
5.01
5.83
5.67
6.6B
6.5B
6.71
7.15
6.69
6.05
5.94
7.15
7.26
5.75
6.91
6.11
6.05
8.31
7.10
6.66
6.49
5.50
4.29
6.77
5.78
6.66
6.33
5.28
5.17
7.21
6.66
SLURRY X ACID "OLE %
SOLIDS INSOLS SULFUR
WT. % 1H SOLD OXiniZED
14.2
14.3
14.0
14.0
14.6
14.8
15.2
15.4
15.9
16.4
16.3
15.7
14.3
14.3
15.1
15.6
IS. 3
14.9
14.7
14.5
15.0
15.2
15.4
15.5
15.4
16.2
16.3
16.0
16.0
15.5
16.3
15.7
14.9
14.6
14.6
14.6
14.6
14.8
14.4
14.7
14.8
14.7
1-4.5
6.83
6.83
t.7I
6.91
7.42
7.70
7.72
ft. 24
«.35
9.43
7.84
7.56
fc.60
6.02
7.14
6.10
5.47
b.69
6.29
5.62
5.09
5.35
b.68
5.92
5.37
6.17
5.74
5.84
6.16
5.62
6.37
6.73
5.75
5.61
5.90
5.88
5.90
5.90
E.51
5.75
6.59
5.21
5.08
24.1
23.9
27.9
15.8
22. 2,
22.1
18.5
13.5
14.6
9.1
11.7
10.0
11.0
8."
1.6
13.8
20.0
11. S
2.5
6.6
20.3
12.2
13.4
14.5
20.7
6.4
9.6
10.0
9.1
24.3
10.3
5.0
9.3
12.3
11.9
9.5
8.1
8.2
11.8
10.3
3.4
15.9
23.5
STQICH
RATIO
1.06
1.06
1.07
1.08
1.10
1.0*
1.08
1.03
1.02
1.08
1.12
1.21
1.23
1.28
1.37
1.31
1.37
1.37
1.40
1.41
1.50
1.32
1.32
1.42
1.40
1.30
1.37
1.32
1.33
1.51
1.41
1.40
1.36
1.30
1.24
1.39
1.32
1.3"
1.35
1.29
1.30
1.39
1.37
SOLI1
IOMIC
I"OAL
-3.7
-2.7
-3.5
-3.6
-3.8
-1.3
-0.1
4.3
4.5
1.2
-1.9
-1.7
-2.8
-5.9
-4.7
-5.8
-7.1
-6.2
-8.?
-4.4
-10.5
-3.7
-3.4
-5.2
-8.9
-5.1
-9.4
-6.6
-4.1
-8.6
-6.9
-7.5
-6.3
-4.7
0.7
-8.8
-5.0
-6.*
-7.2
-2.9
-4.8
-9.8
-8.6
-------
-SOLID ANALYSES AT SCRUBBER INLET-
RUN
NUMDER DATE
708-lA 11/27/75
11/27/75
11/27/75
11/27/75
11/27/75
11/28/75
11/28/75
11/28/75
11/28/75
11/28/75
11/28/75
11/29/75
11/29/75
11/29/75
11/29/75
11/29/75
11/29/75
11/30/75
11/30/75
11/30/75
t) H/^0/75
1 11/30/75
<-° 11/30/75
1-1 12/01/75
12/01/75
12/01/75
12/01/75
12/01/75
12/01/75
12/01/75
12/02/75
12/02/75
709-1* 12/06/75
12/06/75
12/07/75
12/07/75
12/07/75
12/07/75
12/07/75
12/C7/75
1 2/CB/75
12/08/7b
12/08/75
12/08/75
12/38/75
12/08/75
12/09/75
12/09/75
12/09/75
12/09/75
12/09/75
TI1E
0700
1100
1500
1900
2300
0300
C700
1100
1500
1900
2330
030C
0700
1100
1500
1900
2300
0300
07CO
1100
1500
1900
230C
P300
07n()
C701
1100
1CPC
1900
2300
030"
0700
1900
230C
030"
0700
1100
15 f) "
19PD
23PC
P3HO
1700
HOC
150C
1900
2300
P30C
0700
11CO
itor
1900
S02
INLET
pp«i
2BOO
276C
2320
•2360
3360
3680
3560
3040
2ROO
26SC
2720
2800
2800
2600
2780
2720
3400
392P
4150
396fl
3960
3920
3480
4140
4040
4020
3840
3600
3720
368C
34nO
3320
3160
3460
3480
3400
3320
3760
4160
4130
411P
4400
4470
4210
4130
3800
380D
3160
3120
2930
2960
SC2
CUTLET (
PPK
400
400
320
440
820
900
800
640
680
680
6RO
700
700
600
740
610
1020
1400
1460
1380
1300
1110
700
960
900
690
800
800
880
900
760
700
760
840
7£C
720
700
10CO
1040
860
son
960
840
7CO
760
650
7?0
400
48C
420
400
S02
REMOVAL
84.2
84.0
84.7
79.4
73.0
72.9
75.1
76.7
73.1
71.9
72.3
72.3
72.3
74.4
70.5
72.3
66.8
60.4
60.5
61.4
63.6
68.6
77.7
74.3
75.3
75.5
76.9
75.4
73. S
72.9
75.2
76.6
73.4
73.1
75.8
76.5
76.6
70.5
72.3
76.9
78.4
75.3
79.2
80.0
79.6
81.1
79.0
83.2
83.0
84.1
85.1
CAO
WT X
29.30
29.20
2S.50
28.20
27.40
27.30
26.80
27.80
27.20
26.20
26.10
26.80
26.40
26.40
26.40
24.90
25.80
25.40
25.30
23.60
25.10
24.30
24.60
25.70
26.20
27.40
26.30
26.20
25.60
25.50
25.70
26.40
25. «0
26.80
?7.00
26.90
26.80
26. bO
26.60
27.40
27.50
28.00
28.80
29.10
29.10
29.10
29.30
29.30
29.70
30.20
30.20
S02
WT X
20.30
20. BO
18.00
21.30
21.00
23.10
21.30
21.70
23.60
23.20
22.00
25.10
21.20
20.80
24.80
21.70
22.90
22.10
26.10
20.40
26.20
24.00
20.80
22.80
23.90
22.10
23.30
22.40
22.30
24.20
22.60
25.30
21.40
22.70
22.50
20.60
21.30
21.60
21.50
20.10
20.20
20.60
21.20
23.60
22.80
21.60
22.90
20.30
19.70
24.70
23.10
S03
WT %
6.83
8.20
10.00
4.58
b.05
4.73
5.78
6.78
4.90
4.40
5.50
3.73
8.40
8.30
3.90
4.08
5.48
6.58
2.48
5.70
1.36
3.00
5.40
3.40
2.63
4.98
2.48
5.10
3.93
1.45
3.35
2.08
4.45
3.23
3.78
4.75
4.28
4. &0
4.73
5.88
6.45
4.55
5.10
2.70
3.20
4.20
3.78
5.83
4.38
3.63
5.T3
TOTAL S
AS S03
«T. X
32.20
34.20
32.50
31.20
31.30
33.60
32.40
33.90
34.40
33.40
33.00
35.10
34.90
34.30
34.90
31.20
34.10
34.20
35.10
31.20
34.10
33.00
31.40
31.90
32.50
32.60
31.60
33.10
31.80
31.70
31.60
33.70
31.20
31.60
31.90
30.50
30.90
31.50
31.60
31.00
31.70
30.30
31.60
32.20
31.70
31.20
32.40
31.20
29.00
34.50
33.90
C021
WT X
6.64
4.58
5.78
6.77
5.78
4.79
5.29
3.16
3.05
3.17
4.24
3.47
3.11
2.90
2.34
2.94
3.41
2.81
1.23
0.84
2.15
2.42
3.25
3.80
3.04
4.66
4.16
2.80
3.26
3.30
3.47
3.08
4.90
3.76
4.04
5.12
5.23
4.84
4.95
5.59
5.84
6.16
6.22
5.03
6.69
7.50
6.47
9.16
9.57
6.27
7.37
SLURRY
SOLIDS
WT. X
14.2
14. i
14.0
13.9
14.4
14.8
14.7
14.9
14.5
14.4
14.8
13.9
14.3
14.3
14.9
15.6
15.3
14.8
15. G
15. 1
15.0
15.3
15.5
15.1
15.4
14.7
14.9
15.4
15.0
14.7
14.2
14.4
12.5
13.4
14.8
15.1
14.8
14.4
15.5
15.1
15.9
16.6
16.0
15.5
14.7
14.8
15.1
14.5
14.4
14.5
15.0
X ACID
INSOLS
IN SOLD C
5.14
5.11
5.85
5.47
5.88
6.00
5.95
5.89
6.05
6.28
6.22
b.84
5.68
5.75
6.47
7.31
6.52
6.31
7.01
7.98
7.11
7.25
7.14
6.85
7.02
6.01
6.77
7.23
6.82
7.01
6.51
6.48
5. 48
5.97
6.47
6.46
6.33
6.16
6.53
6.13
6.25
6.76
6.19
6.16
5.73
5.64
5.76
b.07
5.29
MOLE X
SULFUR
IXIDIZED
21.2
24.0
30.9
14.7
16.1
14.1
17.8
20.0
14.3
13.2
16.7
10.6
24.1
24.2
11.2
13.1
16.1
19.2
7.1
18.3
4.0
9.1
17.2
10.7
8.1
15.3
7.8
15.4
12.4
4.6
10.6
6.2
14.3
10.2
11.8
15.6
13.8
14.3
15.0
19.0
20.4
15.0
16.2
8.4
10.1
13.5
11.7
18.7
15.1
10.5
14.8
STOICH
RATIO
1.38
1.24
1.32
1.39
1.34
1.26
1.30
1.17
1.16
1.17
1.23
1.18
1.16
1.15
1.12
1.17
1.1"
1.15
1.06
1.05
1.11
1.13
1.19
1.22
1.17
1.26
1.24
1.15
1.19
1.19
1.20
1.17
1.29
1.22
1.23
1.31
1.31
1.29 -
1.28
1.33
1.34
1.37
1.36
1.28
1.38
1.44
1.36
1.53
1.60
1.33
1.40
SOLIT
IONIC
IIBftL
-5.9
-2.0
-5.7
-8.1
-6.9
-8.6
-9.8
0.1
-2.9
-4.7
-9.3
-8.2
-7.6
-•5.0
-3.9
-2.8
-9.4
-8.4
-3.4
2.9
-6.1
-7. a
-6.2
-5. a
-1.7
-5.0
-4.3
-2.1
-3.2
-3.6
-3.3
-4.3
-8.9
-0.5
-1.8
-3.7
-5.6
-6.5
-6.9
-5.2
-7.8
-3.8
-4.4
0.5
-5.6
-7.9
-5.6
-14.4
-9.5
-6.5
-9.7
-------
-SOLID ANALYSES AT SCRUBOER INLET-
O
I
U)
"LK
7 C) ° - 1. 8 12/09/75
12/10/75
12/10/75
12/10/75
12/10/75
12/10/75
12/10/75
12/11/75
12/11/75
12/11/75
12/11/75
12/11/75
12/11/75
12/11/75
12/11/75
12/11/75
12/12/75
12/12/75
12/12/75
12/12/75
710-1/1 12/12/75
12/12/75
12/12/75
12/12/75
12/13/75
12/13/75
12 '1^/75
12/13/75
12/13/75
12/13/75
12/13/75
12/13/75
12/13/75
12/11/75
1 2/11/75
12/14/75
12/11/75
12/14/75
12/11/75
12/14/75
12/15/75
12/15/75
12/15/75
12/15/75
12/15/75
12/15/75
12/15/75
12/15/75
12/16/75
12/16/75
12/16/75
SC2 v)2 S02
INL^T OUTLET REMOVAL
7 I Mr PP •* P P V %
23"0
0300
0700
HOC
15C?
1900
2300
0300
070C
HOP
150 P
1537
1900
2300
23"!
2307
0300
0700
f, 707
1600
1500
1601
1900
2300
0300
0700
1100
1500
1501
1502
1900
23T 1
2301
0300
0701
1100
1500
1501
1902
2300
C3DO
0700
1100
1500
1501
1900
2300
2301
P3PO
07CO
P701
34PP
366C
3 4 a P
362C
3320
32?0
3320
3320
3920
3POO
352P
352"
3320
334"
3000
2860
34HO
3580
3720
372"
3760
388(1
3600
3440
3400
3180
3100
3160
3280
3840
3360
3400
3400
3000
2920
2840
3480
3320
352C
3560
3400
3240
3340
3720
3520
3540
520
620
64C
700
5 "<0
460
1£0
460
660
680
620
6pn
f,cn
600
Ifli
16C
6fiO
730
780
740
620
62 C
480
500
480
500
Iflfl
470
460
680
5RO
560
550
400
340
300
440
3«0
360
360
320
280
320
420
320
330
83.5
81.2
79.
WT X
19.90
22.70
26.10
21.20
22.70
22.70
23.60
23.50
25.90
19.20
25.10
22.80
22.20
22.20
22.30
20.00
24.40
24.30
19.40
20.60
17.30
21.90
20.70
22.00
21.90
21.80
20.30
20.20
20.50
20.40
18.40
21.40
21.40
23.30
21.70
20.70
19.80
22.10
19.80
20.00
18.90
20.10
20.20
21.90
23.10
23.40
SO?
WT %
7.33
5.33
2.28
5.90
5.53
5.63
2.00
3.63
5.23
6.90
4.53
4.80
3.25
3.15
4.03
1.90
7.20
1.53
11.55
1.15
4.08
6.13
8.53
2.00
9.73
8.35
2.13
4.95
1.18
3.80
4. CO
4.55
4.45
3.18
5.08
3.43
3.05
3.68
4.25
4.00
5.08
7.48
4.55
2.83
1.43
1.75
TOTAL S
AS S23
d T . X
32.20
33.70
34.90
32.40
33.90
31.00
31.50
33.00
37.60
30.90
35.90
33.30
31.00
30.90
31.90
26.90
37.70
31.90
35.80
26.90
25.70
33.50
34.40
29.50
37.10
35.60
27.50
30.20
26.80
29.30
27.00
31.30
31.20
32.30
32.20
29.30
27.80
31.50
29.00
29.00
28.70
32.60
29.80
30.20
30.30
31.00
C02
UT X
8.20
6.99
3.60
5.49
6.54
6.43
6.00
6.44
4.30
6.65
6.33
6.00
6.82
6.82
6.82
5.48
4.58
4.58
5.79
6.55
8.42
7.15
7.05
7.58
7.58
7.54
8.14
8.14
9.02
8.09
9.19
7.23
7.23
7.07
8.20
9.35
9.26
9.44
9.08
9.08
10.26
10.29
10.29
8.86
10.34
9.98
SLURRY X ACID "OLE X
SOLIDS IMSCLS SULFUR
UT. X IN SOLO OXIDIZED
15.3
15.8
15.2
16.1
15.7
15.1
15.1
15.3
15.0
15.2
14.9
15.1
15.1
15.0
14.9
14.3
14.3
14.2
16.1
17.4
17.1
15.8
15.3
15.5
16.0
16.0
16.0
16.1
16.0
16.0
16.3
15.3
13.9
13.9
16.5
16.7
16.1
16.1
15.1
15.5
15.5
5.23
5.58
5.98
5.96
5.81
6.99
4.56
6.06
4.32
7.53
7.44
5.97
5.10
4.5.3
4.89
6.R4
5.86
6.54
6.38
6.67
6.50
6.81
5.39
5.33
5.18
5.97
5.66
4.63
5.29
5.37
5.34
5.25
22.8
15.8
6.5
18.2
16.3
16.6
6.4
11.0
13.9
22.3
12.6
14.4
10.5
10.2
12.6
7.1
19.1
4.8
32.3
4.3
15.9
18.3
24. R
6.8
26.2
23.5
7.7
16.4
4.4
13.0
14.8
14.6
14.3
9.8
15.8
11.7
11.0
12.3
14.7
13.8
17.7
22.9
15.3
9.4
4.7
5.7
C,TOICH
RATIO
1.46
1 .3"
1.19
1.31
1.35
1.34
1.35
1.36
1.21
1.39
1.32
1.33
1.40
1.40
1.39
1.37
1.22
1.26
1.29
1.44
1.60
1.39
1.37
1.47
1.37
1.39
1.54
1.49
1.61
1.50
1.62
1.42
1.42
1.40
1.46
1.58
1.61
1.55
1.57
1.57
1.65
1.57
1.63
1.53
1.62
1.59
SOLI^
IONIC
I"BAL
-10.0
-11.0
-1.5
-3.1
-12.6
-9.2
-2.1
-6.5
-5.n
-8.7
-9."*
-6.1
-5.2
-3.9
-7.3
4.0
-2.7
2.1
-9.6
-1.5
-4.9
-10.1
-10.6
-1.8
-22.5
-17.5
-4.7
-5.1
-1.2
-8.2
-13.4
-17.5
-3.9
-22.6
-10.8
-11.5
0.7
0.9
-3.2
1.3
-5.0
-11.6
-5.9
-1.7
-6.5
-5.6
-------
PAGE 13
-SOLID ANALYSES AT SCRUBBED INLET-
d
OO
U>
"UN
NUKPER CATC
71P-1A 12/16/75
12/16/75
12/16/75
12/16/75
12/16/75
12/16/75
12/17/75
12/17/75
12/17/75
12/17/75
12/17/75
12/17/75
12/17/75
12/17/75
12/18/75
12/18/75
12/18/75
12/18/75
12/18/75
12/18/75
12/19/75
12/19/75
12/19/75
12/19/75
12/19/75
12/19/75
12/19/75
12/10/75
12/20/75
12/20/75
12/20/75
12/20/75
12/20/75
12/2C/7r,
12/20/75
12/21/75
12/21/75
12/^1 /75
12/21/75
12/21/75
12/21/75
12/21/75
12/71/75
12/21/75
12/22/75
12/22/75
l?/22/75
12/22/75
711-1« 12/24/75
12/24/7E
12/?4/75
TIME
1100
1500
1501
1900
230C
2301
0300
0700
1100
15CO
1501
1900
2300
23P1
0300
0700
1100
1500
19CC
2300
03DU
C3C1
0700
0701
1100
15Cfi
1900
2300
?300
0700
0701
1100
1500
19CO
2300
0300
0700
0701
1100
1500
1700
1900
21CO
23CO
MOO
0300
05CO
H7CC
150C
i^or
23PO
S02 S02
INLET OUTLFT
P°P FPM
3480
3480
3420
3320
34BO
3500
372C
3720
34PO
3P4P
392C
3560"
2S80
2840
2680
2440
2480
2280
2800
2640
2880
2960
30»0
3080
34PO
2960
2880
3000
3040
2880
2900
2800
2960
328H
328C
3400
3400
344(1
3040
3120
3200
3440
3600
392H
392°
40CC
3880
3«80
sono
2800
26RP
38P
400
3^0
340
42C
410
440
400
4fiO
460
480
320
200
190
1RO
140
160
200
300
240
320
360
360
350
410
3f!0
160
140
130
170
175
1.20
100
303
300
340
340
330
320
360
520
640
640
700
700
700
64C
640
560
44C
400
S02
REMOVAL
X
87.9
87.3
87.4
' '8P.7
86.7
87.0
8 6 »*3
88.1
87.3
86. R
86.5
90.1
92.3
92.6
92.6
93.7
92.9
90.3
88.2
90.0
87.7
86.6
87.1
87.4
86.7
88. 1
93.9
94.9
95.3
93.5
93.4
95.3
96.3
89.9
85.9
89.0
89.0
89.4
88.4
87.2
82.0
79.4
80.3
80.2
80.2
80.6
81.7
81.7
79.?
82.6
83.5
CAO
WT X
32.10
31.80
32.00
31.60
31.70
32.00
31.20
31.20
31.30
30.70
31.30
30.80
30.80
24.00
SO.ftO
31.10
30.90
33.20
32.70
29.80
30.00
22.90
29.90
22.90
29.50
29.90
30.00
30.80
30.30
30.10
29.90
30.10
30.50
29.80
30.00
30.60
30.30
31.80
30.70
29.50
27.80
26.40
26.70
27.10
26.90
26.60
27.30
36.70
26.90
27.00
26.80
S02
UT X
22.00
23.20
23.30
19.40
20.80
20.80
lfi.40
18.40
22.20
22.10
22.00
21.90
20.50
21.30
21.70
19.30
1H.40
21.10
19.00
IP. 20
18.00
18.70
19.50
21.60
20.60
19.40
19.70
18.10
17.30
19.90
19.90
20.20
21.80
20.10
22.00
21.90
20.50
20.50
22.90
22.60
24.40
18.30
24.70
25.60
24.70
21.40
25.40
33.50
22.90
23.00
22.00
S03
UT %
2.3C
1.70
4.18
4.35
4.00
7. 1C
4.50
4.50
2.05
t.78
3.70
0.43
4.28
5.98
1.78
3.48
3.90
1.83
3.C5
3.05
3. CO
4.53
3.13
1.70
2.55
4.35
3.38
4.t8
6.08
3.73
6.73
3.95
3.45
3.78
2.2C
3.43
3.18
6.78
2.68
2.75
2.30
7.53
2.C3
1.41
2.23
3.85
1.86
2.53
2.R8
2.85
3.10
TOTAL S
AS S03
UT. X
29.80
30.70
33.30
26.60
30.00
33.10
27.50
27.50
29.80
29.40
31.20
27.80
29.90
32.60
28.90
27.60
26.90
28.20
26.80
25.80
25.50
27.90
27.50
28.70
28.30
28.60
28.00
27.50
27.70
28.60
31.60
29.20
30.70
28.90
29.70
30.80
23.80
32.40
31.30
31.00
32.80
30.40
32.90
33.40
33.10
30.60
33.60
44.40
31.50
31.60
30.60
C021
UT X
10.05
7.63
7.63
7.88
8.25
8.25
10.20
10.13
10.17
8.14
8.14
8.25
8.75
1.36
9.27
10.70
10.80
8.04
8.71
8.36
8.36
1.95
7.69
1.02
6.13
9.40
7.48
H. 66
8.61
8.91
8.91
8.42
8.14
9.24
6.91
7.87
8.26
8.26
9.07
7.26
4.76
4.68
3.94
3.92
4.21
4.33
4.12
4.31
4.84
5.01
5.86
SLURRY X ACID «OLE X
SOLIDS 1NSOLS SULFUR
WT. X IN SOLO OXIDIZED
16.0
15.4
15.3
15.8
15.8
16.4
16.1
16.1
15.6
15.6
14.9
14.9
14.5
15.8
15.5
14.6
14.6
14.9
14.6
13.9
14.6
15.7
14.6
14.7
15.0
15.1
14.9
14.3
14.3
7.9
14.8
14.2
14.5
14.9
14.9
14.9
14.5
13.5
12.8
14.1
14.9
16.3
15.7
15.3
14. -i
5.59
5.78
5.60
5.63
4.87
5.81
5.73
5. 75
6.08
6.36
5.43
5.98
5.62
b.45
5.38
4.80
2.97
5.47
5.30
3.83
5.52
5.72
4.73
5.20
5.26
5.32
6.23
7.01
7.24
6.84
£.66
6.43
7.7
5.6
12.6
15.2
13.3
21.5
16.4
16.4
6.9
6.1
11.9
1.5
14.3
18.3
6.2
12. £
14.5
6.5
11.4
11.8
11.8
16.2
11.4
5.9
9.0
15.2
12.1
17.7
21.9
13.0
21.3
13.5
11.3
13.1
7.4
11.1
11.0
20.9
».6
8.9
7.0
24.8
6.2
4.2
6.7
12.6
5.5
5.7
9.1
9.0
10.1
STOICH
RATIO
1.61
1.45
1.42
1.50
1.50
1.45
1.67
1.67
1.62
1.50
1.47
1.54
1.53
l.OS
1.58
1.71
1.73
1.52
1.59
1.59
1.60
1.13
1.51
1.06
1.39
1.60
1.49
1.57
1.57
1.57
1.51
1.52
1.49
1.58
1.42
1.46
1.52
1.46
1.53
1.43
1.26
1.28
1.22
1.21
1.23
1.26
1.22
1.18
1.28
1.2"
1.35
SOLin
IONIC
IMBAL
-4.9
1.8
-3.3
5.4
0.5
-5.!!
-3.4
-3.1
-8.1
-0.9
-3.0
2.6
-4.3
-2.4
-4.1
-6.0
-5.5
9.6
8.6
3.6
5.0
3.8
2.8
6.5
6.3
-7.1
2.9
1.6
-0.2
-4.3
-12.0
-3.6
-4.5
-7.4
1.3
-3.3
-1.3
-4.5
-9.1
-5.0
-4.5
-3.2
-5.1
-4.8
-6.1
-1.3
-5.4
0.3
-5.0
-5.6
-7.8
-------
PAGE
-SOLID ANALYSES AT bCRUBE'ER INLET-
d
I
RUI^
NUPPER CATF
Ill-It 12/25/75
12/25/75
12/25/75
12/25/75
12/25/75
12/25/75
12/26/75
12/26/75
12/26/75
12/26/75
12/P6/75
12/26/75
l?/27/75
12/27/75
12/27/75
12/27/75
12/27/75
12/27/75
12/28/75
12/?8/75
12/28/75
12/28/75
12/28/75
12/28/75
12/29/75
12/29/75
12/29/75
12/29/75
12/29/75
12/29/75
12/30/75
12/30/75
12/30/75
12/30/75
12/31/75
711-16 12/30/75
12/30/75
12/30/75
12/31/75
12/31/75
12/31/75
12/31/75
12/31/75
12/31/75
01/01/76
01/01/76
01/01/76
01/01/76
01/01/76
01/01/76
01/02/76
TIfE
03CO
0700
1100
15CO
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
150C
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
150-0
1900
2300
0300
0700
0701
1100
1237
1500
1900
2300
0300
0700
1100
1500
I960
Z3PO
0300
07CO
1100
1500
19CO
2300
0300
scr so? S02
INLET CUTLET REMOVAL
PPH PPM X
2610
2610
26°P
272C
3160
3ROO
3680
3*10
3560
36PO
3520
2960
2800
2880
2800
252C
2520
2810
2680
?840
284U
3140
3320
3600
3840
3720
3520
3080
2960
3000
3400
3400
3*00
3280
3120
3040
3000
3100
3000
3080
2*80
2520
2460
2920
2960
2840
2fl80
3640
400
340
340
340
''40
64r
560
440
410
430
4?n
38C
420
44f
3dP
350
440
540
44P
540
620
820
840
800
940
9£0
800
600
560
660
780
720
7?0
640
780
520
500
500
500
580
380
380
380
460
520
440
440
840
83.2
85.8
86.0
86.2
84.6
81 .4
83.2
85.9
86.3
85.6
86.8
85.8
83.4
83.1
85.0
84.6
80.7
78.9
81.8
78.9
75.8
71.1
72.0
75.4
72.9
71.4
74.8
7fc.4
79.1
75.6
74.6
76.5
76.5
78.4
72.3
81.1
81.6
82.1
81.6
79.1
83.0
83.3
82.9
82.6
80.6
82.9
83.1
74.4
cso
WT *
27.60
2P.BO
27.90
.29.60
29.30
26.30
28.50
29.40
29.60
29.40
28.80
28.80
28.30
28.30
27.70
28.10
27.20
26.20
26.60
?5.60
24.60
25.70
25.70
26.20
26.10
25.70
25.50
25.80
25.40
25.30
26.30
26.60
26.00
25.80
25.30
23.30
26.40
26.70
25.80
24.10
25.90
25.90
26.00
26.30
27.00
27.90
28.00
27.50
SO?
WT x
23.70
22. 7C
24.00
24.00
19.00
21.60
25.30
21.60
26.00
25.30
22.70
22.30
20.70
19.40
16.60
21.20
21.10
19.00
18.70
20.90
21.00
23.30
22.30
20.60
22.50
22.80
22.30
23.80
16.40
20.00
21.80
19.00
18.80
17.30
22.90
17.30
18.60
18.70
19.90
15.90
15.20
15.20
16.50
18.30
18.00
15.00
20.10
21.90
S03
WT x
2.68
4 . f 3
1.90
4.10
7.25
6.40
1.98
6.30
1.01
1.68
1.43
2.63
3.43
6.85
7. Ob
2.80
0.93
4.85
6.53
4.38
2.05
3.08
4.03
4.65
3.18
2.60
2.43
0.65
5. CO
2.80
2.05
3.75
3.60
5.08
1.53
3.98
3.65
3.63
2.03
2.73
4.90
4.90
4.98
3.43
4.10
4.85
3.48
2.83
TOTAL S
AS SC3
WT. X
32.30
32.90
31.90
34.10
31.00
33.40
33.60
33.30
33.50
33.30
29.80
30.50
29.30
31.10
27.80
29.30
27.30
23.60
23.90
30.50
28.30
32.20
31.90
30.40
31.30
31.10
30.30
30.40
25.50
27.80
29.30
27.50
27.10
26.70
31.40
25.60
26.90
27.00
26.90
22.60
23.90
23.90
25.60
26.30
26.60
23.60
28.60
30.20
C02
WT X
4.79
b.78
6.69
5.83
7.98
5.39
4.29
6.82
6.91
5.95
6.26
6.8S
6.01
6.89
7.31
6.22
7.31
3.87
4.22
2.67
2.36
2.63
3.05
4.79
4.13
3.40
4.02
3.32
6.15
5.06
4.46
5.45
5.50
6.33
2.75
4.17
5.93
5.46
5.56
7.87
5.85
5.85
5.19
6.10
7.43
7.98
7.05
5.83
SLURRY % ACID MOLE X
SOLIDS 1NSCLS SULFUR
WT. X IN SOLD OXIDIZED
15.3
16.2
14.8
17.9
14.6
16.1
16,. 2
14.4
14.7
14.3
14.9
14.5
13.6
14.1
15.3
15.0
13.6
13.0
13.9
14.2
14.6
14.9
14.7
14.9
14.9
14.2
15.0
14.7
14.9
lb.3
15.3
lb.6
15.6
14.7
15.1
16.1
15.8
15.0
14.6
15.6
14.8
14.0
13.7
14.6
15.6
14.7
15.4
15.3
6.49
6.22
6.10
6.64
5.13
6.09
6.77
5.08
5.71
£.68
6.31
5.88
5.75
5.30
6.07
6.44
6.17
5.98
E.96
fc.63
7.50
6.90
6.70
6.52
6.75
6.63
7.06
7.19
6.95
7.30
7.17
7.09
7.23
6.62
7.29
7.72
7.20
6.90
7.0£
7.76
7.05
6.66
6.43
6.73
6.79
6.40
6.46
6.61
8.3
13.8
6.0
12.0
23.4
19.2
5.9
18.9
3.0
5.0
4.8
8.6
11.7
22.0
25.4
9.6
3.4
17.0
21.8
14.4
7.3
9.6
12.6
15.3
10.2
3.4
8.0
2.2
19.6
10.1
7.0
13.7
13.3
19.0
4.9
15.5
13.6
13.4
7.5
12.1
20.5
20.5
19.4
13.0
15.4
20.6
12.2
9.4
STOICH
RATIO
1.27
1.32
l.Jfl
1.31
1.47
1.29
1.23
1.37
1.38
1.33
1.38
1.41
1.37
1.40
1.4B
1.39
1.49
1.25
1.26
1.16
1.15
1.15
1.17
1.29
1.24
1.20
1.24
1.20
1.44
1.33
1.28
1.36
1.37
1.43
1.16
1.30
1.40
1.37
1.3«
1.63
1.45
1.45
1.37
1.42
1.51
1.62
1.45
1.35
SOLII
IONIC
It*bAL
-4.1
-5.6
-10.6
-5.H
-8.8
-6.9
-1.8
-8.9
-9.C
-5.1
-0.2
-4.6
0.4
-8.0
-3.9
-1.?
-4.6
4.7
1.0
3.3
7.2
-0.8
-2.1
-4.6
-4.2
-1.6
-3.3
1.1
-1.2
-2.5
0.4
1.5
0.0
-3.8
-0.8
0.?
0.0
3.1
-0.5
-7.3
6.6
6.6
5.6
0.4
-4.1
4.3
-3.6
-3. 9
-------
PAG*: 15
-SOLID ANALYSES ftT SCRUBBER INLET-
d
oo
Ul
"UN
NUMBER
711-1B
71S-1A
712-1R
713-1 A
GATE
01/02/76
01/02/76
01/02/76
fl/02/76
01/02/76
01/03/76
"1/03/76
P1/OV76
01/03/76
01/01/76
0,1/03/76
01/04/76
0,1/04/76
01/04/76
01/04/76
01/04/76
01/04/76
01/05/76
0,1/05/76
01/05/76
ni/05/76
01/05/76
01/05/76
Gl/06/76
01/06/76
Hl/06/76
01/06/76
01/06/76
01/06/76
PI/06/76
fl/07/76
Tl/07/76
fl/07/76
01/07/76
01/07/76
T 1/07/76
01/07/76
01/08/76
01/08/76
01/08/76
01/08/76
01/08/76
01/03/76
PI/08/76
01/08/76
01/08/76
01/08/76
01/08/76
01/08/76
01/08/76
PI/08/76
TIME
0700
1100
1500
1300
2300
0300
0700
1100
1-500
1900
2300
030C
0700
HOC
1500
1900
2300
0300
0700
1100
1500
19CC
2300
C3CO
070.0
07C1
1100
1500
1900
23 OC
03CC
C7nr
1100
2200
223G
2300
2330
0000
003C
PICO
0130
0200
02JO
P30 3
G33C
0400
043C
C50C
053"
1100
15CO
S02 S02 SO?
INLET OUTLET REMOVAL
PPM PPM X
3280
2640
2560
26P.O
2800
3200
3200
3200
3120
3560
3760
3720
3260
3520
3440
2920
3200
3200
3200
3080
3880
3440
2680
2600
,?720
->880.
3000
3200
3360
340C
36PQ
30PO
680
380
340
360
420
3JJC
400
340
280
380
500
460
360
500
400
240
280
275
31"
360
600
400
100
1?C
100
140
160
2sn
360
500
600
740
77.0
84.1
85.3
84.7
83.4
86.9
86.2
88.3
90.1
88.?
85.3
86.3
87.9
84.3
87.1
90.9
90.3
90.5
89.3
87.1
&2.9
87.1
95.9
94.9
96.0
94.7
94.1
90.?
88.2
83.7
81.6
73.4
CAO
ilT X
27.30
29.10
29.80
29.30
29.80
29.80
28.60
30.10
30.00
28.50
28.00
28.50
23.70
29.30
?9.90
31.30
32.10
32.30
32.90
31.90
30.80
30.10
36.00
35.30
34.20
32. 9C
31.90
31.40
30.80
29.40
29.00
27.60
25.70
24. 7C
23.70
22. BG
22.80
21.80
24.50
23.50
S02
WT X
25.30
24.20
24.30
18.00
19.50
18.60
21.80
19.70
19.20
16.70
23.50
20.30
18.70
19.00
22.70
19.80
19.60
19.70
20.80
20.40
19.90
24.00
13.30
14.60
15.30
15.60
17.20
17.60
19.60
19.90
20.10
20.90
21.60
21.30
21.40
22.30
21.40
21.10
16.50
19.50
SOS
yy x
3.18
2.45
0.93
4.10
4.03
5.85
0.95
3.68
4.70
4.93
0.43
3.33
2.03
5.25
2.13
5.25
3.80
3.68
3.90
3.30
5.43
1.60
3.98
3.45
3.48
3.40
3.00
2.80
2.00
2.23
3. Ob
2.18
1.40
2.48
1.6S
0.73
1.05
0.03
3.98
1.63
TOTAL S
AS SOS
yT. X
34.80
32.70
31.30
26.60
28.40
29.10
28.20
23.30
28.70
25.80
29.80
28.70
25.40
29.00
30.50
30.00
28.30
28.30
29.90
28.80
30.30
31.60
20.60
21.70
22.60
22.90
24.50
24.80
26.50
27.10
28.20
28.30
28.40
29.10
28.40
28.60
27.80
26.40
24.60
26.00
CO^
yT x
3.14
4.93
8.11
7.97
8.68
9.13
7.42
10.23
9.85
9.13
5.04
8.75
9.71
8.30
7.06
11.07
11.54
11.38
10.88
9.08
8.53
6.34
19.25
17.82
17.05
15.62
14.19
12.98
11.44
9.90
8.58
7.32
4.68
4.12
3.32
1.97
1.31
1.23
4.46
3.07
SLURRY X ACID HOLE X
SOLIUS INSOLS SULFUR
yT. X IN SOLO OXIDIZED
15.6
15.1
14.7
lb.0
15.2
15.2
15.1
15.5
16.3
15.2
13.1
15.2
14.9
14.6
15.6
13.9
15.2
15.8
14.9
15.7
15.5
16.7
13.9
15.3
14.0
£.62
6.16
5.76
6.07
5.78
5.46
6.52
5.69
5.85
6.13
5.95
6.07
6.25
b.04
5.05
5.37
5.47
6.17
4.99
6.71
7.73
7.50
9.1
7.5
3.0
15.4
14.2
20.1
3.4
13.0
16.4
19.1
1.4
11.6
8.0
18.1
7.0
17.5
13.4
13.0
13.1
11.5
17.9
5.1
19.3
15.9
15.4
14.9
12.3
11.3
7.6
8.2
10.9
7.7
4.9
8.5
5.8
2.6
3.8
0.1
16.2
6.3
STOTCH
KATIO
1.16
1.27
1.47
1.55
1.57
1.57
1.48
1.66
1.62
1.64
1.31
1.55
1.70
1.52
1.42
1.67
1.74
1.73
1.66
1.57
1.51
1.36
2.70
2.49
2.37
2.24
2.05
1.95
1.79
1.66
1.55
1.47
1.30
1.26
1.21
1.13
1.10
1.08
1.33
1.21
soLin
IONIC
IMBAL
-3.9
-0.3
-8.3
1.7
-4.7
-7.4
-2.1
-9.2
-8.9
-4.?
2.5
-9.7
-5.1
-5.4
-1.5
-12.2
-7.6
-6.3
-5.8
0.5
-4.2
-0.4
-8.2
-7.4
-9.8
-9.3
-10.5
-8.0
-7.6
-7.5
-5.3
-5.6
-0.6
-3.8
-l.rt
1.1
6.2
8.0
6,5
5.9
-------
-SOUL) ANALYSES AT SCRUOfcER INLET-
O
i
oo
o
PUN
NUf^EP C«TE
713-1A 01/08/76
rl/08/76
C1/G9/76
Cl /09/76
"1/09/76
'••1/09/76
01/09/76
"1/09/ /ft
"1/10/76
r 1/10/76
'1/1C/76
711-1A 01/19/76
"1/19/76
"1/20/76
"1/20/76
''1/20/76
I1 1 / 2 0 / 7 6
Cl/20/76
01/20/76
f: 1/20/76
"1/21/76
n 1/71/76
Cl/21/76
01/21/76
"1/21/76
PI/21/76
Cl/22/76
PI/22/76
01/22/76
01/22/76
"1/22/76
01/22/76
Cl/22/76
n/23/76
f 1/2^/76
01/23/76
r' 1 / 2 3 / 7 6
"1/2^/76
Pl/2'/76
01/21/76
•'1/21/76
PI/21/76
ri/21/76
"1/21/76
ri/21/76
f 1/25/76
"1/25/76
''1/25/76
01/25/76
"1/25/76
;7 1/25/76
SO;.' C02 S02
TNLFT CUTLET REMOVAL
Y j j* f.* PPM Ppf^ x
1900
2300
D3Pf
0700
1100
1500
1900
2300
03 CO
C7CC
1100
1900
2300
03 Od
0700
0701
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
03 on
0301
0700
1100
1500
1900
23GO
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
230C
0300
P7CO
HOC
1500
1900
230?
2760
2680
280?
3010
2920
2880
3000
2960
2960
3080
3080
3080
28PO
2880
2810
2820
3110
3800
3BOD
388P
3560
2BOO
2360
2280
3200
3280
3010
3P10
2SRP
2680
256T
2800
2P10
3520
368P
3210
2800
?8in
2610
261P
2610
2720
2560
?210
?36P
2ROO
3000
321T
2R8C
2800
27 6f
500
6SC
£Qp
520
700
76t
7P.C
760
R10
fiOP
810
600
120
100
100
1 20
260
210
21P
160
80
70
150
200
360
100
210
215
150
170
270
13°
3?0
610
7rn
560
320
320
170
150
110
110
160
150
210
390
100
500
310
250
300
79.9
72.7
76.3
81.1
73.1
70.8
71.2
71.6
68.6
71.2
69.8
78.1
95.3
96.2
96.1
96.1
91.7
93.0
93.9
95.5
97.6
97.3
93.0
90.3
87.6
86.5
92.1
92.2
91.3
93.0
88.3
83.0
87.5
80. ft
78.3
80.9
87.1
87.5
92.9
93.7
91.2
91.3
93.1
92.6
88. P
81. b
85.3
82. 4
86.9
90.1
88.0
CAO
WT *
22.10
22.30
2 3 . 0 0
22.50
21.20
21.00
23.90
25.10
21.90
21.10
21.50
26. 7U
29.10
29.00
29.60
2 9. .60
?9.00
2&.yo
30.30
28.80
29.90
28.50
28.7:;
28.60
28.10
28.10
27.90
26.80
28.30
2.°. 10
27.50
26.80
27.70
26.83
26.00
26.50
27.00
27.30
2P.10
29.90
29.00
29.10
29.00
28.70
26.90
32.70
27.30
26.70
26.20
26.60
27.10
so;-
UT X
17.10
18.50
16.90
IE. 00
20.90
20.00
19.00
23.50
£1.30
22.20
22. 1C
21.00
22.80
19.70
22.80
22.70
23.50
21.00
23.90
22.20
22.80
22.10
21.10
19.00
20.00
22.50
20.00
19.20
22.90
23.20
20.50
20.10
20.20
19.20
23.10
20.30
21.50
21.10
23.60
22.90
25.10
21.10
25.00
19.10
16.30
21.00
19.60
18.80
22.50
20.20
22.10
SOS
1.43
1.J8
6.68
1.00
3.86
6. 1C
6.15
1.13
6.58
3.35
2.78
1.15
2.00
3.98
3.80
3.93
3.73
5.30
7.73
7.35
6.20
5.98
5.63
6.15
1.90
2.98
1.50
6. 1C
3.18
3.6C
5.U8
1.58
1.95
6.10
2.75
6.93
2.88
3.18
3.70
7.28
3.13
1.58
1.16
7.25
7.13
7.35
6.90
6.00
2.78
5.85
1.00
TOTAL S
AS SD3
WT. X
25.80
27.10
27.80
26.53
30.00
31.10
30.20
33.50
33.20
31.10
30.10
30.70
30.50
28.60
32.30
32.30
33.10
35.30
37.60
35.10
31.70
33.60
32.00
30.20
29.90
31.10
29.50
30.10
32.10
32.60
30.70
30.10
30.20
30.10
32.00
32.30
33.50
33.30
33.20
35.90
31.50
31.70
35.10
31.50
27.80
33.60
31.10
29.50
30.90
31.10
32.00
C02
UT 7,
2.03
1.38
1.76
1.93
1.11
1.51
1.72
1.13
1.82
1.25
1.68
5.23
6.52
7.55
6.71
6.77
6.38
1.16
5.31
5.08
5.19
1.70
5.53
6.00
6.00
5.33
6.26
1.60
5.56
5.83
5.31
1.02
1.79
1.60
3.25
3.68
3.58
3.98
1.37
1.89
6.10
5.71
1,96
5.88
8.21
5.01
3.23
1.55
3.50
1.11
1.16
SLURRY X ACID "IDLE X
SOLIDS INSOLS SULFUR
WT. % IN SOLD OXIDIZED
11.0
li.l
13.5
11.1
11.1
11.2
14.8
15.1
15.6
11.7
12.9
16.6
11.7
11.9
11.3
11.3
16.6
15.1
15.9
16.2
16.3
16.0
13.5
15.0
15.9
15.9
15.9
15.9
16.2
15.6
15.3
15.3
11.1
15.9
15.9
15.8
15.1
11.2
13.9
11.3
11.2
11.5
11.5
11.1
11.8
11.8
15.2
15.3
11.5
13.7
13.9
7.50
7.01
fc.81
7.59
7.21
6.79
7.11
7.02
6.95
7.31
t.15
7.12
6.02
5.95
5.13
5.10
6.32
5.68
5.07
5.78
5.72
6.16
5.23
5.86
6.19
£.70
6.59
6.75
6.60
6.21
6.32
6.72
6.09
6.75
7.26
6.59
6.53
6.02
5.65
1.91
5.12
5.30
5.18
5.39
5.77
1.85
6.35
6.60
6.68
5.82
5.90
17.2
15.6
21.0
15.1
12.9
19.6
21.1
12.3
19.8
10.8
9.1
11.5
6.6
13.9
11. ft
12.2
11.3
15.0
20.6
21.0
17.9
17.8
17.6
21.1
16.1
9.6
15.3
20.3
10.8
11.1
16.5
16.5
16.1
20.3
8.6
21.5
8.6
9.5
11.2
20. 3
9.1
13.2
11.7
23.0
26.7
21.9
22.0
20.1
9.0
18.8
12.5
STOICH
RATIO
1.11
1.09
1.12
1.13
1.09
1.09
1.10
1.08
1.10
1.07
1.10
1.31
1.39
1.18
1.38
1.38
1.35
1.23
1.26
1.26
1.29
1.25
1.31
1.36
1.37
1.51
1.3**
1.28
1.32
1.33
1.32
1.21
1.29
1.28
1.18
1.21
1.19
1.22
1.21
1.25
1.32
1.30
1.25
1.31
1.51
1.27
1.19
1.28
1.21
1.24
1.25
SOLI"!
IONIC
7.M
6.0
l.f.
6.6
c,,7
1.2
2.T
-0.7
-2.7
1.2
1.3
-5.5
-2.0
-2.3
-5.3
-5.6
-8.0
-5.2
-9.1
-7.8
-1.7
-3.6
-2.7
-0.7
-1.7
-1.7
-2.7
-0.5
-4.5
-7.7
-2.9
2.2
1.6
-0.5
-2.1
-3.1
-3.8
-1.0
-1.5
-1.9
-10.1
-7.6
-7.3
-3.0
-11.1
8.5
4.1
0.9
0.4
-1.6
-3.7
-------
PAGE 17
-SOLID ANALYSES AT SCRUBBER INLET-
O
I
NUI^ER HATE
714-1* 01/26/76
"1/26/76
715-14 01/26/76
01/26/76
ri/27/76
C 1/27/76
1 1/27/76
"1/27/76
01/27/76
716-14 01/27/76
11/27/76
'M/28/76
''1/28/76
^1/28/76
717-1? 01/28/76
01/28/76
T'l/28/76
11/26/76
01/28/76
H/29/76
01/29/76
01/29/76
"1/29/76
01/29/76
01/29/76
C 1/3 0/76
01/30/76
01/30/76
ri/3C/7b
.'1/7C/76
"1/70/76
f-1/31/76
M/M/76
"l/M/76
Cl/31/76
01/31/76
pl/31/76
H2/01/76
C2/01/76
"2/01/76
02/C1/76
ra/oi/76
P2/C'?/76
"2/0?/76
C2/02/76
T2/C2/76
C2/C.V76
02/07/76
f>2/P V76
r2/0'/76
C2/C7/76
TIME
0300
07PO
19CO
2300
0300
0700
07P1
1100
150 f!
1900
23 PC
0300
0700
07C1
HOC
1101
1500
19T &
2300
0300
07.00
HOC
1500
1900
2300
030C
07QO
1100
15*0
1^00
2330
0300
0700
lino
1530
1900
2300
0300
0700
1100
1-330
190C
070C
lion
1545
1900
2330
0300
0730
11^0
1530
SC2
INLET
PP*!
26*0
2f.OC
3630
36*0
3480
368"
36RO
3720
320P
3240
3520
3800
3600
3660
3200
324P
2760
2840
2630
2720
3020
3200
3360
3*40
34R*1
3100
?920
2940
3HOO
3040
2Pat)
31SO
36 4 0
3*00
32nn
3000
P96P
266?
3040
3600
32B"
2990
3000
2680
2880
276C
2721.
3060
SC2 S02
OUTLET REMOVAL
PP*i X
210
160
2230
2100
2360
2450
2280
22*0
2*80
2640
3030
3160
3160
850
1*0
360
330
270
300
*30
*(!0
550
610
490
420
300
295
310
710
160
4PO
570
610
3&n
370
200
325
310
370
310
25°.
200
125
1*0
100
1*0
295
91.2
93.2
32.0
33.1
28.9
2fi.2
32.0
22.*
15.1
16.8
10.1
2.6
4.2
70.6
95.3
85.6
87.2
88.9
87.8
84.2
86.2
81.9
80.4
8*.*
85.0
88.6
88.9
88.6
88.7
93.9
83.3
82.7
80.1
87.9
86.*
9?. 6
86.5
88.7
B8.6
84.6
90.5
92.7
95.2
9*. 7
96. 0
94.3
89.5
CftO
wT X
30.50
28.60
28.20
27.30
27.70
24.90
24.90
23. HO
21.40
20.00
14.60
13.80
15.50
12.20
24.00
20.60
28.70
30.50
40.10
41.40
29.70
29.60
28. 2C
27.00
28.10
30.20
29.10
27.90
25.00
26.80
26.90
25.70
27.50
28.30
26.20
26.80
26.40
26.50
26.70
27.50
23.90
24.40
28.00
29.10
28.50
28.20
29.40
25. 1C
28.60
27.40
28.00
S02
*T X
22.70
23.70
21.30
19.10
18.60
16.90
18.10
15.10
11.30
10.90
7.30
7.90
5.80
5.70
3.30
3.30
2.60
2.30
2.20
S.80
15.70
19.00
22.30
22.20
23.30
23.90
23.70
25. CO
21.50
25.30
25.20
22.80
22.50
22.40
24.60
23.60
22.10
21.60
21.50
21.60
23.00
21.10
20.20
22.60
20.80
20.30
23.80
24.20
24.90
22. 5U
23.30
S03
kJT X
4.63
4.38
4.B8
3.73
2.45
3.38
1.58
3.63
3.28
4.48
2.98
0.83
2.15
10.08
4.08
9.78
14.05
12.23
5.15
7.70
4.48
7.75
1.73
1.95
6.98
9.33
7.18
5.96
3.13
1.98
S.fil
2.60
4.&8
6.00
1.25
3.50
6.38
4.50
5.43
6. CO
0.95
2.23
6.95
6.05
7.90
8.13
8.05
*.9&
3.18
0.18
5.08
TOTAL S
AS S03
WT. X
33.00
34.00
31.50
27.60
25.70
24.50
24.20
22.50
17.40
18.10
12.10
10.70
9.40
17.20
8.20
13.90
17.30
15.10
7.90
18.70
24.10
31.50
29.60
29.70
36.10
39.20
36.80
37.20
30.00
33.60
37.30
31.10
33.00
34.00
32.00
33.00
34.00
31.50
32.30
33.00
29.70
28.60
32.20
34.30
33.90
33.50
37.80
35.20
34.30
28.30
34.20
UT X
4.35
4.13
5.92
6.05
6.00
5.39
5.39
5.28
5.68
3.30
2.24
2.30
4.51
4.51
8.64
8.64
13.63
16.76
34.45
18.27
9.46
5.67
b.32
5.71
4.71
3.51
3.85
3.74
4.40
3.69
2.59
2.98
3.74
3.96
3.03
2.37
2.26
3.96
3.58
3.74
2.53
3.14
4.29
4.35
4.40
4.57
3.13
3.74
3.70
4.44
3.36
SLURRY
SOLIDS
JT. X
14.6
14.2
14.9
18.7
15.9
16.6
16.6
15.6
17.7
11.5
13.4
13.5
16.6
16.6
16.4
16.4
16.2
17.5
15.4
14.9
15.5
15.5
16.0
16.6
15.8
15.1
13.7
13.8
14.4
15.2
15.9
14.6
14.8
15.2
14.6
15.9
15.8
16.7
15.5
14.7
14.4
15.2
15.6
14.7
14.6
14.5
15.3
15.3
14.3
14.5
14.9
x ACID MOLE: x
INSOLS SULFUR
IN SOLD OXIDIZED
5.56
5.63
5.94
8.22
7.35
8.24
8.29
8.10
10.25
6.93
9.65
10.18
11.82
10.36
9.50
8.54
5.52
5.67
2.39
3.14
6.24
5.66
7.10
7.38
5.73
4.71
4.92
5.20
6.75
6.75
6.31
6.89
6.19
5. '9 5
6.87
7.10
6.71
7.28
6.57
6.00
7.43
7.65
6.17
5.54
5.45
5.42
5.33
5.94
6.10
7.00
6.01
14.0
12.9
15.5
13.5
9.5
13.8
6.5
16.1
18.8
24.7
24.6
7.7
22.9
58.6
49.7
70.3
81.2
81.0
65.2
41.2
18.6
24.6
5.S
6.6
19.3
23.8
19.5
16.0
10.4
5.9
15.6
n.4
14.8
17.7
3.9
10.6
18.8
14.3
16.8
18.2
3.2
7.R
21.6
17.7
23.3
24.3
21.3
14.1
9.3
0.6
14.9
STOICH
RATIO
1.24
1.22
1.34
1.40
1.42
1.40
1.41
1.43
1.59
1.33
1.34
1.39
1.87
1.48
2.92
2.13
2.43
3.02
8.93
2.78
1.71
1.33
1.33
1.35
1.24
1.16
1.19
1.18
1.27
1.20
1.13
1.17
1.21
1.21
1.17
1.13
1.12
1.23
1.20
1.21
1.15
1.20
1.24
1.23
1.24
1.25
1.15
1.19
1.20
1.29
1.18
SOLI1
IONIC
IMBAL
6.0
-1.7
-5.0
0.9
7.4
3.5
4.3
5.5
9.2
15.6
22.4
24.5
20.4
-45.9
30.2
-0.7
-2.7
-4.7
-23.3
12.1
2.6
1.0
2.4
-4.0
-11.3
-5.7
-5.4
-10.5
-6.5
-5.4
-9.4
0.5
-1.4
-2.0
-0.3
2.5
-1.1
-2.3
-1.8
-1.4
-0.5
1.5
-0.1
-1.6
-3.0
-3.9
-3.6
-1.1
-0.5
7.0
-0.8
-------
1R
-SOLID ANALYSES AT SCRUBBER INLET-
RUN
NUPPER DATE
717-1A 02/0?/76
02/03/76
02/01/76
12/01/76
°2/01/76
"2/04/76
02/01/76
r2/01/76
C2/05/76
P2/05/76
TIME
1930
2330
0330
0730
1130
1530
1930
2330
0330
0730
S02 S02 S02
INLET OUTLET REMOVAL
PPH PPM %
33*31
326C
3100
322C
7440
3280
3120
2900
30<30
3"100
3?5
270
too
550
51"
375
155
285
125
680
89.1
90.9
85.7
81.1
82.6
87.1
83.9
89.1
81.7
77.9
CAO
JT X
32.10
30.00
29.10
25.50
?6.30
27.50
22.80
27.80
2S.OO
26.80
SO?
UT X
23.80
23.10
22.20
19.90
21.90
23.10
20.10
23.10
22.80
23.70
so:1.
UT X
11.95
7.65
7.15
1.93
2.93
1.13
0.50
6.65
6.90
3.68
TOTAL S
AS S03
yT. X
11.70
36.90
31.90
29.80
30.30
33.30
26.00
36.10
35.10
33.30
C02
UT X
3.11
3.71
1.02
2.85
3.29
1.13
2.92
3.25
3.25
1.98
SLURRY X ACID MOLE X
SOLIDS INSOLS SULFUR
UT. X IN SOLO OXIDIZED
15.7
16.9
11.6
11.9
15.6
16.0
16.1
15.6
15.0
15.5
1.03
5.7S
b.36
6.92
7.27
6.61
8.92
5.99
5.73
6.95
28.7
20.7
20.5
16.5
9.7
13.3
1.9
19.0
19.5
11.1
STOICH
RATIO
1.15
1.18
1.21
1.17
1.20
1.23
1.20
1.16
1.17
1.11
soLin
IONIC
I"BAL
-3.6
-2.0
-1.6
3.9
3.1
-1.0
3.8
-5.9
-3.1
3.5
o
I
OJ
00
-------
SUMMARY OF TCA RUNS FRC* JUNE 1975 TO MID-FEBRUARY 1976
PAGr
O
I
CO
RUN
NUMSER
516-2A
517-2A
518-2A
519-2A
S50-2A
551-2A
5-52-2A
553-2A
551-2A
•555-2A
556-2A
557-2A
558-?A
559-2A
560-2A
561-2A
562-2A
562-2B
563-2A
561-2A
565-2A
566-2A
567-2A
568-2A
569-P4
569-2B
570-2S
571-5A
571-2B
572-2A
573-2A
573-2B
571-2A
575-2A
576-2A
576-2B
577-2A
578-28
579-2A
580-2A
581-2A
582-2A
START
CATE
06/06/75
06/18/75
06/23/75
06/27/75
07/02/75
07/00/75
07/10/75
07/19/75
07/25/75
07/29/75
08/01/75
OR/05/75
08/15/75
09/05/75
09/23/75
09/30/75
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
01/12/76
01/13/76
01/15/76
01/17/76
01/22/76
01/22/76
01/29/76
01/29/76
02/01/76
02/01/76
02/11/76
END
DATE
06/17/75
06/23/75
06/27/75
07/02/75
07/08/75
07/10/75
07/11/75
07/21/75
07/28/75
08/01/75
«8/0?/75
OR/13/75
09/02/75
09/22/75
09/29/75
10/06/75
10/30/75
11/06/75
11/11/75
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
01/11/7S
01/13/76
01/11/76
01/17/76
ni/22/76
01/22/76
01/29/76
01/29/76
02/01/76
12/01/76
02/11/76
02/12/76
HRS HUE ALK
ON CR ADON
STRH US PT.
207 LS
112 US
71 LS
112 LS
119 LS
39 LS
86 LS
12 LS
60 LS
63 LS
89 LS
181 LS
398 LS
3S1 LS
112 LS
135 LS
13* LS
131 LS
182 LS
113 LS
109 LS
166 LS
138 LS
162 LS
66 LS
97 LS
111 LS
96 LS
11 LS
151 LS
15 LS
15 LS
12 LS
17 LS
112 LS
3 LS
159 LS
9 LS
62 LS
12 LS
161 LS
18 LS
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
-
GAS
FLY RATE
MGO ASH ACFH
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
N
N
N
N
N
N
H
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
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
Y
30000
30000
3POOO
30000
30000
30000
30000
30000
30000
30000
22500
30000
30000
30000
30000
30000
30000
3QOOO
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
30000
TCA TCA
LIQ L/G NO
RATE GAL/ OF
GPM M«CF BEOS
1000
1000
1000
1000
1000
1000
1200
1200
1200
1200
1200
1200
1200
1200
1200
1200
1200
1200
1200
1200
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1000
1200
1200
1200
12
12
12
12
12
12
50
50
50
50
66
50
50
50
50
50
50
50
50
50
12
12
12
12
12
12
12
12
12
12
12
12
12
12
12
12
12
12
12
50
50
50
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
TOT
BED
HOT
IN.
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
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 NO. OF
SPHERE HOLD
TYPE TANKS
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
TPR
FOAM
FOAM
FOAM
FOAH
FOAH
TPR
FOAH
FOAH
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
FOAM
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
3
1
1
EFFLU
RES SOLID
TIME RECIRC
MIN UT 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
15.0
15.0
15.0
15.0
12.0
12.0
12.0
12.0
12.0
12.0
12.0
12.0
9.0
9.0
9.0
9.0
9.0
9.0
12.0
12.0
9.0
12.0
12.0
12.0
12.0
12.0
9.0
9.0
12.0
12.0
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
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
SOLIDS
DISCH
RANGE
X
35-11
35-13
22
30
37-11
39-11
38-11
32-37
36-10
25
31-15
39-11
31-12
36-12
36-11
37-11
37-13
31-16
36-16
38-15
31-13
31-11
37-13
38-16
33-11
37-11
31-11
31-12
N/A
31-17
N/A
31-13
N/A
35-39
37-12
N/A
39-13
N/A
10-15
N/A
H.E.
SYSTEM
CONFIG
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
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-SP/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
M.E.
WASH
B/T
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
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
If
I/I
I/
It
I/
I/
I/I
I/I
1 11
I/I
I/I
I/I
M.E.
OE- SYSTEP
WATER 0. P. RANGE
SYSTEM IN. WATER
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
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
CL
0.65-0.80
0.65-1.10
0.5R-0.65
0.5R-P.65
0.66-P.R3
0.66-P.fiO
0.68-0.75
0.31-0.36
o.ie-o.io
0.1P-0.23
0.16-P.23
0.36-P.11
0.37-0.13
0.38-0.1?
0.3P-P.12
0.35-0. 11>
0.35-0.13
0.35-0.1!
0.10-0.13
0.38-0.15
0.30-0.35
0.30-P.10
0.35-0.3?
0.33-0.10
0.25-0.35
O.JO-P.35
0.30-P.?5
o.3^-n.;s
K/A
0.30-0.10
N/A
0.30-0.35
N/A
0.3C-P.?P
C.3E-P.10
K/A
0.35-n.ll
N/A
0.15-0. 55
Ik/A
TCA
D.P.
IN.
H20
8.6
7.1
7.0
6.1
6.1
6.6
7.7
8.6
5.2
5.?
5.0
7.1
7.5
7.6
7.6
7.1
7.6
8.3
8.0
7.9
7.7
9.1
9.?
9.3
8.1
7.9
7.1?
7.0
0.0
6.7
0.0
6.9
0.0
6.6
7.5
0.0
8.8
0.0
9.7
0.0
-------
DAGr
d
I
»UN
MUMPER CATC
546-PA 06/06/75
16/07/75
C6/07/75
r?c>/07/7'5
06/08/75
(6/08/75
"C/08/75
Cfi/09/75
CS/09/75
"6/09/75
06/10/75
"6/10/75
06/1C/75
H6/11/75
OS/11/75
P6/11/75
16/12/75
06/12/75
C6/12/75
"6/13/75
"6/13/75
P6/1V75
06/14/75
06/14/75
f!f-/14/75
C6/15/75
"6/15/75
06/15/75
P6/16/75
"f/16/75
C6/16/75
06/17/75
547-2« 06/18/75
06/18/75
06/19/75
C6/19/75
r>6/19/75
C6/20/75
36/20/75
ffi/20/75
"6/21/75
fl6/21/75
06/21/75
06/22/75
06/22/75
C6/2?/75
54B-2A 06/23/75
06/24/75
06/25/75
"6/25/75
°H AT
SCRUPPE^
TIPE INLET
2300
0700
1500
2300
07PO
15CO
23PP
0700
1500
23CO
07CQ
1K00
23P3
07CO
1500
2700
0700
1-500
2300
0700
15CO
2300
07"0
1500
2300
0700
1500
2300
0700
1500
2300
07CO
1500
2300
0700
150C
2300
07CO
1500
2300
0700
1500
23CO
1500
2300
0700
*> i n n
1500
1500
2300
5.95
6.05
5.95
5.90
5.70
5.80
C.70
5.65
5.75
5.85
5.85
6.10
5.95
6.15
5.70
6.00
5.65
5.60
5.65
5.65
5.90
5.95
6.05
5.85
5.85
5.95
5.90
5.85
5.95
5.95
5.85
5.95
5.92
5.90
5.95
6.00
5.90
5.80
6.00
6.00
5.95
6.00
6.00
6.05
5.85
5.95
6.05
6.00
6.10
6.00
CA + +
PPM
1190
1132
116?
1155
1205
2070
?250
2095
1745
1510
1460
1475
1015
1015
1225
1655
inso
1P05
1060
1090
1095
1475
"15
1005
962
1157
8"0
7R2
672
1100
507
62fi
L 1 UU1 U At-iAl
MG«+ NA+
PPM PPH
150
132
16"
179
1B9
207
216
fta
243
229
234
245
229
247
219
245
256
?4R
302
282
252
232
273
267
304
328
269
?83
57?
141
142
123
30
25
31
31
34
38
55
56
46
4?
41
35
40
33
42
39
46
41
46
73
3R
3f>
43
37
45
42
41
48
34
32
22
16
_ T 5L C a
K +
P»M
52
46
64
15
68
64
63
66
65
59
62
44
60
53
64
68
65
57
64
58
53
50
66
51
64
64
59
62
51
52
20
15
i .^> u K LI r
S03--
PFP
120
16
112
32
72
144
120
112
48
120
208
16
160
16
28
2D
152
60
144
80
72
56
36
88
112
304
120
144
24
88
152
104
n L N i IN L :
S04--
PPH
1448
1507
896
1283
1301
2247
1621
1447
1591
1611
1474
1425
1267
1097
1088
1708
1481
368
346
649
1030
1138
418
577
477
450
377
776
837
301
225
364
CL-
PPM
2091
1595
1985
1843
1914
2836
3332
3049
2623
2375
2233
2127
1879
1772
18D8
2375
2623
2233
2056
2056
2020
2446
2233
2162
2233
2020
1843
1595
1489
1666
850
1028
TOTAL SULFATt
IONS SAT. AT
PPM 50 C
5381
4453
4418
453R
4783
7606
7657
6913
6366
5946
5712
5367
4650
4233
4474
6110
6503
4012
4018
4288
4560
5435
3984
4187
4197
436,5
3509
3690
3679
3280
1918
2278
104
102
62
85
86
162
122
117
11C
108
99
95
76
66
7?
116
105
24
21
40
64
78
25
35
28
28
22
42
30
22
14
24
LIQUID
IONIC MAKT PER
I*,BAL. PASS
X M."OL/L
-3.1
-10.3
-3.5
-7.3
-5.0
-5.5
2.5
-2.6
2.5
-6.2
-3.6
6.6
-14.6
0.7
10. C
2.9
8.4
2.2
15.5
10.6
-2.3
1.6
-1.3
-0.2
1.2
16.1
3.8
1.9
28.0
13.6
15.6
7.9
15.?
15.7
10.5
11 .1
19.0
14.0
14.2
13.7
14.6
14.1
13.2
12.1
9.3
9.^
9.7
12.5
13.1
16.7
16.1
17.2
18.3
18.3
15.9
18.6
18.3
14.8
14.4
16.0
15.9
16.3
17.8
13.5
12.8
19.3
17.?
16.3
17.9
15.°
17.0
15.0
15.6
17.2
16.4
15.4
17.1
14.0
14.8
15.5
12.3
-------
PAGE
RUfi
NUCOER
54S-2A
519-20
550-2*
551-2A
55?-2A
557-2A
551-?A
DATE
06/26/75
Q6/26/75
06/27/75
36/27/75
06/27/75
06/28/75
06/26/75
"6/28/75
P6/29/75
C6/29/75
06/30/75
06/50/75
06/30/75
17/01/75
07/01/75
07/02/75
07/05/75
07/03/75
07/04/75
07/01/75
07/05/75
"7/05/75
07/05/75
f;?/06-/75
07/06/75
H7/07/75
07/07/75
07/08/75
07/08/75
P7/09/75
17/09/75
07/10/75
07/11/75
^7/11/75
07/12/75
07/12/75
07/1P/75
"7/13/75
"7/17/75
07/19/75
07/20/75
07/20/75
07/25/75
P7/26/75
07/26/75
f?/2S/75
C7/26/75
C7/27/75
07/27/75
A7/27/75
PH AT
SCRUBBER
TIME INLET
1500
2300
0700
150"
2300
0700
1500
2300
07(?B
1500
0700
1600
2300
1500
2300
2300
1500
2300
1500
2300
0700
1500
2300
1500
2300
1600
2300
1500
23CO
150?
2300
2300
1500
2300
0700
1500
2300
1500
2300
2300
1500
2300
23CO
0700
1500
2300
2301
0700
1500
23"0
6.00
5.90
5.98
5.90
5.90
5.90
5.85
5.85
5.80
5.80
5.90
5.85
5.90
6.00
5.90
5.80
5.89
5.90
5.95
5.90
5.80
5.55
5.80
5.75
5.85
5.90
5.85
6.00
5.95
5.85
5.70
6.05
6.05
5.85
5.90
5.95
6.00
5.95
5.95
5.90
5.50
5.75
6.15
6.00
5.95
6.15
6.15
6.15
6.00
5.80
CA* +
PPf
1195
1175
1200
1130
1830
1975
1950
1150
1285
1510
2120
2815
2235
1820
IfilS
1215
1330
1160
1010
1010
1035
1110
895
965
P22
765
1155
1503
io7n
12PQ
1315
1515
1P5-0
LIQUID ANA
MG+* NA+
PP* PPM
112
100
101
113
122
112
161
167
166
161
113
176
217
211
21&
221
215
251
232
251
233
211
219
2b8
253
269
2&5
272
267
33C!
302
321
271
51
32
29
31
39
10
16
11
15
10
12
53
58
51
53
15
12
39
13
39
10
11
3f>
10
10
13
11
16
8?
12
15
18
83
LYSES fl
K +
PPM
15
16
29
22
22
21
28
32
33
36
56
19
53
13
51
50
11
42
11
13
11
13
13
18
11
18
53
70
91
50
12
53
181
i stKue
S03 —
PPM
101
18
56
88
21
80
111
101
96
18
112
120
72
18
176
10
72
176
1C
72
288
136
112
92
128
181
368
176
61
32
672
56
72
BL1* JLNLI
SOI
PPM
1008
727
971
863
900
792
691
620
957
1120
1372
1611
1260
911
813
551
151
111
162
291
10
398
117
113
202
81
1102
1112
1161
Sbl
1032
2280
1009
CL-
PPK
1701
1630
1701
2091
2907
2942
3081
2181
2091
2116
2978
3722
3019
3297
3332
2659
2517
2310
2269
2162
2310
2310
2091
2269
2127
1985
2233
2310
1915
2199
2556
2506
1986
TOTAL SULFATE
IONS SAT. AT
PP»I 50 C
1186
3728
1090
4611
5«41
5955
6107
4898
4673
5394
7123
8611
6944
6381
6456
1814
4701
4449
4130
38S8
3995
4532
3843
4125
3613
3378
5817
5819
46b1
4714
5961
6779
49f»8
7fi
55
73
66
72
64
55
46
68
82
111
133
96
68
61
36
31
29
30
19
1
29
25
27
12
5
92
93
69
52
65
138
60
LIQUID
IONIC «AKF PER
IMBAL. PASS
X M.MOL/L
17.2
9.2
0.8
4.3
2.2
9.9
7.3
3.8
-0.9
-0.6
15.0
11.2
14.4
-1.5
-•5.0
-4.8
8.C
2.1
-0.9
6.8
0.9
14.5
-3.9
-3.2
-4.3
1.7
-3.9
1.4
1.9
10.4
-18.0
-13.4
13.8
11.3
13.8
12.7
10.5
11.0
11.2
12.5
12. S
13.4
12.7
14.6
15.1
11.6
12.4
11.1
10.2
10.2
12.7
15.2
12.2
11.0
13.3
14.2
14.7
14.1
13.8
14.9
14. «
15.0
13. &
12.6
11.7
11.8
14.4
15.1
14.2
14.9
9.4
9.8
11.7
12.8
13.2
11.5
11.9
11.6
12.3
12.1
8.5
-------
PAGC
d
I
"UN
NUWFR QSTC
555-?A 07/79/75
07/3C/75
?7/30/75
17/31/75
556-2A T7/M/75
"fi/ni/75
OP/01/75
C°/02/75
CP/OP/75
08/02/75
"?/0?/75
! a / 1 T / 7 5
0°/03/75
n?/c<>/7 '
01/04/75
r>8/"5/75
557-7A OP/75/75
0.°/06/75
^8/06/75
"P/07/75
<" ,?/P7/75
"fl/Oft/75
OB/08/75
08/08/75
OP/09/75
Ob/09/75
03/09/75
fo/09/75
OP/10/75
"P/10/75
' 8/10/75
"P/ll/75
no/11/75
;p/i?/75
ffi/l?/75
?"3/l*/75
556-?A OP/15/75
2°/15/75
08/16/75
OP/16/75
"8/16/75
"8/17/75
OP/17/75
08/18/75
"°/18/75
OP/19/75
08/19/75
"8/20/75
^s/20/75
09/21/75
FH ftT
?CRU°-DER
TI"r INLET
23no
1500
2300
2300
1502
1 5 ? 0
2300
0700
1500
2300
0700
1C00
2300
1500
23"0
0700
2300
1500
2300
1500
2300
0700
1600
2300
0700
1500
1900
2300
0700
1500
2300
1500
2300
1500
2300
0700
1500
2300
07CO
1500
2300
p"»00
2300
0700
1500
1500
2300
0700
1500
0700
5.95
6.10
5.85
5.85
6.05
5.95
5.95
5.95
5.95
5.85
5.90
&.2C
6.15
5.95
6.00
6.00
6.10
6.05
5.85
5.80
6.00
5.85
5.95
6.00
5.95
6.00
5.85
5.80
5. 90
6.05
5.90
6.00
5.95
5.95
5.85
5.75
5.70
5.6,0
5.60
5.85
6.05
5.55
6.00
5.95
6.10
5.65
5.75
5.75
CA* +
PPM
ispr
129r
1105
1535
1190
1555
2040
15RO
1570
1530
1390
13^R
1170
1110
1299
1375
1438
11R5
1050
922
745
1055
701
854
820
725
734
680
1507
1165
1010
1210
1190
13«0
1075
985
1195
16RO
1365
----LI'i'JIU »'1 HI
MG++ MA+
ppM p p M
HI
164
164
162
139
186
221
213
241
243
243
260
247
?58
231
255
260
267
283
289
260
313
316
318
314
294
267
233
329
271
211
305
285
337
244
284
34R
348
314
33
34
32
35
32
34
69
45
35
50
46
50
68
46
46
41
41
44
60
41
41
GO
41
44
44
46
41
40
34
41
38
40
38
44
43
41
47
58
42
. IC)C.i »
K +
PPM
33
30
2?
29
31
27
24
43
25
56
55
55
46
47
55
55
55
58
23
62
55
28
55
62
56
59
55
50
54
52
51
52
57
55
42
40
98
60
42
1 o I, n u r
SC J--
PPM
H8
48
56
56
112
112
32
80
120
8
72
88
88
8
96
104
24
112
128
8
144
64
144
80
96
104
88
72
144
144
216
104
168
144
272
120
64
48
168
C L^ 1 PILE
S04 —
PPM
1451
1038
1111
1890
1729
1638
1676
1646
1540
1969
1460
1488
785
584
1777
1872
1920
1628
1331
1152
700
1443
594
1390
1176
1186
988
1633
2603
2143
1911
2170
2094
2196
1948
1875
1810
2513
1744
CL-
PPH
2056
1701
1701
1524
1170
2162
2446
2410
2375
2446
2234
2091
1915
1914
1808
1737
2127
1811
1737
1744
1772
1772
1595
1648
1382
1240
1312
1134
1276
1347
1099
1311
1382
1560
1524
1489
1737
2269
2375
TOTAL SULFATE
IONS SAT. AT
PPM 50 C
5232
4305
4197
5231
4403
5714
6508
6017
5906
6302
5500
5370
4319
3867
5312
5439
5865
5105
4612
4218
3717
4735
3446
4396
3838
3654
3485
4042
5947
5163
4536
5192
5214
5716
5148
4834
5299
6976
6050
99
73
75
132
116
11'4
123
113
104
129
95
95
51
36
112
118
122
98
77
64
38
80
30
70
60
58
51
90
153
122
111
122
120
127
112
101
100
153
105
LIQUID
IONIC CAKE PER
IMBAL. PASS
X M."OL/L
-4.1
11.6
-2.5
9.2
1.7
-3.0
15.3
-4.8
-1.7
-10.3
-2.6
-0.5
12.4
11.3
-3.6
2.4
-4.4
-3.9
-1.3
-0.3
-10.4
0.1
5.0
-7.1
6.0
2.5
3.2
-2.5
10. S
-3.2
-7.7
4.3
-1.0
6.6
-17.8
-11.6
4.9
-0.9
-11.0
9.5
11.1
10.5
8.9
7.?
6.4
5.3
5.1
6.5
6.2
7.7
5.2
5.6
9.2
11.2
11.0
15.4
7.4
7.1
6.4
6.2
6.4
12.4
14.3
13.0
13.4
12.2
13.6
13.3
9.0
11.2
9.5
10.4
7.2
6.9
6.3
9.5
6.4
5.4
4.9
5.2
5.6
11.8
11.1
9.5
11.4
12.3
-------
o
I
rfi-
oo
RLN
MUMPER DATE
55fi-?A nn/21/75
08/22/75
OP/22/75
r-H/23/75
"S/23/75
08/23/75
08/23/75
08/24/75
OP./24/75
"8/24/75
"8/25/75
Cfl/25/75
D8/P6/75
'«/2fi/75
!i8/?7/75
"B/27/75
QS/28/75
?8/?8/75
08/29/75
Tfl/29/75
"8/^0/75
03/30^75
08/30/75
f'8/31/75
"s/31/75
°H AT
SCRUBBER
TI"1: INLCT
23P 0
1500
2300
0700
1500
1900
2300
0700
1500
2300
P7PO
1500
1500
23PO
0700
1500
0700
2300
1500
230.0
0700
1500
2300
0700
1500
07 01
1500
0700
1500
2300
"700
1500
2300
0700
150C
2300
0700
1500
D70D
23"!)
1500
2300
0700
1500
2300
0700
1500
2300
0700
1500
5.95
5.30
5.95
5.90
6.00
5.90
5.80
6.00
5.95
6.00
6.00
6.00
5.90
5.90
5.75
5.75
5.95
5.95
5.70
5.85
5.75
5.70
5.75
5.85
5.90
5.60
5.65
5.35
5.45
5.60
5.50
5.75
5.60
5.60
5.85
6.15
5.75
6.25
5.95
6.20
5.95
5.85
5.85
5.9^
6.05
5.95
5.95
f.,10
6.05
CA + *
pp v
in«5
1320
765
mis
1120
1255
701
830
1045
6*0
945
857
1175
756
fefiO
928
1015
1075
1100
1225
1175
1075
1250
985
840
5?0
541
552
508
5P7
1570
1110
717
756
675
612
LIQUID ANAI
MG++ NA*
PPM PPM
332
215
361
374
349
358
333
289
374
349
369
395
434
357
354
380
380
314
296
350
35?
337
367
297
340
346
346
397
386
355
339
294
374
318
625
28'i
48
49
45
43
49
52
47
45
42
4H
46
50
69
51
50
56
55
47
38
33
45
45
46
44
43
47
42
47
43
42
52
44
4B
48
45
44
.YSts a
K»
PPM
52
52
59
50
55
59
51
50
64
60
64
67
74
63
69
84
72
68
51
40
64
63
64
60
60
59
63
64
62
61
47
62
62
59
64
63
i SCKUB
SC3--
PPM
5fc
56
56
64
64
48
112
96
152
128
192
168
32
80
208
16
24
120
24
112
32
184
336
126
40
88
112
92
136
208
96
136
40
40
SO
96
ULK INL:
S04 —
PP1
1188
2047
998
977
1038
1530
641
1073
1436
798
1428
1221
1683
1287
998
1593
1681
2057
2214
2417
2308
1825
2199
1884
1591
1000
1080
1047
573
825
2467
1321
812
921
918
755
. i------
CL^
PPM
1879
1560
1740
1701
2269
2233
1843
1843
1560
1560
1666
1666
1630
1701
1595
1666
1701
1524
1311
1524
1701
1772
1772
1595
1311
1418
1418
1365
1453
1595
1985
2091
1914
1772
1666
1595
TOTAL SULFATE
IONS SftT. AT
PPM 50 C
4640
5380
4014
4224
4948
5535
3731
4226
4673
3583
4710
4424
5097
4295
3934
4723
4928
5205
5034
5701
5677
53C1
6034
5001
4225
3478
3602
3560
3161
3673
6556
5058
3967
3914
4073
3453
67
121
4fi
52
59
as
31
57
75
36
72
SB
87
60
44
78
85
110
120
130
123
98
120
100
77
39
43
40
22
35
148
77
37
46
32
36
LIQUID
IONIC HAKE PER
I1BAL. PASS
X H.«
-------
d
i
TUN
NU«PER DATE
559-PA (19/16/75
09/16/75
0?/16/75
P9/17/75
09/17/75
19/18/75
"•5/18/75
09/19/75
H9/19/75
C9/20/75
"9/20/75
09/20/75
r: 9/2 1/75
n9/21/75
rg/21/75
09/22/75
560-2A 09/2^/75
09/23/75
C9/24/75
09/24/75
"9/25/75
09/25/75
09/25/75
09/26/75
C9/26/75
"9/27/75
09/27/75
09/27/75
09/28/75
09/28/75
P9/28/75
09/29/75
561-2A 09/30/75
10/01/75
10/01/75
10/01/75
10/02/75
10/02/75
10/03/75
IP/03/75
10/03/75
10/03/75
10/04/75
10/04/75
10/04/75
10/04/75
10/04/75
10/05/75
10/05/75
IC/05/75
f'H AT
SCRUBBER
TIME INLET
0700
150C
2300
0700
1500
0700
2^00
1500
2300
07CO
1500
?300
0700
1500
230C
0700
1500
2300
0700
1500
0700
1500
230C
0700
1500
0700
1500
23DO
0700
1500
2300
0700
2300
0700
1500
1501
2300
2301
1500
1501
2300
2301
0700
0701
1500
1501
2300
0700
1500
1501
6.00
6.30
5.90
5.95
5.70
•S.85
5.90
5.95
6.0C
5.55
f.OO
5.40
5.50
5.85
5.90
5.40
5.20
5.80
5.40
5.80
5.45
5.40
5.70
6.20
5.30
5.70
6.20
5.85
5.70
5.70
6.20
6.00
6.00
6.00
6*00
5.90
5.90
6.00
6.00
5.70
5.70
5.75
5.75
6.05
5.95
5.85
5.85
CA* +
DOM
*35
750
ineo
°.20
1445
1505
635
1J35
807
770
870
920
1030
925
962
795
662
675
818
834
826
866
887
960
864
1007
1455
1485
1360
1315
2250
2165
1425
1020
1010
MG++ NA+
PPM ppq
369
449
402
343
3.PS
407
431
444
354
400
403
329
374
335
356
424
392
324
377
306
345
355
381
357
365
384
352
360
363
352
417
399
351
696
385
49
50
52
51
44
61
54
24
51
54
54
56
51
55
43
49
47
45
46
55
46
46
50
47
•59
53
47
49
48
48
57
56
51
54
49
L 1 ^ t. -:> P
K +
PPM
62
57
64
61
59
68
60
64
50
59
65
65
61
127
68
66
6C
58
62
62
54
54
53
57
60
54
57
56
51
53
55
56
52
53
51
i .> ^ n u r
SC7--
PPM
64
48
204
152
8
64
48
40
112
a
88
56
24
136
48
64
56
48
40
32
48
32
64
24
40
8
48
40
32
24
72
72
56
40
48
UC_"\ 1 F*l.I
S04--
PPM
997
1186
1552
892
2714
1644
833
1294
876
942
1118
1161
1323
1270
1355
752
609
944
980
663
479
682
720
913
628
1024
1156
1085
1119
1138
1676
1676
1039
566
648
CL-
PPM
1808
1879
1879
1914
1772
2800
2095
2091
2020
1914
1879
195G
1953
1843
2020
1879
1808
1772
1844
2269
2269
2190
1666
2095
2198
2410
2481
2491
2623
2623
3332
3297
2854
2552
2588
TOTAL SULFATE
IONS SAT. AT
PP" 50 C
39?4
4419
5233
4233
6435
6549
4356
5097
4270
4147
4477
4537
4816
4691
4852
4029
3&34
3866
4167
4221
4067
4225
3821
4453
4214
4940
5596
5566
5596
5553
7859
7721
5828
4981
4779
43
50
80
45
150
97
39
67
44
.43
54
61
70
66
70
35
27
44
47
36
25
36
37
49
33
54
72
68
68
68
113
113
65
24
35
LIQUID
IONIC MAKE PER
IHBAL. PASS
X H.MOL/L
-11.5
-1.2
0.5
-4.7
0.9
-1.6
4.2
9.7
-7.0
1.8
2.6
-4.5
3.2
-3.1
-6.8
10.4
5.5
-11.1
2.7
-11.1
-3.0
-1.3
19.7
2.6
1.5
-4.6
9.3
12.5
3.0
-0.3
13.2
10.4
0.0
24.2
-2.6
13.8
12.5
11 .9
12.2
13. C
6.9
12.5
14.0
14.5
11.9
14.2
15.1
13.8
13.5
12.8
12.3
13.1
13.1
14.3
15.8
14.5
13.7
13.5
13.1
13.7
12.5
12.3
12.7
9.1
9.0
8.6
8.5
11.8
11.8
13.0
13.2
13.9
14.7
11.9
11. «
-------
PftGf.
RU!\
NUKPER HATE
561-2A 10/05/75
10/05/75
10/06/75
562-2A 10/07/75
10/07/75
10/08/75
10/08/75
10/08/75
10/08/75
10/08/75
10/08/75
10/09/75
10/09/75
10/09/75
10/09/75
10/09/75
10/10/75
10/10/75
10/10/75
10/10/75
10/10/75
in/10/75
10/11/75
10/11/75
10/11/75
10/11/75
10/11/75
10/11/75
10/12/75
10/12/75
10/12/75
10/12/75
10/12/75
10/12/75
10/17/75
10/13/75
10/13/75
f/13/75
10/13/75
10/13/75
10/14/75
10/14/75
10/14/75
10/14/75
10/14/75
lf/15/75
10/15/75
10/15/75
in/15/75
10/15/75
"H AT
SCRUBBER
TI*r INLET
23no
2301
0700
2300
2301
0700
0701
1500
1501
2300
2301
0700
1100
1500
1900
2300
0300
0700
HOC
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
07CC
1500
1900
2300
"300
0700
HOC
1500
19CP
6.00
6.00
5.95
5.80
5.95
5.90
5.90
6.00
6.00
6.00
6.00
5.90
5.90
5.85
5.85
5.80
6.0*
6.10
5.80
5.75
5.90
5.90
5.90
6.00
5.90
6.05
6.00
5.85
5.90
5.85
5.95
5.90
5.85
5.9C
5.75
•5."1?
5.80
6.00
5.75
5.95
5.95
5.90
5.95
5.90
5.80
CA*«
PPq
1040
icio
1057
1047
970
974
1015
1030
1640
1650
1675
1457
1857
1310
1495
1085
1200
1500
1100
1120
7in
679
752
835
1225
LIQUID ANAI
M6*+ NA*
ppty PPM
344
336
350
346
370
378
383
374
339
464
370
373
390
320
338
330
401
338
470
386
327
357
352
345
374
57
59
48
48
74
74
50
50
57
57
52
59
55
53
52
52
50
26
5?
51
50
47
44
49
27
uY^ES «
K +
PPM
55
54
51
53
55
57
51
53
59
59
52
53
52
55
51
52
62
51
68
58
57
59
50
5C
12
1 KCKUfa
SC3 —
PPf*
216
?88
72
64
96
72
88
104
72
104
48
48
64
120
64
48
56
64
40
8
64
52
40
80
BF-K 1NU!
S04--
PPM
662
595
1081
1100
670
699
908
919
1236
1288
1615
1263
1582
572
741
392
752
619
1239
460
516
716
877
948
L 1 ---
CL-
PPM
2375
2198
1808
1808
2304
2304
2166
2198
2410
2446
2659
2765
3226
3155
2765
2694
2552
2233
2233
2340
2162
2162
1772
1879
2127
TOTAL SULFATE
IONS SAT. AT
PPM 50 C
4749
4540
4467
4466
4539
4558
4661
472fi
5923
6068
6471
6018
7226
5585
5018
4705
4956
4606
5234
3794
38»4
3738
4075
4793
38
34
60
61
36
38
49
50
80
77
102
77
102
37
43
23
49
33
67
23
24
35
45
55
LIQUID
IONIC HAKE PER
IMBAL. PASS
X M.MOL/L
-2.5
0.5
11.4
10.3
2.6
3.6
4.0
2.3
18.6
21.0
6.6
1.7
2.3
-8.9
5.8
-9.6
15.8
23.8
20.6
-1.6
-5.7
-9.8
5.0
1.6
12.5
12.fi
12.8
14.2
13.2
14.0
14.2
14.4
12.4
12.2
10.9
10.1
11.8
11.4
11.0
9.8
10.7
9.6
10.8
12.7
12.3
13.5
12.8
14.0
11.8
14.0
13.5
14.8
14.9
14.0
13.1
13.4
12.8
12.5
12.8
14.4
13.9
14.1
14.3
13.8
14.9
13.9
14.3
12.9
11.8
12.1
13.0
13.8
14.6
14.5
13.5
-------
PACT
o
I
-----------Ljyuiu ftNALrats si OLnui:ec.rc lwl_t.l-----------
LIQUIO
^H AT CM + MG++ MA+ K* S03 — S04 — CL- TOTAL SULFATE IONIC MAKF PEP
"UN SCRUBBER IONS SAT. AT IMBAL. PASS
MJ»»r. EP CATE TIMff INLET PP*1 PPM PPM PPM PR« PPM PPM PPM 50 C % M.MOL/L
•i*'-?A in/lK/75
10/16/75
1C/16/75
10/16/75
10/16/75
10/16/75
1C/16/75
10/17/75
ln/17/75
10/17/75
10/17/75
10/17/75
10/19/75
1C/19/75
10/19/75
10/19/75
10/19/75
10/19/75
10/20/75
1T/20/75
10/20/75
10/20/75
10/20/75
10/20/75
10/21/75
10/21/75
10/21/75
10/21/75
l"/21/75
10/21/75
10/22/75
10/22/75
10/22/75
10/22/75
10/22/75
10/22/75
10/23/75
10/23/75
10/23/75
10/23/75
10/24/75
10/24/75
IP/24/75
10/24/75
10/24/75
19/24/75
l"/25/75
10/25/75
10/?5/75
1^/25/75
2300
0300
0700
1100
1500
1900
2300
0300
"700
1100
1500
1501
0300
"700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
07QQ
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
1500
1900
2300
0300
0700
1100
150C
1900
2300
0300
0700
1100
1500
5.75
5.85
1135 417 52 51 32 345 2659 4691
5.30
S.fiO
5.85 977 363 53 63 104 577 2340 4477
5.85 967 368 52 61 112 568 2340 4468
5.90
5.80
5.75
5.75 2700 451 52 60 72 2534 3368 9237
5.75
5.90
6.00
1535 390 56 61 160 752 3297 6251
5.90 1330 606 57 58 64 393 3088 5596
5.90
5.85
5.80
5.85
5.30
5.80
5.95
5.85
5.80
6.00 1095 404 54 67 72 443 2659 4794
6.00
5.75
5.75
5.75
5.95
5.80 2270 388 65 56 48 354 3900 7081
5.85
5.80
5.80 2120 325 60 54 112 307 3084 6062
6.06
5.84 1730 359 53 54 368 296 3120 5980
12.9
13.3
12.2
12.4
12.6
13.0
20 12.2 12.8
13.2
12.0
14.0
32 2.3 15.0
31 2.1 15.0
10. •>
10.1
11.2
173 14.9 11.6
13.7
14.9
14.6
13.5
11.9
48 0.0 11.9
11.5
13.0
13.0
14.1
12.6
21 19.4 12.3
12.3
11.4
15.0
17.0
16.4
16.9
15.8
16.1
16.1
25 6.4 12.9
11.2
11.2
11.4
12.1
11.5
26 20.7 11.6
12.6
13.3
13.9
23 29.6 14.3
12.8
20 13.5 11.7
-------
PAGE
o
I
RUN
NU»RER n,nL
562-PS 10/25/75
10/25/75
10/26/75
10/26/75
l"/26/75
10/26/75
10/26/75
in/26/75
10/27/75
10/27/75
10/27/75
10/27/75
1P/P7/75
1P/J7/75
10/28/75
10/28/75
10/28/75
10/28/75
1C/2S/75
10/28/75
10/28/75
10/29/75
IP/29/75
10/29/75
10/29/75
1C /29/75
10/29/75
10/?9/75
in/30/75
10/30/75
562-26 10/30/75
10/30/75
10/30/75
10/31/75
10/31/75
10/31/75
10/31/75
10/31/75
10/31/75
11/01/75
11/01/75
11/01/75
tt/01/75
11/01/75
11/03/75
11/C3/75
11/OV75
ll/0'
-------
PAOr
O
^
00
PUN
NUMBER DATE
56?~?R 11/04/75
11/04/75
1 1/04/75
11/04/75
11/04/75
11/04/75
11/05/75
11/05/75
11/05/75
11/05/75
11/05/75
11/05/75
11/06/75
11/06/75
563-2* 11/06/75
11/06/75
11/06/75
11/07/75
11/07/75
11/07/75
11/07/75
11/07/75
11/08/75
11/08/75
11/08/75
11/08/75
11/08/75
11/08/75
11/09/75
11/09/75
11/09/75
11/09/75
11/09/75
11/09/75
11/10/75
11/10/75
11/10/75
11/10/75
11/10/75
11/10/75
11/11/75
11/11/75
11/11/75
11/11/75
11/11/75
11/11/75
11/12/75
11/12/75
11/12/75
11/12/75
PH AT
^CRUBSER
TI"E INLET
r>3nn
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
070C
1530
1900
2300
0300
0700
1100
1500
1900
0300
0700
HOC
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
03CO
0700
1100
1500
1900
2300
0300
0700
1100
1500
5.82
5.73
5.7?
5.73
5.71
5.67
5.66
5.7?
5.77
5.82
5.78
5.69
5.77
5.81
5.75
5.79
5.85
5.79
5.91
6.06
6.05
6.03
5.78
5.89
5.86
5.97
5.85
5.89
5.70
5.84
5.77
5.95
5.95
5.96
5.93
5.35
6.40
6.09
6.02
5.76
5.93
5.92
6.07
6.05
6.15
6.15
6.15
6.15
5.85
CA + +
pptf
2569
2280
1735
1380
1330
1295
1215
857
1274
935
8*2
805
614
492
378
398
590
6?3
— --L iy>
PPM
519
432
614
441
445
377
595
399
396
416
628
363
389
317
319
374
39»
386
J 1 U « n « I
V A •*•
PPM
63
68
67
60
59
57
55
5i
51
50
49
46
47
42
35
42
39
46
- I5LC3 H
K +
PPM
58
70
64
69
58
66
56
65
58
61
54
56
55
54
49
56
61
57
) -ic KU L;
SOJ--
ppff
128
136
144
104
168
184
184
152
120
192
64
96
52
104
80
72
160
128
n t_r\ Jt rout
S04--
PPM
1747
1682
873
720
681
941
623
380
758
837
815
817
448
466
384
408
788
486
. i ------
CL-
PP1
i226
3442
2836
2736
2481
2481
2375
2269
2304
2127
1843
1772
1843
1666
1347
1489
1737
1808
TOTAL SULFATE
IONS SAT. AT
PPH 50 C
3310
8110
6333
5510
5222
5401
5103
4175
4961
4618
4335
3955
3448
3141
2592
2839
3773
3534
117
113
50
42
39
56
31
19
45
42
33
40
19
20
14
14
32
21
L13UID
IONIC MAKE PER
IMBAL. PASS
X N.*OL/L
25.4
12.1
26.2
13.5
17.4
5.6
25.4
4.9
16.1
2.8
28.9
5.6
5.3
-10.1
-U.2
3.0
-6.0
3.0
11.9
11.7
12.4
11.6
11.6
12.3
17.4
14.?
13.5
14.0
13.3
13.8
14.5
14.4
14.1
13.0
12.7
14.0
14.1
14.4
14.0
13.6
14.0
14. C
13.7
12.9
13.4
12.5
12.6
13.2
13.0
12.8
13.6
13.6
14.6
14.8
14.3
14.0
15.8
16.0
16.9
17. T!
17.2
16.3
15.7
16.1
17.4
16.0
15.1
14.6
-------
PAGE 10
o
I
RUf<
NUMPER DATE
563-2A 11/12/75
11/12/75
11/13/75
M/1T./75
11/13/75
11/13/75
11/13/75
11/13/75
11/14/75
11/14/75
564-2A 11/14/75
11/14/75
11/15/75
11/15/75
11/15/75
11/15/75
11/15/75
11/15/75
11/16/75
11/16/75
11/16/75
11/16/75
11/16/75
11/16/75
11/17/75
11/17/75
11/17/75
11/17/75
11/17/75
11/17/75
11/18/75
11/18/75
11/18/75
11/18/75
11/18/75
11/18/75
11/19/75
11/19/75
565-2A 11/21/75
11/21/75
11/22/75
11/22/75
11/22/75
11/22/75
11/22/75
11/22/75
11/23/75
11/23/75
11/23/75
11/23/75
LIQUID
PH AT CA+* KG** NA+ K» S03-- S04-- CL- TOTAL SULFATE IONIC MAKE PER
•'CRUBBER IONS SAT. AT IHBAL. PASS
TIPF INLET PP!* PPM PPM PPf* PPK PPM PPM PPM 50 C 1! M.MQL/L
1900
2300
0300
0700
1100
160C
1900
2300
03Cn
0700
1900
2300
0300
0700
1100
1500
1900
2300
0300
070C
1100
1500
1900
2300
0300
070P
1100
1500
1900
23TO
0300
0700
1100
1500
1900
2300
0300
0700
1900
2300
0300
0700
11CO
1500
1900
2300
0300
0700
1100
15 0 0
5.90
6.00
6.10
1015 373
842 365
5.65
5.85
5.70
5.65
6.05 1005 351
5.35
5.10
5.10
5.10 1285 376
5.11
5.25 1360 37S
5.20
5.15
5.15
5.15 1340 344
5.10
5.10 1000 235
5.25
5.25
5.25
5.40 1365 491
5.05
5.00 1470 397
5.00
5.25
5.25
5.25 1310 324
5.20
5.00 1580 325
5.25
5.20
5.25
5.30 1017 372
5. 05
5.50
5.35
5.25 1232 342
5.30
5.25 1085 32C
5.25
5.35
5.25
5.15 1355 40H
5.15
5.30 1260 346
46 55 40 512 2907 4948
46 54 88 356 2410 4161
45 52 144 321 2783 4701
44 58 1C4 2169 2304 6340
45 56 80 2663 2198 6780
45 74 1200 2127 1879 7009
49 60 808 2251 1666 6069
40 57 224 2327 2056 6560
43 5fl 2269
36 SO 704 1759 2056 6239
49 70 1224 2367 1418 7033
69 58 104 2296 1772 S686
39 50 656 1602 1772 5693
37 50 568 1459 1808 5327
3H 59 b!2 2669 1737 6778
35 50 608 2143 1666 6108
29 -10.5
19 -2.9
19 -7.9
119 -14.5
145 -16.7
122 -28.5
124 -56.4
120 -0.3
-104.5
104 -18.3
144 -9.5
112 -16.9
92 -7.7
82 -14.7
142 -12.5
119 -13.5
14.5
14.4
13.7
13.1
14.3
15.5
15.9
15.2
15.3
15.7
13.5
11.1
10.3
10.2
10.2
10.3
9.3
8.7
7.4
8.1
9.6
9.1
9.7
10.0
9.7
10.4
9.1
8.1
7.5
8.6
9.4
10.2
8.3
7.0
9.2
11.5
10.8
12.6
15.1
17.0
14.9
13.7
15.4
13.3
13.1
13.2
12.7
11.9
12.8
13.0
-------
o
Ul
o
PUN
NUMBER OATC
565-?A ll/?3/75
11/23/75
11/21/75
11/21/75
11/24/75
11/21/75
'.1/31/75
11/21/75
11/25/75
11/25/75
11/25/75
11/25/75
11/25/75
11/25/75
11/26/75
566-24 11/26/75
11/26/75
11/26/75
11/26/75
11/27/75
11/27/75
11/27/75
11/27/75
51/27/75
11/27/75
11/28/75
11/28/75
11/28/75
11/28/75
11/28/75
11/28/75
11/29/75
11/29/75
11/29/75
11/29/75
11/29/75
11/29/75
11/30/75
11/30/75
11/30/75
11/30/75
J.l/30/75
11/30/75
12/01/75
12/01/75
12/01/75
12/01/75
12/P1/75
12/01/75
12/02/75
CH AT
^CRUBBER
TI'tF INLCT
1900
2300
030C
0700
HOC
1500
1900
2300
0300
0700
non
1500
1900
2300
0300
0700
1500
19PC
2300
0300
0700
1100
1500
19?C
2?OC
0300
07CO
HOC
150"
19C"1
2300
030C
0700
HOC
1500
19"0
2300
0300
0700
HOC
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
5.35
5.10
5.10
5.20
5.20
5.25
5.35
5.i5
5.20
5.2F
5.25
5.25
5.25
5.10
5.15
5.70
5.75
5.85
5.95
6.90
5.95
5.80
5.85
5.75
5.89
5.95
5.89
5.90
5.85
5.65
5.70
5.75
5.85
5.95
5.90
5.75
5.80
5.80
6.00
5.85
5.80
5.85
5.85
6.00
5.85
5.90
5.90
5.90
CA + *
PP V
1012
91 C
1307
1535
1550
1150
1217
1360
HR5
1370
1780
1710
1055
1020
961
956
LI'J'JIU ANAI
MQ+ + NJ/S +
PPM ppM
161
351
116
218
131
327
161
126
511
111
532
153
598
583
576
565
38
73
36
3(i
31
10
1C
11
18
19
16
If,
18
16
13
11
. T ita A
K*
PPM
60
50
57
59
57
52
56
52
61
56
51
51
56
69
70
66
I b L K U L
S03
PH*
678
616
132
232
188
120
88
86
61
56
88
SB
61
136
70
118
DtK JI^LI
SG4--
PPM
1758
1252
2326
2167
1397
2097
1113
1508
1226
1217
1916
1311
1053
915
1111
1017
_ i ______
CL-
PPM
1808
1560
1595
2110
2268
2127
2116
2181
2971
3226
2671
2765
2907
2269
2116
2375
TOTAL SULFATE
IONS SAT. AT
PPM 50 C
5815
1772
6199
6989
6828
6213
5181
5959
6102
6415
7111
6130
5781
5068
5315
5138
81
61
121
156
115
126
62
85
67
72
112
81
48
43
50
45
LIQUID
IONIC H&KE PER
IMBAL. PASS
x M.MOL/L
-12.3
-11.0
0.7
-21.9
-1.5
-1.2
fa.l
2.4
9.5
-11.9
13.1
14.6
-0.1
15.2
4.6
6.7
13.3
14.3
14.?
13.7
13.4
14.7
13.4
13.3
12.6
11.7
11.3
10.7
11.5
11.3
10.7
11.1
14.?
16.2
16.9
17.0
16.0
15.6
13.8
14.1
16.3
18.3
17.1
15.3
14.1
13.5
13.2
13.6
13.3
14.2
14.3
14.1
15.8
15.7
17.2
18. 0
18.0
18.5
17.3
19.9
18. T
17.7
18.4
19.?
17.0
-------
PAGE 12
d
Ul
PL1*
MUMPER DATE
566-2A 12/02/75
12/02/75
12/0?/75
12/02/75 .
12/02/75
12/03/75
12/03/75
12/03/75
567-2* 12/07/75
12/05/75
12/07/7E
12/04/75
12/04/75
12/04/75
12/04/75
12/04/75
12/0»/75
12/05/75
12/05/75
12/05/75
12/05/75
12/05/75
12/05/75
12/06/75
12/06/75
!2/06/7"5
12/06/75
12/06/75
12/06/75
12/07/75
12/07/75
12/07/75
12/07/75
12/07/75
12/C7/75
12/08/75
12/08/75
12/08/75
12/OR/75
12/08/75
12/08/75
12/09/75
12/09/75
5f8-2A 12/09/75
12/09/75
l?/09/75
12/10/75
12/10/75
12/10/75
12/10/75
LIQUID ANALT'StS A
FH AT CA» + MS + + N!A+ K*
^CRUBBER
TIMF INLET PPM PPM PPM PPM
0700
1100
1500
1900
2300
0300
0700
HOO
1500
1900
2300
0300
f>700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
lino
1500
1900
23° 0
0300
07PO
1100
1500
190 0
23rC
0300
0700
1100
1500
1900
230C
0300
0700
1600
19-CC
2300
0300
0700
1100
150G
6.00 «44 510
5.95
5.95 7B4 547
5.85
5.95
5.90
5.90 1100 386
5.95
5.P5
5.85
6.00
5.95
5.95 584 307
6.00
6.00 682 379
5.95
6.05
6.00
6.00 618 392
6.05
6.05 655 447
6.00
5.97
5.97
5.87 920 371
5. "4
5.88 1080 429
6.00
6.05
5.95
6.02 820 448
*.9R
5.97 1140 3fiO
6.00
6.06
6.03
5.98 980 418
5.93
5.94 727 501
5.95
6.04
6.02
5.99 812 473
5.P6 945 496
5.70
5.63
5.58
5.59 762 43?
5.59
5.47 866 476
46 5fi
40 63
39 50
52 50
33 55
36 50
3ft 56
36 54
43 54
44 54
51 59
43 56
48 55
3? 56
43 57
37 55
2? 62
1 SLKUK
S03 —
PPM
168
88
72
112
112
192
80
24
80
48
40
48
64
56
32
144
136
Ct-K 1NII
S04 —
PPM
658
798
1582
608
792
803
937
843
700
544
597
609
558
1075
1479
1267
1566
CL-
PPM
2375
2198
1879
1524
1666
1595
1843
2269
2410
2375
2410
2056
2020
2020
1915
1773
1843
LIQUID
TOTAL SULFATE IONIC MAKE PER
IONS SAT. AT IMBAL. PASS
PP«I 50 C X M.MOL/L
4659
4518
5108
3217
3719
3686
4056
4517
4796
4333
4677
4210
3973
4531
4967
4476
4972
29 T.O
33 7.6
83 2.1
f
28 -2.4
35 2.6
34 -0.9
38 -1.3
44 -3.5
38 8.5
25 1.9
34 11.4
32 17.0
23 13.3
47 2.2
67 6.2
54 -3.8
68 -3.6
17.5
18.4
16.4
15.7
16.2
i"i.9
15.0
16.0
15.8
16.4
16.2
17.1
18.5
18.5
17.1
17.5
16.7
16.7
16.8
16.4
14.5
12.9
16.0
16.7
15.7
15.4
16.4
15.5
17.0
17.3
17.1
16.2
19.3
19.5
20.3
19.6
19.0
20.7
21.1
20.3
20.7
17.0
17.5
14.7
13.9
14.5
14.4
15.9
15.2
14.4
-------
U
i
«(LK
NUPnER CATE
568-2A l?/10/75
12/10/75
12/11/75
12/11/75
12/11/75
12/11/75
12/11/75
12/11/75
12/11/75
12/12/75
12/12/75
12/12/75
12/l?/75
12/12/75
12/12/75
12/12/75
12/12/75
12/12/75
12/13/75
12/17/75
12/13/75
12/13/75
12/13/75
12/13/75
12/13/75
12/14/75
12/14/75
12/11/75
12/14/75
12/14/75
12/14/75
12/14/75
12/15/75
12/15/75
12/15/75
12/l=i/75
12/15/75
12/15/75
12/15/75
12/15/75
12/16/75
12/16/75
12/16/75
569-2A 12/16/75
12/16/75
12/16/75
l?/16/75
12/16/75
12/17/75
12/17/75
Ll'JUlU lUvALTSL; fl ! iLKUCULK lIVLt 1 -----------
LIQUID
PH AT CA + + MG + + MA* K+ S03 — S04 — CL- TOTAL SULFATE IONIC MAKE PE»
SCRUBBER ION'S SAT. AT 1«8AL. PASS
TIME TNLET °?v PPM °PM PPM PPf PPU PP"1 PP" 50 t I *1.MOL/L
1900
2300
03CO
0700
1100
1500
1501
1900
2300
0300
0700
0701
0702
1100
150 C
1900
2300
2301
0300
0700
1100
1500
1502
1900
2300
0300
07CP
1100
1500
1902
2300
2301
0300
0700
1100
1500
1501
1900
2300
2301
3300
0700
0701
1500
1501
1900
2300
2301
030C
07on
5.43
5.61
5.63
5.56 7C5 41P 32 55 152 1479 1631 4472
5.58
5.63 677 422 33 53 152 1454 159b 43«6
5.63
5.51
5.63
5.49
1512 433 410 52 104 2471 2481 7463
5.42
5.46
5.65 1421 41 50 S2 192 1644 2162 5562
5.54
5.43
5.52
5.45 R96 462 43 62 112 1471 1453 4499
1086 571 4S 55 64 2023 1595 5442
5.56
5.50
5.61
5.45
5.49 856 458 47 52 128 1964 1666 5172
5.52
875 458 4P, 55 104 1984 1595 5099
5.56
5.56
5.46
5.52 1032 45
-------
PAGF 14
Ul
OO
RUK
MUMPER DATE
569-2A 12/17/75
12/17/75
12/17/75
12/17/75
12/17/75
12/18/75
12/18/75
12/18/75
12/18/75
12/18/75
12/18/75
12/19/75
12/19/75
569-2E 12/19/75
12/19/75
12/19/75
12/20/75
12/?0/75
12/20/75
12/20/75
12/20/75
12/PO/75
12/20/75
12/21/75
12/21/75
12/21/75
12/21/75
12/21/75
12/21/75
12/21/75
1.2/22/75
12/22/75
12/22/75
12/22/75
12/22/75
12/22/75
!2/2?/75
12/21/75
12/25/75
12/23/75
570-2A 12/23/75
12/23/75
12/23/75
12/23/75
12/23/75
12/24/75
12/24/75
12/24/75
12/24/75
12/24/75
------LIQUIU ANALTStS Al btKUftLK 1 IMUt. 1 -----------
LIQUID
PH AT CA++ MG* + NA + K+ SQ3 — S04 — CL- TOTAL SULFATE IONIC "IAKE PER
SCRUBBER IONS SAT. AT IMBAL. PASS
TIME INLET PPM PPM PPM PPM PPM PPM PPM PPM 50 C % M.«IOt/L
1100
1500
1501
1900
2300
0300
0700
1102
1500
1900
2300
0300
0700
1500
1900
2300
0300
C700
1100
1500
1501
190D
2300
0300
070P
1100
1500
1501
1900
2250
0300
0700
HOC
1500
1501
1900
23*0
0300
0700
0701
HOC
1500
1501
1900
2300
0300
C7CO
1100
1"?00
1501
5.53
1658 124 50 50 136 2425 1575 6318
5.41
5.5fi 1238 498 55 70 152 2391 2340 6744
5.40
5.36 1971 558 54 53 104 2258 3124 8122
5.53
5.65
5.45
1194 712 60 102 96 2142 3013 7319
5.48 1460 444 47 56 24 2087 2588 6706
5.52
5.5P
5.48 1320 431 51 61 136 2133 1950 6082
5.48
5.47 1220 425 33 52 216 2292 1772 6010
5.47
5.37
5.55
5.51
5.53 1352 501 *4 117 168 2261 1808 6256
5.50
5.51 130R 473 35 51 208 2290 1772 6137
5.51
5.36
5.51
5.60
5.50 1262 502 39 67 64 2448 1545 5927
5.59
5.56 1418 431 37 54 240 2349 1701 6230
5.56
5.54
5.54
5.45
5.62
5. S3
5.70
5.91 1365 435 37 55 104 1984 1347 5327
5.91
5.95
5.68
5.74
5.81 1140 475 41 68 32 Z101 2056 5913
5.78
5.65 1600 454 41 64 104 2695 2127 7085
5.65
15.9
141 18.8 15.2
15. n
14.5
12.8
11. 9
117 -11.8 11. P
10.9
132 6.9 10.5
12.3
12.5
11.9
91 -7.0
116 -3.7 12.5
11.2
11.6
10.6
114 2.2 11.6
11.5
117 -4.5 11.0
11.2
12.2
13.3
12.7
116 10.1 1J.5
13.1
117 3.9 13.0
12.4
13.1
15.5
13.9
120 10.7 14.8
13.0
128 5.8 9.8
9.7
9.9
11.1
10.6
12.3
12.5
12.4
108 23.4 14.2
14.4
14.6
14.9
15.5
102 -3.1 15.3
14.4
150 1.6 14.5
13.8
-------
PAGr 15
a
Ul
"UN
N 'J I»P E R CATC
•57o-?e 12/24/75
12/24/75
12/25/75
12/25/75
12/25/75
12/25/75
12/25/75
12/25/75
12/25/75
12/26/75
12/26/75
12/26/75
12/26/75
12/26/75
12/2*./75
IP/27/75
12/27/75
12/27/75
12/27/75
12/27/75
12/27/75
12/28/75
12/28/75
l?/28/75
12/28/75
12/28/75
12/28/75
12/29/75
12/29/75
571-28 12/29/75
12/29/75
12/29/75
12/29/75
12/30/75
12/70/75
12/30/75
12/30/75
I2/*0/75
12/3C/75
"12/30/75
12/71/75
12/31/75
12/31/75
12/31/75
12/31/75
12/31/75
11/01/76
01/01/76
01/01/76
"1/01/76
-----------L.1UU 11) ANHLTSLO ft I iLKUMIjLK 1 Ul_r, 1 -----------
LIQUID
FH »T CA+* HG+* NA+ K+ S03-- S04-- CL- TOTAL SULFATE IONIC MAKt PE?
SCR'JBSfR IONS SAT. AT IHBAL. PASS
TI^F INLET PPM PPK PPM PPM PPM ppK PP« PPM 50 C % M.MOL/L
)9PP
2300
03C 3
07CO
11CO
1*50 C
1-501
1900
23"0
0300
07CO
1100
150"
1900
2300
0300
07DO
ll'DT!
1500
1900
270D
0300
0700
1I
-------
PAGE 16
a
Ul
»uf<
NUMBER CATE
571-?» 01/01/76
01/01/76
?l/02/76
"1/02/76
571-26 d/02/76
Hl/02/76
rl/02/76
"1/02/76
"1/02/76
nl/0?/76
01/02/76
572-2A 01/03/76
"1/03/76
Cl/03/76
-1/03/76
nl/0^/76
C1A03/76
01/04/76
"1/04/76
Cl/04/76
"1/04/76
01/00/76
01/04/76
31/05/76
01/05/76
01/05/76
PI/05/76
11/05/76
f 1/05/76
"'. INLFT
1900
2300
0300
P700
HOC
1500
1700
1900
2100
2130
2300
0300
0700
11CC
1500
1900
230C
0300
0700
1100
1500
1900
2300
O3or
0700
1100
1500
1900
2300
P300
0700
0701
1100
1500
1900
2300
0300
0700
1100
15PO
1900
2300
0300
C700
1100
1500
1900
2300
"3PO
C700
5.8?
5.85
5.76
5.77
5.86
6.03
5.85
5.73
4.97
4.77
5.21
5.15
5.43
5.09
5.18
5.27
5.23
5.15
5.15
5.40
5.35
5.28
5.13
5.35
5.34
= .26
5.30
5.35
5.24
5.32
5.32
5.32
5.30
5.15
5.22
5.23
5.18
5.27
5.18
5.22
4.95
5.19
5.17
5.15
5.17
5.25
5.30
5.29
5.19
-----------L IHU1U ANBLTiLa «
CA+* M6++ NA+ K*
opH ppfl ppM pptf
1785 >81
2215 489
1875 495
1605 501
1P.10 5C7
1595 488
1655 540
16RO 464
1320 407
1590 411
1490 499
1610 469
1825 513
1R70 5?5
2155 483
4P 61
50 58
4(5 53
47 69
4 i 66
4P 80
50 70
4* 77
4B 65
39 57
41 69
54 67
4H 81
5? 61
50 73
1 a L K U U
S03 —
PPK
160
104
72
224
136
211
208
184
264
224
200
384
248
424
128
DLK 1 nL.1
S04 —
PPM
1835
1755
1978
1652
1996
769
2228
2141
1894
1861
2211
2171
2173
2123
1954
CL-
PPt»
3049
3297
3545
3226
3297
2844
2907
2978
2304
2b52
2591
2942
3226
2978
4077
TOTAL SULFATE
IONS SAT. ftT
PP1 50 C
7419
7968
8066
7324
7861
6035
7658
7568
6302
6734
7101
7697
8114
8033
8920
110
114
119
94
117
46
123
124
104
111
119
123
127
125
125
LIQUID
IONIC MAKE PER
IMBAL. PASS
X M.»«OL/L
3.1
14.4
-3.8
-4.7
-1.5
18.1
-2.0
-5.8
-7.7
0.0
-4.3
-12.0
-3.6
1.1
-5.0
12.5
12.5
13.9
14.4
14.?
14.2
12.5
11.2
7.9
8.4
9.8
10.6
13.2
12.1
12.4
12.7
12.7
12.7
13.9
13.3
12.4
14.0
12.7
10.9
12.6
12.4
12.6
11.6
10.9
8.5
10.1
10.2
10.6
11.1
10.4
11.3
11.6
11.7
10.8
9.3
9.6
7.9
12.9
12.6
13.6
11.2
9.0
8.9
9.0
10.3
-------
PAGt 17
d
Ul
RUN
MUMPER
573-2A
57*-2P
574-2A
575-2A
576-?A
CATE
01/09/76
PI/09/76
"1/10/76
01/10/76
01/l?/76
01/13/76
"1/13/76
°l/l?/76
01/13/76
01/15/76
n/13/76
01/17/76
01/13/76
"1/13/76
01/15/76
Ql/13/76
01/13/76
Hl/13/76
^1/15/76
M/13/76
01/13/76
01/13/76
01/14/76
01/14/76
Hl/14/76
"1/14/76
01/14/76
01/14/76
01/14/76
01/14/76
11/14/76
"1/14/76
01/14/76
ni/14/76
01/15/76
01/15/76
11/15/76
01/16/76
01/16/76
01/16/76
01/16/76
01/16/76
Tl/16/76
11/17/76
01/17/76
01/17/76
01/17/76
PI/17/76
"1/17/76
"1/18/76
-----------L 1 jIUlU ftftflUTSL;. « 1 iLrUL-DC" 1 nut. I ~~~~ ~~~
LIQUID
PH AT CA«+ MG+ + NA + K + SC3 — SOI — CL- TOTAL SULFftTE IONIC 1AKC PER
SCRUBBER IONS SAT. AT IMBAL. PASS
TI"E INLET <=PM ppw ppyi PPM PPM PPM PPM PPM 50 C t M.COL/L
1100
1500
0700
1500
0800
1200
1230
12 6 C
1300
1330
1400
1430
1500
1570
1600
1630
1700
1730
1800
1830
1900
1930
0030
0100
0130
0200
0230
0300
0330
0400
0430
0500
0530
0600
1500
1900
2300
0300
0700
1100
1500
1900
2300
030P
0700
1100
1500
1900
2300
03PO
5.56
2375 647 54 71 144 1724 3616 8631
1970 577 62 81 104 I'ibZ 3900 8656
2300 6?5 63 76 72 2168 4148 9452
5.93 1345 509 61 104 104 790 2978 5891
1180 523 51 102 152 449 297H 5435
5.88
5.88
5.90
5.94
5.95
5.91
5.86
5.82
5.79
5.70
5.66
5.58
5.43
5.29
4.95
4.79
5.92
5.90
5.86
5.83
5.79
5.72
5.67
5.60
5.47
5.33
5.06
4.85
5.68 2070 616 62 80 24 1891 4006 8749
5.57
5.52
5.63
5.49 1690 557 56 67 144 1692 3190 7396
5.35
5.50 1952 583 52 69 136 1629 3190 7611
5.52
5.26
5.56
5.53 2320 517 55 67 120 1825 3970 8874
5.53
5.69 2300 549 64 59 112 1694 4112 8890
5.55
5.82
5.70
12.0
107 19.6
115 -1.9
131 4.1
44 9.9 17.9
24 9.0
20.2
16.2
16.1
14.6
14.5
13.9
12.8
12.1
15.9
15.3
14.5
13.5
12.0
9.4
112 3.6 12.5
13.9
13.6
13.9
95 4.1 1».3
IS. 3
96 14.8 12.6
11.4
11.3
13.4
118 5.8 12.8
14.0
108 6.2 15.7
16.2
17. *
14.3
-------
o
1
Ul
RUN
NUHPER DATE
576-?A 01/18/76
01/18/76
01/18/76
Cl/18/76
01/18/76
01/19/76
01/19/76
01/19/76
01/19/76
01/19/76
f 1/19/76
01/30/76
01/20/76
01/20/76
01/20/76
fl/20/76
01/20/76
?l/20/76
01/21/76
01/21/76
01/21/76
Cl/21/76
01/21/76
ni/21/76
Cl/22/76
01/22/76
Cl/22/76
576-26 01/22/76
LU/22/76
"1/22/76
"1/22/76
ni/22/76
577-25 01/22/76
"1/22/76
Cl/23/76
"1/23/76
01/23/76
01/23/76
01/23/76
P1/2T/76
^1/24/76
01/24/76
•H/24/76
01/24/76
Ql/?4/76
•>l/2a/76
nl/25/76
Tl/25/76
"1/25/76
Cl/25/76
LIQUID
°H AT CA + * MG*» NA» K« S03 — 304 — CL- TOTAL SULFATE IONIC MAKE PER
SCRUBBER IONS SAT. AT IMBAL. PASS
TI»IE INLET PP«! PPM PPM PPM PPM PPM PPM PPM 50 C X M.*OL/L
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
0701
HOC
1500
1900
2300
0300
0700
1100
1500
1900
2300
P300
0301
0355
0430
0500
0530
0600
0630
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
5.48 2230 547
5.58
5.76 1165 517
5.70
5.76
5.56
5.68 2080' 515
5.71
5.73 2420 633
5.63
5.52 1955 552
5.84
5.81
5.81
5.69
5.55 1670 605
5.70
5.56 1575 609
5.64
5.58 1750 534
5.71
5.73 2300 471
5.73
5.75 1885 473
5.71
5.79
5.72
5.66
5.49
5.25
4.9-5
4.80
5.48
5.75
5.79
5.R1 1560 48.0
5.81
5.86 1325 429
5.83
5.85
5.89
5.75 1425 45fi
5.84
5.85 1420 498
5.77
5.76
5.71
5.67 2250 510
5.71
5.71 1675 501
61 120 200 1645 3864 8667
5fi 70 96 1431 3829 7966
63 63 64 1641 4063 8489
67 58 72 1355 4396 9001
65 76 32 1490 4112 8282
59 72 208 1139 3580 7333
64 69 128 1025 3403 6873
65 70 152 1768 3545 7884
59 59 128 2078 4148 9243
55 64 40 1554 3970 8041
68 74 32 1195 3403 6812
4
-------
°AGC
19
d
I
yi
oo
"U
NU""HR DATE
R77-?A f>1/?5/76
01/25/76
"1/26/76
'1/26/76
"1/26/76
"1/26/76
01/26/76
l'l/26/76
"1/27/76
fl/27/76
"1/P7/76
'M/27/76
n/27/76
01/27/76
PI/27/76
?l/28/76
"1/28/76
"1/28/76
01/28/76
01/28/76
"1/28/76
C'l/29/76
"1/29/76
578-24 PI/29/76
Tl/29/76
Tl/29/76
"1/29/76
"1/29/76
"1/29/76
01/29/76
01/?9/76
01/29/76
C' I/ 29/76
Cl/29/76
"1/29/76
01/29/76
579-2A 01/29/76
PI/30/76
01/30/76
01/30/76
"1/30/76
01/30/76
01/30/76
"1/31/76
01/31/76
"1/31/76
"1/71/76
01/31/76
01/31/76
"1/31/76
LIUUiU ftNALTXLa « 1 aLKUWUC-K 1NUCI ------
LIQUID
fH AT CA++ "16+* NA+ K« S03-- S01-- CL- TOTAL SULFATE IONIC MAKT PER
CCRUP,RER IONS SAT. AT IHBAL. PASS
TI^r INLTT PPM PP« PPM PPM PPM PPM PPM PP1 50 C * M.10L/L
I9on
2300
0300
07CO
1100
150"
1900
23?0
0300
070C
0701
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1600
1630
1700
1730
1800
18^0
1900
1901
1930
2000
2030
2100
21*5
2300
0300
0700
1100
154?
1900
2330
0300
0380
0700
lino
1530
19CC
2300
ft. 84
5.83
•=.84
5.93 2250 5bO 33 66 88 Ib81 3545 8113
5.64
5.84 155P 5 "56 54 66 64 1233 3829 73b2
5.79
5.86
5.R2
5.52
5.52
5.56
6.21 1365 572 50 62 64 1213 3510 6836
5.81
5.85
5.85
5.88 1275 509 53 55 248 1030 3084 6254
5.90
5.87 1200 586 47 70 72 1145 3155 6275
5.90
6.00
5.95
5.93 1385 499 55 59 96 1273 3261 6628
5.97
5.93
5.90
5.89
5.86
5.81
5.75
5.75
5.71
5.57
5.36
5.04
5.68
5.39
5.08
5.12 1665 545 56 66 272 2154 3084 7842
5.25
5.35 1575 591 SO 64 256 2272 3261 8079
5.24
5.19
5.26
5.26
5.26 1435 471 37 59 248 2142 2481 6873
5.32
5.23 1590 557 41 57 608 2364 2446 7663
5.19
5.30
16.6
16.0
15.5
101 15.9 15.1
15.0
69 -6.4 17.1
18.1
17.9
18.2
19.6
20.0
18.9
63 -5.8 15.8
16.?
17.5
18.9
55 -5.0 18.3
17.0
56 -2.4 16.7
16.3
16.2
14.5
70 -6.0 15.0
16.6
17.1
16.8
16.1
15.6
12.2
13.6
13.3
119 -5.0 13.1
13.1
118 -10.8 12.3
11.0
11.7
10.8
10.8
116 -6.4 10.3
10.8
126 -3.9 10.6
12.5
13.3
-------
PAGE 20
a
Ul
RUI\
NUMPER CATE
579-PS 02/01/76
H2/01/7G
P2/01/76
580-?« "2/01/76
02/01/76
02/01/76
"2/01/76
"2/01/76
r2/01/76
C2/01/76
5»1-2A C2/04/76
C2/05/76
02/05/76
02/05/76
P2/05/76
T2/05/76
02/05/76
02/06/76
02/06/76
02/06/76
"2/06/76
^2/06/76
02/06/76
C2/07/76
R2/07/76
02/07/76
"2/07/76
"2/07/76
02/07/76
H2/08/76
P2/08/76
C2/OS/76
^2/08/76
02/08/76
02/OP/76
C2/09/76
"2/09/76
02/09/76
"2/09/76
02/09/76
02/C.4
11.7
125 -6.7 12.0
11.1
145 4.4 11.3
11.3
11.2
11.3
126 -5.0 11.2
10.6
124 -3.8 11.5
14.5
14.4
14.3
14.4
14.4
131 -3.1 13.2
11.2
12.4
12.9
104 -6.4 13.3
12.9
-------
PAGE 21
RUN
NUMBER CATE
582-2A 02/11/76
02/11/76
"2/12/76
02/12/76
^2/12/76
T2/12/76
"2/12/76
"2/12/76
•72/12/76
02/12/76
02/12/76
02/12/76
02/12/76
?2/12/76
"2/12/76
02/12/76
TIME
1530
1930
01PO
0130
0200
0230
0300
0330
0400
0430
0500
0530
0600
0630
070P
0710
--• ---L1UUIU BNI
PH AT CA + + «IG*» NA +
SCP.UREER
INLET PPM PPM PPM
5.35 2579 549 46
5.88
5.88
5.86
5.86
5.80
5.40
5.27
5.17
4.68
5.09
4.94
4.81
4.77
4.68
LIQUID
K* S03 — S04 — CL- TOTAL SULFATE IONIC MAKE PER
IONS SAT. AT IMBAL. PASS
PPH PPM PPM PP*1 PPM 50 C % M.MOL/L
74 22 1840 3900 9010 122 16.3 13.7
13.4
14.9
14.6
14.0
14.1
12.9
11.2
9.7
a
-------
PAGE
-SOLID ANALYSES AT SCHUB3ER INLET-
d
I
NUHPEP HATE
546-2A 06/06/75
06/07/75
06/07/75
06/07/75
06/08/75
16/08/75
06/08/75
nfi/09/75
06/09/75
06/09/75
06/10/75
"6/10/75
06/10/75
Ofi/11/75
?.6/ 11/75
06/11/75
n6/l?/75
06/12/75
06/12/75
C6/13/75
^6/13/75
06/13/75
06/14/75
06/14/75
06/14/75
06/15/75
06/15/75
Cfi/15/75
06/16/75
^6/16/75
16/16/75
06/17/75
547-2« 06/18/75
C6/18/75
C6/19/75
06/19/75
^6/19/75
Of /20/75
06/20/75
P6/20/75
06/21/75
06/21/75
06/21/75
06/22/75
06/22/75
06/23/75
548-2A 06/23/75
06/24/75
06/25/75
06/25/75
06/26/75
TIKF
2300
0700
1500
2300
0700
1500
2300
0700
1500
2300
0700
1500
2300
0700
1?00
2300
0700
1500
2300
0700
1500
2300
0700
1500
2300
0700
1500
2300
0700
1500
2300
0700
1500
2300
0700
1500
2300
0700
1500
2300
0700
1500
2300
1500
2300
0700
2300
1500
1500
2300
1500
S02
INLET
PPM
2760
2760
1880
2000
3520
2«00
3240
3360
3680
288C
284C
2720
2280
2120
2320
2RHO
3160
3280
32RO
3120
3240
3200
?960
3520
3360
2600
2640
3000
3120
3280
3680
2440
2400
3680
3320
3240
3480
304P
3280
2800
3200
3320
3120
3080
3400
2520
2760
2960
2320
224C
S02
OUTLET F
PPM
345
320
220
230
410
550
9?0
1100
1250'
600
700
740
740
600
720
760
8PO
600
680
380
340
300
420
540
440
260
340
440
560
660
800
300
360
590
5*0
620
600
500
560
400
680
560
500
600
650
300
400
480
360
420
SO1?
IEMOVAL
X
86.2
87.2
87.1
87.3
84.6
78.2
6P.5
63.7
62.3
76.9
72.7
69.9
64.0
68.6
65.6
69.9
69.1
79.7
77.0
86.5
88.4
89.6
84.3
83.0
85.5
89.0
85.8
83.8
80.1
77.7
75.9
86.4
83.4
82.3
81.3
7S.8
80.9
81.8
81.1
84.2
76.5
81.3
82.3
78.4
78.8
86.8
84.0
82.1
82.8
79.2
CAO
JT X
3?. 30
28.30
27.20
24.10
25.60
26.40
25.60
24.30
26.00
27.60
26.90
27.10
24.90
24.60
23.90
25.90
25.80
26.40
26.80
26.80
29.10
30.30
30.00
28.40
29.40
30.50
30.50
32.60
32.50
31.30
30.60
30.20
30.10
31.10
31.10
30.50
30.60
30.90
32.10
32.10
30.30
30.30
30.10
31.10
31.60
31.10
33.30
32.50
32.30
31.20
30.30
S02
WT X
16.10
20.90
25.50
17.50
21.40
23.50
23.10
20.80
24.80
22.70
21.70
23.50
22.50
20.20
19.10
20.30
22.10
22.70
21.00
23.20
23.20
22.40
22.70
26.00
23.90
22.00
23.20
18.30
lfi.00
20.60
20.00
26.10
24.70
22.30
21.10
23.60
25.30
24.30
24.50
23.20
22.40
15.50
22.30
21.30
23.00
22.30
18.80
18.40
20.90
24.70
19.90
SOS
WT X
6.68
4.98
1.93
5.U3
5.35
4.03
3.73
5.00
3.40
5.93
6.28
4.83
4.18
4.05
3.43
5.73
4.38
4.43
7.35
8.50
5.30
6.90
6.13
1.91
5.13
6.30
4.80
7.13
7.20
7.15
7.60
3.58
4.33
3.83
4.43
3.50
3.88
3.83
4.08
5.50
3.05
6.53
2.83
4.68
3.25
4.03
3.BC
3.80
5.68
3.13
4.93
TOTAL S
ftS S03
>JT. X
26.80
31.10
33.80
26.90
32.10
33.40
32.60
31.00
34.40
34.30
33.40
34.20
32.30
29.30
27.30
31.10
32.00
32.80
33.60
37.50
34.30
34.90
34.50
34.40
35.00
33.80
33.80
30.00
29.70
32.90
32.60
36.20
35.20
31.70
30.80
33.00
35.50
34.20
34.70
34.50
32.30
25.90
30.70
31.30
32.00
31.90
27.30
26.80
31.80
34.00
29.80
C02
yT x
9.59
6.06
3.25
3.75
3.28
3.00
2.92
2.90
2.0C
3.68
3.82
3.25
2.50
2.05
2.55
3.62
3.78
3.10
4.15
2.00
4.68
5.46
5.95
3.49
4.98
5.90
5.96
5.91
9.55
7.12
8.46
5.21
5.34
7.89
7.11
6.36
6.02
7.11
7.21
7.08
6.26
8.26
7.21
7.76
7.98
8.48
11.49
11.30
10.24
7.74
8.99
SLURRY
SOLIDS
UT. X
15.1
16.2
11.2
11.5
13.3
16.5
14.3
13. a
14.2
15.4
13.1
15.1
14.1
14.2
14.9
15.2
15.9
16.3
14.5
14.4
16.1
14.9
15.4
15.8
15.0
15.6
15.2
14.3
15.1
15.0
16.0
15.6
14.3
13.7
15.9
15.4
13.5
14.3
14.4
14.8
15.3
16.3
14.9
15.4
14.5
15.2
13.7
14.5
J2.2
11.1
11.4
X ACID
1NSQLS
IN SOLD C
5.12
5.46
4.96
5.67
5.92
7.25
6.47
6.51
6.40
6.17
5.37
6.27
6.51
7.05
7.67
£.68
7.04
7.16
5.74
5.49
6.06
5.11
5.34
6.68
b.52
5.44
5.44
4.97
4.70
4.91
5.12
5.65
5.19
4.87
5.79
5.68
4.73
4.97
4.72
4.75
5.84
6.18
5.76
5.45
5.09
5.24
4.50
4.93
3.69
3.81
4.04
«OLE X
SULFUR
IXIDIZEO
24.9
16.0
5.7
18.7
16.7
l?.l
11.4
16.1
9.9
17.3
18.8
14.1
12.9
13.8
12.6
18.4
13.7
13.5
21.9
22.7
15.5
19.8
17.8
5.5
14.7
lfl.7
14.2
23.8
24.3
21.7
23.3
9.9
12.3
12.1
14.4
10.6
10.9
11.2
11.8
16.0
9.5
25.2
9.2
14.9
10.2
12.6
13.9
14.2
17.9
9.2
16.5
STOICK
RATIO
1.65
1.35
1.17
1.25
1.19
1.16
1.16
1.17
1.11
1.20
1.21
1.17
1.14
1.13
1.17
1.21
1.21
1.17
1.22
1.10
1.25
1.2ft
1.31
1.18
1.26
1.32
1.32
1.36
1.59
1.39
1.47
1.26
1.28
1.45
1.42
1.35
1.31
1.38
1.3P
1.37
1.35
1.59
1.43
1.45
1.45
1.48
1.77
1.77
1.59
1.41
1.55
IONIC
IMBAL
4.0
-4.3
-2.3
2.0
-4.2
-3.1
-3.7
-4.6
-2.5
-4.0
-5.1
-3.7
-3.7
6.0
6.4
-1.9
-5.5
-2.0
-7.6
-7.5
-3.1
-3.S
-5.8
-0.5
-5.0
-2.3
-2. ">
12.4
-1.5
-2.6
-9.9
-5.9
-4.5
-3.7
l.cj
-2.4
-6.3
-6.E
-4.3
-3.4
-1.0
5.4
-2.0
-2.3
-3.1
-6.6
-1.4
-2.1
-9.4
-7.9
-6.7
-------
-SOLID ANALYSES AT SCRUBBER INLET-
PAGF
U
RL^
MUMPER
548-?A
549-2A
550-2A
551-28
552-2A
553-2A
554-2A
555-2A
GATE
06/26/75
06/27/75
06/27/75
06/27/75
^6/28/75
"6/28/75
06/28/75
Pfi/29/75
06/29/75
06/70/75
"6/30/75
P.&/30/75
07/01/75
07/01/75
07/02/75
07/03/75
07/03/75
07/01/75
07/04/75
Q7/05/75
07/05/75
07/05/75
07/06/75
17/06/75
07/07/75
C7/07/75
07/08/75
07/08/75
07/09/75
"7/09/75
07/10/75
07/11/75
H7/11/75
07/12/75
07/12/75
07/12/75
07/17/75
07/13/75
07/19/75
07/20/75
C7/20/75
Q7/?5/75
07/26/75
07/26/75
07/26/75
07/26/75
07/27/75
C7/27/75
H7/27/75
07/29/75
C7/30/75
TIMF
2300
0700
1500
2300
0700
1500
2300
0700
1500
0700
1600
2300
1500
2300
2300
1500
2300
1500
2300
0700
1500
2300
1500
2300
1600
2300
1500
2300
1500
2300
2300
1500
2300
0700
1500
2300
150C
2300
2300
1500
2300
2300
0700
1500
23QO
2301
0700
1500
2300
2300
150C
S02 S02 S02
INLET OUTLET REMOVAL
ppM ppw X
2920
2560
2080
2210
2240
2600
2760
2880
2640
3160
3120
2400
2600
2200
2080
2080
2680
3160
2360
2280
2720
2840
3240
3040
2880
3040
3080
3120
2960
2760
2640
2680
3320
3280
3240
3400
2080
2520
26 8 C
3080
3060
2680
2920
2840
3000
3120
1880
2320
288"
680
520
4CO
460
440
580
680
700
580
780
68H
5?0
600
420
440
440
620
700
400
500
580
560
840
750
640
640
680
700
360
360
400
42P
560
400
520
540
280
62C
440
600
540
460
620
590
620
760
260
490
720
74.2
77.5
78.7
77.3
78.2
75.3
72.7
73.1
75.7
72.7
75.9
76.0
74.4
78.9
76.6
76.6
74.4
75.5
81.2
75.7
76.4
78.2
71.3
72.7
75.4
7S.7
75.5
75.1
86.6
85.6
83.2
82.7
81.3
86.5
82.2
82.4
85.1
72.7
81.8
78.4
80.6
81.0
76.5
77.0
77.1
73.0
84.7
76.6
72.3
CAO
UT X
29.20
28.80
29.40
29.50
28.80
29.40
29.90
29.30
29.00
35.30
33.80
34.60
34.10
32.70
33.20
33.60
31.80
30.60
36.90
35.00
29.00
29.20
32.70
33.00
32.80
31.30
30.80
34.30
33.80
33.40
31.70
30.90
28.70
30.00
31.60
31. SO
32.30
33.60
29.20
24.50
29.80
26.40
30.50
29.70
29.10
29.10
30. ?0
28.40
28.10
28.70
29.00
S02
UT X
21.10
19.40
18.20
19.50
18.60
19.30
18.50
18.60
20.00
16.90
21.40
23.50
21.50
19.80
18.40
18.50
14.40
16.40
18.20
19.30
19.60
17.80
19.40
19.50
23.00
21.20
21.70
21.50
24.80
2Q.20
18.40
22.00
18.00
21.70
21.10
22.50
23.70
25.20
17.70
13.30
17.90
17.90
16.60
ie.2o
18.30
ie.30
17.90
16.50
15.60
15.80
16.80
S03
UT X
3.63
3.15
5.65
3.73
2.95
3.16
4.08
4.25
2.20
7.18
4.55
2.53
3.33
4.75
10.90
5.58
13.10
6.30
7.55
3.38
4.50
9.55
3.75
4.23
3.35
4.10
4.28
?.?3
3.00
4.55
7.60
5.90
1.90
3.68
3.13
3. b8
4.58
1.41
4.98
5.68
5.43
0.73
4.85
3.95
3.13
3.13
3.73
4.88
8.20
4.05
3.90
TOTAL S
AS S03
UT. %
30.20
27.40
28.40
28.10
26.20
27.30
27.20
27.50
27.20
28.30
31.30
31.90
30.20
29.50
33.90
28.70
31.10
26.80
30.30
27.50
29.00
31.80
28.00
28.60
32,10
30.60
31.40
30.20
34.00
29.80
30.60
33.40
24.40
31.00
29.50
31.70
34.20
32.90
27.10
22.30
27.80
23.10
25.60
26.70
26.00
26.00
26.10
25.50
27.70
23.80
24.90
C02
UT %
6.89
7.37
8.90
7.80
7.45
6.43
7.85
7.64
6.77
9.21
8.20
7.00
7.47
7.59
8.42
6.72
8.01
9.60
10.02
9.42
7.58
7.74
9.31
7.90
7.53
7.90
8.75
9.44
7.80
9.02
9.24
5.90
7.50
6.46
8.36
6.84
7.53
6.69
8.53
5.86
7.42
7.57
9.80
9.73
8.66
8.66
9.15
10.52
7.50
3.77
8.82
SLURRY X ACID HOLE X
SOLIDS INSCLS SULFUR
UT. X IN SOLD OXIOIZED
12.1
12.6
12.8
13.4
14.3
15.0
14.8
15.4
15.7
14.1
15.6
15.1
15.5
14.7
12.5
13.3
lb.1
15.7
15.7
16.1
14.6
15.3
15.4
16.0
15.1
14.6
14.0
14.3
14.3
14.8
15.5
15.4
14.5
14.6
15.7
15.2
15.4
14.8
14.2
16.0
15.3
14.9
13.9
15.0
4.77
5.27
4.77
5.35
6.11
6.34
5.86
6.19
6.73
4.23
5.05
5.16
5.33
5.16
3.26
4.66
4.27
5.66
4.09
5.37
5.74
5.13
5.45
b.86
5.19
5.25
4.90
4.62
4.5R
4.90
4.92
5.43
6.54
5.64
5.76
5.48
5.01
5.25
5.57
7.92
5.86
6.20
12.7
11.5
19.9
13.3
11.3
11.6
15.0
15.5
8.1
25.4
14.6
7.9
11.0
16.1
32.2
19.4
42.1
23.5
24.9
12.3
15.5
30.0
13.4
14.8
10.5
13.4
13.6
11.0
8.«
15.3
24.8
17.7
7.8
12.5
10.6
11.3
13.4
4.3
18.4
25.5
19.5
3.2
19.0
14.8
12.0
12.0
14.3
19.1
29.6
17.0
15.?
STOICH
RATIO
1.42
1.49
1.57
1.50
1.52
1.43
1.52
1.51
1.45
1.59
1.48
1.40
1.45
1.47
1.45
1.43
1.47
1.65
1.60
1.6?
1.48
1.44
1.60
1.50
1.43
1.47
1.51
1.57
1.42
1.55
1.55
1.32
1.56
1.3fl
1.52
1.39
1.40
1.77
1.57
1.48
1.49
1.60
1.70
1.67
1.61
1.61
1.64
1.75
1.49
1.67
1.64
SOLIn
IONIC
INBAL
-2.5
0.7
-6.2
-0.«
3.'
7.1
2.8
1.0
4.6
10.6
4.2
9.6
10.0
7.2
-3.8
14.7
-0.6
-H
7.9
IP. 7
-3.4
-10.1
3.7
8.8
2.2
-0.6
-7.6
3.7
0.1
3.1
-4.fi
0.0
7.1
0.2
0.9
2.H
-3.S
6.0
-2.2
5.8
2.9
2.2
0.3
-4.^
-0.5
-0.5
0.9
-10.1
-3.1
3.0
1.1
-------
PAG?
-SOLID ANALYSES AT SCRUBBER INLET-
ti
I
RUN
NUM°£R
555-2A
556-2A
557-?A
558-2A
CATF
07/30/75
C7/M/75
07/31/75
'8/01/75
r:H/01/75
08/02/75
08/02/75
H9/02/75
Ofi/0"',/75
08/03/75
08/03/75
Ofi/04/75
08/04/75
TsS/05/75
Hfl/05/75
C3/06/75
"8/06/75
OB/07/75
C8/07/75
06/08/75
08/08/75
00/08/75
?8/09/75
Cfi/09/75
"8/09/75
:»/Q9/75
CR/10/75
08/10/75
np,/10/75
CP/11/75
OB/11/75
08/12/75
"S/12/75
CS/13/75
03/15/75
rg/15/75
Dfi/16/75
C8/16/75
C8/16/75
3P/17/75
08/17/75
08/18/75
OR/18/75
18/19/75
P8/19/75
T8/20/75
08/20/75
08/21/75
08/21/75
08/22/75
08/22/75
TIMF
2300
2300
1502
1500
2300
0700
1500
2300
0700
1500
2300
1500
2300
0700
2300
1500
2300
1500
2300
0700
1600
2300
0700
1500
1900
2300
0700
1500
2300
1530
2300
1500
2300
0700
1500
2300
0700
1500
2300
0700
2300
0700
1500
1500
2300
0700
1500
070C
2300
1500
2300
SO?
INLET
ppM
2520
2000
2280
1800
1520
14RO
2013
2000
2600
1480
1600
3200
3840
3720
3600
1640
1640
14RO
1360
1440
3040
3600
3460
352P
3120
3800
3640
2080
3040
2400
296C
1600
1560
1360
2600
1400
1160
1040
1200
1200
3280
2840
2380
2960
3040
2240
2360
2960
SC2
CUTLET '
P°M
500
29C
400
me
190
180
380
400
600
160
180
820
540
880
640
220
280
260
180
220
640
820
920
900
740
1120
1020
350
840
560
900
220
240
170
740
180
140
110
200
140
960
680
540
740
660
360
480
740
SO?
REMOVAL
%
7b.O
84.!)
80.6
89.0
86.2
86.6
79.4
77.9
74.4
88.1
87.6
71.6
72.9
73.8
80.3
85.2
81.1
80.6
85.4
83.1
76.7
74. 8
70.5
71.7
73.7
67.3
68.9
81.4
69.4
74.2
66.3
84.8
83.0
86.2
&«.£
85.8
86.7
88.3
81.6
87.1
67.6
73.5
74.9
72.3
76.0
82.2
77.5
72.3
CAO
JT *
29. 4P
27.40
30.00
29.10
26.90
24.80
28. 60
25.30
25.30
26.40
26.40
27. 20
32.30
31.40
30.80
27.40
2[5.00
22.90
23.20
27.50
27.10
30.00
27.80
28.30
27.80
27.50
28.80
27.80
26.30
26.50
26.80
26.10
28.10
25.60
25.00
24.20
24. 1Q
24.10
22.80
20.10
20.40
26.40
27.50
25.80
26.30
26.00
23.20
26.40
24.90
SO?
.T X
1 7.90
16.00
16.40
13.60
14.20
16.00
17.20
14.70
16.70
17.10
13.20
16.30
15.10
15.70
17.40
20.70
20.40
16.30
16.70
22.90
14.80
17.40
22.20
22.30
18.97
21.10
23.20
22.40
17.80
21.80
24.60
23.90
23.30
21.10
19.90
19.90
17.10
18.90
14.80
14.20
14.30
21.50
20.50
17.90
19.60
17.50
21.40
17.10
18.60
SOS
.T %
3.73
6.40
5.50
9.30
6.75
6.60
4.30
6.93
4.73
3.73
7.70
3.13
4.43
5.68
5.05
2.73
2.00
5.53
3.t3
3.08
5.70
6.05
3.25
3.23
6.59
3.33
4.20
4.50
6.85
5.65
4.65
3.43
6.38
4.13
4.63
5.13
5.33
5.78
7.10
4.35
3.83
3.03
4.08
4.53
2.90
4.83
4.45
5.33
2.85
TOTAL S
AS S03
U7. X
26.10
26.40
26.00
26.30
24.50
26.60
25.80
25.30
25.60
25.10
24.20
23.50
23.30
25.30
26.80
28.60
27.50
25.90
24.50
31.70
24.20
27.80
31.00
31.10
30.30
29.70
33.20
32.50
29.10
32.90
35.40
33.30
35.50
30.50
29.50
30.00
26.70
29.40
25.60
22.10
21.70
29.90
29.70
26.90
27.40
26.70
31.20
26.70
26.10
C02
UT X
9.31
8.98
9.35
9.97
10. C3
8.10
7.27
5.00
7.99
9.43
10.51
9.31
9.74
12.50
11.23
5.11
4.81
2.89
3.21
5.05
8.50
9.09
5.82
6.77
5.62
6.37
7.01
5.52
6.77
3.89
3.21
3.07
2.28
2.88
2.32
2.07
3.87
2.91
2.43
4.20
3.28
3.74
5.28
5.35
4.75
5.68
5.18
5.56
5.65
SLURRY '
SOLIDS
UT. X
14.9
13.6
12.2
11.2
10.8
11.9
13.2
13.4
12. b
14.5
15.4
15.6
13.7
13.8
13.5
14.2
14.9
15.0
15.3
16.0
15.8
16.2
16.0
14.7
15.0
15.2
15.9
15.8
14.6
12.9
11.3
12.9
13.1
12.6
11.8
11.3
11.4
16.4
15.1
15.0
16*5
15.2
15.2
13.9
15.5
X ACID
INSOLS
IN SOLO (
5.91
4.82
4.58
5.54
5.90
5.85
5.03
7.11
6.08
6.38
5.47
5.89
6.19
6.37
6.53
5.77
6.05
5.47
6.22
6.39
6.02
6.05
6.36
6.59
7.59
6.47
6.93
7.79
6.96
6.22
6.25
7.51
*OLE X
SULFUR
1XIDIZED
14.3
24.3
21.2
35.4
27.6
24.8
16.7
27.4
18.5
14.9
31.8
13.3
19.0
22.4
18.9
9.5
7.3
21.3
14.8
9.7
23.6
21.8
10.5
10.4
21.8
11.2
12.7
13.9
23.6
17.2
13.1
10.3
18.0
13.5
15.7
17.1
20.0
19.7
27.7
19.7
17.6
10.1
13.7
16.8
10.6
18.1
14.3
20.0
10.9
STOICH
RATIO
1.65
1.62
1.65
1.69
1.74
1.55
1.51
1.36
1.57
1.68
1.79
1.72
1.76
1.90
1.76
1.33
1.32
1.20
1.24
1.29
1.64
1.59
1.34
1.40
1.34
1.39
1.38
1.31
1.42
1.22
1.16
1.17
1.12
1.17
1.14
1.13
1.26
1.18
1.17
1.35
1.27
1.23
1.32
1.36
1.32
1.39
1.30
1*38
1.39
SOLIC
IONIC
IMBAL
-2.5
-9.^
-0.4
-7.0
-11.5
-16.8
4.4
4.8
-9.0
-12.1
-14.9
-4.1
11.0
-7.2
-7.4
3.1
-1.6
4.7
8.4
-4.1
-2.5
-3.5
-4.8
-7. "5
-2.1
-5.2
-11. K
-7.2
-10.3
-5.7
-7.8
-4.4
1.2
2.2
5.5
2.3
1.9
-0.8
7.8
-3.6
5.0
2.6
-0.1
0.5
4.0
0.2
-0.9
2.3
-2.3
-------
PAGE
-SOLID ANALYSES AT SCRUBBER INLET-
o
I
ON
PUN
NUKPE* DATE
558-2A 08/23/75
08/23/75
OB/23/75
Cfi/23/75
T8/24/75
08/24/75
"P/21/75
3S/25/75
08/25/75
r?./26/75
C8/26/75
CH/27/75
f H/27/75
08/28/75
08/28/75
CS/29/75
r«/29/75
P8/30/75
08/10/75
H8/30/75
C?/31/75
08/31/75
19/02/75
559-2A 09/05/75
09/06/75
r 9/06/75
P9/0«;/75
OS/07/75
P9/07/75
"•5/07/75
OS/OS/75
T'9/08/75
C9/D9/75
C9/10/75
P9/10/75
C9/11/75
C9/11/75
u 9/1 2/75
"9/12/75
"9/13/75
eS/13/75
1-9/13/75
09/14/75
P9/14/75
P9/14/75
r>9/15/75
09/15/75
09/16/75
P.9/16/75
'9/16/75
09/17/75
TI1E
0700
1500
1900
23CO
0700
1500
2300
0700
1500
1500
2300
0700
1500
0700
230C
1500
2300
07CO
1500
2300
0700
1500
0700
150C
0700
1500
2700
0700
1500
23PO
C700
1500
23CO
0700
1500
C7CO
23C3
1500
2300
Q7rn
1500
230C
0700
1500
2300
G7CP
1500
07CO
1500
2300
0700
S02
INLET
ppy
3480
2880
2880
2180
3320
36*0
2640
2560
3120
3540
3000
3240
?6fiP
2700
3120
3360
3820
2920
2R4fl
2800
2720
2600
2520
1720
3160
2920
2840
2400
244n
2600
3340
3680
3680
3R60
384C
3920
3560
3200
2400
3520
3560
3480
328C!
3960
4020
3600
3520
3040
2960
S02 S02
OUTLET REMOVAL
PPM %
620
560
600
400
780
1040
460
400
740
960
660
780
400
500
720
86Q
1000
600
560
440
520
280
380
180
490
SOD
400
360
380
400
700
780
760
960
980
1COO
820
700
440
860
son
740
740
1060
1160
860
840
620
660
80.3
78.5
76.9
82.1
74.0
68.3
80.7
82.7
73.7
69.9
75.6
73.3
83.5
79.5
74.4
71.6
71.0
77.2
78.2
82.6
78.8
88.1
83.3
88.4
82.8
81.0
84.4
83.4
82.8
83.0
76.8
76.5
77.1
72.4
71.7
71.7
74.5
75. tt
79.7
72.9
75.1
76.4
75.0
70.3
68.0
73.5
73.6
77.4
75.3
CAO
JT %
28.10
28.80
28.50
29.10
28.50
28.00
29.10
30.20
28.60
28.70
28.70
28.80
3C.60
29.90
29.50
28.60
28.70
28.80
29.00
2S.7Q
29.10
28.60
28.70
24.50
24.70
27.30
27.60
25.60
27.70
26.90
27.70
29.70
25. 5C
29.30
29.10
29.30
29.80
29.10
28.10
28.60
29. 2Q
28.90
30.10
2*. 70
29.60
30.80
30. 00
30.30
29.80
S02
yT %
19.80
20.40
18.00
18.40
18.10
23.30
21.50
19.60
23.30
22.90
24.40
20.60
18.50
20.30
20.90
18.90
20.50
19.60
17.10
17.60
17.60
19.60
20.80
19.00
19.00
20.70
18.90
19.90
17.90
17.80
18.40
21.50
19.20
17.50
19.50
21.90
22.70
17.00
19.30
19.30
20.90
17.30
20.20
21.10
21.30
25.20
23.23
22.60
18.00
S03
yT x
3.95
3.10
3.70
4.00
4.28
2.88
2. 83
4.20
2.98
5.78
4.20
5.85
5.78
4.93
4.B8
4.98
2.88
2.40
4.03
2.80
3.50
3.90
3.70
3.15
5.35
5.03
4.48
8.03
4.13
3.85
5.20
5.03
7.20
8.23
5.53
4.83
2.73
5.95
2.98
3.08
4.C8
4.98
4.35
5.03
3.58
2.91
2. CO
2.45
4.40
TOTAL S
AS S03
UT. %
28.70
28.60
26.20
27.00
26.90
32,00
29.70
28.70
32.10
34.40
34.70
31.60
28.90
30.30
31.00
28.60
28.50
26.90
25.40
24.80
25.50
28.40
29.70
26.90
29.10
30.90
28.10
32.90
26.50
26.10
28.20
31.90
31.20
30.10
29.90
32.20
31.10
27.20
27.10
27.20
30.20
26.60
29.60
31.40
30.60
34.40
31.00
30.70
26.90
C02
yT %
6.87
6.41
8.19
8.35
9.06
4.10
7.52
6.28
5.87
4.16
4.46
4.50
7.30
5.42
7.34
7.77
4.88
6.36
8.67
7.12
7.06
7.43
6.70
2.83
3.51
5.37
5.70
2.23
5.43
6.34
7.30
6.62
8.33
8.05
5.92
6.54
7.19
8.65
7.28
6.78
6.84
8.66
8.77
6.71
7.57
3.37
5.79
5.91
8.54
SLURRY X ACID MOLE X
SOLIDS INSOLS SULFUR
WT. X IN SOLD OXIDIZED
16.1
16.1
14.3
16.0
15.9
15.3
14.2
14.5
14.9
15.0
15.9
15.9
14.8
14.6
15.0
14.9
16.1
15.2
15.0
15.0
15.4
14.5
13.3
13.1
14.6
15.3
14.5
14.8
14.7
13.7
15.8
14.9
15.5
15.5
15.2
14.9
15.5
15.2
15.1
15.6
16.1
16.3
15.9
14.9
15.6
15.2
15.4
14.8
14.6
6.71
6.77
5.97
6.47
6.30
6.58
5.70
5.77
6.02
5.73
6.19
6.29
5.48
5.74
5.63
5.91
7.58
6.68
6.17
6.63
6.63
5.92
5.40
6.69
6.85
6.34
6.25
6.32
6.59
6.19
6.47
5.54
5.35
5.42
6.00
5.59
6.01
b.83
6.50
6.65
6.34
6.47
5.84
5.58
5.89
5.95
6.27
5.96
5.72
13.8
10.9
14.1
14.fi
15.9
9.0
9.5
14.6
9.3
16.6
12.1
18.5
20.0
16.3
15.7
17.4
10.1
8.9
15.9
11.3
13.7
13.7
12.5
11.7
18.4
16.3
15.9
24.4
15.6
14.8
18.5
15.8
23.1
27.3
18.5
15.0
8.8
21.9
11.0
11.3
13.5
18.7
14.7
16.0
13.0
8.4
6.5
8.0
16.4
STOICH
RATIO
1.44
1.41
1.57
1.56
1.61
1.23
1.46
1.40
1.33
1.22
1.23
1.26
1.46
1.33
1.43
1.49
1.31
1.43
1.62
1.52
1.50
1.48
1.41
1.19
1.22
1.32
1.37
1.12
1.37
1.44
1.47
1.38
1.49
1.49
1.36
1.37
1.42
1.58
1.49
1.45
1.41
1.59
1.54
1.39
1.45
1.18
1.34
1.35
1.5*
SOLIT
IONIC
IM6AL
-2.7
2.1
-1.0
-1.6
-6.7
1.3
-4.4
6.9
-4.8
-2.4
-4.5
3.2
3.4
5.9
-5.3
-4.7
8.8
6.4
0.6
7.9
7.7
-2.7
-2.2
8.4
-0.6
-4.3
2.4
-1.1
8.0
2.0
-4.9
-3.6
-lOel
-7.0
2.1
-5.4
-3.8
-3.4
-0.6
3.2
-2.3
-2.7
-6.0
-2.8
-4.3
7.8
3.0
4.''
c ., ;>
-------
PAG?.
-SOLID ANALYSES AT SCRU3BER 1NLET-
d
"UN
NUMBER
559-2A
560-2A
561-2A,
562-2«
DATE
05/17/75
"9/18/75
09/18/75
r< 9/19/75
OS/19/75
09/20/75
"9/20/75
09/20/75
05/21/75
09/21/75
0°/21/75
09/22/75
09/23/75
G9/23/75
G9/24/75
09/24/75
39/25/75
09/25/75
H9/25/75
09/26/75
09/26/75
T9/27/75
P9/27/75
09/27/75
09/28/75
C9/2B/75
Q9/28/75
09/39/75
09/30/75
1C/01/75
10/01/75
10/01/75
10/02/75
10/02/75
10/03/75
10/03/75
10/03/75
10/03/75
10/0*/75
10/01/75
10/04/75
1C/04/75
10/04/75
10/05/75
10/05/75
IP/05/75
10/05/75
10/05/75
IP/06/75
10/07/75
10/07/75
TlfF
1500
0700
2300
1500
2300
0700
150C
2300
0700
1500
2300
0700
15CO
2300
0700
1500
0700
1500
2300
0700
1500
0700
150C
2300
0700
1500
23CO
070C
2300
0700
1500
1501
2300
2301
1500
1501
2300
2301
070C
0701
1500
1501
2300
0700
1500
1501
2300
2301
0700
2300
2301
SO?
INLf T
op w
3040
3080
1520
3400
3640
372?
296C
3720
3880
3400
3240
3120
3000
3200
3120
3680
429C
3640
336H
3160
3200
3160
2R40
30SO
3200
2120
2120
1920
1520
288C
2860
3280
3340
3440
3560
3160
3120
3320
3300
3800
3800
3900
S02 S02
OUTLET REKOVftL
PPf X
680
5BO
200
940
900
900
660
940
940
720
640
640
f '0
660
600
900
1190
820
700
560
660
520
440
700
730
380
390
280
290
6PO
580
760
780
740
720
840
810
320
810
1020
1180
1150
75.2
79.1
85.4
69.4
72.6
73.2
75.3
72.0
73.2
76.5
78.1
77.3
77.1
77.2
78.7
72.9
69.3
75.0
76.9
80.4
77.2
81.8
82.9
74.8
74.7
80.2
79.6
83.3
83.3
76.9
77.5
74.3
74.1
76.2
77.6
70.5
71.?
72.6
72.8
70.3
65.6
67.3
C«0
HT %
29.30
2S.70
25.30
25.10
23.30
?8.40
23. 6C
28.70
27.90
30.00
30.20
29.70
29.40
29.00
2f.lO
28.80
29.50
28.70
30.10
30.10
32.10
30.70
30.30
31.40
32. 10
31. 60
31.70
31.60
30.70
30. ^0
28.83
28.90
28.80
29.00
29.20
29.40
28.80
28.90
29.60
29.70
29.70
28.70
28.90
28.90
29.20
29.30
29.30
28.80
28.90
sc?
UT %
21.10
20.60
1-3.70
16.90
19.10
19.10
21.90
22.60
15.00
21.30
20.30
17.10
19.80
21.10
18.80
19.90
12.80
21.00
23.20
20.60
21.30
21.00
21.30
15.30
18.80
16.00
19.20
20.70
20.90
21.00
22.10
21.90
24.30
24.40
19.70
20.30
22.50
22.10
20.80
20.80
21.70
22.40
24.10
24.10
24.40
25.00
23.80
21.60
21.50
S03
klT %
1.93
3.15
3.78
7.28
5.?3
4.33
3.53
5.85
5.65
2.88
4.33
5.63
3.05
3.63
4.20
4.33
8.?0
2.45
3.30
5.15
4.38
2.95
3.58
7.28
2.70
4.40
4.80
2.63
2.38
2.55
3. £8
3.63
2.03
1.80
3.78
3.53
2.98
3.88
5.80
5.60
4.48
5.00
2.58
2.88
2. HO
2.26
2.65
3.20
3.23
TOT4L S
AS S03
JT. X
28.30
28,90
28. 40
28.40
29.10
28.20
30.90
34.10
24.60
29.50
29.70
27.20
27.80
30.00
27.70
29.20
24.30
28.70
32.30
30.90
31.00
29.20
30.20
26.40
26.20
24.40
28.80
28.70
28.50
28.80
30.90
31.00
32.40
32.30
28.40
28.90
31.10
31.50
31.80
31.60
31.60
33.00
32.70
33.00
33.30
33.50
32.40
30.20
30.10
C02
UT X
6.31
6.52
3.49
3.73
5.81
6.59
5.52
5.16
8.65
8.38
5.74
8.89
7.13
6.90
5.17
4.99
9.53
7.29
7.06
7.53
7.54
8.76
7.78
8.32
8.82
10.78
7.36
9.09
7.99
8.71
7.24
7.28
5.05
6.65
3.9<>
8.30
4.16
3.98
6.43
6.52
6.54
6.13
5.39
5.68
5.60
5.78
5.37
5.41
5.79
SLURRY * «C10 MOLE X
SOLIDS 1NSQLS SULFUR
UT. X IN SOLO OXIDIZED
14.6
lb.3
13.9
14.1
15.2
15.6
14.8
15.5
16.2
14.8
15.2
15.2
15.5
15.6
16.4
15.4
14.9
15.8
15.1
14.6
14.4
14.0
16.0
15.7
15.0
9.4
15.0
15.7
14.6
14.6
15.0
15. 0
14.4
14.4
14.1
14.1
14.8
15.0
15.0
14.5
15.3
14.5
14.5
15.0
15.0
15.1
14.5
14.5
t.33
fr.44
t.71
6.42
6.28
6.51
6.07
5.79
6.70
5.67
6.00
5.72
6.39
6.26
7.19
6.54
5.58
6.56
5.64
5.33
6.00
5.67
5.74
3.45
5.51
£.79
5.70
5.51
5.91
5.86
6.01
5.77
5.59
5.48
6.28
5.56
5.55
5.49
5.78
5.87
5.79
5.89
5.92
6.05
6.06
5.99
6.8
10.9
13.3
25.6
18.0
15.4
11.4
17.2
23.8
9.8
14.6
21.4
11.0
12.1
15.2
14.8
34.2
8.6
10.2
16.7
14.1
10.1
11.9
27.6
10.3
18.0
16.7
9.9
8.3
8.9
10.6
11.7
6.3
5.6
13.3
12.2
9.6
12.3
18.3
17.7
14.2
15.2
7.9
a. 7
8.4
6.7
8.2
10.6
10.7
STOICH
RATIO
1.41
1.41
1.2?
1.24
1.36
1.43
1.3?
1.2S
1.64
1.52
1.35
1.59
1.47
1.4?
1.34
1.31
1.71
1.46
1.40
1.44
1.44
1.55
1.47
1.57
1.61
1.80
1.46
1.59
1.51
1.55
1.43
1.43
1.28
1.37
1.51
1.52
1.24
1.23
1.37
1.38
1.38
1.34
1.30
1.31
1.31
1.31
1.30
1.33
1.35
SOL in
IONIC
IMBAL
4.5
O.c
3.&
1.3
l.a
0.9
-0.3
-6.1
-1.3
-4.5
6.9
-2.3
2.9
-2.«-
7.5
6.9
1.1
-2.4
-5.1
-3.8
2.4
-3.0
-2.5
7.3
7.8
2. a
6.8
-0.3
1.8
-1.2
-7.2
-7.2
-1.1
-7.?
-3.0
-4.8
6.0
6.1
-2.9
-a. 5
-2.6
-7.6
-3.0
-5.0
-4.3
-5.2
-0.8
2.6
1.5
-------
PAGT
-SOLID ANALYSES AT SCRUBGER INLET-
O
I
RUN
NUKPER CATE
562-2A 10/08/75
10/08/75
10/08/75
10/08/75
10/08/75
10/08/75
10/09/75
10/09/75
10/05/75
10/C9/75
10/09/75
lT/10/75
10/10/75
10/10/75
10/10/75
10/10/75
10/10/75
IP/11/75
10/11/75
10/11/75
in/n/75
10/11/75
10/11/75
lf/12/75
10/12/75
10/12/75
10/12/75
10/12/75
10/12/75
10/13/75
10/13/75
10/13/75
10/13/75
10/13/75
in/n/75
10/14/75
10/14/75
10/14/75
10/14/75
10/14/75
10/15/75
10/15/75
10/15/75
10/15/75
1Q/15/75
10/15/75
10/16/75
10/16/75
10/16/75
IP/16/75
10/16/75
TIHF
0700
0701
1500
150l'
2300
2301
0700
1100
1500
1900
2300
0300
070C
1100
1500
1900
2300
0300
07QO
1100
1500
1900
2300
0300
0700
1100
1500
1900
23DO
0300
0700
1100
1500
1900
2300
0300
0700
1500
1900
2300
0300
0700
1100
1500
1500
2300
C30C
0700
1100
1500
1900
SQ2
INLET
PPM
3R40
3860
3120
3080
2440
2260
2flOC
2680
2640
2480
2600
2200
248C
2960
28RO
3220
3080
3400
2840
3200
3200
3440
3360
3320
3280
3320
3200
3080
3200
3-52P
3640
3605
3800
3640
37«=n
3680
3P40
3360
3120
3120
32ft 0
4000
3920
4060
332P
3120
3120
304C
3060
2920
sonr
S02 S02
CUTLET REMOVAL
PPM %
1060
1040
720
710
360
330
520
480
520
5«0
540
360
400
520
520
700
600
700
560
520
600
60C
500
620
740
720
729
660
720
1100
920
860
1000
940
860
960
1040
S40
820
760
760
1260
1060
1200
700
620
560
6HO
660
500
530
69.4
71!. 1
74.4
74.5
83.7
83.8
79.4
80.2
78.2
74.1
77.0
81.9
82.1
80.6
80.0
76.6
78.4
77.2
78.2
82.0
79.2
80.7
83.5
79.3
75.0.
76.0
75.1
76.3
75.1
6B.9
72.0
73.5
70.8
71.4
74.7
71.1
70.0
72.3
70.9
73.0
74.3
65.1
70.0
67.2
76.6
78.0
80.1
75.2
76.1
81.0
81.6
CAO
WT %
25.50
29.60
28.90
28.90
30.60
30.60
32.00
31.90
30.50
30.50
31.00
32.00
34.50
35. HO
33.80
30.50
30.50
31.80
33.10
34.10
33.90
34.80
34.80
31.60
30.40
31.10
31.60
32.00
30.50
30.00
29.60
31.30
31.30
32.10
31.90
31.30
29.80
29.60
2ft. 70
29.40
29.10
28.60
30.30
29.60
31.30
30.70
30.50
30.00
30.00
30.60
31.80
SOS
WT X
20.20
20.10
25.10
25.20
23*00
22.90
19,30
21.20
21.20
23.10
21.00
lfa.10
It. 20
16.50
17.10
20.30
21.80
20.00
18,20
18.20
19.70
15.10
17.80
17.80
20.20
20.40
18.30
16.90
25.60
27.40
20. 8C
22.30
19.90
22.40
22.30
22.10
20.80
24.40
25.20
22.50
21.90
20.00
22.00
24.70
21.30
23.70
22.10
19.90
20.40
22.00
17.10
S03
yT %
4«£>5
5.08
2.73
2.61
3.85
3.98
4.98
4.50
3.90
2.43
4.25
5.98
4.65
5.28
6.?3
4.43
4.05
5.30
5.35
6.05
5.78
7.03
5.65
10.25
7.35
7.40
10.53
9.38
4.31
3.66
10.40
6,03
8.08
5.90
4.43
6.28
5.30
3.30
1.31
2.98
3.13
4.20
2.70
2.43
4.38
2.38
5.58
4.83
4.40
2.&C
7.53
TOTAL S
AS 303
WT. X
29.90
30.20
34.10
34.10
32.60
32.60
29.10
31.00
30.40
31.30
30.50
26.10
24.90
25.90
27.60
29.80
31.30
30.30
28.10
28.80
30.40
25.90
27.90
32.50
32.60
32.90
33.40
30.50
36.30
37.90
36.40
33.90
31.70
33,90
32.30
33.90
31.30
33.80
32.80
31.10
30.50
29.20
30.20
33.30
31.00
32.00
33.20
29.70
29.90
30.30
28.90
C02
UT %
6.10
5.9'i
4.95
4.99
8.23
7.70
9.65
7.21
8.74
7.60
7.63
11.46
10.92
14.42
12.00
9.11
8.67
7.32
8.10
9.65
10.38
12.31
9.28
9.12
7.26
6.65
7.42
10.95
5.10
4.49
4.S4
4.99
8.68
5.92
6.92
8.fa3
7.37
6.48
5.57
6.77
6.88
7.22
7.83
6.55
9.02
8.20
8.53
7.25
7.75
6.99
9.24
SLUKRY % ACID MOLE X
SOLIDS INSQLS SULFUR
WT. % IN SOLD OXIDIZED
14.3
15.0
15.0
14.3
14.4
15.2
14.9
14.6
15.2
14.9
14.5
15.0
14.9
14.7
15.1
14.6
15.1
15.2
15.5
IS. 4
14.8
14.9
15.3
14.9
15.5
14.7
14.6
14.5
14.6
15.9
15.8
15.3
15.7
15,4
15.4
15.7
15.8
16.6
15.1
15.6
15.1
14.6
14.6
15.0
14.7
14.5
14.7
16.0
15.3
5.65
6.00
6.01
5.00
4.86
5.39
5.39
5.50
5.53
4.98
4.99
f.ll
4.46
5.25
5.35
5.17
5*24
4.73
4.59
4.47
4.70
4.25
5.13
5.03
4.54
4.17
S.17
5.22
4.65
5.59
4.87
5.10
5.17
4.80
5.67
5.86
6.55
6.55
6.02
6.27
5.76
5.61
4.89
5.48
4.8?
5.50
5.50
6.17
5.00
15.6
16.8
8.0
7.6
11.8
12.2
17.1
14.5
12.8
7.B
13.9
22.9
18.7
20.4
22.6
14.9
13.0
17.5
19.1
21.0
19.0
27.1
20.3
31.5
22.6
22.5
31.5
30.7
11.9
9.6
28.6
17. S
25.5
17.4
13.7
18.5
16.9
9.8
4.0
9.6
10.3
14.4
9.0
7.3
14.1
7.4
16. 8
16.3
14.7
9.3
26.0
STOICH
RATIO
1.37
1.36
1.27
1.27
1.46
1.43
1.60
1.42
1,52
1.44
1.46
1.80
1.80
2.01
1.79
1.56
1.50
1.4*
1.52
1.61
1.62
1.86
1.61
1.51
1»41
1.37
1.40
1.65
1.26
1.22
1.24
1.27
1.50
1.32
1.50
1.46
1.43
1.35
1.31
1.40
1.41
1.45
1.47
1.3&
1.53
1.47
1.47
1.44
1.47
1.42
1.59
SOLIH
IONIC
If BAL
2.7
2.7
-4.7
-4.7
-8.S
-6.7
-2.1
3.1
-6.3
-3. fa
-0.^
-2.8
9.1
-2.0
-2.4
-6,5
-e.i
3,9
9.4
4.3
-l.rf
2.b
SS9
-8.S
-5.5
-1.?
-4.0
-10.4
-4.7
-7.6
-7.0
3.P
-4.6
2.5
-6. fa
-11.0
-5.1
-7.9
-«.P
-3.4
-3.5
-3.7
-2.7
-7,0
-6.1
-7.0
-11.9
-0.1
-2.7
I."--
-0*7
-------
PAGE
-SOLID ANALYSES AT SCRUbBEK INLET-
d
I
"IN
M,'f°EP CUTE
562-2A 1C/16/75
1C/17/75
10/17/75
10/17/75
10/17/75
10/17/75
IP/19/75
10/19/75
in/19/75
1C/19/75
IP/19/75
ID/19/75
10/20/75
1P./2C/75
1D/2C/75
10/20/75
IP/20/75
1P/20/75
1C/21/75
10/21/75
10/21/75
10/21/75
1C/21/75
in/21/75
1C/22/75
10/22/75
10/22/75
IP/22/75
10/22/75
10/22/75
1P/23/75
10/23/75
10/23/75
10/23/75
10/21/75
10/24/75
IP/24/75
10/24/75
10/24/75
10/24/75
in/25/75
10/25/75
10/25/75
10/25/75
10/25/75
10/25/75
10/26/75
10/26/75
10/26/75
10/26/75
10/26/75
TI^F
230U
0300
0700
1100
15CC
1501
0300
0700
HOC
1500
1900
23DG
P300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
150G
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
230C
0302
0700
1100
1500
1900
30?.
INLET
PPM
2&00
2920
2RBO
3640
4050
403?
2400
2280
252P
2600
3000
3160
2960
2880
2640
2520
2600
2960
2840
3080
?720
2600
2600
2360
3400
3640
3800
3BOO
34fiO
3520
3480
2800
?520
2640
2600
2600
2400
2420
268P
2840
3000
3000
2720
2480
2120
2640
3320
32P. GO
30.90
28.00
30.40
30.10
31.20
26.40
26.70
26.30
26.30
26.80
23.80
28.40
29.90
29.30
31.10
30.70
29.60
29.30
29.50
29.30
27.10
29.60
31.30
25.90
29.10
31.40
26.70
30.80
32.90
29.50
32.40
32.40
31.60
28.20
22.50
26.60
26.90
26.50
26.50
25.00
22.80
26.60
24.60
22.40
26.80
25.80
28.40
27.40
C02
UT X
9.19
9.46
6.76
6.96
7.74
7.67
6.88
9.35
9.42
11.38
11.66
10. -55
10.67
10.16
8. 30
8.01
7.20
5.78
8.20
6.15
5.40
7.97
9.38
8.04
7.76
10.35
11.11
8.90
12.25
8.18
7.99
10.10
8.42
7.26
7.86
11.57
14.20
10.89
11. 66
10.54
12.04
13.62
14.13
11.06
10.23
12.49
12.10
13.70
12.27
9.68
11.72
SLURRY
SOLIDS
UT. X
14.4
14.7
14.5
17.5
15.2
15.2
14.5
14.6
14.6
15.2
14.5
15.4
11.1
15. 1
14.6
14.0
15.2
15.3
15.4
15.5
14.9
15.6
14.4
15.5
15.9
14.7
15.8
15.1
15.4
15.0
15.0
15.2
14.7
14.8
15.0
15.3
15.0
lb.0
15.0
14.8
15.4
15.6
15.6
14.7
15.0
15.3
16.0
14.9
14.0
14.8
15.0
X ACID
INSCLS
IN SOLO C
5.28
5.18
5.63
7.20
5.81
5.89
5.71
5.57
5.47
4.98
4.78
5.02
3.60
5.75
5.03
5.51
5.28
4.85
4.90
4.88
4.23
4.76
4.87
4.69
5.02
5.31
5.49
4.98
4.26
4.69
4.57
4.69
4.74
4.68
4.52
5.13
b.42
5.27
6.26
2.91
2.99
4.74
4.32
MOLE X
SULFUR
IXIOIZED
7.0
13.4
15.9
11.6
13.7
13.6
8.7
20.0
15.7
19.2
18.3
20.7
14.5
13.3
11.0
16.0
9.2
15.3
15.1
20.7
9.8
13.8
19.8
15.6
ia.i
24.7
16.7
11.2
31.7
18.4
10.3
18.7
8.2
10.9
8.6
9.6
26.1
16.8
17.8
20.3
18.9
19.5
28.7
8.8
17.7
18.0
34.7
46.7
17.3
21.5
STOICH
RATIO
1.58
1.59
1.40
1.45
1.46
1.46
1.40
1.64
1.64
1.79
1.81
1.74
1.67
1.65
1.54
1.50
1.42
1.34
1.5P
1.38
1.33
1.49
1.63
1.49
1.45
1.73
1.69
1.52
1.83
1.48
1.44
1.62
1.47
1.41
1.45
1.75
2.15
1.74
1.79
1.72
1.63
1.99
2.13
1.76
1.76
2.01
1.93
l.ftl
1.62
1.78
SOLI?
IONIC
IHBAL
0.1
-2.1
-5. a
0.4
-6.7
-6.8
-3.8
-1.4
0.4
0.8
-0.5
1.1
-2.0
-3.9
-6.2
-0.4
-0.2
7.5
0.4
9.1
10.6
2.3
3.5
2.9
1.8
6.2
-2.8
1.1
1.4
5.1
1.1
1.1
-3.8
-3.4
-4.4
-2.1
8.5
8.7
3.7
8.3
1.2
-0.2
4.3
1.7
8.0
7.0
11.0
13.6
6.3
3.9
-------
-SOLID ANALYSES AT SCRUBBER INLET-
O
00
"31^
NUMBER CATE
562-2A 10/26/75
10/27/75
10/27/75
10/27/75
IP/27/75
10/27/75
10/27/75
10/28/75
10/28/75
10/28/75
10/28/75
10/28/75
10/28/75
1 P/28/75
10/29/75
10/29/75
1C/29/75
10/29/75
10/29/75
10/29/75
10/29/75
10/30/75
10/70/75
5f?-23 10/30/75
10/T0/75
10/30/75
IP/71/75
10/31/75
10/31/75
IP/31 '75
1C/31/7C,
10/31/75
11/01/75
11/01/75
11/01/75
11/01/75
11/01/75
11/0^/75
11/03/75
11/03/75
11/03/75
11/03/75
11/03/75
11/04/75
11/06/75
11/04/75
11/04/75
11/00/75
11/C4/75
11/05/75
11/05/75
TIME
2300
0300
0700
1100
1500
1900
2300
0300
0301
0700
1111
1500
1900
23HO
0700
1100
1500
1501
1900
2300
2301
0300
0700
1500
1900
2300
Q300
0700
1100
1500
1900
2300
0300
07CO
1100
1500
1900
03" 0
0700
lino
isno
1900
2300
030D
0700
1100
1500
1900
2300
D3CC
0700
SO? TC2 S02
INLET CUTLET REMOVAL
PPM PPM %
3520
356P
368P
3720
3120
2960
3000
3160
3170
3120
304P
2920
2920
2880
3000
3200
3080
3140
3040
30f<0
3040
3440
3240
2960
2920
23Sf.
2760
2920
2920
3000
2S80
30.7
-5,'
-------
PAGE
-SOLID ANALYSES AT SCRUBBER INLET-
O
I
RUK
NUKFER CATE
562-2B 11/05/75
11/05/75
11/05/75
11/05/75
11/06/75
11/06/75
563-2A 11/06/75
11/06/75
11/06/75
11/07/75
11/07/75
11/07/75
11/07/75
11/07/75
11/08/75
11/08/75
11/08/75
11/08/75
11/08/75
11/08/75
11/09/75
11/09/75
11/09/75
11/09/75
11/09/75
11/09/75
11/10/75
11/10/75
11/10/75
11/10/75
11/10/75
11/10/75
11/11/75
11/11/75
11/11/75
11/11/75
11/11/75
11/11/75
11/12/75
11/12/75
11/12/75
11/12/75
11/12/75
11/12/75
11/13/75
11/13/75
11/13/75
11/15/75
11/13/75
11/13/75
11/14/75
TI»<:
1100
1500
1900
2300
0300
07PC
1530
1900
23CC
0300
0700
1100
15CO
1900
0300
0700
lino
1500
1900
2300
03CO
070C
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
19CO
2300
030C
0700
1100
1500
1900
2300
0300
0700
1100
1600
1900
2300
0300
S02
INLET
PP«I
336D
3440
328C
3600
3810
3P40
36*0
3080
?880
3200
31SO
3080
296C
9840
3040
3040
300"
2S40
3120
2880
2ft80
3000
3040
3080
3000
2960
3160
3120
3000
3040
3520
3600
3SOO
392H
3880
3600
?560
3720
4000
3840
3440
3120
3080
3090
2B40
2720
3000
3240
32?0
3160
3240
S02 SO?
OUTLET REMOVAL
PPM X
74P
720
700
900
1000
1020
s?r
590
450
520
460'
340
300
260
360
360
380
380
540
480
46P
460
540
600
400
360
380
300
280
360
500
540
56C
600
580
480
540
620
660
740
540
340
320
340
240
240
280
300
260
280
320
75. -i
76.fi
76.4
72.3
71.1
70.6
72.9
79.1
82.7
82.0
83.9
37.6
88.8
B9.9
86.9
86.9
86.0
85.2
80.8
81.6
82.3
83.0
80.3
78.4
85.3
86.6
86.7
89.4
89.7
86.9
84.3
83.4
83.7
83.1
83.5
85.3
83.2
81.6
81.7
78.7
82.6
88.0
88. b
87.8
90.7
90.3
89.7
89.8
91.3
90.2
89.1
CAC
UT *
29.20
29. 6C
29.40
29.50
27. 7G
29. 3C
29.50
29.40
30.70
31.70
33.60
37.60
36.50
38.60
36.80
34.80
36.30
35.10
34.10
35.30
33.60
32.90
32.60
34.80
35.10
35.90
37.20
34.90
35. 3C
32.30
33.90
33.90
32. bO
32.50
33.00
35.70
32.50
31.60
31.30
30.70
29.80
30.80
31.20
33.50
33.80
29.70
29.50
33.30
35.60
34.10
35.30
SO^
UT X
19.10
23.50
22.30
22.30
23.90
23.20
24.30
20.50
21.80
,22.40
21.50
19.30
17.80
19.20
21.70
19. 1C
18.60
21.10
19.00
21.40
20.20
21.60
20.70
23.90
20.40
23.00
22.20
19.30
22.40
22.30
19.40
2?. 80
23.30
19.40
22.00
20.90
21.00
23.40
27.10
19.50
18.40
20.90
16.00
20.40
18.50
17.50
16.60
20.40
18.30
20.90
20.90
S03
UT y
7.23
5.23
5.73
8.13
3.93
4.50
3.03
4.18
4.25
3.40
4.U3
2.18
5.15
2.00
8.38
4.23
2.65
3.13
3.25
3.25
5.85
1.50
2.53
3.03
1.90
3.25
2.55
3.75
1.50
1.73
1.75
2.50
1.88
3.35
1.60
0.58
0.45
1.65
1.33
5.03
4.10
1.38
4.50
2.80
3.68
6.43
9.55
1.80
3.83
2.88
4.08
TOTAL S
AS S03
UT. X
31.10
34.60
33.60
36.00
33.80
33.50
33.40
29.80
31.50
31.40
30.90
26.30
27.40
26.00
35.50
28.10
25.90
29.50
27.00
30.00
31.10
28.50
28.40
32.90
27.40
32.00
30.30
28.50
29.50
29.60
26.00
31.00
31.00
27.60
29.10
26.70
26.70
30.90
35.20
29.40
27.10
27.50
24.50
28.30
26.80
28.30
30.30
27.30
26.70
29.00
30.20
C02
UT %
6.85
5.30
7.38
4.74
5.96
6.73
6.79
9.35
9.30
9.25
10.18
12.00
13.15
14.84
12.46
9.35
12.76
9.09
10.44
9.72
7.95
8.09
7.70
8.24
12.02
8.45
10.10
13.11
12.56
11.63
13.21
11.13
1.07
11.76
8.91
13.10
12.47
12.06
8.30
11.76
12.43
11.97
14.96
10.83
9.65
12.43
10.65
16.24
14.11
10.66
9.77
SLUKRY r, ACID MOLE X
SOL1CS INSCLS SULFU".
UT. x IN SOLD OXIDIZED
14. jj
15.1
15.0
15.2
lb.3
15.1
14.9
lb.0
14.5
14.8
14.8
15.5
15.0
15.0
14.1
15.2
15.1
15.1
15.1
15.2
15.5
14.8
15.1
14.8
15.2
14.9
15.3
15.8
13.3
14.8
15.4
15.4
15.2
15.0
15.2
15.1
15.2
15.3
15.4
14. S
14.6
15.3
15.0
14.7
15.1
15.4
14.4
15.2
14.7
15.6
•15.4
5.40
5.52
5.22
5.18
f .05
5.58
5.63
5.54
4.99
5.05
4.62
4.63
4.03
3.98
2.73
4.93
4.60
4.89
5.11
4.74
4.91
5.59
5.67
4.65
4.86
4.54
4.50
4.56
4.02
4.99
b.10
4.78
5.07
5.02
5.50
4.78
5.43
5.08
4.99
4.87
5.18
5.61
4.95
4.89
5.22
5.11
4.51
5.03
4.13
5.04
4.68
23.2
15.1
17.1
22.6
11.6
13.4
9.1
14.0
13.5
10.8
13.0
8.3
18.8
7.7
23.6
15.0
10.2
10.6
12.1
10.8
1ft. 8
5.3
8.9
9.2
6.9
10.2
8.4
13.2
5.1
5.8
6.7
8.1
6.1
12.2
5.5
2.2
1.7
5.4
3.P
17.1
15.1
5.0
18.4
9.9
13.7
22.7
31.5
6.6
14.3
9.9
13.5
STOICH
RATIO
1.40
1.2B
1.40
1.24
1.32
1.37
1.37
1.57
1.54
1.54
1.60
1.83
1.87
2.04
1.64
1.61
1.90
1.56
1.70
1.59
1.47
1.5?
1.49
1.46
1.80
1.48
1.61
1.84
1.77
1.71
1.92
1.65
1.06
1.78
1.56
1.89
1.85
1.71
1.43
1.73
1.83
1.79
2.11
1.70
1.66
1.80
1.64
2.08
1.96
1.67
1.59
SOLIT
IONIC
IMBAL
-4.5
-4.7
-12.0
-6.0
-12.9
-9.4
-8.6
-11. f
-10. "
-6.6
-3.0
10.3
1.5
3.8
-10.7
9.2
5.2
8.1
5.5
5.4
5.0
8.0
8.9
3.6
1.7
7.6
8.3
-5.1
-3.9
-10.1
-3.4
-5.9
29.2
-5.6
3.8
0.9
-6.4
-17.1
-12.6
-15. S
-16.9
-12.1
-16.1
-0.4
8.1
-20.1
-17.9
-19.6
-3.0
0.6
4.8
-------
-SOLID ANALYSES AT SCRUBHER 1NLET-
PAGF 10
O
I
RUN
NUMBER DATE
563-2A 11/14/75
564-2A 11/14/75
11/14/75
11/15/75
11/15/75
11/15/75
11/15/75
11/15/75
11/15/75
11/16/75
11/16/75
11/16/75
11/16/75
11/16/75
11/16/75
11/17/75
11/17/75
11/17/75
11/17/75
11/17/75
11/17/75
11/18/75
11/18/75
11/18/75
11/18/75
11/18/75
11/18/75
11/19/75
11/19/75
565-2A 11/21/75
11/21/75
11/22/75
ll/2?/75
11/22/75
11/22/75
11/22/75
11/22/75
11/23/75
11/23/75
11/23/75
11/2S/75
11/23/75
11/23/75
11/24/75
11/24/75
ll/2«/75
11/24/75
11/24/75
ll/?4/75
11 '25/75
11/25/75
TIME
0700
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
23 CO
0300
0700
19CO
2300
0300
07CO
1100
1500
1900
2300
0300
0700
1100
1500
1900
23CO
0300
0700
1100
1500
1900
2300
0300
0700
S02
INLET
PPf
3300
372T.
3720
3360
3240
3200
3000
2940
2920
2520
2960
3360
3440
3600
3600
3420
3280
356C
3160
3080
2920
2EOO
2960
2920
2800
3120
3600
3440
4040
3900
4060
3960
3920
4160
3800
368(1
344T.
3440
3280
336(5
34KO
3800
4150
4280
4240
4320
4300
3760
3480
344H
3120
SO? S02
CUTLET REMOVAL
PPM X
320
1060
1480
1280
1200
1160
960
1080
1160
1020
13CO
1400
1560
1600
1560
1440
1200
1670
1480
1500
1180
940
940
1220
1340
1260
1300
1280
1500
1380
1260
1460
1600
isao
154Q
1460
1240
1310
1230
1220
1300
1540
1720
1850
188C
2000
1800
1500
1260
1320
1160
89.3
68.4
55.9
57.8
58.9
59.8
64.5
59.3
56.0
55.1
51.3
53.8
49.7
50.7
52.0
53.3
59.4
48.0
48.1
46.0
55.2
62.8
64.8
53.7
46.9
55.2
60.0
58.7
58.8
60. e
65.6
59.1
54.7
57.9
55.1
56.0
63.3
57.8
56.7
59.7
58.6
55.1
54. 0
52.1
50.8
48.7
53.6
55.8
59.9
57.5
58.8
CAO
WT X
35.00
27.80
24.50
23.60
23. 80
25.30
25.00
25.00
24.00
23.10
23.40
23.90
24.00
22.90
23.70
23.70
22. 30
21.70
23.00
23.30
24.20
23.80
23.40
23.70
23.70
23.30
24.00
22.60
24.10
23.90
23.90
25.70
24.20
22. 2C
24. OC
23.20
23.30
23.10
23.60
23.50
22.50
22.40
22.10
22.40
22.60
23.00
22.20
21.70
22.00
S02
yT x
17.40
21.90
23.70
22.90
23.80
25.60
24.60
24.60
21.50
20.30
21.60
22.80
20.70
20.40
19.40
23.50
20.00
20.20
19.50
20.40
23.00
22.30
20.80
21.40
19.80
15.90
22.10
19.50
23.00
23.80
25.00
24.30
24.90
21.30
24.80
22.20
23.90
21,50
23.50
22.60
21.70
21.70
20.20
22.90
22.00
21.80
21.90
21.30
22.70
S03
yT %
5.25
8.43
4.68
3.18
2.65
3.11
4.25
4.95
6.73
6.03
4.50
5.00
7.73
5.30
6.55
3.43
5.00
4.25
6.03
5.90
3.85
5.13
6.40
5.15
6.55
6.52
4.08
5.83
3.45
3.35
1.86
2.13
3.38
4.18
2.60
3.20
2.43
5.43
3.33
4.65
4. 08
3*58
5.35
1.88
4.10
5.55
3.43
3.18
1.23
TOTAL s
AS S03
yT. x
27.00
35.80
34.30
31.80
32.40
35.10
35.00
35.70
33.60
31.40
31.50
33.50
33.60
30.80
30.80
32.80
30.00
29.50
30.40
31.40
32.60
33.00
32.40
31.90
31.30
31.40
31.70
30.20
32.20
33.10
33.10
32.50
34.50
30.80
33.60
32.20
32.30
32.30
32.70
32.90
31.20
30.70
30.60
30.50
31.60
32.80
30.80
29.60
29.60
C02
UT X
12.09
3.25
2.08
2.11
0.87
1.04
0.63
0.77
1.43
1.31
1.29
0.65
1.07
1.43
1.49
0.83
0.50
0.33
1.82
1.82
1.35
0.88
0.66
0.99
1.79
1.58
1.98
1.60
1.59
0.97
0.88
1.16
0.84
1.07
0.81
0.87
0.88
1.49
0.61
0.77
0.94
0.83
0.88
0.91
0.77
0.72
1.16
1.10
0.94
SLURRY X ACID MOLE X
SOLIDS INSOLS SULFUR
yT. % IN SOLD OXIDIZED
15.7
13.8
14.3
14.3
13.0
12.2
12.6
12.8
12.8
13.2
13.6
14.6
14.6
14.3
15.0
14.5
14.3
13.7
15.1
14.1
13.4
12.2
11.3
12.1
13.5
14.1
15. a
8.5
10.9
13.5
14.5
15.1
14.8
15.5
15.4
14.4
13.6
13.2
14.4
14.8
15.1
lh.3
15.3
14.8
14.8
15.0
14.4
13.8
13.8
4.63
b.14
6.51
7.04
6.57
5.67
5.84
5.80
5.83
6.41
6.71
6.97
6.63
7.14
7.23
7.16
7.48
7.40
7.42
fc.81
6.53
5.88
5.46
5.89
6.40
6.74
7.62
4.23
5.33
6.64
7.28
7.32
7.08
a. 04
7.64
7.31
6.92
6.40
7.19
7.26
7.76
8.00
7.84
7.91
7.54
7.30
7.52
7.41
7.56
19.5
23.5
13. f
10.0
8.2
8.8
12.2
13.9
20.0
19.2
14.3
14.9
23.0
17.2
21.3
10.5
16.7
14.4
19.8
18.8
11.8
15.5
19.8
16.2
20.9
20.8
12.9
19.3
10.7
10.1
5.6
6.6
9.8
13.6
7.6
10. P
7.5
16. f,
10.2
14.1
13.1
11.7
17.5
6.2
13.0
16.9
11.1
10.7
4.2
STOICH
RATIO
l.«l
1.17
1.11
1.12
1.05
1.05
1.03
1.04
1.08
1.08
1.07
1.04
1.06
1.08
1.09
1.05
1.03
1.02
1.11
1.11
1.08
1.05
1.04
1.06
1.10
1.09
1.11
1.10
1.09
1.05
1.05
1.06
1.04
1.C6
1.04
1.05
1.05
1.03
1.03
1.C4
1.05
1.05
1.05
1.05
1.04
1.04
1.07
1.07
1.06
SOLin
ICNIC
I«BAL
1.9
-5.1
-8.9
-5.8
0.0
-2.4
-1.1
-4.0
-5.7
-2.4
-1.3
-1.6
-3.7
-2.2
1.0
-1.4
2.1
2.8
-2.7
-4.4
-1.5
-l.B
-0.6
0.4
-2.1
-3.0
-3.0
-2.6
-2.0
-2.2
-1.7
5.7
-4.3
-3. '3
-2.4
-2.0
-1.9
-6.?
-0.4
-2.2
-2.c;
-0.7
-2.1
-0.6
-2.3
-3.9
-3.8
-2.7
O.T
-------
PAGE 11
-SOLID ANALYSES AT SCRUBBER INLET-
a
PUN
NUPCEF: COTE
5f,
60.1
59.6
55.7
57.9
75.3
87.1
90.9
50.3
89.7
86.0
86.0
62.7
79.9
7«i. 7
80.7
83.1
83.4
82.7
79.6
79.3
80.4
85.5
86. 0
85.9
78.3
68.6
69.7
74.3
73.5
78.9
84.8
79.7
81.6
80.7
82.8
84.5
83.4
88.0
82. B
82.3
76.8
81.6
84.3
84.2
86.9
84.8
84.1
81.0
CAO
WT 1
21.71'
22. 40
22.00
21. bC
21.50
22.00
24.30
2 3 . 9 G
30.90
31.80
32.80
30.10
2H.60
28.30
28.40
28.40
28.70
29.30
28.80
27.50
26.90
27.20
27. 1C
28.40
28.70
27.90
27.00
26.50
26.80
26.20
25.40
26.00
26.90
27.80
27.10
26.60
27.30
28.10
29.20
30.30
29.10
28.20
27.40
27.30
27. 4Q
27.30
28.40
27.90
27.40
27.70
S02
WT x
21.00
17.60
19.30
20.50
21.30
22.20
22.40
21.60
19.90
22.60
18.80
21.20
24.70
22.10
21.30
2-4.70
21.00
21.80
23.20
24.10
25.20
25.10
22.00
21.30
24.10
19.10
24.70
25.30
25.30
25.50
25.30
25.80
24.40
24.50
24.50
26.20
24.30
24.80
23.80
23.90
24.80
26.50
22.60
25.30
25.20
21.30
23. CO
24.80
19.70
20.10
803
WT •/.
2.45
8.20
5.?e
3.46
2.08
1.85
3.00
2.20
5.33
1.85
6.70
6.80
3.13
4.98
5.08
3.23
7.35
6.75
5.30
4.28
5.41
5.63
9.00
8.66
5.18
7.73
3.23
3.38
4.78
0.63
1.68
2.46
3.20
3.88
2.98
1.16
2.63
1.60
2.35
2.63
4.20
3.48
5.45
4.18
1.41
4.08
3.95
2.20
5.28
7.28
TOTAL S
AS S03
JT. X
28.70
30.20
29.40
29.10
28.70
29.60
31.00
29.20
30.20
30.10
30.20
33.30
34.00
32.60
31.70
34.10
33.60
34.00
34.30
34.40
36.90
37.00
36.50
35.30
35.30
31.60
34.10
35.00
36.40
32.50
33.30
34.70
33.70
34.50
33.60
33.90
33.00
32.60
32.10
32.50
35.20
36.60
33.70
35.80
32.90
30.70
32.70
33.20
29.90
32.40
COS
WT X
1.60
o.-><>
1.96
0.83
0.66
C.66
1.87
1.98
H.b6
9.24
9.78
6.28
5.12
5.94
6.82
5.50
5.56
4.55
4.69
3.58
3.08
3.03
2.68
3.30
4.19
6.11
3.85
3.03
1.79
2.31
2.92
3.14
4.51
4.62
4.51
3.27
3.81
4.68
5.23
5.67
4.62
1.66
4.67
3.50
3.68
4.95
5.83
4.58
6.46
4.41
SLURftY
SOLIDS
WT. %
14.2
14.2
13.8
14.2
14.0
14.0
li.8
15.0
15.2
14.7
15.0
14.5
14.5
14.8
15.3
14.9
15.0
15.0
14.6
14.6
14.8
14.4
14.7
14.8
15.1
14.7
14.6
15.1
14.8
15.0
15.5
15.1
14.1
15.3
14.9
15.5
14.6
15.6
15.5
15.2
15.3
15.4
15.2
15.5
15.7
15.5
15.7
15.6
14.9
15.1
X ACID
INS01.S
IN SOLO C
7.70
6.94
7.10
7.69
7.81
7.68
6.86
7.74
5.25
5.31
4.62
5.05
5.76
5.74
5.86
5.87
5.45
5.52
5.57
5.98
5.90
5.64
5.55
5.42
5.74
5.55
6.20
6.47
6.20
7.20
7.25
6.68
5.94
6.15
6.26
7.00
6.33
6.67
6.33
5.92
5.60
6.42
6.03
6.31
6.99
6.45
6.25
6.62
6.10
5.94
MOLE X
SULFUR
JXIOI2ED
a. 6
?7.2
18.0
12.0
7.2
6.3
9.7
7.5
17.6
6.2
22.2
20.4
9.2
15.3
16.0
9.5
21.9
19.9
15.5
12.4
14.6
15.2
24.7
24.6
14.7
24.5
9.5
9.7
13.1
1.9
5.0
7.1
9.5
11.2
8.9
3.4
8.0
4.9
7.3
8.1
11.9
9.5
16.2
11.7
4.3
13.3
12.1
6.6
17.7
22.5
STOICH
RATIO
1.10
1.06
1.12
1.05
1.04
1.04
1.11
1.12
1.53
1.56
1.59
1.34
1.27
1.33
1.39
1.29
1.30
1.24
1.25
1.19
1.15
1.15
1.13
1.17
1.22
1.35
1.21
1.16
1.09
1.13
1.16
1.16
1.24
1.24
1.24
1.18
1.21
1.26
1.30
1.32
1.24
1.08
1.25
1.18
1.20
1.29
1.32
1.25
1.39
1.25
SOLIO
IONIC
IMBAL
-2.0
-0.1
-5.1
1.6
2.6
1.9
O.K
3.9
-5.0
-3.3
-2.5
-4.1
-6.1
-7.4
-8.H
-8.8
-6.7
-1.1
-4.2
-4.2
-10.7
-9.5
-6.9
-1.9
-4.8
-7.2
-6.6
-7.1
-3.6
1.9
-6.5
-8.9
-9.1
-8.1
-8.1
-4.9
-2.5
-2.5
0.2
1.0
-5.0
1.6
-7.9
-8.2
-1.2
-1.9
-6.6
-4.3
-6.5
-2.2
-------
PAGF: 12
-SOLID ANALYSES AT SCRUBBER INLET-
d
I
324ft
1360
3080
3P40
3120
?920
256P
2280
3000
3080
3000
2S40
3000
2920
3100
3200
30«0
2960
3560
3660
3800
372n
3720
3960
4200
4020
3960
3160
332"
2840
2800
3320
3419
3640
343P
3360
5120
3200
3120
3800
360C
3400
?3SP
3J6P
32CO
2»00
266C
S02 S02
CUTLET REMOVAL
PPM %
560
740
560
500
560
420
380
440
320
260
240
440
420
480
380
380
440
390
440
360
380
48P
560
560
5RO
660
640
800
75"
640
440
520
480
560
940
1060
1040
920
1000
1060
960
940
1360
1200
1040
1050
1040
900
840
8*;5
81. fl
78.0
82.4
82.9
81.6
84.9
86.2
84.4
87.9
88.8
88.4
83.8
84.9
82.3
85.2
86.0
83.3
86.1
84.8
87.1
85. 8
85.1
83.2
63.7
82.7
80.4
82.1
78.9
79.1
82.1
84.6
82.7
61.3
77.9
63.6
65.8
68.3
70. 0
67.0
62.3
66.3
66.6
60.3
63.1
66.1
65.4
65.7
68.8
66. R
65.2
CAO
WT %
27.60
27.90
29.00
28.90
2H.90
28.80
28.80
29.70
30.80
31.00
30.40
29.70
29.80
30.10
29.60
?9.90
30.20
29.90
30.20
30.60
30.70
30.70
30.80
30.90
30.80
30.50
30.50
29.80
29.90
30.70
30.60
30.80
23.50
27.60
27.20
26.50
25.50
25.10
27.50
29.50
26.60
25.00
22.96
22.50
26.90
24.90
27.70
23.20
24.60
24.70
S02
tit %
20.80
19.00
23.90
22.20
25.30
22.20
22.80
23.10
21.70
22.90
22.20
20.80
23.00
16.90
22.00
22.30
20.70
22.20
21.90
20.80
21.10
22.30
23.00
21.10
21.20
21.80
21.80
24.90
28. CO
24.00
27.90
21.10
26.90
27.60
27.20
27.80
24.40
23.40
27.60
26.80
26.30
24.50
22.81
21.40
25.70
25.60
25.80
24.40
23.60
25.10
S03
UT %
6.3U
7.15
3.03
3.25
1.38
3.35
3.10
3.23
4.08
2.98
3.05
4.50
3.75
6.28
3.30
3.33
4.93
3.85
4.33
4.30
3.63
3.63
2.65
4.43
5.10
4.05
5.25
2.68
1.21
4.80
1.83
5.53
3.68
4.11
4.81
3.06
4.80
5.85
7.71
5.51
6.73
6.18
7.81
7.75
7.48
2.51
6.96
3.30
5.60
2.83
TOTAL S
AS S03
UT. %
32.30
30.90
32.90
31.00
33.00
31.10
31.60
32elO
31.20
31.60
30.80
30.50
32.50
27.40
30.80
31.20
30.80
31.60
31.70
30.30
30.00
31.50
31.60
30.80
31.60
31.30
32.50
33.80
36.20
34.80
36.70
31.90
37.30
38.60
38.80
37.80
35.30
35.10
42.20
39.00
39.60
36.80
36.32
34.50
39.60
34.50
39.20
33.80
35.10
34.20
C021
UT %
5.28
6.33
5.94
6.82
5.80
6.59
5.92
7.15
8.80
8.80
8.47
9.21
6.29
9.57
7.92
7.87
8.25
6.22
7.80
8.69
8.97
8.75
8.20
9.16
8.73
8.47
8.20
6.C1
4.64
7.84
5.16
9.38
3.80
2.64
2.15
1.82
1.49
1.72
0.88
0.99
0.94
1.16
0.73
0.59
0.72
0.72'
1.05
1.49
1.54
1.39
SLURRY X ACID MOLE X
SOLIDS INSOLS SULFUR
WT. % IN SOLO OXIDIZED
14.9
15.3
15.1
14.9
15 = 1
14.7
15.0
15.2
15.1
14.8
14.3
14.6
15.8
15.5
15.0
15.1
15.2
15.1
15.4
15.8
15.5
15.3
15.6
15.5
15.7
15.5
15.9
15.4
15.7
15.0
14.7
15.0
14.2
1.4.0
14.5
15.7
14.7
14.3
14.9
14.8
15.1
15.8
15.7
15.2
lb.2
14.5
14.2
14.0
5.89
5.89
5.96
5.88
6.14
5.87
6.05
5.71
5.28
5.23
5.30
5.25
6.02
S.58
5.69
5.67
5.44
5.80
5.59
5.64
5.63
5.40
5.65
5.38
5.36
5.50
E.45
5.83
6.11
4.9?
5.41
4.95
5.89
7.21
5.55
6.94
6.30
19.5
23.2
9.2
10.5
4.2
10.8
9.8
10.1
13.1
9.4
9.9
14.8
11.6
22.9
10.7
10s7
16.0
12.2
13.7
14.2
12.1
11.5
9.0
14.4
16.2
13.0
16.2
7.9
3.3
13.8
5.0
17.3
9.9
10.6
12.4
8.1
IS. 6
16.7
18.3
14.1
17.0
16.8
21.5
22.5
18.9
7.3
17.7
9.8
16.0
8.3
STOICH
RATIO
1.30
1.37
1.33
1.40
1.32
1.39
1.34
1.41
1.51
1.51
1.50
1.55
1.35
1.64
1.47
1.46
1.49
1.36
1.45
1.52
1.54
1.51
1.47
1.54
1.50
1.49
1.16
1.32
1.23
1.41
1.26
1.53
1.19
1.12
1.10
1.09
1.08
1.09
1.04
1.05
1.04
1.06
1 .04
1.03
1.03
1.04
1.05
1.08
1.08
1.07
SOLIO
IONIC
IMBAL
-6.4
-6.5
-5.6
-"5.2
-5.6
-4.8
-3.1
-5.7
-7.4
-7.6
-6.5
-11.4
-3.3
-4.3
-7.0
-6.6
-6.2
-0.5
-6.4
-5.5
-5.7
-8.2
-5.8
-7.6
-8.0
-7.7
-8.9
-5.1
-4.6
-11.9
-5.5
-11.4
-8.7
-10.2
-10.0
-8.7
-4.4
-6.7
-11.6
3.1
-8.8
-9.0
-14.9
-10.7
-6.5
-0.7
-4.0
-10.2
-7.9
-r y
-------
PAGE 13
-SOLID ANALYSES AT SCRUBBER INLET-
"UN
NUKPER DATE
568-PA 12/12/75
12/12/75
12/12/75
12/12/75
12/12/75
12/12/75
12/13/75
12/13/75
12/13/75
12/13/75
12/13/75
12/13/75
12/13/75
12/14/75
12/14/75
12/14/75
12/14/75
12/14/75
12/14/75
M 12/14/75
I 12/15/75
-si 12/15/75
w 12/15/75
12/15/75
12/15/75
12/15/75
12/15/75
12/15/75
12/16/75
12/16/75
12/16/75
569-2A 12/16/75
12/16/75
12/16/75
12/16/75
12/16/75
12/17/75
12/17/75
12/17/75
12/17/75
12/17/75
12/17/75
12/17/75
12/18/75
12/18/75
12/18/75
12/18/75
12/18/75
12/18/75
12/19/75
12/19/75
TI^E
0702
1100
1500
1900
2300
2301
0300
0700
1100
1500
1502
1900
2300
0300
0700
1100
1500
1502
230C
23D1
0300
0700
1100
1500
1501
1900
230C
2301
0300
07BO
0701
1500
1501
1900
2300
2301
0300
0700
1100
1500
1501
1900
2300
0300
0700
1102
1500
1900
2300
0300
0700
S02
INL5IT
PPW
2640
3200
3160
3520
3480
3500
3560
3680
3400
3200
3280
3200
3080
3480
332(1
3080
2720
2840
2840
2800
3360
3360
3600
3600
3360
324C
3320
3720
3720
3720
3520
3800
3800
3540
3720
3600
4000
4000
3560
3000
2780
2520
2400
2240
2720
2640
2640
SO?
OUTLCT 1
PPM
830
1000
8Bf!
1240
1360
1*70
1380
1500
1240
1100
1300
1140
1060
1380
1260
11CO
900
900
910
960
1140
1100
1240
1260
12CO
1100
1210
1320
1400
1400
1200
1500
1480
1000
1260
1000
1460
1480
1160
900
830
600
620
540
720
623
700
SO?
REMOVAL
X
65.2
65.4
69.1
60.9
56.7
5f>.6
57.0
54.8
59.6
61.9
56.1
60.5
61.8
56.0
57.9
60.4
63.3
64.9
64.5
62. C
62.4
63.7
61.8
61.2
60.4
62.4
59.6
60.7
58.3
58.3
62.2
56.2
56.8
68.7
62.5
69.2
59.5
59.0
6 3-. 9
66.8
66.9
73.6
71.4
73.3
70.7
74.0
70.6
CSC
'JT %
23.50
20.80
24.70
25.40
24.20
23.30
24.10
21.50
24.40
24.90
24.62
23.80
23.50
21.50
24.80
23.10
22.00
25.00
24.60
22.30
24.00
26.50
24.60
26.30
24.00
24.40
26.90
24.70
24.90
25.00
23.70
23.10
24.10
24.20
25.20
22.90
23.60
24.40
23.70
28.20
23.50
24.40
23.80
22.50
24.20
24.40
23.50
22.50
SOS
UT X
25.00
22.30
?3.30
22.10
22.20
22.40
23.20
21.30
24.30
19.10
23.30
23.10
22.20
21.60
25.50
24.10
25.80
24.90
25.10
21.10
21.00
23.50
24.00
23.90
21.10
25.30
25.30
24.90
25.70
27.40
23.40
23.20
23.10
22.90
22. 9C
19.30
20.80
23.40
20.90
20.90
21.10
22.90
19.70
18.10
18.00
17.10
19.10
13.10
S03
UT X
7.36
5.53
11.88
11.78
3.95
4.30
3.80
7.88
9.63
15.23
10.78
4.73
5.45
4.30
8.63
6.08
10.16
5.68
4.43
5.83
7.65
8.63
4.40
7.63
7.23
2.88
5.98
3.48
2.78
0.76
3.55
6.50
3.63
4.58
9.68
5.38
5.50
3.35
6.38
8.28
5.03
5.18
6.28
6.08
5.60
6.23
5.33
6.58
TOTAL S
AS S03
WT. X
38.60
33.40
41.00
39.40
31.70
32.30
32.80
34.50
40.00
39.10
39.90
33.60
33.20
31.30
40.70
36.20
42.40
36.80
35.80
32.20
33.90
38.20
34.40
37.50
33.60
34.50
37.60
34.60
34.90
35.00
32.80
35.50
32.50
33.20
38.30
29.50
31.50
32.60
32.50
34.40
31.40
33.80
30.90
28.70
28.10
27.60
29.20
29.20
C02
«T X
1.39
0.83
1.09
0.90
1.38
1.38
1.49
1.57
1.00
0.67
0.63
1.32
1.32
1.24
0.92
1.24
1.83
1.38
1.38
1.49
0.96
0.70
0.61
0.61
0.43
0.44
0.44
1.10
0.72
0.53
0.71
0.71
1.27
1.44
1.44
2.28
1.53
1.46
1.05
1.05
0.99
0.73
1.76
1.70
1.11
1.63
1.79
1.62
SLURRY
SOLIDS :
YT. x :
14.7
14.7
15.9
15.1
15.2
15.2
lb.1
15.2
14.8
16.0
15.1
14.7
14.5
15.6
15.5
15.3
14.7
15.0
14.9
15.5
15.7
14.3
15.9
15.8
15.8
15.6
15.6
15.6
15.3
15.3
14.3
14.3
14.6
14.7
15.5
14.4
14.6
14.2
14.3
14.6
15.4
14.6
14.3
14.5
* ACID
[NSCLS
IN SOLJ C
6.22
7.46
5.81
5.61
7.41
7.46
7.31
7.12
5.81
b.30
5.82
7.01
6.90
8.07
6.00
6.93
5.71
6.51
6.79
7.67
7.13
6.72
7.40
7.71
6.58
7.35
7.42
7.67
7.61
7.47
6.77
5.57
7.30
7.11
7.56
6.82
7.23
7.27
MOLE X
SULFUR
IXIDIZEO
19.1
16.6
29.0
29.9
12.5
13.3
11.6
22.8
24.1
38.9
27.0
14.1
16.4
13.8
21.7
16. 8
24.0
15.4
12.4
18.1
22.6
23.1
12.8
20.3
21.5
8.3
15.9
10.1
8.0
2.2
10.8
18.3
11.2
13.8
25.3
1K.2
17.5
10.3
19.6
24.1
16.0
15.3
20.3
21.2
19.9
22.6
18.2
22.5
STOICH
RATIO
1.07
1.U5
1.05
1.04
l.OQ
1.03
1.08
1.0ft
1.05
1.03
1.03
1.07
1.07
1.07
1.04
1.06
1.08
1.07
1.07
1.08
1.05
1.03
1.03
1.03
1.02
1.02
1.02
1.C6
1.04
1.03
1.04
1.04
1.07
1.08
1.07
1.14
1.09
1.08
1.06
1.06
1.06
1.04
1.10
1.11
1.07
1.11
1.11
1.10
SOL IP
IONIC
I"BAL
-22.6
-17.6
-21.9
-13.2
1.0
-4.7
-3.2
-21.7
-20.1
-13.4
-16.9
-6.0
-6.1
-9.3
-19.7
-If.. 6
-45. fa
-10.1
-9.1
-9.7
-4.0
-4.3
-1.1
-2.6
-0.3
-1.3
0.0
-3.6
-1.9
-0.6
-0.8
-11.6
-1.2
-3.7
-13.7
-2.9
-1.8
-1.2
-1.7
9.8
1.0
-1.1
-0.4
1.0
12.8
12.3
3.3
-0.1
-------
it
-SOLID ANALYSES AT SCRUBBER INLET-
d
I
-vl
"UN
NUMPER DATE
56-5-26 12/19/75
12/19/75
12/19/75
12/20/75
12/20/75
12/20/75
12/20/75
12/20/75
12/20/75
12/20/75
12/21/75
12/21/75
12/21/75
12/21/75
12/21/75
12/21/75
12/21/75
12/2?/75
12/22/75
12/22/75
12/2?/75
12/22/75
12/22/75
12/22/75
12/27/75
12/23/75
12/23/75
570-2A 12/23/75
12/23/75
12/23/75
12/23/75
12/23/75
12/24/75
12/24/75
12/24/75
12/24/75
12/24/75
12/24/75
12/24/75
12/?5/75
32/25/75
12/25/75
12/25/75
12/25/75
12/25/75
12/25/75
12/?6/75
12/26/75
12/26/75
12/26/75
12/2&/75
TIME
1500
1900
2300
030C
0700
1100
1500
1501
1900
2300
0300
0700
1100
1500
1501
1900
2300
0300
0700
1100
150P
1501
1900
2300
0300
0700
0701
1100
1500
1501
1900
2300
0300
0700
1100
1500
1501
1900
2300
0300
07CC
1100
1500
1501
1900
2300
0300
0700
noa
1500
1900
S02
INLET
PPM
2960
2840
2880
2880
2880
2800
2920
2950
3240
3200
3240
32 4 n
3000
3080
3000
3320
3800
3840
3800
3520
?440
2420
2440
2640
2640
2920
2960
2800
2840
2860
2960
3360
3600
3440
3320
3000
2860
5600
2600
2480
P4RP
2600
2560
2560
3080
3520
3280
3200
3200
3320
3200
SC2 S02
OUTLET REMOVAL
PPM X
900
980
960
1100
960
900
10£0
1080
1200
1000
1120
1020
860
940
960
1140
1240
1500
1340
1340
820
810
800
820
98-0
500
900
780
560
550
600
920
10&P
940
960
66P
630
600
640
540
500
580
5fiO
570
700
980
820
P40
840
880
840
66.3
61.7
63.1
57.7
63.1
64.4
59.0
59.4
58.9
65.4
61.7
65.1
68.2
66.2
64.5
61.9
63.8
56.7
60.9
57.8
62.7
62.9
63.7
65.6
6S.1
65.8
66.3
69.1
78.2
78.7
77.6
69.7
67.4
69.7
68.0
75.6
75.6
74.4
72.7
75.9
77.7
75.3
74.9
75.3
74.8
69.1
72.3
70.9
70.9
70.6
70.9
CAO
«iT X
23.20
22.60
23.30
23.80
22.10
23.80
25.20
23.10
24.60
24.70
24.80
23.90
23.70
25.00
23.90
25.40
25.40
24.80
24.30
24.20
23.90
23.80
24.00
24.10
24.10
24.50
24.60
25.20
28.30
26. 1C
25.30
25.70
24.30
26.30
25.60
29.00
26.10
25.30
26.10
24.70
26.00
26.20
28.20
26.20
26.00
26.20
26.40
2S.OC
26.90
26.10
SC2
•*T X
21.10
17.60
21.80
22.90
18.70
23.10
23.00
21. 5?
23.80
24.00
23.50
24.40
23.00
23.00
20.40
24.00
24.90
23.20
20.20
22.20
22.10
21.80
20.60
19.90
19.60
19.60
18.60
19.00
18,90
18.20
21.10
22.70
22.50
25.10
23.70
23.70
22.20
21.40
23.20
22.50
24.30
23.90
23.90
21. bO
22.40
24.20
21.70
23.40
24.20
2 1 . * 0
S03
UT X
3.73
6.60
2.75
2.68
4.83
3.23
9.15
3.93
3.05
3.30
3.73
2.00
2.85
6.95
5.00
3.60
3.08
2.90
5.45
3.95
7.88
2.85
4.65
5.53
5.70
6.20
6.75
5.05
8.98
4.65
4.J3
3.83
1.78
2.73
3.58
6.08
5.55
4.95
4.60
2.78
3.73
4.43
9.63
5.25
3.70
2.55
5.38
2.75
3.45
3.65
TOTAL S
AS S03
HT. %
30.10
28.60
30.00
31.20
28.20
32.10
37.90
30.80
32.80
33.30
33.10
32.50
31.60
35.70
30.50
33.60
34.20
31.90
30.70
31.70
35.50
30.10
30.60
30.40
30.20
30.70
30.00
23.80
32.60
27.40
30.60
32.20
29.90
34.10
33.20
35.70
33.30
31.70
33.60
30.90
34.10
34.30
39.50
32.50
31.70
32.80
32.50
32.00
33.70
31.10
C021
yr %
1.06
1.85
1.64
0.65
1.36
1.27
1.27
1.16
1.42
1.35
1.52
1.25
1.54
1.54
1.43
1.35
1.60
1.52
1.70
0.94
0.94
1.16
1.13
1.45
1.61
1.51
2.05
3.30
3.52
4.95
3.74
2.86
2.97
2.75
3.03
3.03
3.36
3.26
2.79
2.79
2.71
3.19
3.19
4.24
4.31
4,02
4.11
3.69
3.73
4.91
SLURRY X ACID MOLE %
SOLIDS INSOLS SULFUR
UT. % IN SOLD OXIDIZED
15.2
15.2
14.7
14.9
15.1
15.1
15.1
15.9
15.3
15.4
15.3
16.2
15.4
15.4
15.5
16.1
15.7
15.5
15.1
14.5
14.5
14.4
14.8
14.0
14.7
14.7
14.7
15.3
15.3
14.9
15.3
15.5
15.7
15.3
15.0
15.0
15.0
14.4
13.2
X3.8
14.1
ie.3
18.3
16. a
15.3
14.7
14.0
14.9
14.7
15.1
7.85
7.64
7.61
7.67
7.98
7.55
6.03
fi.07
7.39
7.37
7.27
8.15
7.72
6.60
7.65
7.52
7.31
7.56
7.29
7.15
6.37
7.39
7.33
fc.79
7.15
7.01
G.90
7.20
5.82
6.84
7.03
7.10
7.87
6.81
6.78
5.70
fa. 44
6.49
5.78
£.66
t.27
7.84
6.13
6.82
6.78
6.55
5.95
6.75
6.31
6.63
12.4
23.1
9.2
fi.3
17.1
10.1
24.2
12. «
9.3
9.9
11.3
6.2
9.0
19.5
16.4
10.7
9.0
9.1
17.8
12.5
22.2
9.5
15.9
18.2
18.9
20.2
22.5
17.5
27.5
17.0
13.8
11.9
6.0
8.0
10.8
17.0
16.7
15.6
13.7
9.0
10.9
12.9
24.4
16.2
11.7
7.8
16.6
8.6
10.3
12.4
STOICH
RATIO
1.06
1.12
1.10
1.04
1.09
1.07
1.06
1.07
1.0«
1.07
1.08
1.07
1.09
1.08
1.09
1.07
1.09
1.09
1.10
1.05
1.05
1.07
1.07
1.09
1.10
1.09
1.12
1.21
1.20
1.33
1.22
1.16
1.18
1.15
1.17
1.15
l.lfl
1.19
1.15
1.16
1.14
1,17
1.15
1.24
1.25
1.22
1.23
1.21
1.20
1.29
SOLIO
IONIC
IMBAL
3.^
0.9
0.8
4.7
2.H
-1.3
-11.8
0.2
-0.&
-1.4
-1.7
-l.<3
-1.7
-7.9
3.0
0.6
-2.3
2.1
2.6
3.?
-9.1
5.2
4.7
4.0
3.7
4.4
4.0
3.3
3=^
2.3
-3.6
-1.9
-l.h
-4.1
-5.9
0.-3
-5.8
-4.2
-3.8
-2.0
-5.2
-7.2
-12.5
-7.5
-6.5
-7.2
-6.1
-4.3
-5.4
-7 -
-------
-SOLID ANALYSES AT SCRUBBER INLfT-
PAGr. 15
Ul
PUN
NUMBER
570-2A
571-?A
571-26
57?-2«
HATE
12/26/75
12/27/75
12/27/75
12/27/75
12/27/75
12/27/75
12/27/75
12/28/75
12/28/75
12/28/75
12/28/75
12/28/75
12/28/75
12/29/75
l?/29/75
12/29/75
12/29/75
12/29/75
12/25/75
12/30/75
12/30/75
12/30/75
12/30/75
12/30/75
12/30/75
12/30/75
12/31/75
12/31/75
12/31/75
12/31/75
12/31/75
12/31/75
01/01/76
Rl/01/76
01/01/76
Cl/01/76
Cl/01/76
n 1/01/76
01/02/76
01/02/76
01/02/76
01/02/76
01/02/76
"1/02/76
Cl/02/76
"1/02/76
01/02/76
01/03/76
01/03/76
01/03/76
01/03/76
TIME
2300
0300
0700
HOC
1500
1900
230C
0300
0700
1100
1500
1900
230C
0300
0700
1100
1500
1900
2300
0300
0700
0701
1100
150C
1900
2300
030C
0700
1100
1500
1902
2300
03CC
0700
1100
1500
1900
2300
0300
0700
1100
1500
1700
1900
2100
2130
2300
C3CC
0700
1100
1500
S02
INLET
PPM
276D
2560
2680
2600
2320
2360
2600
2490
2680
2760
2950
3140
3480
384P
3810
3380
28-80
2720
2720
3160
304P
3040
2P80
2760
2700
2700
?6«0
2720
272C
2360
2220
2120
-2500
3160
2680
2480
?52P
2560
3240
3320
2800
2760
2560
2440
2480
250C
2480
2840
3160
3200
3200
SC2 S02
OUTLET REMOVAL
PPM %
GRO
6?0
680
660
560
5?0
720
560
640
840
820
880
1200
1340
1300
1040
780
680
580
760
720
700
700
720
700
700
660
660
580
510
390
370
54C
760
580
480
510
540
960
960
520
480
540
620
1120
1070
860
1060
9F.O
1180
1140
72.7
73.2
71.9
71.9
73.3
72.3
69.3
75.0
73.5
66.3
69.3
68.9
61.8
61.3
62.5
65.
-------
PAGF 16
-SOLID ANALYSES AT SCRUBBER INLET-
b
RUN
NUMCER DATE
572-2A 01/03/76
01/0 V76
Pl/04/76
Gl/04/76
01/01/76
rl/04/76
Cl/04/76
Cl/04/76
Pl/05/76
Cl/05/76
01/05/76
Cl/05/76
01/05/76
Pl/05/76
f 1/06/76
Cl/06/76
B 1/06/76
01/06/76
01/06/76
01/06/76
01/06/76
^1/07/76
01/07/76
01/07/76
"1/07/76
Cl/07/76
01/07/76
Ol/Ofi/76
01/08/76
01/08/76
01/08/76
Cl/08/76
01/08/76
01/09/76
"1/09/76
573-2A " 01/09/76
01/09/76
Cl/10/76
01/10/76
573-2B 01/1^/76
01/13/76
01/13/76
01/13/76
01/13/76
Cl/l?/76
01/13/76
01/13/76
01/13/76
M/17/76
01/13/76
r.l/13/76
TIME
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
0701
1100
1500
1900
23CO
0300
0700
1100
1500
1900
2300
D300
07 RO
1100
15PO
1900
2300
C300
G70C
1100
1500
0700
1500
0800
1200
1230
1260
1300
1330
1400
1430
150C
153G
1600
163C
S02
INLET
PPP
3240
3240
3320
3680
3683
328(1
384C
3720
3400
3640
3760
3640
332"
2920
2440
3000
2980
3080
2960
3000
352C
3640
3500
3360
2680
2520
2480
3240
3400
3480
3080
252f>
2480
2600
2840
2720
348C
3640
3000
2960
2880
3000
S02 S02
OUTLET REMOVAL
PPM %
1120
1120
1200
1360
144C
1200
1480
1560
1520
1500
1640
1500
1360
1100
1000
1280
1240
1280
1100
1240
1580
1640
1500
1500
1100
920
1120
1100
1280
1220
1200
1000
9fifl
loan
lion
760
600
4?0
420
400
54C
660
61.7
61.7
59.9
59.0
56.6
59.4
57.3
53.5
50.4
54.3
51.6
54.3
54.6
58.2
54.6
52.7
53.9
53.9
58.8
54.2
50.2
50.0
52.5
50.5
54.5
59.5
49.9
62.4
58.3
61.1
56.8
56.0
56.2
53.9
57.1
69.0
80.9
87.?
84.5
85.1
79.2
75.6
CAO
WT %
22.30
22.80
22.33
22.40
22.00
22.40
23.10
23.70
22.40
21.80
22.50
22.80
23.00
23.40
23.90
24.00
24.30
24.40
23.60
22.70
23.50
23.10
22.20
23.40
21.90
21.60
21.20
20.80
20.10
20.70
19.80
1.9.50
20.40
21.20
21.20
22.70
34.00
33.20
35.30
33.80
33.10
31.90
30.30
30.00
28.50
27.70
27.50
S02
yT %
18.70
18.60
18.30
19.20
18.50
19.20
20.80
21.20
17.30
17.40
16.80
20.00
20.70
17.90
18.30
21.10
20.90
21.40
21.20
19. 4C
21.10
19.70
19.40
21.40
14.30
14.40
18.10
17.40
13.70
14.90
15.80
13.70
16.10
19.20
16,20
16.80
15.50
17.80
16.50
18.20
17.20
19.10
20.80
20.80
19.90
21.70
23.00
S03
UT %
3.83
4.55
4.53
2.60
3.46
2.40
1.70
2.90
5.48
4. 65
6.70
4.30
4.23
6.63
7.33
5.03
5.38
6.75
5.30
5.75
5.93
6.48
5.65
5.05
10.83
9.50
4.38
4.75
6.38
5.18
3.25
5.68
4.38
1.20
4.55
5.30
5.03
3.05
4.08
2.65
4.90
3.93
3.40
3.30
3.63
3.08
3.45
TOTAL S
AS SOS
UT. X
27.20
27.80
27*40
26.60
26.60
26.40
27.70
29.40
27.10
26.40
27.70
29.30
30.10
29.00
30.20
31.40
31.50
33.50
31.80
30.00
32.30
31.10
29.90
31.80
28.70
27.50
27.00
26.50
23.50
23.60
23.00
22.80
24.50
25.20
24.80
26.30
24.40
25.30
24.70
25.40
26.40
27.80
29.40
29.30
28.70
30.20
32.20
C021
yT %
1.06
1.71
2.09
1.27
1.98
1.63
1.39
1.71
1.42
1.44
1.65
1.55
1.35
1.75
1.60
0.39
0.23
0.74
1.10
1.32
0.93
1.16
1.02
0.61
0.39
0.53
2.48
0.61
1.73
1.49
2.04
1.91
1.38
1.05
1.01
1.39
10.92
12.43
16.42
13.29
11.49
10.57
8.41
7.30
7.23
6.63
5.30
SLURRY % ACID MOLE %
SOLIDS INSOLS SULFUR
UT. X IN SOLD OXIDIZED
13.7
14.1
14.7'
15.7
15,1
14.7
14.9
14.6
14.4
14.3
-14.8
14.6
14.3
13.5
14.4
14.6
13.6
13.2
14.9
15.4
14.9
14.4
16.3
14.2
14,9
15.8
13.8
12.9
13.6
14.2
14.5
14.2
14.5
13.6
15.5
17.3
7.45
7.40
7.75
8.72
8.27
8.11
8.13
7.53
7.64
7.15
6.71
6.66
6.67
7.22
7.52
7.64
7.14
8.04
7.25
8.01
3.88
7.82
7.33
8.09
8.22
8.33
8.36
8.20
7.22
5.24
4.74
14.1
16.4
16.5
9.8
13.1
9.1
6.2
9.9
20«2
1?.6
24.2
14.7
14.1
22.9
24.3
16.0
17.1
20.2
16. T
19.2
18.4
20.8
18.9
15.9
37.7
34.6
16.2
17.9
27.1
21.8
14.1
24.9
17.9
4.8
18.4
20.2
20.6
12.1
16.5
10.4
18.6
14.1
11.6
11.3
13.3
10.2
10.7
STOICH
RATIO
1.07
1.11
1,14
1.09
1.14
1.11
1.0"
1.11
1.10
1.10
1.11
1.10
1.08
1.11
1.10
1.02
1.01
1.04
1.06
1.08
1.05
1.07
1.06
1.03
1.02
1.04
1.17
1.04
1.13
1.11
1.16
1.15
1.10
1.08
1.07
1.10
1.81
1.89
2.?1
1.95
1.79
1.69
1.52
1.45
1.46
1.40
1.30
SOLin
IONIC
I»IBAL
8.5
5.0
2.0
9.6
3.8
8.2
8.3
3.9
7.2
6.6
4.4
1.3
0.8
3.7
3.0
6.3
8.0
0.0
-0.3
0.0
-1.3
-0.7
-0.2
1.5
5.9
7.7
-4.1
7.0
7.1
10.3
5.5
5.6
7.3
10.4
12.0
11.0
8.8
-1.1
-8.3
-2.7
-0.1
-3. 3
-3.3
0.6
-2.9
-6^.9
-6.t
-------
PAGE 17
-SOLID ANALYSES AT SCRUBBER 1NLET-
t)
I
"UK
NUI-6ER
57J-2B
574-2A
575-2A
576-2A
DATE
01/13/76
!H/l?/76
Cl/13/76
ri/13/76
01/13/76
91/13/76
01/11/76
^1/14/76
Cl/14/76
Cl/14/76
Cl/14/76
01/14/76
11/14/76
Tl/14/76
01/14/76
01/14/76
•U/14/76
fil/14/76
01/15/76
M/l«j/76
PI/15/76
01/16/76
PI/16/76
01/16/76
"1/16/76
ri/lo/76
ri/16/76
01/17/76
01/17/76
31/17/76
01/17/76
fU/17/76
01/17/76
Cl/18/76
01/18/76
01/18/76
01/18/76
fU/18/76
Cl/18/76
01/19/76
Cl/19/76
01/15/76
01/19/76
01/19/76
Cl/19/76
01/20/76
01/20/76
ri/20/76
fil/20/76
01/20/76
01/20/76
TIfE
1700
1730
1800
1830
190."
1930
0030
0100
0130
0200
0230
030C
0330
0400
0430
OSOr;
0533
0600
1500
1900
2300
03CO
0700
1100
1500
1900
2300
0300
0700
1100
15CO
1900
2300
0300
0700
1100
1500
1900
2300
0300
0700
1100
1500
1900
2300
030P
0700
0701
11PO
1500
1900
sr>2
IMLrT
PPM
3000
3120
352H
3040
3000
2960
2960
2960
3000
2600
3200
3100
3160
3200
3200
3120
2800
2680
2760
2600
30SO
3400
352'0
3560
3040
3400
3520
3400
3520
3120
3040
3160
3240
3240
3000
2720
260?
2840
2800
3480
3800
388P
?^ 2
OUTLET '
pen
740
1000
1460
500
540
620
760
980
1380
580
920
880
8ftO
860
1000
1040
920
820
600
54D
800
840
88C
680
720
B20
1040
820
960
800
840
760
82C
820
720
500
509
560
570
960
1320
1060
SO 3
*C«OVAL
*
72.7
64.5
5«.0
81.8
80.1
76.8
71.6
63.3
49.0
75.3
66.1
68.5
69.1
70.2
65.4
63.1
63.6
66.1
75.9
77.0
71.2
72.6
72.3
78.8
73.8
73.3
67.3
73.3
69.8
71.6
69.4
73.4
72.0
72.0
73.4
79.6
78.7
78.2
77.5
69.4
61.5
69.7
CAO
*T %
25.90
25.70
25.60
24.70
24.50
24.40
28.70
28.60
28.20
27. 8C
27.00
27.30
29.10
29.00
28.30
28.00
27.70
27.30
26.10
24.20
25.00
23.70
24.90
25.10
25.00
24.00
24.40
24.80
24.20
23.20
24.40
25.20
26.80
26.20
23.60
24.50
26.00
25.30
25.00
24.60
25.40
26.00
26.60
26.40
27.30
27.40
28. 20
28.20
?7.00
25.90
26.30
S02
WT %
23.00
23.10
22.90
23.70
22.80
21.50
19.90
18.60
21.40
20.20
22.60
23.50
23.10
24.50
24.00
23.80
24.20
22.70
22.80
18.90
23.10
18.20
24.30
24.80
25.70
22.40
24.60
22.30
20.30
20.70
21.40
16.90
21.30
22.10
21.20
21.90
22.40
21.30
23.20
20.30
21.10
21.50
23.20
24.10
25.50
20.90
21.80
21.80
27.20
24.30
23.20
SO 3
HT %
0.35
1.43
3.68
1.88
3.30
4.E3
4.23
4.15
2.25
3.55
1.45
4.23
10.73
10.78
9.60
9.85
9.65
10.63
4.20
6.38
4.53
6.65
3.53
3.10
3.18
5.50
2.15
2.63
3.63
2.43
2.55
5.38
3.08
2.58
3.30
3.33
3.50
4.78
3.20
5.13
3.83
4.33
5.20
3.58
2.03
5.68
5.25
5.25
2.01
5.43
6.80
TOTAL S
AS S03
JT. X
29.10
30.30
32.30
31.50
31.80
31.40
29.10
27.40
29.00
28.80
29.70
33.60
39.60
41.40
39.60
39.60
39.90
39.00
32.70
30.00
33.40
29.40
33.90
34.10
35.30
33.30
32.90
30.50
29.00
28.30
29.30
26.50
29.70
30.20
29.80
30.70
31.50
31.40
32.20
30.50
30.20
31.20
34.20
33.70
33.90
31.80
32.50
32.50
36.00
35.80
35.80
C02
MT X
4.55
3.99
2.91
2.32
1.58
1.63
8.76
9.40
8.94
7.95
6.25
3.62
4.11
2.81
2.18
1.51
1.28
1.00
3.00
3.30
1.88
3.72
1.17
1.48
0.88
1.16
1.04
2.71
3.43
2.69
2.97
6.16
5.12
4.38
2.24
2.53
3.58
3.41
2.29
3.05
3.00
3.05
2.97
3.03
3.71
5.51
5.67
5.78
2.64
1.65
2.70
SLURRY
SOLIDS
WT. X
15.4
13.6
14.9
15.3
14.0
14.7
15. 4
15.3
15.3
15.1
15.8
15.0
14.3
15.8
15.0
14.8
14.5
14.8
15.8
14.9
14.6
14.7
15.0
14.8
14.6
15.5
14.5
15.2
15.9
14.2
14.2
15.1
15.3
15.6
X ACID
INSCLS
IN SOLD C
7.08
6.05
6.91
7.27
6.57
6.93
7.22
7.11
7.21
7.47
7.70
7.34
7.73
7.86
6.86
6.63
6.71
7.47
7.72
6.77
6.61
6.95
7.01
6.97
6.62
6.52
6.35
6.59
6.39
5.55
5.54
6.54
6.60
6.35
HOLE X
SULFUR
IXIOIZED
1.2
4.7
11.4
6.0
10.4
14.4
14.5
15.2
7.8
12.3
4.9
12.6
27.1
26.0
24.3
24.9
24.2
27.3
12.9
21.3
13.6
22.6
10.4
9.1
9.0
15.9
6.5
8.6
12.5
8.6
8.7
20.3
10.4
8.5
11.1
10.8
11.1
IS. 2
10.0
16.8
12.7
13.9
15.2
10.6
6.0
17.9
16.2
16.2
5.6
15.2
19.0
STOICH
RATIO
1.28
1.24
1.16
1.13
1.09
1.09
1.55
1.62
1.56
1.50
1.38
1.20
1.19
1.12
1.10
1.07
1.06
1.05
1.17
1.20
1.10
1.23"
1.06
1.08
1.05
1.06
1.06
1.16
1.22
1.17
1.19
1.42
1.31
1.26
1.14
1.15
1.21
1.20
1.13
1.18
1.18
1.18
1.16
1.16
1.20
1.32
1.32
1.32
1.13
1.01
1.14
SOLID
IONIC
I«BAL
-1.1
-2.4
-2.9
-1.3
0.9
1.'
-9.9
-9.0
-12.4
-9.0
-6,5
-3.1
-13.3
-12.3
-7.8
-5.9
-6.8
-4.7
-2.4
-4.2
-3.2
-6.9
-1.4
-2.7
-3.4
-3.3
0.1
-0.1
-2.0
-0.2
0.4
-4.8
-2.0
-2.0
-0.5
-0.9
-2.4
-4.1
-1.9
-2.6
1.7
1.0
-4.3
-4.0
-4.3
-6.9
-6.?
-6iB
-5.9
-5.3
-8.4
-------
PAGE IP
-SOLID ANALYSES AT SCRUBBER INLET-
d
I
^J
00
"UN
NUMBER HATE
576-2A 01/20/76
fll/21/76
01/21/76
Cl/21/76
"1/21/76
"1/21/76
01/21/76
01/22/76
'1/22/76
Cl/22/76
576-2!- Cl/22/76
01/22/76
"1/22/76
Cl/22/76
01/^2/76
577-2A 01/22/76
01/22/76
ni/23/76
01/23/76
Pl/?3/76
r -1/23/76
01/23/76
f'1/23/76
11/24/76
01/24/76
Cl/24/76
01/24/76
01/21/76
r-t/24/76
01/25/76
01/25/76
01/25/76
ri/25/76
' 1/2^/76
01/25/76
f 1/26/76
r 1/26/76
'1/26/76
dl/26/76
Cl/26/76
fl/26/76
Cl/27/76
f 1/27/76
01/27/76
01/27/76
01/27/76
01/27/76
rl/27/76
f 1/28/76
ri/28/76
"1/28/76
TI1E
2300
nsoo
0700
1100
1500
1900
2300
0300
0301
03*5
0130
050C
"530
0600
0630
1900
2300
03CO
C700
1100
15CC
1900
23 CO
03CO
0700
1100
1500
1900
23PO
0300
0700
1100
1500
190C
2300
ojon
07on
1100
1500
190?
2300
1300
C7CC
C701
1100
1500
19GO
23GO
0300
07CO
HOD
SO?
INLET
PP1
1000
3600
2«40
?.1HQ
2100
3320
34*0
3320
3350
3360
3010
3360
3010
3560
3800
3560
3000
3010
2880
2B80
2B90
2920
2810
?160
25fiC
3D80
3210
3100
3080
300C
3010
2880
2760
2800
3320
3680
3760
3560
3720
3710
3880
3110
3160
352C
3920
3720
340P
S02 S02
OUTLET REMOVAL
PPM X
1000
10 20
71C
520
580
800
900
800
780
1020
1200
780
ISO
620
700
560
120
160
120
100
12C
120
100
740
120
5?C
52C
700
110
360
4fiO
100
360
10Q
580
760
860
610
580
550
82R
600
560
700
8&C
760
660
72.3
68.6
71.1
76.8
73.2
73.3
71.3
73.3
71.2
66.1
56.2
71.3
82.5
80.7
79.6
82.6
81.5
83.3
83.9
81.6
83.9
81.1
81.1
81.7
81.8
81.3
82.2
77.2
81.2
86.7
82.5
81.6
85.6
81.2
80.7
77.1
71.7
80.1
82.7
83.7
76.6
73.8
90.4
78.0
75.7
77.1
78.5
CAO
yT x
27.20
26. bO
24.70
25.00
21.10
21.00
24.90
21.40
26.20
24.80
21.70
24.10
23.10
23.40
22.80
24.00
25.20
26.20
26.00
27.80
28.40
28.40
28.10
33.30
29.20
29.60
29.60
2S.50
28.10
33.20
21.20
25.50
2.7.60
27.60
?7.6D
30.80
2fi.80
28.80
28.20
28.60
27.90
29.50
28. 1C
28.20
27.60
27.60
27.90
26.60
26.20
27.20
26.40
S02
yT %
19.flO
20.20
22.90
22.20
22.30
20.90
23.20
20.40
22.90
18.00
20.00
21.10
21.80
21.20
20.80
22.60
18.90
22.90
21.60
19.10
25.30
24.90
22.80
25.40
23.30
22.60
26.80
24.10
22.00
23.90
17.70
18.50
24»90
21.70
23.40
24.90
20.80
22.10
24.50
22.90
22.50
23.80
24.20
24.20
24.40
25.10
23.40
21.40
21.60
23.10
23,30
S03 TOTAL S
AS S03
UT X UT. X
10.25
10.75
1.38
4.45
3.23
3.68
2.20
3.50
1.G8
6.50
5.10
1.63
3.65
5.60
5.00
2.65
5.38
1.08
2.20
6.43
1.88
2.68
4.10
4.26
6.18
5.05
2.91
4.38 -
4.10
5.03
1.88
5.98
1.98
4.38
2.75
2.68
5.60
5.78
4.08
4.88
4.28
1.95
3.15
3.05
2.60
1.43
3.35
4.85
3.40
3.53
2.*8
35.00
36.00
33.00
32.20
31.10
29.80
31.20
29.00
29.70
29.00
30.10
31.00
30.90
32.10
31.00
30.90
29.00
29.70
29.20
30.30
33.50
33.80
32.60
36.00
35.30
33.30
36.40
34.50
31.60
34.90
24.00
29.10
33.10
31.50
32.00
33.80
31.60
33.40
34.70
33.50
32.40
31.70
33.40
33.30
33.10
32.80
32.60
31.60
30.40
32.40
31.70
C021
WT X
2.17
1.33
1.35
2.07
2.31
2.64
2.66
3.31
3.64
4.07
3.58
2.75
1.93
1.10
1.27
1.87
2.36
3.64
4.66
5.24
4.98
4.52
4.35
5.88
5.58
5.01
4.06
5.79
5.21
4.72
2.99
5.37
4.01
4.93
4.73
4.40
4.78
4.99
4.52
4.72
b.83
5.78
4.95
5.01
4.73
4.41
5.24
3.70
3.16
4.46
5.34
SLURRY X ACID IDLE X
SOLIDS INSOLS SULFUR
yT. % IN SOLD OXIDIZED
15.2
14.7
13.8
14.2
15.4
15.5
15.5
15.4
15.?
15.0
13.5
13.5
14.8
15.7
14.1
15.5
15.4
14.7
14.7
15.4
14.2
14.9
15.6
14.4
15.2
15«6
14.9
15.6
15.3
15.7
15.4
15.7
14.8
14.7
15.3
16.0
15.2
16.0
16.0
16.0
15.1
15.2
14.9
14.2
14.6
14.3
14.2
5.79
5.67
6.53
6.65
7.53
7.64
7.56
7.53
7.56
6.85
6.76
6.81
7.05
7.56
6.61
6.28
6.38
6.04
6.07
4.94
5.02
b.62
5.92
5.29
6.25
5.24
e.54
6,85
6.62
6.56
fc.59
6.10
5.67
5.60
6.03
6.24
6.05
6.49
6.51
6.52
6.38
6.60
6.10
6.15
6.77
6.12
6.22
29.3
29.9
13.3
13.8
10.4
12.3
7.1
12.1
3.6
22.4
17.0
14.9
11.8
17.5
16.1
8.6
18.5
3.6
7.5
21.2
5.6
7.9
12.6
11.8
17.5
15.2
8.0
12.7
13.0
14.4
7.8
20.5
6.0
13.9
8.6
7.9
17.7
17.3
11.8
14.6
13.2
6.2
9.4
9.2
7.9
4.4
10.3
15.4
11.2
10.9
8.1
STOICH
RATIO
1.11
1.07
1.07
1.12
1.14
1.16
1.16
1.21
1.22
1.26
1.22
1.16
1.11
1.06
1.07
1.11
1.15
1.22
1.29
1.31
1.27
1.24
1.24
1.30
1.29
1.27
1.20
1.31
1.30
1.25
1.23
1.34
1.22
1.28
1.27
1.24
1.28
1.27
1.24
1.26
1.33
1.33
1.27
1.27
1.26
1.24
1.29
1.21
1.19
1.25
1.31
SOL 1C
IONIC
IMBAL
-0.3
-1.6
-0.6
-0.8
-1.3
-1.0
-1.4
-0.5
2.9
-2.6
-3.8
-4.6
-3.0
-2.1
-2.3
-0.1
7.5
2.9
-1.5
-0.4
-5.0
-3.6
-1.0
1.6
-9.0
-0.4
-3.6
-6.9
-2.1
8.2
2.7
-6.8
-2.5
-2.7
-3.1
4.9
2.0
-3.3
-6.6
-3.1
-8.0
-0.2
-5,7
-5.4
-5.8
-3. '6
-5.8
-0.9
3,4
-4,7
-------
PftGT 1"
-SOLID AfCALYSES AT SCRUBBER INLET-
RUN
NU»»C'EP
577-2A
578-2A
579-?A
580-2A
581-2A
CATF
01/28/76
01/28/76
Cl/28/76
01/29/76
01/29/76
01/29/76
ri/29/76
PI/29/76
01/29/76
01/25/76
ri/29/76
Cl/29/76
01/29/76
Pl/29/76
PI/29/76
01/29/76
01/29/76
01/29/76
01/29/76
01/30/76
01/30/76
01/30/76
01/30/76
01/30/76
1U/30/76
01/31/76
01/31/76
01/31/76
Cl/31/76
01/31/76
01/31/76
01/31/76
02/01/76
02/01/76
"2/01/76
02/01/76
02/01/76
B2/01/76
02/01/76
02/01/76
02/01/76
02/01/76
02/04/76
02/05/76
02/05/76
P2/05/76
02/05/76
02/05/76
02/05/76
C2/06/76
02/06/76
TIPF
1500
1900
2300
0300
0700
1600
1630
1700
1730
1800
1830
1900
1901
1930
2000
2030
2100
21*5
2300
030C
0700
1100
15*0
1900
2330
0300
03fiO
0700
1100
1530
1900
23CG
0300
0700
1100
1530
1900
2055
2130
2200
2230
2315
2330
0330
0730
1130
1530
1930
2330
0330
0730
S02
INLFT
PPM
32
-0.1
2.5
1.2
0.9
-1.7
1.4
-3.6
-2.3
-2.5
-1.3
4.5
-1.0
2.1
6.8
-2.9
-3.1
4.0
-------
PAGE
-SOLID ANALYSES AT SCRUBBER INLET-
o
I
00
o
RUN
NUKPER C/iTE
581-2A 02/06/76
02/06/76
02/06/76
02/06/76
02/07/76
02/07/76
02/07/76
^2/07/76
02/07/76
"2/07/76
02/08/76
T2/08/76
12/08/76
P2/08/76
C2/08/76
02/08/76
02/09/76
02/09/76
02/09/76
02/09/76
02/09/76
V/09/76
02/10/76
02/10/76
02/10/76
02/10/76
02/10/76
02/10/76
12/11/76
?2/ll/76
32/11/76
5R2-2A 02/11/76
C2/11/76
.'2/12/76
"2/12/76
02/12/76
P2/12/76
02/12/76
12/12/76
02/12/76
C2/12/76
02/12/76
"2/l?/76
r2/l?/76
02/12/76
C2/12/76
02/12/76
TIME
1130
1530
1930
2330
0330
0730
1130
1530
1930
2330
0330
0730
1130
1530
1930
2330
0330
0700
1130
1530
1930
2330
033"
0730
1130
1530
1930
2330
0330
0730
1130
1530
1930
0100
0130
0200
0230
0300
0330
0»
2140
2440
2760
2810
27RO
2960
2930
27RO
2ft60
2980
2940
2850
25RC
2620
2580
2560
2560
2540
2360
2440
3400
3480
34RO
3660
3440
3260
2620
2840
29£0
3040
2880
2800
2623
2920
2P80
2900
2980
2960
™^5
3040
SO? S02
OUTLET REMOVAL
PPK X
125
160
270
330
400
425
330
350
530
590
660
540
450
450
410
410
390
400
335
250
610
700
720
.860
660
700
470
465
490
430
410
290
90
100
12!)
240
300
480
aco
1100
93.6
92. a
89.2
87.2
84.1
84.1
87.5
86.1
79.5
78.1
75.1
79.0
80.7
81.0
82.4
82.3
83.1
82.6
84.3
88.7
80.1
77.7
77.1
74.0
78.8
76.2
80.1
B1.9
81.7
82.5
84.2
92.1
96.2
96.2
95.4
90.9
88.9
82.1
70.5
59.9
C&O
WT X
28.70
28.40
26.40
27.30
28.20
28.50
25.60
26.40
26,40
27.40
28.20
25.50
26.40
25.10
24.70
26.60
24.80
22.10
21.60
?3.0D
21.90
26.00
26.80
26.10
25.30
25.80
26.20
25.10
29.00
28.00
29.50
32.20
35.80
38.80
37.70
36.30
34.70
34.10
34.40
33.20
33.00
29.30
28.40
28.60
27.70
28.00
27.70
S02
yT x
17.00
17.30
17.70
18.80
18.30
17.90
18.00
21.70
24.80
19.00
lfl.00
19.60
18.70
19.60
18.70
18.80
17.20
15.60
15.60
19.00
18.30
19.50
21.40
20.90
18.90
18.60
23.10
22.30
21.20
16.50
21.50
lfi.90
14.70
15.10
16.20
17.20
17.70
17.40
19.00
19.80
20.50
20.50
20.30
21.50
20.80
20.90
21.40
S03
UT %
7.85
9.58
8. 06
9.00
10.13
9.13
5.00
6.28
3.60
12.85
14. bO
5.80
8.33
7.80
9.63
10.40
10.10
8.40
7.10
8.15
9.33
12.73
10.75
10.08
10.18
13.25
8.93
3.33
11.50
14«48
11.43
13.18
10.23
10.73
10.55
8.60
9.28
9.85
10.15
9.55
11.18
8.38
9.33
9.93
9.3C
11.58
11.25
TOTAL S
AS 503
WT. X
29.10
31.20
30.20
32.50
33.00
31.50
27.50
33.40
34.60
36.60
37.30
30.30
31.70
32.30
33.00
33.90
31.60
27.90
26.60
31.90
32.20
37.10
37.50
36.20
33.80
36.50
37.80
31.20
38.00
35.10
38.30
36.80
28.60
29.60
30.80
30.10
31.40
31.60
33.90
34.30
36.80
34.00
34.70
36.80
35.30
37.70
38.00
C021
UT X
6.23
4.74
4.60
4.29
4.46
4.71
4.59
3.58
1.53
2.48
2.48
2.63
3.26
3.32
3.05
3.14
3.25
3.34
3.40
1.35
1.14
1.98
1.54
1.49
2.20
1.33
0.81
1.41
1.53
3.69
3.03
5.94
10.95
13.81
12.43
12.82
10.40
10.12
9.74
8.20
6.55
6.22
4.90
3.74
3.47
1.87
1.54
SLU'RRY X ACID "IDLE X
SOLIDS INSOLS SULFUR
WT. X IN SOLD OXIDIZED
16.3
14.9
14.5
15.7
13.9
13.9
14.0
14.1
14.5
15.0
15.0
15.2
14.9
15.0
14.7
15.4
15.1
14.4
16.0
15.4
14.7
15.3
15.2
15.4
15.7
14.8
20.4
15.7
15.6
14.9
14.9
17.0
15.2
5.92
5.61
6.04
6.08
5.08
5.24
6.47
b»88
6.53
5.19
4.76
6.95
6.21
6.45
6.19
5.93
6.34
6.92
8.09
7.24
6.93
5.55
5.61
(.04
6.40
5.44
8.04
7.67
5.28
4.86
4.72
4.39
3.83
27.0
30.7
26.8
27.7
30.7
29.0
18.2
1R.8
10.4
35.1
39.7
19.2
26.3
24.2
29.2
30.7
32.0
30.1
26.7
25.fi
29.0
34.3
28.7
27.fi
30.1
36.3
23.6
10.7
30.3
41.2
29.8
35.8
35.8
36.2
34.3
28.6
29.5
31.2
30.0
27.9
30.4
24.6
26.9
27.0
26.4
30.7
29.6
STOICH
RATIO
1.39
1.28
1.28
1.24
1.25
1.27
1.30
l.l"
l.Ofi
1.12
1.12
1.16
1.19
1.19
1.17
1.17
1.19
1.22
1.23
1.03
1.06
1.10
1.07
1.07
1.12
1.07
1.04
1.08
1.07
1.19
1.14
1.29
1.70
1.85
1.73
1.77
1.60
1.58
1.52
1.43
1.32
1.33
1.26
1.18
1.18
1.09
1.07
SOLID
IONIC
IHBAL
1.3
1.8
-2.?
-3.4
-2.1
1.5
1.9
-•S.9
0.8
-•5.1
-3.9
3.6
0.2
-7.0
-9.^
-4.3
-6.0
-7.7
-6.3
-4.6
-9.6
-9.7
-5.3
-4.4
-4.7
-5.7
-5.0
5.8
1.5
-4.6
-4.0
-3.6
5.1
1.?
0.8
-3.1
-1.6
-2.7
-5.1
-3.8
-3.4
-8.3
-7.6
-6.8
-5.2
-2.3
-3.2
-------
The following codes are used in the database tables as indicated below:
Lime or Limestone Column
L = lime addition
LS = limestone addition
Alkali Addition Point Column
DNC = alkali added into downcomer from the scrubber before
entering the effluent hold tank
EHT = effluent hold tank
MgO and Fly Ash Columns
N = no
Y = yes
Spray Tower Header Configuration
1 = spray nozzle bank 1 (the lowest) on
2 = spray nozzle bank 2 (second lowest) on
3 = spray nozzle bank 3 (second from top) on
4 = spray nozzle bank 4 (top header) on
Mist Eliminator System Configuration Column
1-3P/OV = one three-pass, open-vane mist eliminator installed
2-3P/CV = two three-pass, closed-vane mist eliminators installed
Mist Eliminator Wash, Bottom/Top Column
I = intermittent wash (see Summary Table for details)
C = continuous
i. e. I/C = intermittent bottom wash/continuous top wash
D-81
-------
Dewatering System Column
CL = clarifier used for thickening solids for disposal
CE = centrifuge used for thickening solids for disposal
F = filter used for thickening solids for disposal
i. e.CL/CE = clarifier and centrifuge used in series
TCA Sphere Type Column
TPR = thermoplastic rubber spheres used in TCA beds
Foam = solid nitrile foam spheres used in TCA beds
D-82
-------
Appendix E
TEST RESULTS SUMMARY TABLES
FOR THE VENTURI/SPRAY TOWER
E-l
-------
Table E-l
SUMMARY OF LIME RELIABILITY TESTS
ON VENTURI/SPRAY TOWER SYSTEM
Run No. i
St»rt-o.'-Run Date
End-of-Rur Date
On Stream Hours '
^as Raie. acirr. •$- 330°F
Spray Tower Gas Vel, fps @ 125°F
Venture Spray Tower
^iquor Rales, gpm
Spray Tower L/G, gal/mcf
Percent Solids Recirculated
Effluent Residence Time, min.
Solids Disposal System
Stoichiometric Ratio, moles Ca
added /mole SOj, absorbed
Avg % Lime Utilization, lOQx
molea SOj aba. /mole Ca added
Inlet SOg Concentration, ppm
Percent SOg Removal
Scrubber Inlet pH Range
Scrubber Outlet pH Range
Percent Sulfur Oxidized
Loop Closure, «*„ Solida Diachg.
Calculated Avg % Sulfate Saturation
in Scrubber Inlet Liquor @ 50°C
Dissolved Solids, ppm
Total AP Range, Excluding
Mist Eliminator in, H2O
Venturi AP, in, H2;O
Mitt Eliminator AP, in. HjO
Absorbent
Mint Eliminator
Scrubber Internals
of Run
Method of Control
Run Philosophy
Results
601-1A
10/9/73
i /B/74
2153
25,000
6,7
600/1200
60
7-9
12
Clarifier Only Clarif & Intermittent Clarifier &r Filter
(10/9-11/7) Filter (11/7-12/15) (12/15-1/8)
1. 01-1. 28 1. 02-1. 18 1.04-1. 19
87 91 90
1600-3900 1600-4000 • 2100-4400
68-91 75-95 75-95
7.4-8,5 7, 5-8,5 7,7-8.4
4.7-5.5 4.7-5.5 4.8-5.3
10-30 10-30 10-30
20-26 20-2? 42-52
150 120 180
5700-7500 4600-7300 9800-12, 300
11.0-11.5 11.0-12.0 11.7-12.3
999
0. 16-0. 31 0.21-0.51 0, 51-1.26
to EHT.
(~14 gpm) plus available clarified liquor (-26 gpm). Con-
tinuous wash rate of 0.8 gpm/ft2. 12/15 - 1/8: Bottom
washed with, available makeup water (~'5 gpm} plus available
cycle of 3-1/2 min on/1-1/2 min off. Also, top was washed
All nozzles (7 /header) on top 3 headers aprayed downward.
Scrubber inlet pH controlled at 8. 0 i 0. 2
Initially started as lime reliability verification test. Sub-
sequently, due to apparent reliability of the run, decision
was made that test continue as long-term reliability teat.
Routine inspection on 11/7/74 showed system was generally
clean after 666 hours of operation with clarifier only for
solids disposal. Run was terminated on 1/8/74 due to ID
fan vibration and rapidly increasing pressure drop across
mist, elim. Sulfate based scale formed on moat scrubber
walls and in slurry piping. Top of rnist eliminator SQ^o re-
stricted with solids that fell from outlet duct-work. Mist
eliminator top vanes heavily scaled (300 mils avg. ).
602-1A
3/15/74
4/1/74
393
25,000
6.7
toOO/1200
60
7.5-9. 5
12
Clarifier & Filter
1.02-1. 18
91
2100-3800
87-97
7. 6-8. 3
4.9-5.4
5-28
42-48
165
9500
U. 0-12.0
9
0. 19-0.27
makeup water and added to
EHT.
makeup water (-5 gpm} phis
available clarified liquor
(-34 gpm). Wash rate of 1
on/ 1 min off.
All nozzles on 4 headers
zlea/header on top 3 headers.
System cleaned chemically
(Na2CO3/ sugar/lime stone/
flyash soln, ) followed by
rnech. cleaning. EHT sealed.
spray downward instead of
upward. Capped middle
Scrubber inlet pH controlled
at 8.0 i 0.2
Intended long-term. Sealed
EHT In attempt to reduce
sulfite oxidation and thereby
degree of aulfate saturation.
Run terminated due to scale
(125 mils avg.| and solids de-
posits on mist eliminator top
vanes. Sulfite oxidation and
aulfatfi saturation were not
reduced. Steady state oper-
ation not achieved.
603-1A
4/2/74
4/19/74
395
25,000
6.7 '
600/1200
60
13, 5-16
12
Clarifier & Filter
1.00-1.13
94
2100-4300
85-98
7.8-8.2
4, 8-5. 3
12-22
46-54
135
8200-10,900
11.0-12.0
9
0. 16-0.33
makeup water and added to
EHT.
makeup water (~5 gpm} plus
available clarified liquor
{~21 gpm). Wash rate of 1
All nozzles on 4 headers
ale s /header on top 3 headers.
6 nozzles on bottom header.
Mist eliminator cleaned.
Scrubber inlet pH controlled
at 8. 0 ± 0. 2
Intended long-term* Recir-
cuiated 15% aolHe in attempt
to reduce degree of fulfate
•«tu ration. EHT lealed.
Degree of oulfat* saturation
waa reduced, but run was
terminated due to scale (60
mils avg. } and solids buildup
on the mist eliminator top
vane a.
E-2
-------
Table E-l (continued)
Run No,
Start-of-Run Date
End -of -Run Date
On Stream Hours
Gas Rate, acfm @ 330°F
Spray Tower Gas Vel, fps @ 125°F
Venturi/Spray Tower
liquor Rates, gpm
Spray Tower L/G, gal/mcf
Percent Solids Recirculated
Effluent Residence Time, rnin.
Solids Disposal System
Stoichiometric Ratio, moles Ca
added/mole SO2 absorbed
Avg % Lime Utilization, lOOx
moles SO2 aba. /mole Ca added
inlet SO2 Concentration, ppm
Percent SO2 Removal
Scrubber Inlet pH Range
Scrubber Outlet pH Range
Percent Sulfur Oxidized
Loop Closure, % Solids Discing.
Calculated A vg%Sulfate Saturation
in Scrubber Inlet Liquor @ 50°C
Dissolved Solids, ppm
Total AF Range, Excluding
Mist Eliminator, in. H2O
Venturi AP, in. H2O
Mist Eliminator /* P, in. H2O
Absorbent
Mist Eliminator
Scrubber Internals
System Changes Before Start
of Run
Method of Control
Run Philosophy
Results
604- 1A
4/26/74
7/15/74
1828
25,000
6.7
min. {"-I00)/1200
60
7.5-9.0 ^
17
Clarifier & Filter
1.03-1.30
88
2000-3800
70-92
7.7-8.4
4. 5-5.4
8-30
50-60
130
11,600-13,700
3.3-3.8
1,2-1.5 (Plug 100% open) -
0.20-1,25
Lime slurried to 20 wt % with
scrubber downcomer.
Bottom washed with available
makeup water ("~-5 gpm) plus
1 gpm/ft' on cycle of~3 1/2
min on/1 1/2 min off.
sprayed downward. 7 noz-
zles/header on top 3 headers.
Mist eliminator and outlet
duct cleaned. Sealed EHT
provided with N£ gas purge.
EHT overflow blanked. Lime
slurry makeup added to
scrubber downcomer.
Scrubber inlet pH controlled
at 8. 0 ± 0, 2
Intended 2 wks. To observe
sulfite oxidation and degree of
sulfate saturation with lime
add'n to downcomer, minimum
slurry rate to venturi, sealed
EHT purged with NU gaa, and
8% solids recirculated.
Degree of sulfate saturation
was about 130%. Solids from
outlet duct fell to top of mist
eliminator. Run was termin-
ated due to heavy scale (500
mils avg. ) and solids buildup
on mist eliminator.
6Q5-1A
7/31/74
8/6/74
141
25,000
6. 7
min. (~100)/1200
60
8.0-9.3
17
Clarifier & Filter
1.10-1.17
88
2500-3300
73-81
8.8-9.2
4.9-5. 1
12-28
48-52
115
6, 000-7, 400
3.2-3. 9
1. 5-2. 0 (Plug 100% open)
0.23-0.28
scrubber downcomer.
Bottom washed with available
makeup water only (~5 gpm).
off.
sprayed downward. 7 noz-
zles/header on top 3 headers.
System cleaned.
Scrubber inlet pH controlled
at 9. 0 * 0. 2
Intended long-term. Control
at higher pH in attempt to
reduce sulfite oxidation and
thereby degree of sulfate
saturation. Wash mist elim-
inator with water only.
Run wag terminated due to
scale formation (up to 150
mils) on top mist eliminator
vanes.
606- 1A
8/7/74
8/14/74
170
25, 000
6.7
min. (MOO)/1ZOO
60
7.7-9.0
17
Clarifier
1.10-1. 15
89
2400-3200
67-79
7.8-8.2
5.0-5.2
12-22
18-23
120
5,000-7,000
3.6-3.7
1.9-2.3 (Plug 100% open)
0.23-0.31
scrubber downcomer.
Bottom washed continuously
with 15 gpm (0. 3 gpm/ftz)
raw water only. (Rate was
water).
sprayed downward. 7 noz-
zles/header on top 3 headers.
Mist eliminator cleaned.
Scrubber inlet pH controlled
at 8.0 * 0.2
Intended short-term. Mist
eliminator washed continuous-
ly with raw water only (at rate
greater than available tpakeup
water).
Run was terminated due to
scale formation (50 mils avg.)
on top mist eliminator vanea.
608-1A
8/21/74
9/17/74
610
25,000
6.7
600/1200
60
7.7-9.4
12
Clarifier & Filter
1,05-1.25
87
2000-3750
75-95
7.6-8.4
4.8-5. 1
12-28
48-58
130
7, 500-9, 500
11. 5-12. Q
9
0.22-0.44
scrubber downcomer.
Bottom washed with available
makeup water only ("5. 5 gpm]
Wash rate of 150 gpm (3 gpm/
ft*) for approx. 9 min. every
4 hours.
sprayed downward. 7 noz-
zles/header on top 3 headers.
Mist eliminator cleaned.
Provided for Freon gas
blanket over EHT,
Scrubber inlet pH controlled
at 8. 0 f 0. 2
Int'd 2 wks, 12 min res time,
venturi in service. EHT seal-
ed with Freon. Mist elim. on
4 hr wash cycle. Observe
effects of lime add'n to down-
comer and scaled EHT (com-
pare with Run 601-1A).
Run terminated due to slight
increase in mist eliminator
A P. Inspection revealed
scale buildup (88 mil* »vg. )
on the mist eliminator top
vanes.
E-3
-------
Table E-l (continued)
Run No.
Start-of-Run Date
End-of-Run Date
On Stream Hours
Gas Rate, acfrn @ 330°F
Liquor Rates, gpm
Spray Tower L/G, gal/mcf
Percent Solids Recirculated
Effluent Residence Time, rnin.
Solids Disposal System
added/mole SO2 absorbed
Avg % Lime Utilization, 1 OOx
molea SO? abs. /mole Ca added
Inlet SO;> Concentration, ppm
Percent SOj Removal
Scrubber Inlet pH Range
Scrubber Outlet pH Range
Percent Sulfur Oxidized
Loop Closure, % Solids Dischg.
Calculated Avg % Sulfate Saturation
in Scrubber Inlet Liquor @ 5Q°C
Dissolved Solids, ppm
TotalAP Range, Excluding Mist
Eliminator, in. H2O
VenturiAP, in. HaO
Mist Eliminator AP, in. H2O
Mist Eliminator
Scrubber Internals
System Changes Before Start
of Run
Method of Control
Run Philosophy
Results
609- 1A
9/20/74
IG/2/74
277
25, 000
6.7
. .
60
7.9-9.0
24
Clarifier & Filter
1.07-1.2'5
87
2250-3600
80-96
7.6-8.6
4.7-5.4
12-30
47-52
110
8, 000-10, 000
11.0-11. 9
9
0. Z3-0. 28
1 ' d t 20 ttf
makeup water and added to
scrubber downcomer.
Btm washed with makeup wtr $
2. 7 gpm/ft2 for -±:8 min every
4 hrs. Simultaneous top wash
with remaining makeup wtr at
1 gpm/ft2 through a single
nozzle covering about 14 ft2.
Tot, makeup wtrC^ 5 gpm avg.
sprayed downward, 7 noz-
zlea/header on top 3 headers.
Miat eliminator and outlet duct
cleaned. A single nozzle in-
stalled to provide top wash for
and several holes drilled in
the top vanes of a aecond
Scrubber inlet pH controlled
at 8. 0 ± 0.2.
Intended 2 wks. To observe
the effect of rnist eliminator
the effect of increased resi-
dence time on aulfate satura-
Run terminated as planned.
Sulfate saturation reduced to
vane a clean where top washed.
610-1A
10/2/74
10/13/74
253
25,000
6.7
60
7.8-8.6
24
Clarifier fit Filter
1. 10-1. 25
85
1800-3800 :
87-98
7.8-8.4
4, 8-6. 0
16-26
43-48
110
9, 000-12,000
11.0-12.2
9
0.20-0.33
makeup water and added to
effluent hold tank.
Btm washed with makeup wtr (E
2. 7 gpm/ft for^LS min every
4 hra. Simultaneous top wash
with remaining makeup wtr at
1 gpm/ft2 through a single
nozzle covering about 14 ft .
Tot. makeup wtr'H 5 gpm avg.
sprayed downward. 7 noz-
zles/header on top 3 headers.
Relocated lime addition to
effluent hold bank.
Scrubber inlet pH controlled
at 8.0 ± 0.2.
Intended 2 wka. To observe
the effect on sulfate satura-
tion of lime addition to the
effluent hold tank vs addition
Run terminated as planned,
Sulfate saturation 145%,
clean where top washed.
6H-1A
10/25/74
11/11/74
392
25, 000
6.7
60
8.0-9.3
6
Clarifier & Filter
0. 93-1. Q5*a*
101
-------
Table E-l (continued)
Run No.
Start~o£~Run Date
End-of-Run Date
On Stream Hour3
Gas Rate, acfm @ 330°F
Spray Tower Gas Vel, fps @ 125°F
Venturi/Spray Tower
Liquor Rates, gpm
Spray Tower L/G, gal/mcf
Percent Solids Recirculated
Effluent Residence Time, min.
Solids Disposal System v
Stoichiornetric Ratio, moles Ca
added/male SC*2 absorbed
moles SO2 abs. /mole Ca added
[nlet SO2 Concentration, ppm
Percent SO2 Removal
Scrubber Inlet pH Range
Scrubber Outlet pH Range
Percent Sulfur Oxidized
Loop Closure, % Solids Dischg.
Calculated Avg % Sulfate Saturation
in Scrubber Inlet Liquor @ 50°C
Dissolved Solids, ppm
Total AP Range, Excluding Mist
Eliminator, in, H2O
VenturiAP, in. H2O
Mist Eliminator AP, in. &2O
Absorbent
Mist Eliminator
Scrubber Internals
System Changes Before Start
of Run
Method of Control
Run Philosophy
Results
6 19-1 A
12/19/74
1/2/75
327
25,000
6,7
600/1200
60
7-10
12
Clarifier fc Filter
1,07-1.23
87
1150-4000
70-98
7.3-8.3
4.9-5.7
14-34
53-60
125
6400-8000
10. 8-12, 0
9
0,60-1.10
scrubber downcomer.
Bottom washed with makeup
water at 2. 6 gpm/ft2 for ~ 8
min every 4 hrs. Total make
up"^ gpm avg.
All nozzles on 4 headers
sprayed downward, 7 nozzles/
header on top 3 headers. 6
place. Effluent hold tank
agitator raised to original
Scrubber inlet pH controlled
at 8. OfO. 2.
Intended 2 wks. To observe
the rate of scale buildup on
sloped mist eliminator using
an intermittant, high pressure
fresh water bottom wash.
Run terminated as planned.
The mist eliminator was 25-
30% restricted but the test wa
invalid since 3 of the 9 mist
eliminater underwash nozzles
had lost alignment causing
uneven wash coverage.
621-1A
1/18/75
1/23/75
113
25, 000
6.7
600/1200
60
8-9
12
Clarifier & Filter
1. 20-1.27
81
1600-3600
82-95
7.8-8.3
5. 2-5. 6
12-26
57-61
130
5600-6500
11.3-12.0
9
0. 63-0. 70
Lime slurried to 20 wt % with
scrubber downcomer.
Bottom washed continuously
at 0. 69 gprn/ft2 using a mix~
ture of -^5 gpm fresh water
and ~35 gpm clarified liquor.
All nozzles on 4 headers
sprayed downward. 7 nozzles/
header on tap 3 headers. 6
cleaned.
Scrubber inlet pH controlled
at 8.0j0.2.
Intended 2 wks. To observe
the rate of scale/solids build-
up on the sloped miat elim-
inator washed with a contin-
uous bottomwash using all
available makeup water and
clarified liquor.
Run terminated as planned.
Bottom of mist eliminator top
vane coated with solids (60
mils avg, ).
622-1A
1/30/75
3/5/75
787
25,000
6.7
600/1200
60
7. 2-8. 8
17
Clarifier and
Centrifuge (or filter)
1. 06-1.20
88
2200-3900
71-91
7.1-8.3
4. 7-5. 3
12-28
50-62
115
6500-10, 000
11. 1-12. 5
9
0. 20-0. 30
scrubber downcomer.
3ottom washed with makeup
water at 3.0 gpm/ft2 for
~8 min every 4 hrs. Total
makeup .~5 gpm avg.
All nozzles on 4 headers
sprayed downward. 7 nozzlea/
header on top 3 headers. 6
izontal mist eliminator at an
elevation 1 foot higher than
tal mist eliminator.
Scrubber inlet pH controlled
at 8. Ojt-0. 2.
Intended 2 wks. To establish
base conditions for the per-
formance of the new open-van
(of old design) mist eliminator
with underside washing only.
Run terminated as planned.
Mist eliminator 5% restricted
by scale and solids.
623-1A
3/12/75
3/19/75
162
25,000
6.7
600/1200
60
7.4-8.9
17
Clarifier & Centrifuge
1.07-1.17
89
2700-3700
74-88
7.7-8. 3
4.85-5.1
ll»2i
53-60
105
7000-8400
11.4-11.7
9
0.17-0.20
scrubber downcomer.
Top washed sequentially with
fresh water. Each nozzle (6
total) on 4 min (at 0. 5 gpm/
ft2) with 76 min off between
nozzles. Btm washed with re-
maining makeup wtr at 3 gpm/
t2 for «-3. 5 min every 4 hrs.
All nozzles on 4 headers
sprayed downward. 7 nozzles/
leader on top 3 headers. 6
outlet duct. Installed mist
eliminator sequential topwash
Scrubber inlet pH controlled
at 8. 010. 2.
Intended long term. To ob-
serve the rate of scale/solids
buildup on the mist eliminator
with bottom wash and sequen-
tial topwash.
Run terminated in order to
test higher gas velocities
when inspection revealed the
mist eliminator to be clean
with only a light scattered
dust on the mist eliminator
vanes.
E-5
-------
Table E-l (continued)
Run No.
Start-of-Run Date
End-of-Run Date
On Slream Hours
Gas Rate, acfm @ 330°F
Spray Tower Gas Vel, fps @ 125°F
Venturi/Spray Tower
Liquor Rates, gpm
Spray Tower L/C, gal/mcf
Percent Solids Recirculated
Effluent Residence Time, min.
Solids Disposal System
added/mole SO2 absorbed
Avg % Lime Utilization, lOOx
moles SO2 abs. /mole Ca added
Inlet SO2 Concentration, ppm
Percent SC2 Removal
Scrubber Inlet pH Range
Percent Sulfur Oxidized
Loop Closure, % Solids Dischg.
PI 1 ri A <7 S If t Satu
in Scrubber Inlet Liquor @ 5QDC
Dissolved Solids, ppm
Total ,lP Range, Excluding Mist
Eliminator, in, H2O
Venturi \P, in. H2O
Mist Eliminator /IP, in. H2O
Absorbent
Mist Eliminator
System Changes Before Start
of Run
Method of Control
Run Philosophy
Results
b24-iA
3/19/75
4/23/11
823
30, 000
8.0
600/1200
50
7-10
1?
Clarifier & Centrifuge
1.03-1,20
90
2250-3750
70-87
7.8-8.3
4.8-5.2
12-30
48-58
95
6000-10,000
12. 0-13. 4
9
0. 25-0. 35
scrubber downcomer.
Top washed sequentially with
total) on 4 min (at 0. 5 gpm/
ft2) with 76 min off between
maining makeup wtr at 3 gpm/
sprayed downward. 7 nozzles/
header on top 3 headers. 6
No changes.
Scrubber inlet pH controlled
at 8.0*0.2.
Attempt to operate at an in-
creased gas velocity (8. 0 vs
6. 7 ft/sec).
Run terminated due to Boiler
outage. Mist eliminator 100
percent clean after 823 oper-
ating hours.
625-1A
6/20/75
7/9/75
319
30, 000
8.0
600/1200
50
7.5-9
12
Clarifier & Filter
1. 00-1. 25
89
2000-3350
67-90
7. 6-8. 6
4.4-5. 3
12-38
55-60
115
8500-12, 500
11. 9-12. 4
9
0. 15-0.30
Lime slurried to 20 wt % with
scrubber downcomer.
Top washed sequentially with
total) on 4 min (at 0. 5 gpm/
ft2) with 76 min off between
makeup water at 1. 5 gpm/ft2
header on top 3 headers. 6
System cleaned.
Scrubber inlet pH controlled
at 8. OJ-O. 2.
Intended short term to test
mist eliminator reliability at
one-half the bottom wash rate
used in Run 624- 1A.
Run terminated as planned.
clean except for a light dust
covering ( <2% restricted).
626-1A
7/9/75
8/4/75
569
35, 000
9.4
600/1400
50
8-9
12
Clarifier & Filter
1.05-1.30
85
1750-3250
68-88
7. 7-8. 3
4. 8-5. 2
12-32
52-60
100
8000-12,000
14.2-15
9
0.37-0.40
Lime slurried to 20 wt % with
makeup water and added to
scrubber downcomer.
Top washed sequentially with
total) on 4 min (at 0. 5 gpm/ft2)
makeup water at I. 5 gpm/ft2
All nozzles on 4 headers
aprayed downward. 7 nozzles/
header on top 3 headers. 6
No changes.
Scrubber inlet pH controlled
at 8. 0+0. 2.
Attempt to operate at an
increased gas velocity (9.4
va 8. 0 ft/sec).
Run terminated aa planned.
changed during run, « 2%
restricted).
627-1A
8/5/75
8/13/75
187
35,000
9.4
600/1400
SO
14.8-15.8
20
Clarifier & Filter
1.15-1.33
82
1400-3500
69-93
8.0-8.2
4.7-6.25
12-19
52-56
65
7500-10,000
14-15.4
9
0. 37-0.42
Lime slurried to 20 wt %with
makeup water and added to
EHT.
Top washed sequentially with
total) on 4 min (at 0. 5 gpm/ft2)
2,lea. Bottom washed with
makeup water at 1. 5 gpm/ft^
for 6 min (constanti/4hrs.
All nozzles on 4 headers
sprayed downward. 7 nozzles/
leader on top 3 headers, b
Fan damper cleaned.
Scrubber inlet pH controlled
at 8. 0+0. 2.
Attempt to operate at a gas
vel. of 9.4 ft/sec with 15%
solids reclrc. Also to deter-
mine aulfate sat. with increas-
ed % solids recirc. , higher
res, time (20 min va 12 min)
and lime add'n to the EHT.
Run terminated ae planned to
System developed sulfite/ear-
bonate scale due to low sulfur
coal (max. outlet pH = 6. 25).
Scale diminishing at end o£ run.
Mist elim 2-3% restricted
(1075 hrs since last cleaning).
E-6
-------
Table E-l (continued)
Run No,
Start-of-Run Date
Jnd-of-Run Date
On Stream flours
Gas Rate, acfm @ 33QDF
Spray Tower Gas Vel.fr* @ 125°F
renturi/Spray Tower
Liquor Rates, gpm
aray Tower L/G, gal/mcf
Percent Solids Recirculated
Effluent Residence Time, min.
Solids Disposal System
Stoicbiometric Ratio, moles Ca
added/mole SO^ absorbed
Avg % Lime Utilization, lOOx
moles SOz abs. /mole Ca added
Inlet St>2 Concentration, ppm
*erceat SO2 Removal
Scrubber Inlet pH Ranee
Scrubber Outlet pH Range
Percent Sulfur Oxidized
joop Closure, % Solids Dischg.
Calculated Avg % Sulfate Saturation
in Scrubber Inlet Liquor @ 50°C
Hssolved Solids, ppm
Total ,i P Range, Excluding Mist
Eliminator, in. HaO
Venturi ^P, in. HaO
Aiat Eliminator .iP, in. E^O
Mist Elimination
Absorbent
Mist Eliminator
Scrubber Internals
System Changes Before Start
of Run
Method of Control
Run Philosophy
Results
6Z8-1A
8/16/75
9/18/75
717
17,000-35,000
4.5-9.4
600/1400 (through 8/25)
600/1600 (after 8/25)
50-117
8-12
12
Clarifier fc Filter
1.04-1. 16
91
1500-4400
70-98
6.2-8,2
4.5-5.5
10-30
52-59
100
5500-9000
10.4-14.6
9
0, 08-0.45
i-paas, open-vane, 316L SS,
Lime slurried to 20 wt % with
makeup water and added to
scrubber downcomer.
Top washed sequentially with
fresh water. Each nozzle (6
total) on 4 min (at 0. 5 gpm/ft2
with 76 min off between noz-
zles. Bottom washed with
makeup water at 1. 5 gpm/ft2
for 6 min (constant)/4 hrs.
All nozzles on 4 headers
sprayed downward, 7 nozzles
leader on top 3 headers. 6
Sy stern cleaned.
Scrubber outlet prl controlled
at 5. OHhO. 5.
Override: Inlet pH^. 8. 0
Attempt to test operability and
controllability of system under
cycling gas load. With venturi
plug A P fixed at 9 in. H2O.
Gas flow range corresponds to
60-160 Mw of boiler load.
Run terminated aa planned.
Mist eliminator 2% restricted
No problems experienced
controlling system.
623- IB
9/18/75
10/7/75
426
19,000-35,000
5.1-9.4
600/1600
57-105
8-10
12
Clarifier & Filter
1.04-1. 17
90
2000-4000
72-96
7.1-8.3
4.3-5.3
14-27
52-56
90
6700-10,000
6,5-14.6
4.0-9.0
0.10-0.40
3-pass, open~ vane, 316L SS,
Lime slurried to 20 wt % with
makeup water and added to
scrubber downcomer.
Top washed sequentially with
fresh water. Each nozzle (6
total) on 4 min (at 0. 5 gpm/ft2)
with 76 min off between noz-
zles. Bottom washed with
makeup water at 1. 5 gpm/ft
for 6 min (conBtant)/4 hrs.
All nozzles on 4 headers
sprayed downward. 7 nozzles/
leader on top 3 headers. 6
No cleaning. Venturi plug
position held constant.
Scrubber outlet pH controlled
at B.OfO. 5.
Override: Inlet pH^ 8.0
Attempt to teat opeTabilityand
controllability of system under
cycling gas load with fixed
venturi plug position (AP =
9 in. HzO at max. gas rate).
Run terminated as planned.
Mist eliminator unchanged
since end of 628-1A (Z%
restricted). No problems
experienced controlling
system.
E-7
-------
Table E-2
SUMMARY OF LIMESTONE TESTS ON
THE VENTURI/SPRAY TOWER SYSTEM
».nNo.
Start-of-Run Date
End-of-Run Date
Cn Stream Hours
Gas Rate, acfm @ 330°F
Spray TowerGas Yel. fps@12S°F
Venturi /Spray Tower
Liquor Rates, gpm
Spray Tower L/C, gal/mcf
Percent Solids Recirculated
Effluent Residence Time, min.
Solids Disposal System
Stoichiometric Ratio, moles Ca
added/mole 3O2 absorbed
A vg '"o Lime stone Utilization, lOOx
moles SC2 abs. /mole Ca added
Percent SO2 Removal
Scrubber Inlet pH Range
Scrubber Outlet pH Range
Percent Sulfur Oxidized
Loop Closure, % Solids Dischg.
Calculated Avg % Sulfate Saturation
in Scrubber Inlet Liquor® 50°C
Dissolved Solids, pprn
Total AP Range, Excluding Mist
Eliminator, in. H2O
Venturi iP, in. H2O
Mist Eliminator &P, in. HgQ
Mist Elimination
Absorbent
Mist Eliminator System
Washing Scheme
Scrubber Internals
of Run
Method of Control
Run Philosophy
Results
7G1-IA
10/9/75
10/12/75
73
35, 000
9.4
600/1600
57
14. 4-17
20
Clarifier & Filter
I. 3-1. 65
68
2400 3250
84-92
5.8-6,0
5.45-5. 65
9-22
58-63
30
8000-9400
14. 5-15.0
9
0. 35-0. 70
3-pass, open-vane, 316L S3,
with clarified process liquor
and added to EHT.
Top washed sequentially with
fresh water. Each nozzle (6
total) on4min(atQ. 5 gpm /ft )
zles. Bottom washed with
makeup water at 1. 5 gpm/ft2
for 6 min (conatant)/4 hrs.
All nozzles on 4 headers
sprayed downward. 7 nozzles/
header on top 3 headers. 6
at 5. 9,+G. 1.
First limestone reliability
test on the venturi/ spray
Run terminated when inspec-
tion revealed mist eliminator
to be 50-60% restricted with
solids.
702- 1A
10/14/75
10/17/75
60
35,000
9.4
600/1400
50
14.8-15.9
20
Centrifuge
1.2-1.7
68
2600-4200
74-92
5.7-5.9
_
5-13
58-65
25
7000-8400
13. 9-14. 6
9
0. 35-0. 60
3-pass, open-vane, 316LSS,
with clarified process liquor
and added to EHT.
Top washed sequentially with
fresh water. Each nozzle (6
total)on4min {at 0. 5 gpm/ft2)
zles. Bottom washed with
makeup water at 1. 5 gprn/ft2
for 6 min (constantf/4 hrs.
All nozzles on 4 headers
sprayed downward. 7 nozzles/
neader on top 3 headers. 6
Mist eliminator cleaned.
at 5. 9_+0, 1.
tical to Run 627- 1A (except
eliminator performance when
different alkali used.
Run terminated when inspec-
tion revealed mist eliminator
to be 45-50% restricted with
solids.
703-1A
10/19/75
11/1/75
319
35,000
9.4
600/1400
50
14-16
20
Centrifuge
1. 0-1. 15
93
2000-4000
50-68
5.1-5.3
4. 6-4. 8
4-22
60-67
100
10,500-13,000
14. 1-15.0
9
0. 30-0.40
3-pasa, open-vane, 316LSS,
with clarifiedprocess liquor
and added to EHT,
Top washed sequentially with
fresh water. Each nozzle (6
total)on4min (atO. 5 gpm/ft2)
zles. Bottom washed with
makeup water at 1. 5 gpm/ftz
for 6 min (constant)/4 hrs.
sprayed downward. 7 nozzles/
leader on top 3 headers. 6
at 5. 2_fO. I.
Observe operability of miat
her inlet pH).
Run terminated after 319
hours. Mist eliminator 1%
restricted and showing
evidence of descaling.
704-1 A
11/3/75
11/6/75
66
35, 000
9.4
600/1400
50
15. 2-16. 3
20
Centrifuge
1.2-1.7
69
2600-4200
81-91
5.6-6.0
5. 0-5. 65
10-40
59-65
55
8700-12, 700
14. 6-14. 7
9
0.35-0.76
3-pas3, open-vane, 316LSS,
with clarified process liquor
and added to EHT,
Top washed sequentially with
fresh water. Each nozzle (6
total) on 4 min fat 0. 5 gpm /ft 2)
zles. Bottom washed with
makeup water at 1. 5 gpm/ftz
for 6 min (conatant)/4 hrs.
All nozzles on 4 headers
sprayed downward. 7 nozzles/
header on top 3 headers. 6 ,»
No changes.
Scrubber inlet pH controlled
at 5.9+0. 1. Override:
Stoich, Ratio ^1.8
Limestone utilization data run
and replication of Run 702- IA
eliminator fouling.
Run terminatedafter 66 hours.
Mist eliminator 45-50%
restricted.
E-8
-------
Table E-2 (continued)
Run No.
St»rt-ol'-Uun O»tr
End-o>t-Run Dale
On Stream Hours
Gas Rate, acfm @ 33Q°F
Spray Tower Gas Vet, fps@ 125°F
Venturi/Spray Tower
..ttjuor Rates, gpm
Spray Tower L/G, gal/rncf
Percent Solids Recirculated
Effluent Residence Time, min.
Solids Disposal System
Stoichiometric Ratio, moles Ca
added/mole SC>2 absorbed
Avg % Limestone Utilization, lOOx
moles SO2 abs. /mole Ca added
Inlet SC>2 Concentration, ppm
Percent SO2 Removal
Scrubber Inlet pH Range
Scrubber Outlet pH Range
Percent Sulfur Oxidized
Loop Closure, % Solids Dischg.
Calculated Avg % SuUate Saturation
in Scrubber Inlet Liquor© 50°C
Dissolved Solids, ppm
Total AP Range, Excluding Mist
Eliminator, in. H2O
Venturi &P. in- HzO
Mist Eliminator aP, in. HzO
Mist Elimination
Absorbent
Mist Eliminator System
Washing Scheme
Scrubber Internals
System Changes Before Start
of Run
Method of Control
Run Philosophy
Results
705-IA
11/7/75
11/13/75
136
35,000
9.4
600/1500
54
14.6-15,8
20
Clarifier fr Filter
1. 1-1.3
83
2800-3900
78-89
5. 6-6. 0
4.95-5,7
2-18
53-66
40
5700-8700
14.0-15.1
9
0,35-0.43
3 pass, open-vane, 316L SS,
Limestone slurried to 60 wt
-------
Table E-2 (continued)
Run No.
Start- of- Run Date
End-of-Run Date
On Stream Hours
Gas Rate, acfm @ 330°F
Spray Tower Gas Vel, fps@ 125°F
Verituri /Spray Tower
Liquor Rates, gpm
Spray Tower L/C, gal/mcf
Percent Solids Recirculated
Effluent Residence Time, min.
Sohds Disposal System
St ' h" " R f r
added/mole SO2 absorbed
Avg % Limestone Utilization, lOOx
moles SO£ abs. /mole Ca added
Inlet SO2 Concentration, ppm
Percent SO2 Removal
Scrubber Inlet pH Range
Scrubber Outlet pH Range
Percent Sulfur Oxidized
Loop Closure, % Solids Dischg.
Calculated Avg % Sulfate Saturation
in Scrubber Inlet Liquor @50°C
Dissolved Solids, pprn
Total A P Range, Excluding Mist
Eliminator, in. HjO
Venturi &F, in, H2O
Mist Eliminator &P, in. H2O
Mist Elimination
Absorbent
Mist Eliminator System
Washing Scheme
Scrubber Internals
System Changes Before Start
of Run
Method of Control
Run Philosophy
Results
709-IA
12/6/75
12/12/75
134
35, 000
9.4
600/1400
50
14. 5-16
12
entriuge
1. 15-1,35
80
2800-4400
74-86
5.6-6. 0
5. 35-5. 65
6-23
61-65
30
5500-6900
13.7-14.4
9
0. 33-0,40
3-pass, open-vane, 316LSS,
Limestone slurried to 60 wt %
with clarified process liquor
and added to EHT.
Top washed sequentially with
fresh water. Each nozzle (6
total) on 3 min (at 0,5 gpm/ft2)
with 7 min off between noz-
zles. Bottom washed contm
0.4 gpm/£t2.
All nozzles on 4 headers
sprayed downward. 7noazles/
header on top 3 headers. 6
Mist eliminator cleaned.
at 1.25 moles Ca/mole SO2
absorbed.
Limestone utilization data run
inator operability with a con-
tinuous underwash at a stoi-
chiornetric ratio of 1.25.
Mist eliminator <1%
restricted.
710-1A
12/12/75
12/22/75
234
35,000
9-4
600/1400
50
14-16
12
1.4-1.6
67
2500-4000
79-97
5.8-6.2
5.55-5.85
1-26 '
57-63
25
5100-6800
14.3-15
9
0.33-0.40
3-pass, open-vane, 316LSS,
with clarified process liquor
and added to EHT.
Top washed sequentially with
fresh water. Each nozzle (6
total) on 3 min (at 0. 5 gpm/ft2)
zles. Bottom washed contm
0.4 gprn/ft2.
All nozzles on 4 headers
sprayed downward. 7 nozzles/
header on top 3 headers. 6
No changes.
at 1. 5 moles Ca/mole SO
absorbed.
Limestone utilisation data
Mist eliminator 5-7%
restricted.
711-1A
12/24/75
12/30/75
144
35, 000
9.4
600/1400
50
14,2-15
6
Centrifuge
i. 14-1. 42
78
2600-3900
73-87
5.4-6. 0
5.0-5.5
2-26
59-65
65
4600-9600
14.5-15.4
9
0. 35-0. 40
3-pass, open-vane, 316LSS,
•with clarified process liquor
and added to EHT.
Top washed sequentially with
fresh water. Each nozzle (6
total)on3rnin (atO. 5 gpm/ft2)
0.4 gpm/ft2.
All nozzles on 4 headers
sprayed downward. 7 nozzles/
header on top 3 headers. 6
EHT agitator lowered. No
cleaning.
Stoichiometric ratio controlled
at 1.25 rnolea Ca/mole SO2
absorbed.
Limestone utilization data
low residence time on the pH
vs. utilization relationship
and on saturation.
Run terminated when control
method changed due to dif-
ficulties in controlling atoi-
residence time.
711-1B
12/30/75
1/2/75
71
35,000
9.4
600/1400
50
14-16
6
1.3-1.54
70
2500-3500
78-84
5. 5-5. 9
5.05-5.2
4-22
56-62
85
10,000-12,700
14.5-15.4
9
0.33-0.38
3-pass, open-vane, 31&L SS,
with clarified process liquor
and added to EHT.
Top washed sequentially with
fresh water. Each nozzle (6
total) on 3 min (at 0, 5 gpm/ft2)
zles. Bottom was ed contm
0.4 gpm/ft2.
All nozzles on 4 headers
sprayed downward. 7nozzles/
header on top 3 headers. 6
No changes.
Scrubber inlet pH controlled
at 5.6±0. 1.
Continuation of 711-1A with
inlet pH controlled at 5. 6*0. 1.
Lime atone utilization wan
70%. Miet eliminator waB
5-7% restricted.
E-10
-------
Table E-2 (continued)
lun No.
Start -of -Run Date
Ind-of-Run Date
On Stream Hours
Gag Rate, acfm @ 330°F
Spray Tower Gas Vel.fpa® 125°F
Venturi/Spray Tower
Aquor Rates, gpm
Spray Tower L/G, gal/mcf
Percent Solids Recirculated
Affluent Residence Time, rnin.
Solids Disposal System
added/mole SO, absorbed
Avg #0 Limestone Utilization, lOOx
moles SOz abs. /mole Ca added
nlet SCj Concentration, pprn
'ercent SO2 Removal
Scrubber Inlet pH Range
Scrubber Outlet pH Range
Percent Sulfur Oxidized
Loop Closure, % Solids DUchg.
Calculated A vg%Sulfate Saturation
in Scrubber Inlet Liquor® 50°C
Dissolved Solids, pprn
Total A P Range, Excluding Mist
Eliminator, in. H2O
Veaturi aP, in. H2O
Mist Eliminator AP, in. ^z°
Mist Elimination
Syatem Configuration
Absorbent
Mist Eliminator System
Washing Scheme
Scrubber Internals
System Changes Before Start
of Run
Method of Control
Run Philosophy
Results
712-1A
1/2/76
1/7/76
119
35,000
9.4
600/1400
50
14.7-15.8
6
Centrifuge
1.3-1. 55
70
2600-4000
84-91
5.6-6.1
5-15-5.65
3-19
60-63
25
6, 500-10, 700
14.6-15.2
9
0, 36-0. 40
3-paaa, open-vane, 316LSS
chevron mist eliminator.
with clarified process liquor
and added to EHT.
Top washed sequentially with
fresh water. Each nozzle (6
total) on 3 min (at 0. 5 gpm/ft )
with 7 min off between noz-
zles. Bottom washed contin-
uously with dil. clar. liq. at
0.4 gpm/ft2.
All nozzles on 4 headers
aprayed downward. 7 nozzles/
header on top 3 headers. 6
nozzles on bottom header.
No changes.
Stoichiometric ratio controlle<
at 1. 5 moles Ca/mole SO-
absorbed.
Limestone utilization data
run to observe the effect of
low residence time on the pH
vs. utilization relationship
Limestone utilization was 70%
Mist eliminator was 10-15%
restricted.
713-1A
1/8/76
1/10/76
52
35,000
9.4
600/1400
50
14-15
6
Centrifuge
1.05-1. 35
83
2600-3260
69-80
5.15-5,4
8-25
59-60
120
10,400-12,100
14.3-15.3
9
0. 38-0. 40
3-paas, open-vane, 316LSS.
chevron mist eliminator.
Limestone alurried to60wt %
with clarified process liquor
and added to EHT.
Top washed sequentially with
fresh water. Each nozzle (6
total) on 3 min (at 0. 5 gpm/ft2)
with 7 min off between noz-
zles. Bottom washed contin-
uously with dil. clar. liq. at
0.4 gpm/ft2.
All nozzles on 4 headers
sprayed downward. 7 nozzles/
header on top 3 headers. 6
nozzles on bottom header.
No changes.
Scrubber inlet pH controlled
at 5.2+0. 1.
Limestone utilization data
run to observe the effect of
low residence time on the pH
vs. utilization relationship
Average limestone utilization
was 83%. Miat eliminator
was 10-12% restricted.
714- 1A
1/19/76
1/26/76
157
35,000
9.4
600/1400
50
14.5-16
6
Centrifuge
1. 15-1. 35*a*
80(i)
2300-3800
84-97
5.3-5.8
_
9-21
57-62
95
25,000-30,500
14.6-15.6
9
0.33-0.40
3-pass, open-vane, 316L SS,
chevron miat eliminator.
Limestone slurried to60wt%
with makeup water and added
to EHT.
Top washed sequentially with
fresh water. Each nozzle (6
total) on 4 min (at 0. 5 gpm/ft2)
zles. Bottom washed with
makeup water at 1, 5 gpm/ft
for 6 min (constant)/4 hrs.
All nozzles on 4 headers
sprayed downward. 7 nozzles/
header on top 3 headers. 6
nozzles on bottom header.
Mist eliminator cleaned.
Stoichiometric ratio controlled
at 1.2 moles Ca/mole SO,
absorbed.
To observe the effect of MgO
addition on the pH vs. utiliza-
tion relationship and on SC>2
removal at 5000 ppm liquor
Average limestone utilisation
was 80%. Mist eliminator
was 2% restricted.
(a)Total stoich. ratio for Ca
& Mg Is 1.18-1.39 (avg.
alkali util. = 78%),
715-1A
1/Z6/76
1/27/76
23
35, 000
9.4
600/0
0
14-18
20
Centrifuge
1.3-1.55^
70{b)
3200-3800
17-32
4. 9- 5. 6
-
9-20
56-66
110
26,000-28,500
13.1-13.9
9
0,35-0.40
3-pass, open-vane, 316L SS,
chevron mist eliminator.
Limestone elurriedtofeO wt %
with makeup water and added
to EHT.
Top washed sequentially with
freshwater. Each nozzle (6
total) on 4 min (at 0. 6 gpm/ft2 )
with 76 rnin off between noz-
zles. Bottom washed with
makeup water at 1. 5 gpm/ft2
for 6 min (constant)/4 hrs.
All nozzles on 4 headers
aprayed downward. 7 nozzles/
header on top 3 headers. 6
nozzles on bottom header.
No changes.
Stoichiometric ratio controlled
at 1, 2 moles Ca/mole SO-
absorbed.
To observe the effect of MgO
addition on the pH va. utiliza-
tion relationship and on SO,
removal at 5000 ppm Hquor
venturi only operation.
Average Hmeatone utilization
was 70%. Run terminated due
to SO, evolution from EHT
and centrifuge and possible
blinding of limestone by
calcium sulfite solid.
(b)Total Btoich. ratio for Ca
& Mg If 1.34-1.59 (avg.
alkali util. = 68%).
E-ll
-------
Table E-2
Run No.
Start-of-Run Date
End- of- Run Date
Co Stream Hours
Gas Rate, acfm @ 330°F
Spray Tower Gas Vel, fps® 125°F
Venniri'Spray Tower
Liquor Rates, gpm
Spray Tower L/C, gal/mcf
Percent Solids Recirculated
Effluent Residence TLme, min.
Solids Disposal System
Stolchiom.tric Ratfo. mol.» Ca
Avg "?„ Limestone Utilization, lOQx
moles SO2 abs. /mole Ca added
Inlet SO2 Concentration, ppm
Percent SQz Removal
Scrubber Inlet pH Range
Scrubber Outlet pH Range
Percent Sulfur Cxidized
Loop Closure, *.. Solids Dischg,
Calculated Avg^,Sulfate Saturation
in Scrubber Inlet Liquor@50°C
dissolved Solids, ppm
Total &F Range, Excluding Mist
Eliminator, in. H2O
Yenturi OP. in. HzC
Mist Eliminator &P, in. HzO
Mist Elimination
System Configuration
Absorbent
Mist Eliminator System
Washing Scheme
Scrubber Internals
System Changes Before Start
of Run
Method of Control
Run Philosophy
Results
716- 1A
1/27/76
1/28/76
18
35, 000
9.4
600/0
0
13-16
20
Centrifuge
1.6-Z.35m/ft
for 6 min (constant)/4 hrs.
All nozzles on 4 headers
nozzle, on bottom header.
No changes.
at 1. 1 moles Ca/rnole SO2
absorbed.
To observe the effect of MgO
addition on the pH va. utiliza-
tion relationship and on SO,
removal at 5000 ppm liquor
venturi only operation.
Average limestone utilization
was 51%. Run terminated due
centrifuge and possible blind-
ing of limestone by calcium
sulfite solid.
Total stoich. ratio for Ca
& Mg is 1.65-2.42 (avg.
alkali util. = 49%).
717-IA
1/28/76
2/5/76
181
35, 000
9-4
600/1400
50
14.5-16
6
Centrifuge
i.i-i.25(b>
85(b)
2700-3700
80-96
5.3-5,6
1. 15-5.4
3-24
53-59
90
23,000-31,000
13.6-15,6
9
0.25-0. 50
3-pags, open-vane, 316 L, SS,
chevron mist eliminator.
with makeup water and added
to EHT,
?op washed sequentially with
fresh water. Each nozzle (6
total) on 4 min (at 0. 5 gpm/ft2 )
sles. Bottom washed with
Tiakeup water at 1 . 5 gpm/ftz
411 nozzles on 4 headers
io»le. on bottom header.
Vo changes.
at 1. 1 moles Ca/mole SO2
absorbed.
To observe the effect of MgO
addition on the pH vs. utiliza-
tion relationship and on SO_
removal at 5000 pprn liquor
Average limestone utilization
was 85%. Mist eliminator
Total stoich. ratio for Ca
& Mg is 1. 13-1,29 (avg.
alkali util. = 83%).
E-12
-------
Appendix F
GRAPHICAL OPERATING DATA FROM THE
VENTURI/SPRAY TOWER TESTS
F-l
-------
BEGIN HUN 62S1*
END RUN 6251,
POWER FAILURE -
FAN COUPLING FAILURE
- PUMP PROBLEM
TEST TIME. Houn
I 6/21 I 6/22 I 6/23 I 6/24 i 6/25 I 6/26 I 6/27 I 8/28 t 6/29 I 6/30 I 7/1
CALENDAR DAY
3,500
3.000
2,500
2,000
1,500
! 7/7 I 7/8 I 7/9 I
0 TOTAL DISSOLVED SOLIDS
O CALCIUM tCa^i ^ 9
O SLJLFATE (S04=!
A CHLORIDE ICI-)
NOTE: SPECiES WHOSE
CONCENTRATIONS ARE LESS
THAN 500 ppm ARE NOT
PLOTTED
AA '
00
QD
00
00
TEST TIME, Houn
I 6/21 1 6/22 I 6/23 I 6/24 j 6/25 | 6/26 I 6/27 | 6/28 I 6/29 | 6/30 i 7/1 ! 7/2
CALENDAR DAY (1975J
440
7/8 1 7/9
10.QC
9,000
8.000
7.000
6.000
5.000
4.000
3.000
2,000
1.000
Gas Rate = 30,000 acfm @ 33Q °F
Spray Tower Gas Velocity * 8.0 ft/sec
liquor Rate to Venturi - 608 gprrt
Uquor Rate to Spray Tower a 1200 gpm
Venturi L/G - 25 gal/mcf
Spray Tower L/C = 50 gal/mcf
No. of Spray Headers = 4
EHT Residence Time = 12 min
Percent Solids Recirculated = 7.5-9 wt %
Venturi Pressure Drop - 9 in.H^O
Total Pressure Drop, Excluding Mist Elim. = 11.9-12.4 in.H^O
Scrubber Inlet Liquor Temperature - 124-130 °F
Liquid Conductivity = 6,600-10,000 u. mhos/cm
Discharge (Clarifier and Filter) Solids
Concentration = 5&-60 wt %
Ume Addition to Scrubber Downcomer
Figure F-1. OPERATING DATA FOR VENTURl^PRAY TOWER RUN 625-1A
F-2
-------
; 3EG1NRUN626-1A
I wo I
I 7/12 I 7/13 I 7/14 I :
TEST TIME, Houra
1 I 7/1B I 7/19 I 7/20 I 7/21 I 7/22 1 7/23 I 7/24 I 7/26 I 7/26 I 7/27 | 7/28 |
CALENDAR OAY
,-*?
E<
11
M"'
10,000
9,000
Oj 8,000
Z >• 8,000
§S S.OOO
8l
Q -J 4,000
> £
8 S 3'000
^ 2.000
1,000
A A
TOTAL DISSOLVED SOLIDS
O CALCIUM (Co**!
D SULFATE (S04"t
A CHLORIDE (Cf~>
NOTE: SPECIES WHOSE
CONCENTRATIONS
ARE LESS THAN 500 f
ARE NOT PLOTTED.
** *A AA *A A* 4*
O XX
O ^o oO OO ^o O
DQ QD DD DO D
OO O
^*AA4 A * A
0 000° O g 00
DUC
10.000
0.000
8,000
7.000
6.000
6,000
4.000
3,000
2,000
1,000
I 7/10
TEST TIME. Ham
I 7/15 I 7/1< I 7/17 I 7/11 I 7/19 I 7/20 I 7/21 I 7/22 I 7/23 I 7/24 I 7/26 I 7/2« I 7/27 I 7/M |
CALENDAR DAY (1975)
G« Raw - 39,000 acfm @ 330 "F
Spray Town G« Velocity - 9.4 ft/nc
Uquor Ran to Vinturl - 600 gpm
Uquor Ran to' Spray Tower - 1,400 gpm
Venturl L/G - 21 gri/mcf
Spray Tower L/G • 50 gal/mcf
No.ofSpnyHeaden-4
EHT Reildenn Time • 12 min
Percent Sdlds Redrculated - 8-9 wl %
Venturl Prenure Drop • 9 In. H20
Total fnuun Drop, Excluding Mtit Ellm. • 14.2-15 In. HjO
Scrubber Inlet Uquor Temperature -130-133 °F
Uquld Conductivity - 11,000-17,000 u. mhos/cm
DlKherge IQarltler and FDterl SolldJ
Concentration » 5240 wt %
lime Addition to Scrubber Oowarcomar
Figure F-2. OPERATING DATA FOR VENTURI/SPRAY TOWER RUN 626 -1A
F-3
-------
RUN 626-1 A CONTINUED
< END RUN 826-1A
3,500
3,000
2,500
2,000
1,500
I 8/3 I 8/4 1 8/5
TEST TIME, Hour*
I 8/7 i 8/8 1 8/9 I 8/10 1 6/11 I 8/12 I 8/13 I 6/14 I 8/15 I 8/16 I 8/17 1
CALENDAR DAY
23-
S " '
lif
Mi
Z D 2
sis
*g*
11*
gal
• TOTAL DISSOLVED SOLIDS
11,000
10,000
9,000
8,000
7,000
6,000
5,000
4,000
3,000
2,000
1,000
0
~9 A • • V CALCIUM (Ca ) THAN SOO ppm ARE NOT
• P SULFATE (SO4=) PLOTTED.
A CHLORIDE (Cl~)
_
"
A A
_A A
-oooo
. °o o <>o °
D na ODD DDDDD
t i I i i i i 1 i i i
11,000
10,000
9,000
8,000
7,000
6,000
5.000
4,000
3,000
2,000
1,000
0
I 7/3) I B/t I fl/2 I 8/3 I 8/4 I 8/5 I fl/6 1
TEST TIME.IIoun
/7 I 8/B I 8/9 1 8/10 |
CALENDAR DAY (1975J
8/11 I 8/12 I 8/13 i 8/14 E 8/15 I 8/16 I 8/17 1
Gas Rate • 35,000 acfm @ 330 °F
Spray Totter Gas Velocity - 9.4 ft/sec
Ljquor Rate to Venturi c 6QO gpm
Llquw Rate to Spray Tower * 1,400 gpm
Liquor L/G • 21 gal/mcf
Spray Tower L/G - 50 gal/mcf
No. of Spray Headers * 4
EHT Residence Time - 12 min
Percent Solids Recirculated • 8-9 wt %
Venturi Pressure Drop - 9 in. HjO
Total Pressure Drop, Excluding Mist Elirn. - 14,2-15 in. HjO
Scrubber Inlet Liquor Temperature - 130.133 °F
Liquid Conductivity 11,000-17,000 ji mhos/cm
Discharge (Qarifier and Filter) Solids
Concentration - 55-60 wt %
Ume Addition to Scrubber Downcomer
Figure F-3. OPERATING DATA FOR VENTURI/SPRAY TOWER RUN 626-1A (Continued)
F-4
-------
BEGIN RUN «ZMA
END RUN t27-1A !
-Joj>
«< e
J «
3.SOO
3.000
2.6W
2,000
_i_
_i_
_i_
_j_
_i_
_1_
_j_
40 BO 120 1BO 200 240 2«0 320 3SO 400 440
TEST TIME, Hotifi
VB I v? I ve I ve I vio I vn I via I v» I VM I vis I vie I vi? I vie I vie I v» I V2i I VK I ens I e«4 I
CALENDAR DAY
l.»
tt « »
5*8 "
ill "
1.0
111 "
g|| *>
lit '°
*• gS o
?1BO
m, —
« S
s|| 1<0
IsS »
*s| ,
10,000
9,000
!_ "°°
1 i 7-' * * .
° 0 * A A * *
oo o o
°OOO OO O <£>
D °n o °
°. D DD.D,, 0° ° 0
1.3
1.2
1.1
1.0
30
20
10
0
1SO
100
BO
0
10,000
9.000
8,000
7,000
8,000
5,000
4,000
3,000
2.000
1.000
a
°0 40 «J 130 leo 200 240 2«0 320 3B 420 410 4»
TEST TIME. Houn
1 ve 1 e/7 1 vi 1 ve 1 vio 1 i/ii 1 v» 1 v» 1 vu 1 vie 1 vie 1 vi7 1 vii 1 vie 1 v» 1 V2i 1 m 1 vn 1 1/24 1
CALENDAR DAY (1975)
6n Rite - 35,000 nfm @ 330 °F
Spriy Tower Gn Vdodty - 9l4 ft/Me
Uquor Rite to Venturl - 600 gpm
Uquor Ritt to Spray Tower - 1,400 gpm
Venturl UB • 21 gd/mcf
Spray Tower L/G - 50 gri/mcf
No.ofSpnyHeiden>4
EHT Rwidence Time - 20 mln
Penint Solldi Reclrculitid • 14.4-15.2 wt %
Venturl Prenure Drop " 9 In. H,0
Total Prenure Drop, Excluding Mln Ellm. - 14-15.4 In. HjO
Scrubber Inlet Uquor Tempiratyra - 126-133 °F
Uquld Conductivity-7,500-11,225 a. mhoi/tm
Ditcharge (Clarifier end FDter) Solid!
Concentration - 52-56 wt %
Lime Addition to EHT
Figure F- 4. OPERATING DATA FOR VENTURI/SPRAY TOWER RUN 627 - 1A
F-5
-------
i §/)7 t 8/1» I i/is I i/ze I a/2i I im I am ! 1/2* I was I t/a I iw I »vzi I i/zs I
O CALCIUM
-------
E 5 i
5
i J \
3.600
3.WO
^ .^ mru;v~ r
' ' sj U
I ». I lf> I *. I » I ,/» I KI1 I ,m I ./.I ! «,. I MS I I/I. I .:,. I ,:,. I ,.',. I ,'» I «„ I
Gas Rate = 17,000-35,000 acfm » 330 °F
Spray Tower Gas Velocity = 4.5-9.4 ft/sec
Liquor Rate to Venturi = 600 gpm
Liquor Rate to Spray Tower -- 1,400,1,600 (after 8/25)
Venturi L/G - 21-44 aal/mtf
Spray Tower L/G = 50-117 gal/mcf
No. of Spray Headers - 4
E HT Residence Time • 12 min
Percent Solids Recirculated - 9-12 wt %
Venturi Pressure Drop = 9 in. rUO
Total Pressure Drop, Excluding Mist Elim. - 10.4-14.6 in. HjO
Scrubber Inlet Liquor Temperature - 129-132 °F
Liquid Conductivity = 7,000-8.600 u. mhos/cm
Discharge (Clarifier and Filterl Solids
Concentration = 52-59 wt %
Lime Addition to Scrubber Downcomer
Figure F-6. OPERATING DATA FOR VENTURI/SPRAY TOWER RUN 628 - 1A (Continued)
F-7
-------
0<>00
3 g o o<>og
u
o °<> °
o Oo0o
40 90 120 180 MO MO 2*0 320 :
B I 9/w I em I */» I t/n \ m« \ ws \ wx I va I Mi I t» i «-» I 10-1 I wa i ,
Gas Rate » 19.000 - 35,000 acfm @ 330 °F
Spray Tower Gas Velocity - 5.1-9.4 ft/sec
Liquor Bate to Venturi = 600 gpm
Liquor Rate to Spray Tower = 1,600 gpm
Venturi l/G = 21-39 gal/mcf
Spray Tower L/G = 57-105 jal/mcf
No, of Spray Headers = 4
EHT Residence Time = 12 min
Percent Solids Recirculated '- 8.6-9.7 wt %
Venturi Pressure Drop • 4.0-9.0 in. HjO
Total Pressure Drop, Excluding Mist Elim. = 6.S-14.6 in,
Scrubber Inlet Liquor Temperature = 129-131 °F
Liquid Conductivity-8,000-11,500 u. mhos/cm
Discharge (Clarifier and Filter) Solids
Concentration • 52-56 wt %
Lime Addition to Scrubber Downcomer
Figure F- 7. OPERATING DATA FOR VENTURI/SPRAY TOWER RUN 628-18
F-8
-------
0 j nuNTOI-IA ! ! RUNTOMA 1
£ S 100
95
< 90
Sl-
£ *
80
75
0.6
3 5 Z- 0.4
|| § 0.2
G.O
6.25
6.00
£ > 5.75
35*
g w 5.50
K
5.25
5.00
4,000
3.500
tu t/ •i-°°0
zo
0 2,500
? WO
n
1
M ^ /I/
\A nftf 1 /l^
- V J
Urt
/ W -J
/ /
-— —-^ ___^/
•
-
-
y — tNLET
"/^\ >st: /~ 'NLET
/ V^^^ x/^L-
r\A
- / Y\s
/ ^ — OUTLET
J
r n/l i
n
./wlj^Wx \AJ \y.
I ^~\A
/
i i i t i i i i i i i
100
95
90
as
80
75
0.6
0.4
0.2
0.0
6.26
6.00
5.75
6.50
5.25
5.00
4,000
3,500
3,000
2,500
0 40 80 120 160 200 240 280 320 360 400 440 480
TEST TIME, Hour*
10/10 1 10/11 1 10/12 1 10/13 | 10/14 I 10/15 1 10/16 I 10/17 I 10/18 1 10/19 1 10/20 I 10/21 1 10/22 t 10/23 1 10/24 1 10/25 1 10/26 1 10/27 1 10/28 1 10/29
CALENDAR DAY
g j | 1.6
1 1 i * ?
r
-^y
05 E ,,L J
K #
a jg £ X
\ll *>
g 2 3 10
K S £
*" x z o
r
*^^S\
\ \_v
1.6
1.4
1.2
1.0
30
20
10
0
O
0 150
HI
~> as ia
!ig -
s2l
c
9 I i"00
5 2,000
1.000
0
-V
\.
•-— ~fc^ /•*--*
"^^
• TOTAL DISSOLVED SOLIDS -
.* O CALCIUM 1C***)
90 • • Q SULFATE (S04=)
• A CHLORIDE )CI~)
* NOTE : SPECI ES WHOSE
CONCENTRATIONS ARE LESS
THAN 500 ppm ARE NOT
PLOTTED.
* * "* A. A A ;
• ^
O <>£> -.O O O
a
a, Daa t t Oo a a , , , , , ,
150
100
SO
0
10,000
9,000
9.000
7,000
6,000
5.000
4.000
3,000
2.000
1,000
w 80 120 160 200 240*280 320 360 400 440 480
TEST TIME. Houn
10/10 I 10/11 I 10/12 | 10/13 1 10/14 | 10/15 1 10/16 I 10/17 I 10/18 1 10/W 1 10/20 | 10/21 1 10/22 1 10/23 I 10/24 1 10/25 1 10/26 1 10/27 1 10/28 I Wtt9 I
CALENDAR DAV (1975)
Gas flan = 35,000 acfm @ 330 °F
Spray Tower Gas Velocity - 9.4 ft/sec
Liquor Rate to Vcmuri = 600 gprn
Liquor Rate to Spray Tower =
1,600 gpm (701-1A), 1,400 gpm 1702-1 A)
Venturi L/6 - 21 gal/mcf
Spray Tower L/G - 57 gal/mcf (701-1 A),
50 gal/mcf (702-1 A)
No, of Spray Headers - 4
EHT Residence Time - 20 min
Percent Solids Recireulatid * 14.4-17 wt % (701-1 A),
14.8-15.9 wt% (702-1 A)
Venturi Pressure Drop = 9.0 in. H.O
Total Pressure Drop, Excluding Mist Elim. = 14.5-15.0 in. HjO
(701-1 A), 13.9-14.6 in. HjO (702-1A)
Scrubber Inlet Liquor Temperature = 123-128 °F
Liquid Conductivity = 10,000-12,000 JL mhos/cm
Discharge (Clarifier and Filter, 701-1 A; Centrifuge, 702-1 A)
Solids Concentration = 58-65 wt %
Limestone Addition to EHT
Figure F- 8. OPERATING DATA FOR VENTURI/SPRAY TOWER RUNS 701-1A & 702-1A
F-9
-------
0 40 80 120 160 200 240 2BO 320 360 400
TEST TIME, Hours
10M9 | 10'20 I 10,'21 I 10/22 I 10/23 1 10/24 I 10/25 I 10/26 i 10/27 t 10/28 I 10/29 I 10/30 | 10/31 I 11/1 ! 11/2 I 11/3 I 11/4 I 11/5 I 11/6 I 11/7
CALENDAR DAY
C i J
!|
^ o"
II 1
1*.
si
5 tr~
ss
: ~ O
xz
o ~
X?
§1
= s
XS
u- 9
O -J
Sg|
ffi
m "e
EC a.
™i
irt .
9 o
S2
S£
5
'i
1!
;;
30
20
10
0
150
100
50
0
16.000
14,000
12.000
10,000
8,000
6.000
4,000
2,000
Q
_
.
(^ .-^, „ /~«,
*- *s*\ / V/ • ^ ^ • /***, j* «L_
r ^--^^^- ^-v f~~^/\> ^ ^w \^ \/^^^—
i. "" ^V
1 -
l\ l\
i \ I \ • A\
/ *--*^^A /^ \ / \ A / ^~*^^\
"*~+^_J \^/ *
A
"^-^. -__^--^^^__^__](^ A\ / ^v^
\ T f -^
•
-
9 TOTAL DISSOLVED SOLIDS
O CALCIUM (Ca++l
0 o u *• e© a SULFATE (S°4a'
« O « ®,»»* ©®0 ® A CHLORIDE (C!-|
NOTE: SPECIESWHOSE
CONCENTRATIONS ARE LESS
THAN 500 ppm ARt NOT
AAAAAA* AAAA PLOTTED.
A A A A *A * *
A * * A * *
ooo o o oo o° °° °o ° o° °o oo
"° ° D a D oa an an aa D aa Da aa
i i i i iu i i i i i i
40 80 120 160 200 240 280 320 360 400 440 4
TEST TIME, Hourj
10/1S | 10/20 1 10/21 | 10/22 I 10/23 ! 10/24 I 10/25 1 10/26 I 10/27 1 10/28 ! 10/29 I 10/30 | 10/31 I 11/1 1 11/2 | 11/13 | 11/4 | 11/5 1 11/6 1 11/7
CALENDAR DAY (1975)
1.3
' 2
il 1
1C
30
20
ID
0
ISO
100
50
0
16,000
14,000
12.000
10.000
8,000
6,000
4,000
2,000
JO
Gas Rite - 35,000 actm e 330 °F
Spr«v Tower Gas Velocity - 9.4 ft/sec
Liquor Rate to Venturi ~ 600 gpm
liquor Rate to Spray Tower = 1,400 gpm
Venturi L/G - 21 gal/mcf
Spray Tower L/G ' SO gal/mcf
No. of Spray Headers - 4
EHT Residence Time = 20 min
Percent Solids Recirculated = 14-16 wt %
Venturi Pressure Drop - 9.0 in. H,0
Total Pressure Drop, Excluding Mist Elim. - 14.1-15.0 in. HjO
Scrubber Inlet Liquor Temperature - 126-128 °F
liquid Conductivity = 11,000-16,400 M. mhos/cm
Discharge (Centrifuge) Solids
Concentration = 60-67 wt %
Limestone Addition to EHT
Figure F-9. OPERATING DATA FOR VENTURI/SPRAY TOWER RUN 703-1A
F-10
-------
si"
HUM /0<-1A i
END RUN 706-1A.
4,000
3,500
3,000
2.500
2,000
1,500
TEST TIME, Hour*
I 11/6 I 11/7 I 11/8 1 11/3 I 11/10 I 11/11 I 11/12 I 11/13 t 11/14 I 11/15 I 11/16 I 11/17 | 11/18 I It/19 I 11/20 Il1/21 I 11/22 I
CALENDAR DAV
4.5
4,500
4,000
3,500
3,000
2.500
2,000
1,500
8'?
f ^
" 3
o 1
S I
er
-1 (O
(CENT SULFt
:ED IN SCRU
si
X
o
H
£ S
|1
cc ^
°- 5
«
ffl
11
Hi
S E
||
Q 3
o z
S ~
a
1 '•'
1.4
1.2
M f. •
- PA;
j
' /
y
-/
A
1.0 1- f
30
:" 20
-
'J
* Ok.
U IRfl
1
®
§ 1W
IJ SO
UJ
S. o
13,000
12,000
11,000
10.000
9,000
8,000
6,000
5,000
4,000
3,000
2,000
1.000
-
~ ~~\
\
^—^
U
" *•
•
<
I AA A
-
- O^* O
^v*
^^\^
^^~^\f^^-^
-
-
lA -^\HAA :
* \ / If*1**-. /^^
•
-
"
\ — -^^^
^ ^ *^
1.8
1.6
1.4
1.2
1.0
30
20
10
0
ISO
100
50
J o
• TOTAL DISSOLVED SOLIDS fWTE: SPECIES WHOSE 1
0 CALCIUMS, rSrARl^"88 1
Q SULFATE (S04-J PLOTTED.
A CHLORIDE (C!~)
• •
.
AAAAAAA
* A
• DQ ° 0<> °<> °0
9n nDi , yO QD|CJ i i i i i i
0 40
13.000
12.000
11.000
10,000
9,000
8,000
7,000
6.000
5,000
4,000
3,000
2.000
1,000
80 120 160 200 240 280 320 360 400 440 480
TEST TIME. Hourt
1 11/4 1 11/5 t 11/6 1 11/7 1 11/8 1 11/9 i 11/10 1 11/11 ! 11/12 I 11/13 1 11/14 1 11/1S I 11/16 1 11/17 t 11/18 1 11/19 t 11/20 1 11/21 1 11/22 1 11/23
CLALENDAR DAV (1975)
Gas Rate = 35,000 aclm » 330 °F
Spray Tower Gas Velocity = 9.4 it/sec
Liquor Rate to Venturi ' 600 gpm
Liquor Rate to Spray Tower *
1,400 jpm (704-1A], 1,500 gpm (705-1AI
Venturi L/G - 21 gal/mcf
Spray Tower L/G = 50 gal/mcf 1704-1 A),
54 gal/mcf (705-1 A)
No. of Spray Headers " 4
EHT Residence Time = 20 min
Note: Only solids data points with
ionic imbalances between i 8.5%
are plotted.
Percent Solids fleciculated = 15.2-16.3 wt % (704-1A),
14.6-15.8 wt%(705"1AI
Venturi Pressure Drop = 9.0 in. H«0
Total Pressure Drop, Excluding Mist Elim. - 14.6-14.7 in. H,0
(704-1AI,14-15.1 in. HjO (705-1A)
Scrubber Inlet Liquor Temperature = 126-131 °F
(704-1A). 124-128 °F (705-1 A)
Liquid Conductivity - 10,000-18,000 OL mhos/cm (7M-1A),
7,800-13,000 a. mhos/cm (705-1 A)
Discharge (Clarifier and Filter, 705-1 A, Centrifuge, 704-1 At
Solids Concentration - 59-65 wt %
1704-1 A), 53-66 wl% (705-1 A)
Limestone Addition to EHT
Figure MO. OPERATING DATA FOR VENTURI/SPRAY TOWER RUNS 704-1A & 705-1A
F-ll
-------
40 80 120 ISO 200 240 280 320 360 400 440
TEST TIME.Moofi
1 11/14 I 11/15 I 11/16 I 11/17 I 11/18 1 11/19 I 11/20 I 11/21 I 11/22 I 11/23 1 11/24 I 11/25 1 11/26 I 11/27 I 1V28 1 11/29 I 11/30 I 12/1 I 12/2
CALENDAR DAY
4.5
4,000
3,500
3,000
2,500
2,000
1,500
O TOTAL DISSOLVED SOLIDS
O CALCIUM (Ca**)
D SULFATE (SO4°)
A CHLORIDE (Cl~)
NOTE: SPECIES WHOSE
CONCENTRATIONS ARE LESS
THAN 500 pptn ARE NOT
PLOTTED.
-J o
10,000
8,000
7,000
6,000
5,000
4,000
3,000
2.000
40 80 120 ISO 200 240 280 320 360 400 440
TEST TIME, Hours
1 11/14 1 11/15 S 11/16 I 11/17 | 11/18 ! 11/19 I 11/20 i 11/21 I 11/22 | 11/23 I 11/24 I 11/25 I 11/26 I 11/27 I 11/28 I 11/29 I 11/30 ! 12/1 I 12/2
CALENDAR DAY (1975)
Gas Rate = 35,000 acfm @ 330 °F
Spray Tower Gas Velocity ™ 9.4 ft/sec
Liquor Rate to Venturi = BOO gpm
Liquor Rate to Spray Tower ~ 1,400 gpm
Venturi L/G = 21 gal/mef
No. of Spray Headers = 4
EHT Residence Time = 12 mtn
Note: Only solids data points with
ionic imbalances between ±8.5%
are plotted.
Percent Solids Recirculated = 14 15wt%
Venturi Pressure Drop -= S.O in. H20
Total Pressure Drop, Excluding Mist Elim. * 14.5-15,2 in.
Scrubber Inlet Liquor Temperature = 126-128 °F
Liquid Conductivity = 9,700-11,500 .u. mhos/cm
Discharge (Centrifuge) Solids
Concentration = 54-76 wt %
Limestone Addition to EHT
Figure F-lt. OPERATING DATA FOR VENTURI/SPRAY TOWER RUN 706-1A
F-12
-------
' BEGIN RUN 707-1A
sTi
4.5
4,500
END RUN 707-1A
-JL_
40
80
_JL_
120 160 200 240 280 320 360 400 440
I 11/22 I 11/23 I 11/24 I 11/25 I 11/26 I 11/27 I 11/28 ! 11/29 1 11/30 I 12/1 1 12/2 I 12/3 ! 12/4 1 12/5 f 12/6 I 12/7 I 12/8 I 12/9 ! 12/10 j
CALENDAR DAY
4.5
4,500
4,000
3.500
3,000
2,600
2.000
|i
S|
So
*§
cc
il
Hi
is
_j 5
8§
Q w
u) 2
1*
5
a
EC 100
2 SO
5
£ o
10,000
9,000
0,000
7,000
8,000
5,000
4,000
3.000
2,000
1,000
0
"
•
• V-^. y"~~
\x"
• TOTAL DISSOLVED SOLIDS NOTE: SPECIES WHOSE
A /\ ** CONCENTRATIONS ARE LESS
• * . • ° "LCIUM IC.«I THAN 500 pp™ ABE NOT
0 • O SULFATE JSO4") PLOTTED.
* • A CHLORIDE tC\~)
•
-
A
. * AA *A ** A
•
• o o o
oO <^> 0 oo
• a an <> a n
i DJ l I 1 1 1 1 1 1 1 1
150
100
50
0
10,000
9,000
8,000
7,000
6,000
5.000
4,000
3.000
2,000
1,000
0
120 160 200 240 2» 320 MO 400
TEST TIME. Hour,
111/22 I 11/23 111/24 I 11/2S I 11/26 I 11/27 I 11/28 I 11/29 I 11/M I 12/1 I 12/2 I 12/3 I 12/4 I 12/6 I 12/8 I 12/7 I 12/8 I 1Z/9 112/10 I
CALENDAR OAV (1975)
Gss Rate = 35,000 acfm @ 330 °F
Spray Tower Gas Velocity - 9.4 ft/sec
Liquor Rate to Venlurt - 600 gpm
Liquor Rate to Spray Tower - 1,400 gpm
Venturi L/G = 21 gal/mcf
Spray Tower L/G = SO gal/mcf
No. of Spray Headers = 4
EHT Residence Time - 12 min
Note: Only solids data points with
ionic imbalances between t 8.5%
are plotted.
Percent Solids Recirculated = 14.3-16 wt %
Venturi Pressure Drop = 9.0 in. HnO
Total Pressure Drop, Excluding Mist Elim. - 14-14.9 in. HjO
Scrubber Inlet Liquor Temperature - 126-129 °F
Liquid Conductivity = 9,000-13,000 it mhoi/cm
Discharge (Centrifugal Solids
Concentration - 58-73 wt %
Limestone Addition to EHT
Figure F-12. OPERATING DATA FOR VENTURI/SPRAY TOWER RUN 707-1A
F-13
-------
4.5
4,000
3,500
3,000
2,500
2,000
1,500
I 11/27 I il/;
TEST TIME, Hour!
12/1 I 12/2 I 12/3 I 12/4 1 12/5 ! 12/6 I 12/7 I 12/8 I 12/9 1 12/10 i 12/11 I 12/12 I 12/13 I 12/14 i 12/15 I
CALENDAR DAY
ss
£2
o *-
10,000 |-
9,000
8,000
7,000
6,000
5,000
4,000
3,000
2.000
1.000
• 0
**
• TOTAL DISSOLVED SOUDS
O CALCIUM (Ca**(
O SULFATE {S04=i
A CHLORIDE ICri
o
1
1
1
1
1
1
1
1
1
1
i
NOTE:SPECIES WHOSE
CONCENTRATIONS ARE LESS
THAN 500 ppm ARE NOT
PLOTTED.
7.000
6.000
5.000
4,000
3,000
2,000
1.000
40 BO 120 160 200 240 280 320 360 400 440 460
TEST TIME, Hour*
I 11/27 I 11/28 I 11/29 I 11/30 I 12/1 I 12/2 I 12/3 I 12/4 I 12/5 I 12/6 I 12/7 I 12/8 I 12/9 I 12/10 I 12/11 j 12/12 I 12/13 1 12/14 | 12/15 I
CALENDAR DAY (1975)
Gas Rale = 35,000 acfm @ 330 °f
Spray Tower Gas Velocity = 9,4 fi/sec
Liquor Rate to Venturi = 600 gprn
Liquor Rate to Spray Tower = 1,400 gpm
Venturi L/G = 21 gal/mef
Spray Tower L/G = 50 gal/mcf
No. of Spray Headers - 4
E HT Residence Time = 12 rnin
Note: Only solids data points with
ionic Imbalances between ± 8.5%
are plotted.
Percent Solids Recirculated = 14.2-15.4 wt %
Venturi Pressure Drop - 9.0 in. H ,0
Total Pressure Drop, Excluding Mist Elim. - 14.8-15.2 in.
Scrubber inlet Liquor Temperature = 124-129 °F
Liquid Conductivity = 9,50000,500 ,u mhos/cm
Discharge (Centrifuge) Solids
Concentration - 59-65 wt %
Limestone Addition to EHT
Figure F-l?. OPERATING DATA FOR VENTURi/SPRAY TOWER RUN 708-1A
F-14
-------
II , . . isai rime, nwun
12/7 1 12/8 I 12/9 I 12/10 I 12/11 I 12/12 I 12/13 I 12/14 112/16 I 12/16 I 12/17 I 12/18 | 12/19 I 12/20 I 12/21 I 12/22 I 12/23 I 12/;
CALENDAR DAY
ec
IT
ii
If
o
-j 3
° H
lg
5
6.000 p • • • V CALCIUM «.**> -| B.OOO
7.000
B.OOO
5.000
4.000
3.000
2.000
1.000
0
Q SULFATE ISO4°]
• — A A m A CHLORIDE (Cl~l
* * . A • . •» -
•» * * • • * •«
* * * £ * NOTE: SPECIES WHOSE
* CONCENTRATIONS ARE LESS •
,4 THAN 500 ppm ARE NOT
A A PLOTTED.
AA A. *A .A *^
4* AA A * 4 **AA A A
O AA o
* <*>
_ MO ^O ^5 ^D ^ g o ^ °^ QC <>^ ^
D D Q OO n n ™ Q^O ^ o
^ i i 1 1 1 * 1 » 1 1 1
7,000
6,000
5.000
4.000
3,000
2,000
1,000
0
200 240 KO
TEST TIME. Hour*
I 12/7 I 1OT I 12/9 I 12/10 I 12/11 I 12/12 I 12/13 I 12/14 I 12/15 I 12/1S I 12/17 I 12/18 112/19 I 12/20 I 12/21 I 12/22 I 12/23 I 12/24 I 12/251
CALENDAR DAY (1975)
Gas Rate - 35,000 acfm @ 330 °F
Spray Tower Gas Velocity = 9.4 ft/sec
Liquor Rate to Venturi = 600 gpm
Liquor Rate to Spray Tower« 1,400 gpm
Venturi L/G = 21 gal/mcf
Spray Tower L/G = SO gal/mcf
No. of Spray Headers = 4
EHT Residence Time = 12 roin
Note: Only solids data points with
ionic imbalances between ±8.5%
are plotted.
Percent Solids Recirculated ' 13.7-14.4 wt % (709-1 A),
14-16 wt% (710-1 A)
Venturi Pressure Drop = 9.0 in. H20
Total Pressure Drop, Excluding Mist Elim. = 13.7-14.4 in. H2
(709-1AI, 14.3-15 in. H20(710-tAI
Scrubber Inlet Liquor Temperature = 127-130 °F
(709-1A), 126-129 °F(710-1A)
Liquid Conductivity = 7,100-10,400 ii. mhos/cm (709-1A),
6,900-9,400 ii. mhos/cm (710-1A)
Discharge (Centrifuge) Solids Concentration = 61-65 wt %
(709-1A), 57-63 wt% (710-1 A)
Limestone Addition to EHT
Figure F-14. OPERATING DATA FOR VENTURI/SPRAY TOWER RUNS 709-1A & 710-1A
F-15
-------
12/25 1 12/26 I 12/27 I 12/28 I 12/29 I 12/30 I 12/31 1
240 280
TEST TIME, Hoari
1/2 I 1/3 1 1/4 I 1/5 I 1/6 I 1/7 1 1/8 I 1/9 I 1/10 I 1/11 I
CALENDAR DAY
./izl
O TOTAL DISSOLVED SOLIDS
O CALCIUM iCa*"*}
D SULFATE
-------
•BEGIN RUN 712-1A END RUN 712 I
< END RUN 713-1A
p 0 INSPECTION ft DEPLETION , BEGIN RUN 713-1A
EC Ct
gs «
90
5 85
sTi*
S »
75
70
0,6
_t m 9*
* D r °'*
ill u
0.0
6.5
* j. 6,0
hi
S" "
5.0
4,000
3.500
8 I ""
ii «-
2,000
" ^A/i r*\ 1
-rV VW V
\
' A l\-
m
MA J
\
-
-
_
S\-~ INLET
-Tf\T~f^~1 \
M/A-^-vJ^' \
" -^ / X, ^.-r
^ OUTLET
n
/Hr\ f1^ l
\ /'^^'^ VyAr^
•
1 1 1 I i I i I 1 1 I
«
90
85
80
75
70
0.6
0.2
0.0
6.5
G.O
5.5
5.0
4,000
3,500
3.000
2.500
2,000
0 40 80 120 160 ZOO 240 280 320 360 400 440 480
TEST TIME. Hourt
1/2 ! 1/3 1 1/4 I 1/5 1 1/6 1 1/7 1 1/8 1 1/9 1 1/10 1 1/11 I 1/12 1 1/13 I 1/14 1 I/IS I 1/16 1 1/17 1 1/18 1 1/19 I 1/20 1 1/21 1
CALENDAR DAY
o ~ J 1.1
ill "
"* a: 12
:yv-vuy\ -
\ ,
1.6
1.4
1.2
5 a* V\ .
Ill "
g|| 20
if § 10
2^5 „
^*s
- ,* . .^ii , fv/M
. r \f\ fJ*k^l~*^\ V
/ " V^ V
30
20
10
SgZ 0-
o 150
|ij| ,00
|*1 K,
|2t
z
"12,000
11,000
10.000
£ <>.«»
S f
i I »-000
11 7.00.
§1 6.000
S2
S J 5,000
IU u|
Q S '•<**>
$~
S 3,000
2,000
1,000
^— -
.
m^*— ^*^-~— -^*^-^^^"
_ * • TOTAL DISSOLVED SOLIDS NOTE: SPECIES WHOSE
y\ ** CONCENTRATIONS ARE LESS
O CALCIUM (C.^1 THAN 500 ppn, ARE NOT
• ^ * D SULFATE
-------
; B£GiN RUN J14-1A
END RUN 714-1A '
4,000
3,SOO
2.600
2,000
f EST TIME, Houn
i 1/20 I 1/21 I 1/22 I 1/23 I 1/24 I 1/25 I 1/26 I 1/27 I 1/28 I 1/29 1 1/30 I 1/31 I 2/1 I 2/2 I 2/3 i 2/4 i 2/5 I 2/6 I 2/7 I
CALENDAR DAY (1976)
•:STOICH. RATIO VALUES ARE
CORRECTED FOR SULFUR
JW THE LIQUID,
£ *
III
1^1
80 120 160 200 240 280 320 380 4
TEST TIME, Hovn
I V22 | 1/23 t 1/24 I 1/25 I 1/26 I 1/27 I 1/28 I 1/29 I 1/30 I 1/31 I 2/1 I 2/2 1 2/3 I 2/4 I
CALENDAR DAY (1976)
,£
3 I
y "
Z F
Is
82
a*
8
5
35,000
30,000
25.000
20.000
15.000
10.000
5.000
0
• TOTAL DISSOLVED SQUDS NOTE: SPECIES WHOSE
A ++ CONCENTRATIONS ARE LESS
. «« V CALCtUM (&**) THAN 500 ppm ARE NOT
« « • D SULFATE (S04°) PLOTTED.
A * •. C • *A
O • Bw^>w 4 CHLORIDE (Cl~)
O O MAGNESIUM IMg")
-»•
D Q
a° DDanDaDaaD°
-aDDD
-Afii22AAsaAfift^66A^*6A
AAAA^AAA6AAAAO(&AAAA^ , , , , , , ,
35,000
30,000
25,000
20,000
1G.OOO
10,000
5,000
D
REVISED AUGUST 1876
Gas Rate = 35.000 aefm @ 330° F
Spray Tower Gas Velocity ~ 9.4 ft/sec
Liquor Rate to Venturi - 600 gpm
Liquor Rate to Spray Tower - 1,400 gpm
Venturi L/G « 21 gai/mcf
Spray Tower L/G - 50 gal/mcf
No. of Spray Headers = 4
EHT Residence Time = 6 min
Note: Only solids data points with
Ionic imbalances between 1 8.5%
are plotted.
Percent Solids Recirculated - 14.5-16 wt %
Venturi Pressure Drop - 9.0 in. HjQ
Total Pressure Drop, Excluding Mist Elim. » 14.6-15.6 in.
Scrubber Inlet Liquor Temperature = 126-130° F
Liquid Conductivity =18,000-28,000 u. mhos/cm
Discharge {Centrifuge} Solids
Concentration = 57-62 wt %
Limestone Addition to EHT
Figure F-17. OPERATING DATA FOR VENTURI/SPRAY TOWER RUN 714-1A
F-18
-------
52 'MNM '
1" *
30
25
J
8|* »
15
10
s
0.6
I*5*-
^ ec I 0.4
*** ^ •-
1 £ S «
•«* £ 5,8
is*
£ « "
&i
4.S
4.000
3.SOO
8*1 3-MO
Z o 2,500
2,000
1 500
-
ft
\
\
\
\
U
~~~ -_
.
-
-
s^
\ A
A-
.
A-|
.
-
.
'
36
30
25
20
IS
10
5
0.8
0.4
0.2
0.0
6.0
5.S
s,o
4.6
4,000
3,500
3,000
2,500
2,000
0 40 80 120 160 200 240 280 320 300 400 440 480
TEST TIME. Hour*
1 1/27 1 1/28 I 1/29 1 1/30 1 1/31 1 2/1 1 2/2 t 2/3 I 2/4 1 2/5 | 2/6 1 2/7 1 2/6 1 2/9 1 2/10 1 2/11 I 2/12 1 2/13 1 2/14 1 2/15
CALENDAR DAY (1970)
2.0 — in
111 '•'
1S» «
ItS
ill "
1.2
Sj S * 3«
||g »
III "
"• 9 Hi °
f NOTE : STOICH. ft ATIO VALUES ARE
/ CORRECTED FOR SULFUR
/ IN THE LIQUID.
f I
' ^/ I
-
r l
" /\l
^v y
-
1.8
1.8
1.4
1.2
30
20
10
0
8s
u 150
!!$
||; 100
ill »
fc w z 0
35,000
30,000
= 1 26,000
yr
£ t 20.000
is
a i '5.|>o|>
g j^
2 3 10.000
S 5,000
n
-
s.
.
-
^ * TOTAL DISSOLVED SOLIDS NOTE: SPECIES WHOSE
* 0 CALCIUM
ISO
100
so
0
35,000
30,000
26,000
20,000
16.000
10,000
6.000
0
1/27 I 1/28 I t/29
1/30 I 1/3! I 2/1 I 2/2 I 2/3 I 2/4 I 2/5 I 2/C I 2/7 I 2/8 I 2/9 I 2/10 I 2/11 I 2/12 I 2/13 I Z/14 I 2/1E
CALENDAR DAV {19781
REVISED AUGUST 1978
Gas Rate - 35,000 acfm I? 330° f
Spray Tower Gas Velocity - 9.4 ft/sec
Liquor Hate to Venturi = 600 gpm
Liquor Rate to Spray Tower = 0 gpm
Venturi L/G « 21 jal/mcf
No. of Spray Headers = 4
EKT Residence Time ~ 20 min
Note: Only solids data points with
ionic imbalances between - 8.5%
are plotted.
Percent Solids Uncirculated = 14-18 wt % (715-1AI,
13-16wt%(716-1A)
Venturi Pressure Drop ~ 9.0 in. r^O
Total Pressure Drop, Excluding Mist Elim. = 13.1-13.9 in. HjO
(715-1A), 12.9-13.8 in. H20 I716-1A)
Scrubber Inlet Liquor Temperature • 128-129" f (715-1A)
Liquid Conductivity " 19,000-21,000 u. mhos/cm (715-1A)
Discharge (Centrifuge) Solids Concentration - S6-66 wt %
(715-1A), 70-73 wtK (716-1 A)
limestone Addition to EHT
Figure F-18. OPERATING DATA FOR VENTURI/SPRAY TOWER RUNS 715 - 1A & 716 - 1A
F-19
-------
• BEGIN flU* 717 1A
END RUN 717 1A >
96 -
90 -
5.0
4.000
3,500
3,000
2,600
2,000
1.SOO
TEST TIME, Hour*
1/29 I 1/30 I 1/37 I 2/1 I 2/2 I 2/3 I 2/4 I 2/5 I 2/6 I 2/7 I 2/8 I 2/9 1 2/10 I 2/11 1 2/12 1 2/13 I 2/14 I 2/16 I 2/16 I
CALENDAR DAV (1976)
!i ...
IS a*
'Is
NOTE: STIOCM. RATIO VALUES ARE
CORRECTED FOR SULFUR
IN THE LIQUID.
H* 'I
> g « 100
|l- *>
*si ,
30,000
25.000
|_ 20,000
S r 16000
si
8 of
9 g 10.000
Si ,
2 K '.*»
o a:
a - s.ooo
a
2.SOO
0
A^x-A/--v^ -
^^^V V
.
~_ - • 0 • TOTAL DISSOLVED SOLIDS
• « A. • . •• •* A «.
• * • •*•— V CALCIUM iGiii
• * O SULFATE (SO4"i
D D A CHLORIDE (CI-)
DD n _
DnOD^ DDn SULFITE
-------
Appendix G
AVERAGE LIQUOR COMPOSITIONS FOR THE
VENTURI/SPRAY TOWER TESTS
G-l
-------
Table G-l
AVERAGE LIQUOR COMPOSITIONS FOR VENTURI/SPRAY TOWER
LIME RUNS FROM JUNE 1975 TO OCTOBER 1975
Run No.
625-1A
6Z6-1A
627-1A
628-1A
628-1B
Percent Perc
Solids Sul
Discharged Oxid
55-60 12-
52-60 12-
52-56 12-
52-59 10-
:ent
fur Sample Point
ized
38 Scrubber Inlet
Scrubber Outlet
Clarifier Overflow
32 Scrubber Inlet
Scrubber Outlet
Clarifier Overflow
19 Scrubber Inlet
Scrubber Outlet
Clarifier Overflow/
30 Scrubber Inlet
Scrubber Outlet
Clarifier Overflow
52-56 14-27 Scrubber Inlet
Scrubber Outlet
Clarifier Overflow
PH
8. 15
4. 80
8.35
8.00
4. 80
8. 20
8. 05
5.25
8. 40
7. 55
5. 00
7. 90
7. 55
4. 80
8. 35
Liquor Species Concentrations
Ca + +
3300
3430
2890
2820
2920
2340
2640
3000.
2020
1960
2110
1780
2200
2450
1960
++
Mg
160
150
150
220
220
180
105
180
100
270
260
245
280
285
250
Na
55
50
60
65
60
50
60
70
70
65
60
60
65
60
55
K +
130
130
110
140
130
110
125
145
155
140
140
130
125
130
110
so3"
70
490
100
80
600
120
60
95
55
70
390
60
45
450
60
so4=
1370
1760
1160
1280
1760
1090
810
1460
640
1440
1990
1260
1210
1780
1060
mg/1 (ppm)
c
-------
Table G-2
AVERAGE SCRUBBER INLET LIQUOR COMPOSITIONS FOR VENTURI/SPRAY TOWER
LIMESTONE RUNS FROM OCTOBER 1975 TO FEBRUARY 1976
Run No.
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
713-1A
714-1A
715-1A
716-1A
717-1A
Percent
Solids
Discharged
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
59-60
57-62
56-66
70-73
53-59
Percent
Sulfur
Oxidized
9-22
5-13
4-22
10-40
2-18
9-28
3-24
1-25
6-23
l-£6
2-26
4-22
3-19
8-25
9-21
9-20
8-24
3-24
PH
5. 90
5. 80
5.20
5. 75
5.65
5. 30
5. 75
5.65
5.85
6. 00
5. 70
5. 55
5. 80
5.25
5. 55
5. 30
4. 80
5.45
Liquor Species Concentrations, mg/1 (ppm)
Ca++
2310
1970
3040
2850
1550
1800
1580
1650
960
910
1410
2210
1610
2690
620
780
1130
540
Mg++
420
530
630
770
600
670
910
830
760
780
730
690
760
910
5000
5150
5480
4940
Na +
70
60
90
110
75
70
75
85
75
70
65
75
70
70
60
60
65
65
K +
110
90
115
120
105
115
120
115
150
120
110
115
125
120
90
105
95
90
SO3~
40
60
115
105
85
195
140
105
85
80
60
90
85
95
1280
1960
3870
1250
SO/
440
405
1460
790
730
2350
950
1170
860
700
1390
1460
520
2100
14, 300
13, 200
12, 000
14, 300
co3=
75
75
25
95
115
30
95
80
110
145
110
90
100
25
60
15
4
70
ci-
4920
4780
6210
6200
4020
3830
4410
4560
3660
3400
3740
4930
4940
5570
5280
5710
5340
4180
Total
8400
8000
11,700
11, 000
7300
9100
8300
8600
6700
6200
7600
9700
8200
11,600
26, 700
27,000
33,700
25,500
Calculated Percent
Sulfate Saturation
at 50°da>
30
25
100
55
40
125
45
55
30
25
65
85
25
120
95
110
120
90
o
Note: The values in this table are averages for the steady-state operating periods.
(a)
(activity Ca++) x (activity SO 4 (/(solubility product at 50°C). Estimated solubility product for CaSC>4' 2H2O
at 50°C is 2. 2 x 10~5 (Radian Corporation, "A Theoretical Description of the Limestone-Injection Wet
Scrubbing Process", NAPCA Report, June 9, 1970).
-------
Appendix H
TEST RESULTS SUMMARY TABLE FOR THE TCA
H-l
-------
Table H-l
SUMMARY OF LIMESTONE TESTS ON TCA SYSTEM
Run No.
Start-of-Run Date
End-of-Run Date
On Stream Hours
Gas Rate, acfm @- 300°F
Gas Velocity, ips , 0
Stoich. Ratio ^ t. 6
acheme.
Run terminated due to unsuc-
ation. Bottom mist eliminatoi
stage Tii 5% restricted.
H-2
-------
Table H-l (continued)
Run No,
Start-of-Run Date
End-of-Run Date
On Stream Hours
Gas Rate, acfm 6 3")0°F
Gas Velocity, fps 2 absorbed
Avg % Limestone Utilization, !00x
moles SOg abs/mole Ca added
nlet SO2 Concentration, ppm
Percent SOz Removal
Scrubber Inlet pH Range
Scrubber Outlet pH Range
'ercent Sulfur Oxidized
Solids Disposal System
Loop Closure, % Solids, Dischg.
Calculated Avg % Sulfate Saturation
in Scrubber Inlet Liquor @ 50°C
Total Dissolved Solids, ppm
Total flP Range Excluding Mist
Elimination System, in. HjO
Mist Elimination System
OP Range, in. HgO
.flJP Range, in. H2O
Mist Elimination
Absorbent
Mist Elimination System
Washing Scheme
Scrubber Internals
System Changes Before
Start -of -Run
Method of Control
Run Philosophy
Results
548-2A
6/23/75
6/27/75
71
30,000
12,5
1000
42
11-14
15
1.35-1.45
71
2000-3000
79-87
5.9-6.1
5.4-5.7
11-16
Clarifier
C=! 22
35
2000-4500
6. 8-7.2
0.58-0.65
Top stage: 0.45-0. 50
Btm stage: 0, 13-0. 15
Two 3-pass. closed-vane,
in series.
with clarified process liquor
and added to EHT.
Top :100 gpm (2. 0 gpm/ft2)
Btm; continuous 26 gpm JO. 53
gpm/ft2) makeup water.
No wash for top stage. Total
makeup.
spheres/stage. AH beds worn
run.
place.
Scrubber outlet pH controlled
at S.5J-0. 1
Overrides:
Inlet pH ^6, 0
Stoich, Ratio ±sl. 6
Observe the operability of the
a continuous raw water bottom
stage underwash (system
operated open loop).
Run terminated as planned.
stage of mist eliminator 100%
clean and top stage 95% clean
549-2A
6/27/75
7/2/75
112
30, 000
12.5
1000
42
12. 5-16
15
1.48-1. 60
65
2200-3100
74-79
5. 8-6. 0
5.3-5.5
12-20
Clarifier
OJ 30
65
2000-3100
6.2-6.6
0.58-0.65
Top stage: 0.45-0. 50
Btm stage: 0. 13-0. 15
in series.
with clarified process liquor
and added to EHT.
Top; 100 gprn (2. 0 gpm/ft2}
Btm: continuous 14 gpm (0,29
gpm/ft2) makeup water.
No wash for top stage. Total
makeup.
spheres/stage. All beds worn
run.
Scrubber outlet pH controlled
at 5.5*0. 1
Overrides:
Inlet PH ^6.0
Stoich. Ratio ^.1.6
Observe the operability of the
a reduced rate of bottom stage
raw water continuous under-
wash (system operated open
loop).
Run terminated when inapec-
inatora to be approximately
5% restricted. Restriction
appeared to be due to a gap in
bottom stage mist eliminator.
550-2A
7/2/75
7/S/75
119
30,000
12. 5
1000
42
14. 6-15.7
15
1.31-1.67
67
2400-3000
74-78
5.6-6.0
5.4-5.6
15-21
Clarifier
37-41
75
6000-7000
6. 1-6.8
0.66-0.83
Top stage: 0. 50-0.60
Btm stage: 0. 16-0.23
.n series.
with clarified process liquor
and added to EHT.
Top; 100 gpm (2. 0 gpm/ft2)
Btm Continuous 16 gpm (0. 33
gpm/ft2). Clarified
liquor (~8 gpm} and
^Io wash for top stage.
spheres/stage. All beds worn
~
place.
Scrubber outlet pH controlled
at 5. 5fO. 1
Overrides:
Inlet pH <= 6. 0
Stoich. Ratio fcl.6
Observe the operability of the
gas velocity of 12, 5 ft/sec
with a bottom wash using
diluted clarified liquor.
Run terminated when inspec-
mist eliminator to be 15%
restricted and the top stage
5-8% restricted with solids.
551-2A
7/8/75
7/10/75
39
30, 000
12. 5
1000
42
14. 3-14.7
15
1.4-1. 6
66
2700-3100
73-83
5. 8-6. 0
5.5-5.6
13-15
Clarifier
39-41
20
3900-4300
6. 5-6. 6
0,66-0. 80
Top atage: 0.50-0.60
Btm stage: 0. 16-0. 20
n series.
ith clarified process liquor
nd added to EHT.
tm. (upstream)m. elim. wash:
Top: 100 gpm (2.0 gpm/ft2)
Btm:continuous l6gpm(Q. 33
gpm/ft2). Clarified
liquor [y.B gpm) and
o wash for top stage.
pheres/stage. All beds worn
~
place. Replaced 4 underwaah
nozzles on bottom mist elim-
inator with a single large
nozzle.
Scrubber outlet pH controlled
at 5, 5iO. 1
Overrides
Inlet pK £6.0
Stoich. Ratio 4.1. 6
Observe the operahlltty of the
a single nozzle underwaih on
the bottom (upstream) mlat
eliminator.
Run terminated when iriapec-
miat eliminator to be 10-15%
restricted and the top atage
< 3% restricted with solids.
H-3
-------
Table H-l (continued)
Start- of- Run Date
End-of-Run Date
On Stream Hours
Gas Rate, acfm @ 300°F
Gas Velocity, fps @ 125°F
Liquor Rate, gpm
L/C. gal/mcf
Percent Solids Recirculated
Effluent Residence Time, min.
Stoichiometric Ratio, moles Ca
added/mole SO2 absorbed
Avg <"<, Limestone Utilization, 1 OOx
Inlet 302 Concentration, ppm
Percent SC2 Removal
Scrubber Inlet pH Range
Scrubber Outlet pH Range
Percent Sulfur Oxidized
Solids Disposal System
Loop Closure. % Solids. Dischg.
Calculated Avgl Sulfate Saturation
Total Dissolved Solids, ppm
Total AP Range Excluding Mist
Mist Elimination System
* P Range, in, H2O
Chevron Mist Eliminator
aP Ranga, in. H2O
Mist Elimination
System Configuration
Absorbent
Mist Elimination System
Washing Scheme
Scrubber Internals
Start-of-Run
Results
552-2A
7/10/75
7/14/75
86
30,000
12.5
1200
SO
14.4-15.6
15
1.42-1.48
69
3100-3200
79-84
5.95-6. 02
5. 42-5. 60
13-16
Clarifier
38-41
20
3500-4500
7.5-7.9
0.68-0. 75
Top stage: 0. 50-0. 55
Btm stage: 0. 18-0.20
rwo 3-pass, closed-vane,
in series.
Limestone slurried to 60wt %
ind added to EHT.
Top:100 gpm (2. 0 gpm/ft2)
makeup water for con-
stant 30 aec, once /1 0 min
gpm/ft2). Clarified
liquor (fit 14 gpm) and
makeup water £8 gpm).
•Jo wash for top stage.
3 stages (4 grids) with 5 inches
spheres/stage. All beds worn
run.
eliminator with 4 nozzles.
at 5. 5±-0. 1. Changed to SO2
on 7/11.
Overrides:
Inlet pH 4i 6. O/
Stolen. Ratio — 1.6
mt.t .limi^tion system ».b,g
Run terminated when inspec-
mist eliminator to be 8-10%
restricted and the top stage
553-2A
7/19/75
7/21/75
42
30, 000
12.5
1200
50
15.5-16.4
15
1.57
64
2300-2500
81-83
5. 6-6. 0
5, 1-5.45
18-26
Clarifier
32-37
90
5800-5900
8. 5-8.8
0. 31-0. 36
0.31-0.36
3-pase, open-vane, 316LSS,
and added to EHT.
makeup water. Each nozzle
(6 total) on 4 min (at 0. 55
gpm/ft2) with 76 min off
washed with makeup water
at 2. 5 gpm/ft2 for 5 min
every hour.
3 stages <4 grids) with 5 inches
spheres /stage. All beds worn
run.
to spray tower mist eliminator]
84+2%.
Overrides:
Inlet pH fefe. 0
Stoich. Ratio ^.1,6
new mist elimination system
velocity.
Run terminated when ingpec-
with solids.
554-2A
7/25/75
7/28/75
60
22, 500
9.4
1200
67
14.8-15.0
15
1.58-1.62
63
2300-3000
76-84
5.95-6.09
5.45-5.65
18-21
Clarifier
36-40
55
4800-6200
5.1-5.3
0, 18-0,40
0. 18-0. 40
3-pass, open-vane, 3I6L SS,
Limes-tone slurried to 60 wt %
and added to EHT,
makeup water. Each nozzle
(6 total) on 4 min (at 0. 55
gpm/ft2) with 36 min off
washed with makeup water
at 2. 5 gpm/ft2 for 6 min
every 2 hours.
3 stages (4 grids) with 5 inches
spheres /stage. All beds worn
run.
84+2%.
Inlet pHfc 6. 0
Stoich. Ratio ^1.6
velocity.
Run terminated when inspec-
with solids.
555-2A
7/29/75
8/1/75
63
22, 500
9. 4
1200
67
13.4-13. 7
15
1. 72
58
2100-2300
77-83
5-95
5. 35
15-1?
Clarifier
^25
95
4200-5400
5. 0-5.4
0. 18-0.23
0. 18-0.23
3-paas, open-vane, 316L SS,
and added to EHT,
makeup water. Each nozzle
6 total) on 4 min (at 0. 55
gpm/ft2) with 36 min off be-
cont. with water at 0. 4gpm/ft2
open liquor loop).
3 stageg(4gri
-------
Table H-l (continued)
Run No.
End -of- Run Date
On Stream Hours
Gas Rate, acfm @ 300°F
Gas Velocity, fps @ I25°F
,iquor Rate, gpm
L/C, s.l/mcf
3ercent Solids Recirculated
Affluent Residence Time, min.
Stoichiometric Ratio, moles Ca
added/mole SO2 absorbed
Avg % Limestone Utilization, IDOx
moles SCz abs. /mole Ca added
diet SO2 Concentration, ppm
Percent SO2 Removal
Scrubber Inlet pH Range
Scrubber Outlet pH Range
"ercent Sulfur Oxidized
Solids Disposal System
Loop Closure, % Solids, Dischg.
Calculated Avg. %Sul£ate Saturation
in Scrubber Inlet Liquor @ 50°C
total Dissolved Solids, ppm
total aP Range Excluding Mist
Elimination System, in. H2O
Mist Elimination System
^P Range, in. H2O
Chevron Mist Eliminator AP
Range, in. H2O
Mist Elimination
Absorbent
Mist Elimination System
Washing Scheme
Jcrubber Internals
System Changes Before
Start- of- Run
Method of Control
Run Philosophy
Results
556-2A
8/1/75
8/5/75
89
22, 500
9.4
1200
6?
12.9-15,1
15
1.42-1.51
68
1500-2700
75-86
5.8-6.2
5.3-5.7
15-25
Clarifier
31-45
105
5600-6000
4. 8-5. Z
0.16-0.23
0. 16-0. 23
3-pass, open-vane, 316L SS,
Limestone slurried to 60 wt %
with clarified process liquor
and added to EHT.
Top washed sequentially with
makeup water. Each nozzle (t
total} on 4 min (atO. 55 gpm/ft2
with 36 min off between noz-
zles. Btm washed cont. with
Jil. clar. liq. (all makeup
at 0.4 gpm/ft2.
3 stages (4 grids) with 5 inche
spheres/stage. All beds worn
run.
moved scale test atrip under
ference with mist elim. under
spray. Removed Ceilcote
test panel under N. E. slurry
nozzle to minimize flue gas
maldistribution.
8412%
Overrides:
Inlet pH<£ 6. 0
Stoich. Ratio ^1.6
Observe mist eliminator
of makeup water and clarifiet
liquor.
Run terminated when inspec-
tion revealed the rnist elim-
with solids.
557-2A
8/5/75
8/13/75
181
30,000
12. 5
1200
50
14.8-16.2
15
1. 08-1. 62
74
1500-3000
80-90
5.8-6,0
5.2-5.6
10-21
Clarifier
39-44
70
4000-6000
7. 3-7. 5
0. 36-0.44
0.36-0.44
3-pass, open-vane, 3161. SS,
Limestone slurriedto 60 wt %
with clarified process liquor
and added to EHT.
Top washed sequentially with
makeup water. Each nozzle (6
total) on4 min (at 0, 55 gpm/ft2)
with 36 min off between noz-
zles. Btm washed cont. with
dil. clar. liq. (all makeup
at 0. 4 gpm/ft2.
3 stages (4 grids) with 5 inche
spheres/stage. All beds worn
~*
84 ±2%
Overrides:
Inlet pH-^6,0
Stoich. Ratiot 1, 6
Observe operabUity of mist
eliminator at 12. 5 ft/sec
same wash scheme used for
Run 556-2A.
Run terminated when inspec-
tion revealed the mist elim-
with a olid s.
558-2A
8/15/75
9/2 /7B
398
30, 000
12.5
1200
50
14.4-15.2
15
1. 24-1.45
74
2200-3200
70-81
5.7-5.95
5.2-5.5
10-20
Clarifier
34-42
85
3400-6000
7.3-7.7
D. 37-0.43
0. 37-0.43
-pass, open-vane, 316L SS,
Limestone slurried. to 60 wt %
with clarified process liquor
nd added to EHT.
makeup wtr. Eachnoz. (6
total) on 6 rnin (at 0.55 gpm/ft^)
with 24 min off between noz-
zles. Btm washed cont. with
dll. clar, liq. (all makeup wtr
gpm/ft2. (N. E. topwaah noz.
0. 83 gpm/ft2 after 8/29).
3 stages (4 gr£ds)with 5 inchea
spheres /stage. All beds worn
run.
84+2%
Overrides:
Inlet pH ^ 6. 0
Stoich. Ratio ^_ 1. 6
Observe operability of miat
eliminator at 12. 5 ft/sec
wash.
Run terminated when inspec-
with solids.
559-2A
9/5/75
9/22/75
384
30,000
12.5
1200
50
14-16
15
1.2-1.6
71
2000-4100
68-86
5.6-6. Z
5,0-5.8
7-24
Clarifier
36-42
70
3000-6000
7. 0-8. 1
0.38-0.42
0. 38-0.42
-pass, open-vane. 316 L SS,
Limestone slurried to 60 wt %
with clarified process liquor
nd added to EHT.
makeup wtr. Each noz, (6 total;
n 3 min (atO. 55 gpm/ft2, 0. 83
pm/ft2 for N. E, and N. C. )
with 7 min off between nozzles.
Btm washed cont. with dil.
ecess. clar. liq, J at 0. 4
pm/ft2.
stages (4grids)with Sinches
pheres / stage. All beds worn
run.
cleaned. Streamlined windows.
miat eliminator (from 42" to
36").
84j-2%
Overrides;
Inlet pH/_ 6.0
Stoich. Ratio / I. 6
eliminator at 12, 5 ft/aec
scrubber gae velocity with
«ash.
•tun terminated when inspection
7% restricted with solids.
H-5
-------
Table H-1 (continued)
K«N..
Start-of-Run Date
On Stream Hours
Gas Rate, acfm @ >00°F
Gas Velocity, fps ($• 125°F
Liquor Rate, gprn
L'G. Ral/mcf
Percent Solids RecircUated
Effluent Residence Tim*, mis.
added/mole SC2 absorbed
Av£ % Limestone Utilization, lOOx
moles SO2 abs. /male Ca added
Inlet SG2 concentration, ppm
Percent SO2 Removal
Scrubber Inlet pH Range
Scrubber Outlet pH Range
Solids Disposal System
Loop Closure, <*„ Solids, Dischg.
in Scrubber Inlet Liquor @ 50°C
Total Dissolved Solids, PPm
Total aP Range Excluding Mist
Elimination System, in. H2O
Mist Elimination System
n.P Range, in. H2O
Range, in. H2O
Mist Elimination
Absorbent
Mist Elimination System
Washing Scheme
Scrubber Internals
System Changes Before
Start-of-Run
Method of Control
Run Philosophy
Results
560-2A
9/23/75
142
30, OOP
12.5
1200
50
14.6-15
15
1. 3-1. 7
65
2800-3800
69-83
5,3-6.2
4.6-5.6
9-17
Clarifier
36-41
45
3700-4900
7. 0-8. 1
0. 35-0. 40
3-pass, open-vane, 316LSS,
Limestone slurried to 60 wt %
and added to EHT.
Top washed sequentially with
makeup wtv. Each noz. (6 total
on 3 min (at 0.55 gpm/ft2,, 0. 83
gpm/ft2 for N. E- and N. C.
cont. with dil. clar. lie,, (all
clar. liq. } at 0. 4 gpm/ft2.
3 stages (4 grids) with 5 inches
run.
Mist .liminator cleaned.
SO2 removal controlled at;
84 i 2%
Overrides:
Inlet pH^L 6. 0
Stoich. Ratio^ 1. 6
Observe operability of mist
eliminator at 12. 5 ft/sec
mist elimfnator T-beamS
suspended from top.
lion revealed the mist elim-
561-2A
9/30/75
135
30, 000
12.5
1200
50
14-16
15
1.24-1.48
74
2000-4000
70-S4
5. 7-6. 2
5. 15-5. 65
6-18
Clarifier
37-44
55
3900-6000
7. 3-7. 6
0. 35-0. 40
3-pass, open-vane, 316 LSS,
Limestone slurried to 60 wt %
and added to EHT.
Top washed sequentially with
mskeupwtr. Each noz. (6 total)
on 3 rnin (at 0. 55 gpm/ft2)
Oil. clar. liq. (all makeupwtr
plus necesa. clar. Hq. ) at
3 stages (4grids) with 5 inches
run.
half of mist eliminator rotated
8 4 ±Z%
Overrides:
Inlet pH^. 6.0
Stoich. Ratio 4 1. 6
Observe operability of mist
eliminator at 12.5 ft/eec
east half of rniat eliminator
wash vane shadowing.
tion revealed the mist elim-
562-2A
10/7/75
495
30,000
12.5
17,00
50
14-15.5
12
1, 2-2. 0
63
2000-4000
70-90
5. 75-6. 05
5.2-5.7
5-30
Clarifier
37-43
40
4000-7000
7. 2-7. 9
0. 35-0.43
3-pass, open-vane, 316LSS,
Limestone slurried to 60wt %
and added to EHT.
Top washed sequentially with
mafceupwtr. Each no=. (6 total)
on 3 mm (at 0. 55 gpm/ft2, 0.83
gpm/ft2 for N. E. and S. E.
cont. with dil. clar. Hq. (all
clar. liq. } at 0. 4 gpm/ft2.
33tag«3 {4gridH)with5inches
TPR spheres from previous
Single mist eliminator btm
at 5.9+0. 1.
First limestone utilization
gas velocity.
the mist eliminator to be
5&2-2B
10/30/75
134
30, 000
12. 5
1200
50
M-15
12
1. 2-1. 6
71
2500-4000
72-87
5. 6-5. 8
5.0-5.3
10-30
Clarifier
34-46
70
5000-8000
8. 0-8. 6
0. 35-0.43
3-paas, open-vane, 316LSS,
Limestone .lurried to 60 wt %
and added to EHT.
Top washed sequentially with
makeup wtr. Eachnoz. (6 total)
on 3 min (at 0. 55 gpm/ft2, 0. 83
gprn/ft2 for N. E. and S. E.
tween nozzles. Btm washed
cont. with dil. clar. liq. (all
clar. liq. ) at 0. 4 gpm/ft2.
3 stages (4 grids) with 5 inches
at 1. 4 moles Ca/rnole SO2
absorbed.
Attempt to obtain better lime-
stone utilization data by con-
"
the mist eliminator to be 7%
H-6
-------
Table H-1 (continued)
Run No.
Start-of-Run Date
End-of-Run Date
On Stream Hours
Gas Rate, acfm £ 30Q°F
Gas Velocity, {ps £ 12?=>F
^iquor Sate, Rpm
L/C. gal/mcf
Percent Solids Recirculated
Effluent Residence Time, min.
Stoichiometric Ratio, moles Ca
added/mole SO2 absorbed
Avg w. Limestone Utilization, lOOx
moles SOg abs. /mole Ca added
Inlet SOz concentration, ppm
Percent SOz removal
Scrubber Inlet pH Range
Scrubber Outlet pH Range
'ercent Sulfur Oxidized
Solids Disposal System
Loop Closure, % Solids, Dischg.
Calculated Avg%5ulfate Saturation
in Scrubber Inlet Liquor @ 50°C
Total Dissolved Solids, ppm
Total &P Range Excluding Mist
Elimination System, in. H2O
Mist Elimination System
aP Range, in- H2O
' p
Range, in. H..C
Mist Elimination
Absorbent
Mist Elimination System
Washing Scheme
Scrubber Internals
System Changes Before
Method of Control
Results
563-2A
11/6/75
11/14/75
182
30, 000
12.5
1200
50
14. 8-15. 6
12
1. 3-2. 1
59
2700-3900
80-91
5.7-6.1
5-2-5.9
2-23
Clarifier
36-46
25
3300-5500
7.8-8.1
0.40-0. 43
0.40-0.43
3-pass, open-vane, 316LSS,
with clarified process liquor
Top washed sequentially with
makeup wtr. Each noz. {6 total)
on 3 min (at 0. 55 gpm/ft2,0. 83
gpm/ft2 for N. E. and S. E.
nozzles) with 7 min off be-
cont. with dil. clar. liq. (all
clar. liq, } at 0. 4 gpm/ft2.
3 stages (4 grids) with 5 inche
spheres/stage. All beds worn
TPR spheres from previous
run.
No changes.
at 1. 7 molea Ca/mole SO2
absorbed.
r
with 12 min single tank
Mist eliminator was 7% re-
stricted at the end of the run.
stone utilization was 59% at
an average inlet pH of 5. 9.
564-2A
11/14/75
11/19/75
113
30,000
12,5
1200
50
13.4-15
12
1.0-1,1
95
2500-4000
46-66
5.0-5,4
4.5-4.9
9-23
Clarifier
38-45
120
5700-7600
7. 6-8. 2
0.38-0.45
0, 38-0.45
3-pass, open-vane, 316 L SS,
with clarified process liquor
Top washed sequentially with
makeup wtr. Each noz.(6total)
on 3 min (at 0.55 gpm/ft2, 0. 83
gpm/ft2 for N. E. and S. E.
nozzles) with 7 min off be-
cont. with dil. clar. liq. (all
clar. liq. ) at 0. 4 gpm/ft2.
3 stages (4 grids) with 5 inches
spheres/ stage. All beds worn
TPR spheres from previous
No changes.
at 5.2_+0. 1.
...
with 12 min single tank
Mist eliminator was 3% re-
structed at the end of the run.
stone utilization was 95% at
an average inlet pH of 5. 2.
565-2A
11/21/75
11/26/75
109
30,000
12.5
1000
42
13. 8-15. 4
14.4 (3 tanks)
1.0-1. 08
96
2800-4300
50-64
5.1-5,3
4.4-4,8
5-19
Clarifier
34-43
105
4800-7000
7.4-8. 0
0.30-0.35
0, 30-0. 35
3-pass, open-vane, 316L SS,
with clarified process liquor
series.
Top washed sequentially with
makeup wtr. Each noz. (6 total)
on 3 min (at Q. 55 gpm/ft2, 0.83
gpm/ft2 for N. E. and S. E.
nozzles) with 7 min off be-
cont. with dil. clar. liq. (all
clar. Hq. ) at 0.4 gpm/ft2.
spheres/ stage. All beds worn
TPR spheres from previous
run.
Three series connected ef-
lirnestone makeup to the first
tank. Mist eliminator, outlet
duct and bottom grid cleaned.
at 5. 2+0. 1.
with 3 tanks in series at a
Mist eliminator 0% restricted
at end of run. Average 1 irate -
566-2A
11/26/75
12/3/75
166
30, 000
12.5
1000
42
13.8-15.5
14.4 (3 tanks)
1. 1-1. 3
83
2500-4000
74-90
5. 7-6. 0
5.0-5.4
2-25
Clarifier
34-44
60
4700-6700
8.7-10. t
0. 30-0.40
0,30-0.40
-pass, open-vane, 316L SS,
with clarified process liquor
eries.
sop washed sequentially with
makeup wtr. Each noz. (6 total)
on 3 min (at 0. 55gpm/£t2,0. 83
gpm/ft2 for N. E. and S. E.
nozzles) with 7 min off be-
cont. with dil. clar. liq. {all
clar. liq. ) at 0,4 gpm/ft.
3 stages (4 grids) with 5 inches
spheres/stage. All beds worn
TPR spheres from previous
run. 3000 new TPR spheres
added to top and middle beds
osses.
top and middle beds.
at 5. 9+0. 1.
. .
with 3 tanks in series at a 12
Mist eliminator 0% restricted
at end of run. Average lime-
a one u i iza ion was a % at an
H-7
-------
Table H-l (continued)
SunN0.
Start-of-Run Date
End-of-Run Date
On Stream Hours
Gas Rate, acfm (3 300«F
Gas Velocity, fps (a" 12S°F
Liquor Rate, gpm
L/C, gal/mcf
Percent Solids Recirculated
Effluent Residence Time. min.
Stoichiometric Ratio, moles Ca
added/mole SO2 absorbed
Avg % Limestone Utilization, lOOx
Inlet S02 concentration. ppm
Percent SO; Removal
Solids Disposal System
Loop Closure. **e Solids, Dischg.
in Scrubber Inlet Liquor® 50°C
Total Dissolved Solids, pprn
Total a P Range Excluding Mist
Elimination System, in. HjO
JiP Range, in. HO
Cbevrcr: Mist Eliminator aP
K«E«. la. HEC
Mist Elimination
Absorbent
Mist Elimination System
Washing Scheme
Scrubber Internals
System Changes Before
Start-of-Run
Run Philosophy
Results
1
V,T-2A
12/3/75
12/0/75
138
30. 000
12.5
1000
42
14. 7-15. 6
14.4 (3 tanks!
I. 2-1. 5
74
2000-3400
79-90
5. 9-6. 1
5.3-5.6
4-24
Clarifier
37-43
35
3700-5300
8, 8-9. 6
0. 35-0. 38
3-pass, open-vane, 316LSS,
and added to first tank in
series-
Top washed sequentially with
makeup wtr. Each noz. (6 total)
on 3 min (at 0. 55 gpm/ ft2, 0. 83
gpm/ft2 for N. E. and S. E.
cont. with dil. clar.liq. (all
clar. liq. ) at 0.4 gpm/ft2.
3 stages (4 grids) with 5 inches
aphe res /stage, AH beds worn
No changes.
led at 1. 4 moles Ca/mole
SO2 absorbed.
with 3 tanks in series at a
utilization was 74% at an aver
age inlet pH of 6. 0.
•
568--2A
12/9/75
12/16/75
162
30, 000
12.5
1000
42
14. 5-15. 3
14.4 (3 tanks)
0.9-1- 1
100
2600-3800
55-70
5-4-5. 6
4.7-5- 0
7-30
Clarifier
38-46
75
4500-5700
8.6-10.0
0. 33-0, 40
and added to first tank in
aeries.
Top washed sequentially with
makeup wtr. Eachnoz. (6 total)
on 3 rnin (at 0.55 gpm/ftz, 0. 83
gpm/ft2 for N. E. and S. E.
nozzles) with 7 rnin off be-
tween nozzles, Btm washed
with makexip water at 1. 5
3 stagea (4 grids) with 5 inches
spheres/stage. All beds worn
run.
wash.
at 5. SHt. 1.
Mist eliminator wash scheme
569-2A
12/16/75
12/19/75
66
30, 000
12.5
1000
42
14.4-15.4
10.8 (3 tanks)
1. 03-1. 13
93
2200-4000
57-77
5.4-5.6
4.6-4.9
6-23
Clarifier
33-44
115
5200-8400
7.9-8.9
0. 25-0, 35
Limestone slurned to60wt %
and added to first tank in
series.
Top washed sequentially with
makeup wtr. Each noz. (6 total)
on 3 min (atO. 55 gpm/ft2, 0. 83
gpm/ft2 for N. E. and S. E.
nozzles) with 7 min off be-
with makeup water at 1. 5
gpm
3 stages (4 grids) with 5 inches
spheres/stage. All beds worn
run.
No changes.
at 5. 5+Q. I.
"rtric™a™tth.7,d. 1.
min total residence time
using new nitrilc foam
spheres.
Mist eliminator was < 1%
pH of 5. 5-
H-i
-------
Table H-l (continued)
Run No.
Start-of-Run Dale
;nd-of-fcun Date
On Stream Hours
Gas Rate, acfm (3 300°F
Gas Velocity, fps revious run.
No changes.
with 3 tanks in series at a
pH of 5.23,
573-ZA
1/9/76
1/11/76
45
30,000
12.5
1000
42
14. 5-15. 5
14.4 (3 tanks)
91
2600-2900
57-69
5. 35-5. 65
.
6-28
Clarifier
34-43
80
8700-9300
6. 7-7. I
0. 30-0. 35
0. 30-0. 35
-paas, open-vane, 316L SS,
with clarified process liquor
and added to first tank in
No top wash. Bottom washed
with makeup water at 1. 5
gpm/ft2 for 4 min/hr.
spheres/stage. All beds
irevious run.
No changes.
at 5. 540. 1.
analytical difficu ties en
Mist eliminator was < 1%
age limestone utilization wa§
5. 5,
H-9
-------
Table H-l (continued)
Run No.
Stari-of-Run Date
End- of- Run Date
On Stream Hours
Gas Velocity, fps 6 1Z = 'JF
Liquor Rate, gpm
L/C. gal/mcf
Effluent Residence Time, mirs.
added/mole SC, absorbed
Avg =•; Limes'sne Utilisation, lOOx
moles SO? abs. /mole Ca added
Inlet S02 concentration, ppm
Percent SC2 Removal
Scrubber Inlet pH Range
Scrubber Outlet pH Range
Percent Sulfur Oxidized
Solids Disposal System
Loop Closure. % Solids, Dischg.
Calculated Avg% SuUate Saturation
in Scrubber Inlet Liquor @ 5Q°C
Tota.1 Dissolved Solids, ppm
Total A P Range Excluding Mist
Elimination System, in. HzC
3P Range, in. HZO
Range, in. HjO
Mist Elimination
System Configuration
Absorbent
Washing Scheme
Scrubber Internals
System Changes Before
Start- of -Run
Run Philosophy
i
Results
575-2A
1/15/76
1/17/76
47
30, 000
12- 5
1000
42
14-1 5. 5
14. 4 (3 tanks}
!. 02-1. Z
90
2600-3400
62-78
5- 35-5. 55
4. 55-4. 85
6-23
Cla-rifier
35-39
105
7300-9000
6. 1-7. Z
0. 30-0. 38
0. 30-0. 38
3-pass. open- vane 316 L SS,
with makeup water and added
No top wash. Bottom washed
with makeup water at I. 5
gprn/ft2 for 4 rnin/hr.
Mist eliminator cleaned.
it 5. 5+0. 1.
Limestone utilization lest with
total residence time.
5.45.
576-EA
1/17/76
1/22/76
112
30, 000
12.5
1000
42
14, S- 15. 5
14. 4 (3 tanks)
1.02-1. 25
88
2500-4000
65-79
5. 5-5. 8
4. 75-5- Z
6-23
Clarifier
37-42
95
7000-9300
7. 1-7, 9
0. 35-0.40
0. 35-0. 40
3-pags, open-vane, 316L SS,
-with makeup water and added
No top wash. Bottom washed
with makeup water at 1. 5
gpm/ft2 for 4 min/hr.
No changes.
at 5, 7+0, 1.
Limestone utilization testwith
total residence time.
pH of 5. 65.
577-2A
1/22/76
1/29/76
159
30, 000
12,5
1000
42
14-15. 5
14, 4 (3 tanks)
1. 15-1. 35
80
2800-3800
77-87
5.65-5.9
5.1-5.35
5-ZO
Clarifier
39-43
70
6300-8300
8. 0-9. 6
0, 35-0. 41
0. 35-0.41
3-pass, open-vane, 316LSS,
with makeup water and added
Top washed sequentially with
makeup wtr, Eachnoz,{6 total)
on 3 min {at 0. 55 gpm/£tz, 0. 83
gpm/ft2 for N. E. and S. E.
with makeup water at 1 , 5
gpm /ft2 for 4 min/hr.
apherea/atage. All beds with
bed new nitrile foam spheres.
led at 1.25 moles Ca/mole
SO2 absorbed.
Run conditions chosen similar
12 min residence time to
level. 2
leakage.
579-2A
1/29/76
2/1/76
62
30, 000
12.5
1000
42
J4.5-15.3
10. 8 (3 tanks)
1. 0-1. 06
97
2500-3900
53-68
5.1-5.3
4. 4-5. 0
12-28
Clarifier
40-45
120
7000-8200
9. 3-10. 1
0.45-0. 55
0.45-0.55
3-pas3, open-vane, 316L SS,
with makeup water and added
Top washed sequentially with
makeup wtr. Each noz. (6 total)
on 3 min (at 0. 55 gpm/ft2. 0.83
gpm/ft2 for N. E. and S. E,
tween nozzles. Btm washed
with makeup water at 1. 5
gpm/ft2 for 4 min/hr.
3 stages (4 grids] with 5 inches
apheres/stage. All beds
No changes.
at 5. 2*0. 1.
Limestone utilization tost
min total residence tim«.
A«rage Um«.loM uttllx»U<>n
H-10
-------
Table H-l (continued)
*vg <*<, Limestone Utilization, lOOx
moles SO, abs. /mole Ca added
tari-of-Run Da»e
nd-of-Run Date
i Hours
as Rate, acfm S 330°F
t^Velocity. fes Jj i 2 ~°F
.,/C. gll/mcf
toichiometric Ratio, moles Ca
dded/mole SO2 absorbed
r Inlet pH Ranee
•ubber Outlet pHJRfnBe
grcent Sulfur Oxidized
Solids Disposal Syste:
..oop Closure. % Solids, Dischg.
Calculated Avg %Sulfate Saturatie
Scrubber Inlet Liauor@ IiOoC
Total Dissolved Solida, ppm
Total AP Range Excluding ktist
Elimination System, in. HgO
ist Elimination System
^P Range, in. H2O
Range, in. H-O
Mist Elimination
Mist Elimination Syste!
Washing Scheme
Icrubber Internals
System Changes Befoi
Start-of-Run
Method of Control
Jun Philosophy
27,500-30,000
7,000-10,000
3-pass, open-vane, 316L SS,
; alurried to 60 wt
to first tank to
Top washed gequentiaily with
lakeupwtr- Eachnoa. (6 total)
i 3 min(atO. ^5 gpm/ft2, 0. 8;
gpm/ft2 for N. E and S, E.
tween nozzles. Btm washed
h makeup water at 1. 5
gpm/ft2 for 4 min/hr.
3 atages(4 grids) with 10,000
spheres/stage (aboutSinches
stage). All beds new 6. 5
gram nitrile foam spheres.
led at 1, 10 moles Ca/mole
SO2 absorbed.
Limestone utilization test
ith one tank at 12 min re
ence time. Also to condition
ew beds of foam spheres
stabilize sphere shrinkage
jrage limestone utilization
i 87% at an average inlet
pH of ">. 5. SOg removal was
high due to a flooded bed-
H-ll
-------
Appendix I
GRAPHICAL OPERATING DATA FROM THE TCA TESTS
1-1
-------
* BEGIN RUN G67-2A
£MO RUM 5S7-2A
TEST TIME. Hour*
1 fl/6 I 8/7 ! 8/8 | 8/9 I 8/10 I #11 I B/12 1 3/13 I 8/14 I 8/15 I 8/16 !
CALENDAR OAV
320
'18 i I
300 400 420
I 9/20 \ a/21 I 8/22 i a/23 | 8/24 I
4.6
3,000
2,500
2,000
1,600
1,000
ff
h
1^
I E
- C
So
it
> £
e^ Z
5
3,000
5.030
4,000
3.000
2.000
1.000
o
@ ® TOTAL DiSSOLVED SOLIDS
® _, O CALCIUM fCn**)
©
t$ ® D SULFATE (SO4")
.9 * « ^ A CHLORIDE (C)~)
* * NOTE: SPECIES WHOSE
CONCENTRATIONS ARE LESS
THAN 600 ppm ARE NOT
PLOTTED.
" 4 ft@ * A AAA A A
<->O O pa D * 0 A * j^
- O v ^o»^i /\ C> v^P.
D ^3
6,000
S.OOO
4,000
3,000
2,000
1.0W
o
40 60120160200240200320380400440
TEST TIM£. Houn
I 8/7 I 1'8 I a-9 I «/10 I VII I IS/12 I 1/13 I W14 I I/IS I I/1> I W17 I VII I 8/19 1 8/20 I 8/21 I 8/22 I 8/23 I S/24 I
CALENDAR DAY (1975)
Gas Rate • 30,000 acfm 300 °F
Gas Velocity-12.5 Wsec
Uquor Rate-1200 gpm
UB = 50 gsl/mcf
EHT Reddence Time = 15min
Three Stages, S in spheres/stage
Percent Solids Recirculated - 14.8-16.2 wt %
Total Pressure Drop, Excluding Mist Ellm.
• 7.3-7.5 in. H,0
Scrubber Inlet Liquor Temperature * 126-129 °F
Liquid Conductivity*4,300-5,300 u. mhos/cm
Discharge (Darifier) Solids
Concentration- 3S-44wt%
Limestone Addition to EHT
Figure I- I OPERATING DATA FOR TCA RUN 557-2A
1-2
-------
BEGIN HUN H8-2A
END RUN H9-2A I
120
180
380
400
200 240 290 320
TEST TIME. Houn
I 8/18 I 8/17 I 8/18 I 9/19 I 8/20 I 8/21 I 8/22 I 8/23 I 8/24 I 8/2S I 8/28 I 8/27 I 8/28 I 8/29 I 8/30 I 8/31 I 9/1 I 8/2 I 9/3 I
CALENDAR DAY
1.4
J, 1.3
1.2
1.1
i
II
8 2 3,000
Is 2-000
TOTAL DISSOLVED SOLIDS
O CALCIUM (Cl**»
O SULFATE (SO4")
A CHLORIDE
-------
BEGIN RUN 55*2A
END RUN S59-2A
120 160 200 240 280 320 360 400 440
•TEST TIME, Hours
9/6 I 9/7 ! 9/8 | 9/9 t 9/10 1 9/11 ! 9/12 I 9/13 t 9/14 I 9/15 1 9/16 1 9/17 I 9/18 1 9/19 I 9/20 I 9/21 I 9/22 I 9/23 I 9/24
CALENDER DAY
II
NOTE: SPECIES WHOSE
CONCENTRATIONS ARE LESS
6,000
5,000
4.000
3.000
3.000
1.000
0
_ • O SULFATE (SO4= } THAN 500 ppm
• • A CHLORIDE (Cr) AOE NOT PLOTTED
» * • * * *
* ****-*** * ** *
« *
n A
£>»*, ... ..•:••-. -s- le"—
^ ^OO O O DO D nD n O^^n Q QQ R
i t i t t i i i i i i
6.000
5,000
4.000
3.000
2.000
i.ooo
n
t 9/6 I 9/7 I 9/8 I 3/9 I 9/10 I 9/11 !
200 340 280 320 360 4OO 440
TEST TIME. Houn
/13 I 9/14 I 9/15 I 9/16 I 9/17 \ 9/18 ] 9/19 I 9/20 I 9/21 I 9/22 ! 9/23 I 9/24 I
CALENDAR DAY (1975)
Gas Rate « 30,000 acf m 9 300 ° F
Gas Velocity =12.5 ft/sec
Liquor Rate = IZOOgpm
L/G = 50 gal/mcf
EHT Residence Time = 15 min
Three Stages, 5 in. spheres/stage
Percent Solids Retirculgted ~ 14-16 wt %
Total Pressure Drop, Excluding Mist Elim.
• 7.0-8.1 in. H20
Scrubber Inlet Liquor Temperature = 125-127 °F
Liquid Conductivity = 3,60(M,500 u. mhos/cm
Discharge (Clarifier) Solids
Concentration = 36-42 wt %
Limestone Addition to EHT
Figure 1-3. OPERATING DATA FOR TCA RUN 559 - 2A
1-4
-------
•BEGIN HUN 56fr2A
ENDRUN560-2A j
sii
* £ i
11 5
0*1
K a
tu ij
Z O
4.500
4.000
3.500
3.000
2.500
2,000
-
/ • A r\
- / \, A M
vi r \L/ u U
-^JK/^ vu y ^ V^
-
1. L L 1 1 1 1 1 1 1 1
4.500
4,000
3.500
3,000
2,500
2.000
160 200 240 280 320 360 400 440
TEST TIME, Hours
! 9/24 I 9/25 I 9/26 I 9/27 t 9/28 I 9/29 I 9/30 I 10/1 I ID/2 I 10/3 I 10/4 I 10/5 I 10/6 1 10/7 I lO/« I 10/9 I 10/10 I 10/11 I 10/12 I
CALENDAR DAY
120
160
320
360
WO
440
a
j|
LiDS IN
UOR, m»
SB
Q J
||
5
5,000
4,000
3,000
2.000
1,000
0
' • « * • TOTAL DISSOLVED SOLIDS NOTE: SPECIES WHOSE
• • • A • * x\ 4.4. CONCENTRATIONS ARE LESS
• • • CALCIUM (C^i THAN 500 ppm ARE NOT
• O SULFATE (SO4"( PLOTTED.
A CHLORIDE (CO
~44A»AAAA
* A
•6$§o aaS® Qo&S ^
1 • i I J i 1 1 * 1 *
5.000
4.000
3,000
2,000
1.000
0
200 240 280
TEST TIME, Hour*
9/24 I 9/25 ! 9/26 I 9/27 I 9/28 t 9/29 I 9/30 I 10/1 I 10/2 I 10/3 ( 10/4 | 10/5 I 10/6 I 10/7 I 10/8 I 10/9 I 10/10 I W11 I 10/12"!
CALENDAR DAY (1975)
Gas Rate = 30,000 acfm @ 300 °F
Gas Velocity =12.5 ft/sec
Liquor Rate- IWOgpm
L/G - 50 gal/mcf
EHT Residence Time •= 15 min
Three Stages, 5 m. spheres/stage
Percent Solids Recirculated = 14.6-15 wt %
Total Pressure Drop, Excluding Mist Elim.
= 7.0-8.1 in. H20
Scrubber Inlet Liquor Temperature = 123-126 °F
Liquid Conductivity = 4,900-6,500 u. mhos/cm
Discharge (Clarifier) Solids
Concentration = 36-41*1%
Limestone Addition to EHT
Figure I-4. OPERATING DATA FOR TCA RUN 560 - 2A
1-5
-------
I BEGIN RUN 561-2A END RUN 561 2A |
4.000
3,500
3.000
2.50.
2,000
1 BOO
J)
- f
-yv/uV^
-
(
prJk/U
1 V VI v
-
r ^
1 , 1 1 1 1 1 1 1 1 1 1
4.000
3,500
3,000
2,500
Z.OOO
1500
280
360
400
440
40 80 120 160 200 240
TEST TIME, Hours
I 10/1 i 10/2 1 10/3 I 10/4 I 10/5 I 10/6 | 10/7 i 10/8 I 10/9 1 10/10 I 10/11 I 10/12 I 10/13 I 10/14 1 10/15 | 10/16 | 10/17 | 10/16 | 10/19
CALENDAR DAV
1 5
ill "
- g tn 13
1 2
1.1
1* OT
2 -1 i
O a:' 20
<° O
g° 10
i 5 i*j
§- °
U 150
S°o
co in
3 0 O
n ~ ^0
w £ o
9,000
_, 7,500
OLVED SOLIDS IN SC
INLET LIQUOR, mg/l )
0
^^
/ \
""^'' ^v^V
-
-
-
"\ /\^
- v^_-— ^\yv ^^^
j
•
V.
L
O TOTAL DISSOLVED SOLIDS
d O CALCiUM (Ca+'t'l
D SULFATE (SO4=)
Q Jk CHLORIDE (C!~t
= « NOTE- SPECIES WHOSE
- * * CONCENTRATiONSARE LESS
9 THAN 500 ppm ARE NOT
A PLOTTED.
&AA A 0AAA ^
1 i D l 1 l t i i i i i
1.5
1 4
l.i
1,2
1.1
30
20
10
0
150
100
50
0
9,000
7,500
6,000
4,500
3,000
1,600
0
280
400
440
1 10'
40 80 120 160 200 240
TEST TIME. Hours
I 10/2 I 10/3 I 10/4 I 10/5 I 10/6 1 10/7 | 10/8 I 10/9 I 10/10 I 10/11 I 10/12 I 10/13 ! 10/14 I 10/15 I 10/16 1 10/17 t 10/16 I 10/19 I
CALENDAR DAY (1975)
Gas Rale = 30,000 acfm @ 300 °F
Gas Velocity = 12.5 ft/sec
Liquor Rate = 1200 gpm
L/G = 50 9»l/mcf
EHT Residence Time ~ 15 min
Three Stages, 5 in. spheres/stage
Percent Solids Recirculated = 14-16 wt %
Total Pressure Drop, Excluding Mist Elim.
= 7.3-7.6 in. H20
Scrubber Inlet Liquor Temperature = 124-128 °F
Liquid Conductivity -- 6,000-7,800 u. mhos/cm
Discharge (Clarified Solids
Concentration = 37-44 wt %
Limestone Addition to EHT
Figure I- 5. OPERATING DATA FOR TCA RUN 561-2A
1-6
-------
40
160
360
400
200 240 2f>0 320
TEST TlME,Houn
10/8 I 10/9 1 10/10 I 10/11 I 10/12 I 10/13 I 10/14 ! 10/15 I 10/16 I 10/17 I 10/18 t 10/19 I 10/20 I 10/21 I 10/22 I 10/Z3 t 10/24 I 10/25 I 10/26 I 10/27
CALENDAR DAY
480
9,000
7,500
6.000
4,500
3,000
1,600
.* A
O
D
• TOTAL DISSOLVED SOLIDS
O CALCIUM (Cs**)
D SULFATE 1S04"I
A CHLORIDE ICI~)
•••»
_1_
NOTE: SPECIES WHOSE
CONCENTRATIONS ARE LESS
THAN 600 ppm ARE NOT
PLOTTED. -
O
D
O
D
_1 L
A
O
,
A*
00 f
0 40 M 120 180 200 240 280 320 360 400 440
TEST TIME.Hixin
I 10/8 I 10/9 I 10/10 I 10/11 I 11/12 I 10/13 I 10/14 I 10/16 I 10/16 I 10/17 I 10/18 I 10/19 I 10/20 I 10/21 I 10/22 I 10/23 110/24 I 10/26 I 10/28 I
CALENDAR DAY U975)
7,500
6.000
4.600
3.000
1.600
0
Gi. Rm-30,000 acfme 300 °F
Gil Velocity = 115 ft/MC
Liquor Fl«ti» 1200 opm
L/G > 50 Jil/mtf
EHT Retidiwt Timi - 12 min
Thru Slttn, 5 in. sphHa/ittgc
Pirant Solids RecirculiMd • 14-15.5 wt %
Toul Pranira Drop, Excluding Min Elim.
- 7.2-7.9 in. HjO
Serubbir Inltt Liquor Timpirnun » 128-130 °F
liquid Conductivity - 5,570-8.100 u. mhoi/cm
Ditthirji (Chrlfitr) Solidi
Concintritlon • 37-43 wt K
Umntom Addition to EHT
Figure 1-6. OPERATING DATA FOR TCA RUN 562-2A
1-7
-------
END HUN 562 2A • ! &EGIN RUN 562-28
END RUN 562-28*
- UNIT 10 OUTAGE
—L-
_J „_ -
I 520 560 600 640 680 720 760 800 840 880 920
TEST TIME, Hours
I 10/28 I 10/29 I 10/30 1 10/31 I 11/1 I 11/2 t 11/3 I 11/4 I 11/5 I 11/6 1 11/7 I 11/8 I 11/9 I 11/10 1 1i,t! I 11/12 I 11/13 I 11/14 | 11/15
CALENDAR DAY
J 50
• 4,000
- 3,500
- 3,000
< 2,500
2.000
1,500
IE
6,000
4.500
3,000
1 500
0
4S
. *
- A A
u co
Qll
0
1 10/28 i
»®
0
* ** *>
O -o n§
n n
520 SGO
10/29 1 10/30 i 10/31 1
••
**
oo
DO
600
11/1 1
• 1OIAL DISSOLVED SOLIDS
O tA'UUM iCa*^
D SUif-ATE iSO^I
A CHLGFODf (Ci~j
NOTE SPECIES WHOSt
CONCENTRATIONS AHf- I.!
THAN 500 pp™ Ant NOT
PLOTTED
I 11/4
" A
°o o
DD D
TEST TIME, rtouis
i 11/5 I 1V6 I 11/7 | 11/8 i 11/9 | 11/10 ! i)M1 1 11/12 | il/11 I il/l
CALENDAR DAY (1975)
170
0
9,000
7,500
6,000
4.b(tQ
3,000
1.&UO
Gas Rate-30,000 acfm@ 300 °F
Gas Velocity = 12.5 ft/sec
Liquor Rate - 1200 gpm
L/G = 50 gsl/mcf
EHT Residence Time = 12 rrin
Three Stages, 5 in. spheres/stage
Discharge (Clarifier) Solids
Concentrator! = 37-43 wt % (562-2A),
3446 wt % (562-28)
Percent Solids Recireulated « 14-15.5 wt % (562-2AI,
14-1Swt%(562-2B)
Total Pressure Drop, Excluding Mist Elim. « 7.2-7.9 in. HjO
(562-2A), 8.0-8.6 in. HjO (562-28)
Scrubber Inlet Liqucr Temperature = 128-130°F
(562-2A), 124-126°F{562-2B)
Liquid Conductivity-5,570-8,100 -u, mhos/cm (562-2A),
7,000-8,400 H, mhos/cm (562-28)
Limestone Addition to EHT
figure I-7. OPERATING DATA FOR TCA RUNS 562-2A(Continued) &562-2B
1-8
-------
BEGIN RUN S63-2A
END RUN 563-2A;
- FAN DAMPER PROBL£M
5.0
4,000
3.500
3.000
2,500
2.000
40 80 120 160 200 240 280 320 360 400 440
TEST TIME, Hour*
I 11/7 1 11/8 I 11/9 I 11/10 I 11/11 ! 11/12 I 11/13 ! 11/14 1 11/15 I 11/16 I 11/17 I 11/18 1 11/13 I'll/a* I 11/21 I 11/22 I 11/23 I 11/24 I 11/25 I
CALENDAR DAY
* £ -
2§ g
£ Q -
11$
_ «# t50
Iss
£ a ®
> 3 a 100
o g a
§0 3 SO
55E&
S3z o
6,000
(t
us
|_ 5.000
|| 4,000
~ O 3.000
8 I
£ H 2,000
8 " 1,000
O
n
.
.
•"X^ s--*—
^^-—\_ -^^_
• TOTAL DISSOLVED SOLIDS NOTE: SPECIES WHOSE
A A .. CONCENTRATIONS ARC LESS
• • , O CALCIUM (Ci**) THAN 500 wm ARE NOT
A • D SULFATE ISO4") PLOTTED.
— * m
• 0 * A CHLORIDE (Cl~) _,
* A
A 4 . A
A
0 O O^ A /N
° 0° aS ^>O flo °
a , , Q 6,6 °u ,Da o ,
150
100
50
0
6,000
6,000
4,000
3,000
2,000
1,000
0
I 11/7 I
280 320 360 400 440
TEST TIME, Hour)
I 11/10 I 11/11 t 11/12 i 11/13 | 11/14 ! 11/15 I 11/16 I 11/1? I 11/18 I 11/19 t 11/20 I 11/21 I 11/22 I 11/23 I 11/24 I 11/26 I
CALENDAR OAV (1975)
Gas Rate ~ 30,000 acfm H> 300 °F
Gas Velocity = 12.5 ft/sec
Liquor Rate = 1200 gpm
L/G = SO gal/mcf
EHT Residence Time = 12 min
Three Stages, 5 in. spheres/stage
Note: Only solids data points with
ionic imbalances between t
are plotted.
8.5%
Percent Solids Recirculated = 14.8-15.6 wt %
Total Pressure Drop, Excluding Mist Elim.
'• 7.8-8.1 in. H?0
Scrubber Inlet Liquor Temperature - 121-127 °F
Liquid Conductivity = 3,700-7,200 u. mhos/cm
Discharge (Clarifier) Solids
Concentration = 36-46 wt %
limestone Addition to EHT
Figure 1-8. OPERATING DATA FOR TCA RUN 563-2A
1-9
-------
END HUN 5*4 2A
3.000
2.500
2.000
4.S
4, HM
4,000
3,500
3.000
2.500
2,000
TEST TIME, Hourj
I 11/15 I 11/16 I 11/17 I 11/18 i 11/19 1 11/20 I 11/21 I 11/22 I 11/23 I 11/24 I 11/25 I 11/26 I 11/27 I 11/28 I 11/29 I 11/30 I 12/1 I 12/2 I 12;
CALENDAR DAY
I IB
2 % 1 '3
< 1 1
i 5 "" 1'2
til 1.1
1.0
c i i 30
3 § M
!? -
OK10
- 0
1 °= 1M
X 2 100
O o
z o
$ 3 50
Z 0
IN SCRUBBER
§ | 4,000
S 9
o -> 3.000
|i 2.000
5 1,000
0
-
- ^L^-v
y\^y\rv^ ^/
-
i >, h* p. .n
\ „* \/ v/ \
W/
-
~ A-^— _v\ Ax
- ^^~^\/ x
-
-
- • TOTAL DISSOLVED SOLIDS NOTE- SPECIES WHOSE
• O CAICIUMIC."! CONCENTRATIONS ARE LESS
(ft * _ • THAN 500 ppm ARE NOT
• 0 • ° SULFflIE IS
-------
0 BEGIN RUN 665- 2A ! ENDRUNHS-2A
<°
55 M
66
~s "
g SS
so
45
0.6
Hf "
||| M
Q
0.0
6.0
6.5
S X
II i 5.0
y (ft
4.5
4.0
4,500
4.000
8 I **°
if 3-°°°
2,500
2,000
1
In A
-uuv I/I/
h/
;
-____
> — INLET
•n V
J Wv^^v^W^A-
\ t~*.r*s\ rA. . yS Al VA
- VM/ M^V« ^r
^ ^ — OUTLET
^ /I
- X^/ V
\yV
•
70
66
80
66
SO
45
O.B
0.4
0.2
0.0
8.0
5.5
5.0
4.5
4.0
4,500
4.000
3,500
3,000
2.SOO
yafKi
0 40 SO 12O 160 200 240 280 320 380 400 440 480
TEST TIME, Noun
I 11/22 1 11/23 \ 11/24 t 11/26 1 11/26 I 11/27 I 11/28 1 11/29 | 11/30 I 12/1 1 12/2 E 12/3 1 12/4 1 12/5 1 12/S 1 12/7 I 12/8 ! 12/9 E 12/10 1 12/11
CALENDAR DAV
14 * *
a j 1 1.3
ijJ8~
o 1 i 1.1
ti S 1
1.0
5 * 30
11!
3|| »
£03 10
* x 5 0
-
*\y \ «^.*^-A.->^-A **-^** *
L i/v— ^-^v j
•
f . , . |\
\yVry\j V
.
1.3
1.2
1.1
1.0
30
20
10
0
o
c u 15°
1 * 10°
i*l
*SI o
8,000
IE 7,000
03
11 6-0
-------
BEGIN PUN S66-2A
END RUN 666 2A i
40 80 120 160 ZOO 240 280 320 360 400 440
TEST TfME, Hour*
11/27 I 11/28 I 11/29 I 11/30 I 12/1 1 12/2 I 12/3 I 12/4 I 12/5 I 12/6 I 12/7 j 12/8 I 12/9 I 12/10 | 12/11 I 12/12 I 12/13 I 12/14 I 12/15
CALENDAR DAY
4.5
4,000
3.500
3.000
2,500
2,000
1.500
11
9,000
8.000
7,000
6.000
5,000
4,000
3,000
2,000
1,000
0
© TOTAL DISSOLVED SOLIDS NOTE: SPECIES WHOSE
~ ++. CONCENTRATIONS ARE LESS
O O SULFATE
-------
80
120
320
400
160 200 240 280
TEST TIME, Hours
I 12/4 I 12/5 I 12/6 I 12/7 I 12/8 I 12/9 I 12/10 I 12/11 | 12/12 ! 12/13 I 12/14 I 12/15 I 12/18 | 12/17 1 12/18 | 12/19 I 12/20 ! 12/21 I 12/22 I
CALENDAR DAY
i*s
3Sg
S^S
B P3
K ^ l~
"Si
50
0
6.000
5,000
4.000
3.000
2,000
1,000
A * A *
A.
*
ftft
oo
22
• TOTAL DISSOLVED SOLIDS
O CAtCtUM (C.^1
Q SULf=AT£ (SO4")
A CHLORIDE tell
NOTE: SPECIES WHOSE
CONCENTRATIONS ARE LESS
THAN 500 ppm ARE NOT
PLOTTED.
I 12/4 t 12/5 I 12/6 I 12/7 I 12/8 ! 12/9 I 12/10 I
200 240 280 320 380 400 440
TEST TIME. Hourt
12/11 I 12/12 I 12/13 I 12/14 I 12/16 I 12/16 I 12/17 | 12/18 | 12/19 I 12/20 ! 12/21 | 12/22 t
CALENDAR DAY (1975)
50
0
6.000
5,000
4,000
3,000
2,000
1,000
0
Gas Rate = 30,000 acfm * 300 "f
Gas Velocity' 12.5 ft/sec
Liquor Rate = 1000 gpm
L/G = 42 gal/mcf
EHT Residence Time = 14.4 min (3 tanks)
Three Stages, 5 in. spheres/stage
Discharge (Clarifier) Solids
Concentration = 37-43 wt % (567-2A),
38-46 wt % I568-2A)
Percent Solids Reeireulated = 14.MS-6wt% (5S7-2A),
14.5-15.3 wt% (562-26)
Total Pressure Drop, Excluding Mist Elim. = 8.8-9.6 in. H^O
(567-2A). 8.6-10.0 in. HjO (568-2AI
liquid Conductivity = 5,700-6,800 a. mhos/cm (567-2A),
4,800-8,100 it mhos/cm (568 2A)
Limestone Addition to First EHT
Note: Only solids data points with
ionic imbalances between - 8.5%
are plotted.
Figure 1-12. OPERATING DATA FOR TCA RUNS 567-2A & 568-2A
1-13
-------
u Sj
4.000
3.500
3.000
2.500
2.000
1 500
rt !f \ f]jin
\A/ 1 W
\ n/JV / *
- \ jvy^ i /
- l/v U
-
i i i i i i i t i i i
4.000
3,500
3.000
2,500
2,000
l.SOO
400 440
TEST TIME, Moun
1 12/17 1 12/18 | 12/19 I 12/20 1 12/21 I 12/22 1 12/23 I 12/24 1 12/26 I 12/26 I 12/27 | 12/28 I 12/29 I 12/30 t 12/31 I 1/1 i 1/2 I 1/3 | 1/4
CALENDAR DAY
jg Bf 20
1 ,2/17 1 12/18 I 1
0 200 240 280 320 360 400 440
TEST TIME. Houri
12/23 I 12/24 1 12/25 I 12/26 I 12/27 t 12/28 t 12/29 I 12/30 I 12/31 I 1/1 I 1/2 I 1/3 I 1/4
CALENDAR DAY (1975/1976)
§1°;
> 1 ®
" z
|E
§?
z |*
If
Q -"
|z
5
150
100
50
0
V_— ^— -
'.
i
8,000 r- • tt TOTAL DISSOLVED SOLIDS NOTE: SPECIES WHOSE
7,000
6.000
5,000
4,000
3.000
2,000
1.000
0
0 Q ++ CONCENTRATIONS ARE LESS
CALCIUM
-------
Is
<2
EC (C
~s
af >
JIH HUH 57Q.2A
END RUN 57&2A!! BEGIN RUN S712A
JENDRUN571.2A
0.2 -
0.0 *~
TEST TIME, Houn
I 12/24 i 12/25 t 12/26 I 12/27 ! 12/28 I 12/29 I 12/30 I 12/31 I 1/1 I 1/2 I 1/3 1 1/4 I 1/5 I 1/6 1 1/7 I 1/8 I 1/9 I 1/10 I 11/11 I
CALENDAR DAV
III
" S S
Iff
s*
§11
Hi
z - a
§12
"" x 2
0
K £*
1|1
|||
s«|
c
i -E
" 1
it
-1
o a
a jf
> J
I1
o
1.3
1.2
j /ILVHA
/ , /\ / s
fA AA /^/Vv*^ \y) \
1.4
1.3
1.2
1,1 *- w • w " J 1.1
30 r- > -t 30
20
10
0
]i
Sf»AtA/\N\\ f.AA/
\ A/\A/^ v V* /V\n N\\
' v v V^ ^ ^wj V \ y V >
v ** \y
150
100
50
0
*. .*,
/ \^_ --^ ^- - ^^^ ^, ^^^ X^^,
. *~- v ^^-»
"
.
20
10
0
150
100
50
0
•
8,000
7.000
6,000
5.000
4.000
3.000
2,000
1,000
• • TOTAL DISSOLVED SOLIDS
• • • • s\ -M.
0 ^ »•* ^ CALCIUM (Ca**)
* • D SULFATE (SO4=)
• * A CHLORIDE (CI-)
NOTE: SPECIES WHOSE
CONCENTRATIONS ARE LESS
THAN SCO ppm AR E NOT
_ PLOTTED,
• H
A
A . * A
D pA A* .A A A *
Q ** i" A° QO DO 0°D 0 0 ^ Q
& ^ oo oo ^ ° o^ ° °
" v
1 I 1 1 t 1 1 1 1 1 1
8,000
7,000
6.000
5.000
4,000
3,000
2.000
1,000
D 40 BO 120 160 200 240 280 320 360 400 440 490
TEST TIME, Hour*
1 12/24 1 12/25 1 12/26 1 12/27 1 12/28 ! 12/29 I 12/30 ! 12/31 I 1/1 1 1/2 L 1/3 t 1/4 | 1/5 1 1/6 1 1/7 1 1/8 1 1/9 I 1/10 I 1/11 I
CALENDAR DAY (197S/1976)
Gas Rate > 30,000 acfm @ 300 °F
Gas Velocity' 12.5 ft/sec
Liquor Rate = 1000 gpm
L/G= 42gal/mrf
EHT Residence Time " 10.8 min (3 tanks)
Three Stages, 5 in. spheres/stage
Discharge (Clarifier) Solids
Concentration = 34-41 wt % (570-2A),
34-42 wt»(571-2A)
Percent Solids RecirculaUd - 13.8-15.4 wt % (570-2A),
14.2-16.8*1% (571-2A1
Total Pressure Drop, Excluding Mist Elim. =6.9-8.1 in. HnO
(670-2A), 6.7-7.3 in. HjO I571-2AI
liquid Conductivity - 5,800-9,900 it mhos/cm (570-2A),
6,400-10,400 it mhos/cm (571-2A)
Limestone Addition to First EHT
Note: Only solids data points with
ionic imbalances between i 8.5%
are plotted.
Figure 1-14. OPERATING DATA FOR TCA RUNS 570-2A & 571-2A
1-15
-------
4.5
4,000
3,500
3,000
2.500
2,000
TEST TIME, Hour*
I 1/3 I 1/4 I 1/5 I 1/6 I 1/7 I 1/8 I 1/9 I 1/10 I 1/11 1 1/12 I 1/13 I 1/14 I 1/15 i 1/16 ! 1/17 I 1/18 I 1/19 I 1/20 I 1/21
CALENDAR OAV
I 1/22
£
11
y —
s I
9g
sl
S H
0 2
ft
Q
8,000
7,000
6,000
5,000
4.000
3.000
2.000
1,000
«-. * * * A o.iriiiu fr++i CONCENTRATIONS ARE LESS
- *• «A *** THAN 500 ppm ARE NOT
tyW W W D SULFATE lSO4=f PLOTTED,
~ ® A CHtORIDE(CI~t
@
~
A AA
AA A A
"AAAA^A
, AA A
- :r g g DO njrj Q 9B A Q "
LJ 0 AA&^tJy->*~> LJQ
D
1 1 1 i 1 I 1 1 1 1 1
> 40 80 120 160 200 240 280 320 360 400 440 4
TEST TIM6. Houn
8,000
7.000
6,000
5,000
4.000
3,000
2,000
1,000
o
»
CALENDAR DAY (1976)
Gas Rate = 30,000 acfm @ 300 °F
Gas Velocity « 12.5 ft/sec
Liquor Rale = 1000 gpm
L/G =42gal/mcf
EHT Residence Time = 10.8 Tlin , 3 tanks
(572-2A); 14.4 min , 3 tanks (573-2A)
Three Steges, 5 in. spheres/stage
Discharge (Clarifier) Solids
Concentration = 34-47 vrt % (572-2A),
34-43 wt % (573 2A)
Percent Solids Recirculated = 14-15 wt % (572-2A),
14.5-15.5 wt%(573-2A)
Total Pressure Drop, Excluding Mist Elim. =6.3-7.1 in. HjO
(572-2A), 6.7-7.1 in. HjO (673-2AI
Liquid Conductivity = 7.100-J1.000 ju. mhos/cm (572-2A),
limestone Addition to First EHT
Note; Only solids data points with
ionic imbalances between 1 8.5%
are plotted.
Figure 1-15. OPERATING DATA FOR TCA RUNS 572-2A & 573-2A
1-16
-------
JENDRUN676-2A
-Ju
40 80 120 160 200 240 280 320 360 400 440
TEST TIME, Houra
i 1/16 I 1/17 I 1/18 I 1/19 I 1/20 I 1/21 I 1/22 I 1/23 I 1/24 I 1/25 I 1/26 I 1/27 I 1/28 i 1/29 I 1/30 I 1/31 i 2/1 I 2/2 I 2/3 I
CALENDAR DAY
4.5
4.000
3,500
3,000
2.500
2,000
1.500
0
ill
|§;
tC. (_" t~
o, § j
oc
11
11
II
8g
> m
§?
0
150
100
50
0
r .
- ~^s— ^v-^-. /\
^/
.
10.000 r • TOTAL DISSOLVED SOLIDS NOTE: SPECIES WHOSE
9.000
8,000
7,000
6,000
5.000
4.000
3.000
2.000
1,000
o
• O CALCIUM
-------
40 00 120 160 200 240 280 320 360 400
TEST TIME, HOIBI
1/23 I 1/24 I 1/25 ! 1/26 I 1/27 1 1/28 i 1/29 I 1/30 I 1/31 I 2/1 I 2/2 I 2/3 I 2/4 I 2/5 ! 2/6 I 2/7 | 2/8
CALENDAR DAY
1 2/10 i
l = ;
111
5 »• £
•.«!
s_
11
11
Is
82
S^
> 13
|S
5
ISO
100
so
0
[ A -^^ "
/^V ^^\_ __ ^__.^
«
150
100
50
0
8,000 r- A * A TOTAL DISSOLVED SOLIDS ~l B-°00
7,000
6,000
S.QOO
4,000
3.000
2.000
1,000
® 0 O CALCIUM (Ca4^)
® • 9 • g * g SULFATE
-------
tNO RUN 58! 2A ;
Si
ct ce
£! a 95
O
90
85
sl ' M
X
75
70
65
06
11? Od
ill o?
o
00
60
£ > 55
5 5! 50
« '
4 5
4 000
3.500
s" I 3'°°°
sJJ o"
1 § 2-BO°
2.000
1.500
ii| "4
iff "
B 6 1 , o
cc ^
a m "» ™
| | 1
sag »
||l ,0
SI 5 iS o
5 2
o
- tt oU 150
£ a S
> 3 tt 100
$ O J 50
SS J
Z o
6,000
7,000
S - 6.000
| =!, 5,000
jjjg 4000
gs
2 ^ 3000
£ ~ 2,000
1,000
0
: . • . , 1
rt AR H
/ ft
- aTU \
¥ j
A 11 JinM r
|\ V h/
1 v \ f
< \ju
I
-
-1
"•^~v— /^~^~'^s
-
-
, INLET
- V-^X- f-, j\^
•'•< -^ "^ ^_y-
— OUTLET
•
A/V
\Ai ^y\ I/A
! / t[\ \f
\ / -V^J
1 1 1 1 i 1 1 1 1 1 I
) 40 80 120 160 200 240 280 320 360 400 440 4E
TEST TIME. Hours
CALENDAR DAY
:,//M/v- v/ :
V^-'"..'
A /I • /•
r \ , N / /-, Aj\ \' -
,-*J\AM / u v/ j
- J ' U '/ \/
V
_
q
/•• — • -~^r^— ~+/^~ . » — •
• / 'v
••
•
•
• • TOTAL DISSOLVED SOLIDS NOTE; SPECIES WHOSE
/v +. CONCENTRATIONS ARE LESS
• O CALCIUM 1C,". THAN 600 ppm ARE NOT
D SULFATE (S0431 PLOTTED
A CHLORIDE (CO
*•
*» *
. ** ** *
A
* * 0° a o
• A o<> °^ a° m o o
- 00
np i i i i i 1 1 1 ' 1 1
9S
90
Bfi
BO
75
70
65
0.6
0.4
0.2
0.0
6.0
5,5
5.0
4.5
4.000
3,500
3.000
2,500
2,000
to
1-6
1.4
1.2
1.0
30
20
10
0
150
100
50
0
8.000
7.000
6,000
5.000
4.000
3,000
2,000
1,000
0
200 240 • 280 320 360 400
TEST TIME, Mou-s 4
I 2/5 I 2/6 I 2/7 I 2/8 I 2/9 I 2/10 I 2/11 I 2/12 I 2/13 I 2/14 ! 2/15 ! 2/16 1 2/17 I 2/18 I 2/19 I 2/20 ! 2/21 I 2/22 I 2/23 I 2/24
CALENDAR DAY (1976)
Gas Rate = 27,000-30,000 acfm S> 300 °F
Gas Velocity = 11.5-12.5 ft/sec
liquor Rate- 1200gpm
L/G - 50-54 gal/mcf
EHT Residence Time - 12 min
Three Stages, 8 in. spheres/stage
Note: Only solids data points with
ionic imbalances between ± 8.5%
are plotted.
Percent Solids Recirculated - 14-15.5 wt %
Total Pressure Drop, Excluding Mist Elim.
" 8.7-14.4 in. H20
Liquid Conductivity ' 5,300-8,300 M mhos/cm
Discharge (Clarifier) Solids
Concentration = 35-42 wt %
Limestone Addition to EHT
Figure I -18. OPERATING DATA FOR TCA RUN 581-2A
1-19
-------
Appendix J
AVERAGE LIQUOR COMPOSITIONS FOR THE TCA TESTS
J-l
-------
Table J-l
AVERAGE LIQUOR COMPOSITIONS FOR TCA LIMESTONE RUNS
FROM JUNE 1975 TO NOVEMBER 1975
Run No.
546-2A
557-2A
558-2A
559-2A
560-2A
Percent Per
Solids Sul
Discharged Oxid
35-44 10-
39.44 10-
34-42 10-
36-42 7-
cent
fur Sample Point
ized
25 Scrubber Inlet
Scrubber Outlet
Clarifier Overflow
21 Scrubber Inlet
Scrubber Outlet
Clarifier Overflow
20 Scrubber Inlet
Scrubber Outlet
Clarifier Overflow
24 Scrubber Inlet
Scrubber Outlet
Clarifier Overflow
36-41 9-17 Scrubber Inlet
Scrubber Outlet
Clarifier Overflow
pH
5.85
5. 40
7. 15
5. 95
5. 55
7. 25
5. 85
5.35
6. 85
5. 85
5. 30
7.25
5.65
4. 95
7. 10
Liquor Species Concentration,
Ca++
1440
1450
1190
990
1050
1100
1060
1130
1100
910
920
1050
860
840
940
Mg++
190
190
170
280
270
290
330
315
290
370
365
400
360
370
380
Na +
40
35
35
70
65
80
45
45
45
45
50
50
65
65
50
K
60
50
45
85
85
110
60
60
50
60
60
65
85
80
60
S0,=
90
170
75
85
175
180
110
150
120
95
110
80
50
105
8
SO 4
1310
1320
1140
1270
1470
1210
1610
1770
1630
1390
1320
1500
910
950
840
mg/1 (ppm)
co,=
90
80
85
80
90
75
70
65
40
100
110
80
100
110
80
cr
2220
2200
2060
1690
1620
1700
1660
1600
1750
1770
1660
1810
1970
1840
2200
Total
5400
5500
4800
4600
4800
4700
4900
5100
5000
4700
4600
5000
4400
4400
4600
Calculated Percent
Sulfate Saturation
at 50°C(a)
90
90
75
70
80
70
85
100
90
70
65
75
45
45
40
Note: The values in this table are averages for the steady-state operating periods.
(a) (activity Ca ) x (activity SO =)/(solubility product at 50°C). Estimated solubility product for CaSO4-2H2O
at 50°C is 2. 2 x 10"' (Radian Corporation, "A Theoretical Description of the Lime stone-Injection Wet
Scrubbing Process", NAPCA Report, June 9, 1970).
-------
Table J-2
AVERAGE SCRUBBER INLET LIQUOR COMPOSITIONS
FOR TCA LIMESTONE RUNS MADE FROM NOVEMBER 1975 TO FEBRUARY 1976
Run No.
561-2A
562-2A
562-2B
563-2A
564-2A
565-2A
566-2A
567-2A
568-2A
569-2A
569-2B
570-2A
571-2A
572-2A
573-2A
575-2A
576-2A
577-2A
579-2A
581-2A
Percent
Solids
Discharged
37-44
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
Percent
Sulfur
Oxidized
6-18
5-30
10-30
2-23
9-23
5-19
2-25
4-24
7-30
6-23
4-23
5-25
3-23
10-29
6-28
6-23
6-23
5-20
12-28
18-40
PH
5. 90
5.90
5.65
5.85
5.15
5.25
5.85
5.95
5.55
5. 50
5. 50
5.80
5.80
5.25
5. 55
5.50
5.70
5.80
5.25
5.45
Liquor Species
Ca + +
1270
1350
1730
830
1300
1220
1220
820
870
1340
1330
1430
1800
1740
2220
2010
2010
1560
1580
1890
Mg++
370
370
450
400
360
370
525
410
460
500
460
490
480
490
620
570
550
510
590
470
Na +
50
50
60
50
45
35
45
45
45
55
40
40
45
50
60
55
60
55
60
45
K +
55
55
65
55
60
55
55
55
65
70
60
65
70
70
75
70
70
60
. 65
60
Concentrations ,
SO3 =
60
70
115
115
600
540
95
80
130
160
140
75
95
215
105
105
110
75
255
105
S°4=
950
710
1120
580
2260
1960
1410
730
1770
2280
2270
2200
2150
1920
1950
1760
1530
1290
2270
2110
mg/1 (ppm)
co3=
70
80
140
170
17
23
130
150
60
80
70
65
75
45
40
30
70
85
20
40
cr
2600
2700
2980
2070
1960
1800
2490
2020
1790
2060
1880
2310
2900
3050
3890
3590
3910
3490
3260
3430
Total
5400
5400
6700
4300
6600
6000
6000
4300
5200
6500
6300
6700
7600
7600
8900
8200
8300
7100
8100
8200
Calculated Percent
Sulfate Saturation
at 50°C
55
40
70
25
120
105
60
35
75
115
120
115
130
110
120
105
95
70
120
125
OJ
Note: The values in this table are averages for the steady-state operating periods.
(a)
(activity Ca ) x (activity SO (/(solubility product at 50°C). Estimated solubility product for CaSO4* 2H?O
at 50°C is 2.2 x 10"' (Radian Corporation, "A Theoretical Description of the Limestone-Injection Wet
Scrubbing Process", NAPCA Report, June 9, 1970).
-------
Appendix K
ANALYTICAL PRECISION AND ACCURACY PROCEDURES
K-l
-------
ANALYTICAL PRECISION
Precision of an analytical method refers to the reproducibility of the
results by that method of multiple analyses performed on the same
sample.
Analytical precision is determined at Shawnee from repeated analysis
of routine liquor and solid samples. These samples are chosen to
encompass the ranges of concentration of the substance being analyzed
and of the concentrations of interfering substances usually encountered
in the analytical procedure. For each procedure, a mean normalized
precision P, an upper warning limit UWL, and an upper control limit
UCL have been developed. For example, numbers made up to sim-
ulate the results of duplicate analyses by a single procedure performed
on each of fifteen samples are tabulated in Table K-l. Calculations
of the normalized precision value P for each sample pair, the mean
normalized precision P, the upper -warning limit UWL, and the upper
control limit UCL for the analytical method using this data are also
shown. It can be seen from the calculations that if precision were
perfect, Pwould be zero. From these parameters, "Modified Shewhart
Precision Control Charts"*, have been produced. Use of this kind
of control chart is discussed below.
"Handbook for Analytical Quality Control in Water and Wastewater
Laboratories," EPA Quality Control Laboratory, Cincinnati, Ohio.
K-2
-------
Representative upper control limits (UCL) for the liquid and solid
analyses performed at Shawnee are shown in Figures K-l and K-2,
respectively. These UCL values were based on analyses performed
during June and July of 1975. The data shown in Figures K-l and K-2
are used to flag analytical methods that are unsuitable for the Shawnee
laboratory. For example, because the precision of the liquid sulfite
procedure was poor, as indicated by the large value of its upper control
limit ( shown in Fig. K-l), this procedure or the equipment used
had to be improved or replaced (see Subsection 9. 2. 3).
Precision control charts such as that in Figure K-3 are also used to
warn of analytical difficulty. In practice, these charts are used as
follows. The normalized precision P of the replicate analyses is
calculated as shown in Table K-l. This value is plotted on the control
chart. If the precision is greater than the UCL, the results of the
analysis are out of bounds and are not considered valid. Efforts to
rectify the problem are undertaken. If the precision lies between the
UWL and UCL, analyses are continued while efforts are made to iso-
late the cause of the variation in the data. If the precision is less
than the UWL, the results are considered satisfactory.
K-3
-------
ANALYTICAL DATA ACCURACY
The accuracy of an analytical procedure refers to the degree of differ-
ence between the measured value determined by use of the procedure
(for example, the concentration of a substance in a sample) and the
actual value.
Accuracy is currently determined at Shawnee by the use of carefully
prepared synthetic liquor samples or spiked slurry solids sent as blind
samples from Bechtel, San Francisco to the Shawnee Laboratory.
The samples are selected to span the normal concentration ranges.
The accuracy of the analytical results at Shawnee has been evaluated
using a modification of the general procedures and calculations outlined
by the EPA. * Accuracy is indicated by two parameters - range R, and
average error X. Both measures of analytical accuracy are required
for complete evaluation of accuracy data.
An example calculation of range and average error for the results of
three replicate analyses on each of five separate samples analysed by
the same analytical method is shown in Table K-2. The same cal-
culation procedure may alsobe used on five sets of triplicate analyses,
"Handbook for Analytical Quality Control in Water and Wastewater
Laboratories," EPA Analytical Quality Control Laboratory, Cin-
cinnati, Ohio, June 1972.
K-4
-------
4K
all drawn from the same sample but done at different times or done
by five different analysts to determine valid measures of R and X.
Limits to range and average error for the example are also calculated
in Table K-2. These are:
Upper control and warning limits (UCLR, UWLR) for the
range, R.
Upper control and upper warning limits (UCL — and UWL—)
on the average error.
X
The constants A and Doused in the calculations are given inTable K-3.
These values are used in control charts in the same way as described
above for precision upper warning and upper control limits, except that
there are two measures of analytical accuracy. Hence, two control
charts should be employed, one for the range R and one for the average
error X.
Limits on R or X alone do not completely characterize the accuracy
of analytical procedures. For example, the range may be zero (all
answers the same), yet the answers could be incorrect by any amount.
Thus, limits on R alone are insufficient. Similarly, the differences
between found and actual concentrations could cancel exactly (high
results canceling low results) but the range of results could be wide.
In this case the range would indicate the accuracy of the data and
K-5
-------
limits on X alone would be insufficient. Only limits on both X and
R will provide adequate characterization of accuracy data collected
as part of a quality assurance program.
The UCL^. and UCL,, values for selected liquor analyses are shown
X K.
in Figure K-4. Accuracy data are not yet available for liquid sulfite
and carbonate analyses, or for solid calcium, sulfur, magnesium, or
carbonate analyses. The accuracy of the solid calcium, sulfur and
magnesium analyses has been assessed, but not in a manner that
lends itself to the development of control charts (see discussion,
Section 9).
K-6
-------
Table K-l
EXAMPLE CALCULATIONS
OF NORMALIZED PRECISION VALUES,
UPPER CONTROL LIMITS AND UPPER WARNING
LIMITS, FOR A REPRESENTATIVE ANALYSIS PROCEDURE
Duplicate Concentration
Values Found
XI
51
40
37
22
78
83
50
62
48
50
71
82
77
40
43
X2
52
38
37
25
77
82
50
57
46
49
73
83
76
40
45
Normalized Precision, P =
XI - X2
XI + X2
0.0097
0.0156
0
0.0638
0.0064
0.0061
0
0.0420
0.0213
0.0101
0.0139
0.0061
0.0065
0.0526
0.0227
Number of Duplicate Pairs, n = 15
Mean Normalized Precision, P = 0.016
1 Standard Deviation of P,*"p= 0.018
Upper Warning Limit, UWL = 2&p= 0.035
Upper Control Limit, UCL = 3*p= 0. 053
Note
Mean Normalized Precision = (2P)/n = P
--2 2 1/2
Standard Deviation of P = [(SIP. - nP )/(n-l)]
K-7
-------
Table K-2
EXAMPLE CALCULATIONS OF THE CONTROL LIMITS FOR
AVERAGE ERROR AND RANGE FOR A REPRESENTATIVE
ANALYTICAL PROCEDURE
ACTUAL
VALUE
990
560
1050
870
960
VALUE
FOUND
1010
1100
980
570
520
590
1110
1040
1050
910
850
850
960
990
980
AVERAGE
X
+0.
0
+0.
0
+ 0.
ERROR
040
016
017
RANGE
R
0. 121
0. 125
0. 067
0. 069
0. 031
X =
Found - Actual
Actual
High Found - Low Found
R = Actual
number of observations
per subgroup = 3
X =
n = number of subgroups = 5
= 0.413 = 0.083
R = jf^Jl
n
Upper Control Limit (UCLri)
X
and Upper Warning Limit (UWL— )
X
_ for Average Error
= A?R = 1. 02 x 0.083 = 0. 085
. £*
UWL x= (2/3) A2R = 0. 056
Upper Control Limit (UCL )
rv
and Upper Warning Limit (UWL )
R
for Range
UCLR = D4R = 2. 58 x 0. 083 = 0. 214
UWLR = (2/3)(D4R - R) +"R = 0. 170
K-8
-------
Table K-3
FACTORS FOR COMPUTING
ACCURACY CONTROL AND WARNING LIMITS*
Observations in Factor Factor
Subgroup (1) A? _ D4
2 1.88 3.27
3 1.02 2.58
4 0.73 2.28
5 0.58 2.12
6 0.48 2.00
7 0.42 1.92
8 0.37 1.86
*
Reference: "Handbook for Analytical Quality Control in Water and
Wastewater Laboratories," EPA Quality Control Laboratory,
Cincinnati, Ohio, 1972.
K-9
-------
.6
FIGURE K -1
UPPER CONTROL LIMITS FOR LIQUID ANALYSES
DULPLICATE PRECISION (NORMALIZED) 6/9/75 TO 6/22/75 AND 7/1/75 TO 7/10/75
.5
.4
O
cc
.3
O
O
cc
III
a.
a,
D
.2
CGWD.
Mg
Na
K
ANALYSIS
SO-.,
SO,
TS
CO*
C!
-------
FIGURE K-2
UPPER CONTROL LIMITS FOR SOLIDS ANALYSES
DUPLICATE PRECISION (NORMALIZED) 6/9/75 TO 6/22/75
.25 i-
.20
£ .15
o
cc
O
o
cc
HI
o.
Q.
D
.10
.05
Ca
Mg
S03
so.
TS
CO-
ANALYSIS
-------
z
O
OT
U
UJ
DC
o.
O
UJ
N
oc
o
z
0.25
0.20
0.15
0.10
0.05
0.0
i
FlGUREK-3
MODIFIED SHEWHART
PRECISION CONTROL CHART
FOR SOLID SULFATE ANALYSES
I
J2HEL
O 1816
10/1/75 -10/14/75
• 2816
A 2818
4 282S
J-*
0±0
|a:
UCL = .142
UWL = .094
123123123123123123123123123123123123123123
10/1 10/2 10/3 10/4 10/5 10/6 10/7 10/8 10/9 10/10 10/11 10/12 10/13 10/14
1975
DATE/SHIFT
-------
FIGURE K-4
UPPER CONTROL LIMITS (UCL) FOR LIQUID ANALYSIS ACCURACY
.40
o
D
IX
O
.35
.30
.25
H
i
o
tr
.20
0
u
cc
UJ
0.
0.
3
.15
.10
.05
Ca
Mg
Na K
ANALYSIS
SO
4
Cl
K-13
-------
Appendix L
THIRD TV A INTERIM REPORT OF CORROSION STUDIES:
EPA ALKALI SCRUBBING TEST FACILITY
by
G. L. Crow
H. R. Hor smart
March 1976
L-l
-------
EPA ALKALI-SCRUBBING TEST FACILITY—SHAWNEE POWER PLANT
THIRD INTERIM REPORT OF CORROSION STUDIES
G. L. Crow and H. R. Horsman
Tennessee Valley Authority
Division of Chemical Development
Muscle Shoals, Alabama
Summary and Conclusions
The first and second interim reports of corrosion tests con-
ducted at the EPA alkali—scrubbing test facility at the Shawnee Power
Plant were released in October 1973 and May 1974, respectively. These
reports covered tests conducted in the venturi, the Turbulent Contact
Absorber (TCA), and the marble-bed scrubber systems during the periods
August 1972 to February 1973 and June to September 1973* respectively.
The current report gives results of the third series of tests
which is the longest test period to date, approximately 1—1/2 years.
Tests in this series were conducted only in the venturi and in the TCA
scrubber systems during the period October 1973 through April 1975-
(The marble-bed scrubber has been idle since July 11, 1973•) Materials
that were attacked severely at some locations in the earlier tests were
eliminated and a few alloys not used in the previous tests were included
in the third series. Because of this, a comparison of results from the
current tests with those from the previous tests is rather vague. Disk-
type specimens of 27 alloys were tested in the third series1. The number
of specimens used ranged from 1 of Type 446 stainless steel to 26 of
Type 3l6L stainless steel. Because of this, a realistic comparison of
their corrosion resistance could not be made. However, 20 to 26 specimens
were tested of each of eight alloys. The comparative resistance of the
eight alloys based on the decreasing occurrence of negligible corrosion
rates is as follows:
Number of tests in which
Alloys corrosion was negligible
1. Hastelloy C-276 l4 of 22
2. Inconel 625 12 of 22
3. Carpenter 20Cb-3 9 of 22
4. Incoloy 825 8 of 21
5- Type 316 L 3 of 26
6. Type 201 5 of 23
? (Monel 400 1 of 20
" (Hastelloy B 1 of 20
L-2
-------
Several other alloys showed promise but were not tested at
enough locations to make a reasonable comparison. Twenty of the twenty-
seven alloys tested showed negligible attack at one or more test loca-
tions. At other test locations the corrosion rates ranged from < 1 to
> 872 mils per year. In general, corrosion of specimens in the third
series of tests was less severe than in the first and second series.
The fourth series of tests now in progress at Shawnee will give more
information on some of these alloys.
Hastelloy C-2J6 and Inconel 625 continued to show good
resistance to corrosion at all test locations. Heynes 6B had low rates
(some negligible) in 14 of 15 tests. Corrosion of Type Jl6L stainless
steel was negligible to 1 mil per year in 13 tests and 21 mils in an
erosion—corrosion test; however, crevice and/or pitting attack occurred
in 11 tests. Type 317 did not appear to be superior to Type 3l6L which
is definitely superior to Type 304L in the lime/limestone scrubber
service. Nitronic 50 (formerly Armco 22-13-5) experienced localized
attack which had not occurred in earlier tests of shorter duration. In
this report where penetration by crevice corrosion and/or pitting is
more prominent than general corrosion, low corrosion rates determined
by weight loss are omitted.
One specimen (strip type) each of nine elloys was tested on
the bottom of the TCA effluent hold tank (EKT) to evaluate these materials
for resistance to erosion. A tightly adhering, deposited coating on
the specimens showed that erosion of the tank bottom is not a problem.
Corrosion was negligible for Haynes 6B, Inconel 702, Incoloy 800,
Incoloy 825, and Type 3l6 sta'inless steel. The four other alloys suf-
fered pitting and/or crevice corrosion.
The Type 316 stainless steel guides below the adjustable plug
in the venturi had worn to depths of 0.5 to 1.5 inches. Test bars of
Type 201 stainless steel and of Inconel 625 mounted on the guides failed
in less than 90 days with penetration rates > 0.5 inch per year. Speci-
mens of Type 3l6 stainless steel pipe fitted to shield the guides failed
with wear rates of 1.5 to 2.5 inches per year.
Inlet stack gas, after being humidified with spray weter,
attacked stainless steel ducts and nozzles as follows: slight erosion
of bare duct surfaces; concentration cell—type corrosion (pitting and
crevice) of surfaces underlying deposits; and severe corrosion and
erosion of surfaces subjected to impingement. In general, the neoprene-
lined towers end tanks were in good condition. However, in the venturi
scrubbing system minor repair was required for the neoprene lining in
the flooded elbow and the neoprene—covered "blades of the egitator in the
EHT. Other neoprene-coated agitators showed moderate wear. Only a
few joints of neoprene—lined piping were opened for inspection. One
4-inch pipe ell had blisters in the lining. It is not known whether
L-3
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the lining was defective or if the damage was due to operating conditions.
At the time of the current inspection, the slurry circulating pumps had
"been reassembled in preparation for subsequent operation. However, the
components that had been replaced in pump G-201 were available for inspec-
tion. The liner on both the suction and the seal sides was worn badly,
and the covering on the impeller was worn and damaged from impact with
circulating debris. These components had been in service 1^,000 operating
hours in the TCA system.
The Type Jl6L bull nozzle that discharged lime—scrubbing process
slurry into the venturi failed with a penetration rate of 185 mils per
year. In the towers of the two systems, pitting and crevice corrosion
were common on Types J(A- and 3l6 stainless steel removable parts; this
occurred in stagnant areas (under deposits of solids). Movement of mobile
packing (hollow plastic spheres) caused slight erosion of the 3/8—inch-
diameter grid rods in the TCA tower.
Severe corrosion occurred on some areas of chevron—type mist
eliminators of Type 3l6L stainless steel. Pitting occurred under deposits
of solids; the attack was accelerated in the closed—loop system by con-
centration of chloride and sulfur compounds. Continuous or frequent
washing of the mist eliminator with makeup water reduced corrosion of the
unit.
Stellite alloy No. 6 nozzles have proven to be more durable
than the original stainless steel nozzles for spraying lime slurry in
the venturi spray tower. After about ^200 hours of service, the four
Type 3l6 stainless steel nozzles In the TCA tower that spray limestone
slurry showed little wear of the discharge throat, but the swirl vanes
had several erosion grooves.
Exhaust gas stacks of Type 3l6 stainless steel exposed to gas
reheated to between 235° and 265°F were attacked by general corrosion and
pitting. Cracking occurred in expansion joints downstream from the induced
draft (l.D.) fans. General corrosion, severe cold—working of the Type 31&L
stainless steel during fabrication of the joints, and fatigue caused by
vibration of operating equipment could have contributed to the failures.
Alloy Inconel 625 and a change in design of the expansion joint should be
considered for use at this location.
A small crack occurred in one shroud of the i.D. fan in the
venturi scrubber system. It originated on the periphery of the shroud in
the heat-affected zone of a weld and progressed about k inches. The cause
for the crack was probably a combination of stress corrosion and fatigue
from vibration.
Bondstrand downcomers to the EHT's were in good condition; down-
comers of Type 3l6L stainless steel were pitted.
L-4
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Flakeline 103 linings in the EHT's and clarifier tanks were
generally in good condition. Cracks in the lining near attachments
(such as baffles and weirs) to the walls in the EHT's were covered with
a protective deposit of scale and those in the clarifier tanks had not
changed appreciably since the last inspection.
^ venturi and TGA scrubber systems had been in operation
(intermittently) about 2-2/3 years in May 1975. Inspection of plant equip-
ment at that time revealed that some areas were in good condition while
other areas had deteriorated appreciably during the last 1—1/2 years of
operation. As additional hours of operation accumulate, the resistance of
the facility to further deterioration is Uoportant.
Program and Facilities
Program
The experimental program for removing sulfur dioxide and
particulate from stack gas at the coal—fired Shawnee Power Plant is a
cooperative effort of the EPA, Bechtel Corporation, and TVA. The lime/
limestone — wet—scrubbing program for sulfur dioxide removal is funded
and directed by EPA. The Bechtel Corporation designed the plant facility
and TVA built it. TVA is operating the plant under a test program devel-
oped and directed by Bechtel. Identification and solution of corrosion
and erosion problems associated with construction materials are important
goals in a program for the design and evaluation of limestone — wet—scrubbing
systems. At the request of EPA in 1972, the Process Engineering Branch of
TVA started corrosion tests in the scrubber systems.
Plant Facility
Much of the information about plant equipment, process flow,
and preparation of corrosion test specimens was given in the report on
the first and second series of tests and is repeated here for convenience.
The test facility at Shawnee used in the third series of tests
at the coal-fired power plant consists of two parallel scrubber systems:
(l) a venturi followed by a spray tower, and (2) a TCA. Each of these
systems has the capacity to treat 30,000 acfm of gas containing l800 to
4000 ppm of sulfur dioxide and 2 to 7 grains of particulates per standard
cubic foot. Figures 1 and 2 are schematic views of the venturi and the
TCA scrubbing systems.
L-5
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Power plant stack gas at an average temperature of 320°F (300°—
350°F) flows through a 40—inch duct to each system where slurry sprays
humidity and cools the gas. It then passes through lime/limestone slurry
in a particular type of test scrubber for sulfur dioxide removal. After-
ward, it is passed through a mist eliminator, reheated to "between 235° and
265°F to vaporize any residual mist and discharged through a fan and duct
to the atmosphere. Scrubber effluent is clarified to remove solids which
are discarded and the liquor is then recirculated.
Some features common to both systems are described below. The
40-inch—diameter duct that conveys the flue gas at 320°F from No. 10 boiler
to each scrubber is insulated. The first section of duct is made of 10—
gage carbon steel, ASTM A—283; this joins a section of Type 31&L stainless
steel duct that contains humidification sprays and a soot blower. The
shell of each scrubber tower is constructed of 1/4—inch—thick carbon steel
and it has a lining of I/^—inch—thick neoprene. Downstream from each
sulfur dioxide absorber and mist eliminator unit there is a stainless
steel duct, a refractory—lined reheater fired with fuel oil, an I.D.
fan of Type 3l6L stainless steel, and a stack of Type 3l6 stainless
steel. For liquor handling there is a slurry recirculation tank, a
scrubber effluent tank, and a liquor clarification system. The EHT and
the clarifier tank are made of carbon steel A-283 coated inside with
Flakeline 103 which is a Bisphenol polyester resin—fiberglass coating
manufactured by the Ceilcote Company. The recirculation tank, clarified
water storage tank, and reslurry tank are made of carbon steel lined with
neoprene.
Distinguishing features of the systems are as follows. In the
venturi scrubber system shown in Figure 1, the gas is scrubbed in a
venturi unit made of Type 31&L stainless steel and then passed through
a spray tower (afterscrubber) with a chevron—type separator in the top
for removal of mist. In the TCA scrubber system, shown in Figure 2, gas
is scrubbed in a mobile bed of wetted balls, some of the remaining partic—
ulate is removed in a wash tray, and mist is removed by a separator in the
top of the tower. The wash tray was removed from the TCA scrubber tower
at the end of the third series of tests.
Corrosion Tests
The third series of corrosion tests was conducted during the
period October 2k, 1973, to April 2k, 1975- Specimens were installed at
10 test locations in the venturi system. Tests conducted in the TCA
scrubber system consisted of two phases—A and B. Specimens were tested
at 7 locations during test phase A and at 9 locations in test phe.se B.
L-6
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Phase A included runs 525-2A through 530-2A made during the period
October 24, 1973, to April 17, 1974, for a total of 295^ hours of plant
operation. Fresh spools of test specimens were installed at the beginning
of test phase B (runs 531-2A through 5^5-^A, May 10, 1974, to April 21,
1975) to show the effect that magnesium oxide in the slurry would have on
corrosion of alloys. Additions of MgO were made in an attempt to maintain
the slurry liquor sulfate concentration "below the saturation level. After
three runs (total of 1690 hours), the addition of MgO was discontinued,
"but it was impractical to remove specimens at that time, so they remained
in the system for a total of 6456 hours. The combined exposure period of
phases A and B was 94lO operating hours.
Twenty-seven alloys were tested in the third series, but all
alloys were not exposed at the 26 test locations. Some alloys that showed
poor resistance to attack at some locations in the first and/or second
series of tests were not included at those locations in the third series.
Tables I, II, and III list the alloys tested and identify the filler metal
used in preparing welded specimens. Alloys not included in the first and
second series of tests but added in the current tests were: Cor—Ten A,
Haynes 6fi, Carpenter 7-Mo, Jessop 700, AL 6X, and AL 29-4. The last three
alloys listed were tested only in the exhaust gas stacks at locations below
and above the I.D. fans. Stressed specimens were not included in the current
tests.
Four plastic-4mse materials were tested only in the exhaust gas
stack downstream of the reheater at which locations the gas attained tem-
peratures higher than that recommended by the manufacturers as maximum
service temperatures for their products. Therefore, the four materials
failed and further discussion is not warranted except to state that these
plastic-base materials are being tested in the fourth series of corrosion
tests at other locations in the two scrubber systems.
Preparations of Test Specimens and Equipment
Disk—Type Specimens
Disk—type specimens, 2 inches in diameter, were prepared of 27
metals. A weld was made (according to manufacturer's recommendations)
across the diameter, and after being welded, the metal was cooled slowly
in still air to simulate conditions of constructing or of repairing large
equipment. Whenever it was available, metal stock of 1/8—inch minimum
thickness was used and the surfaces were machined smooth after welding.
Some alloys available only in thinner gages could not be machined, so the
weld beads were smoothed by grinding. A hole, 23/64 inch in diameter,
was drilled in the center of each disk for mounting.
L-7
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Wear-Bar Specimens
Wear-bar test specimens were prepared to monitor erosion-
corrosion of the Type 316 stainless steel sliding guides in the venturi
cone nozzle and to evaluate other alloys for use in this service. These
guides are located immediately below the venturi throat where maximum
gas—slurry velocities are attained. The specimens were of Type 201
stainless steel and of Inconel 625. The bars were lk inches long by
approximately 1/4—inch wide and either 1/8— or 1/4—inch thick, depending
on the stock available from which the bars could be sheared. Slitted
sections of 1—inch Type 3l6L stainless steel pipe were tested as shields
for the guide bars. Also, strips cut from 1/4—inch rubber sheets were
used to protect the guide bars.
Mounting Test Specimens
Spools for mounting the test specimens and also the suspension
equipment for installing them in the plants were constructed mainly of
Type Jl6 stainless steel. Bolts and nuts were annealed to remove stresses
caused by cold-working in threading operations. To prevent loss of fasteners
through vibration of equipment, two nuts were locked by forcing them together.
At some test locations inside plant equipment, brackets were
attached as permanent fixtures by welding, and then the spools of specimens
were bolted to them. In other locations, spools were fastened to existing
pipe by the use of band-type clamps. In a tank, spools were suspended by
means of a 1/8—inch strip or by a 3—inch pipe that was bolted to the rim
at the top of the tank. Sleeves (3/8-in wall by 6 in long) of soft butyl
rubber were placed around the 3—inch specimen support pipe as cushions to
prevent abrasion damage to the Flakeline coating or neoprene lining on a
tank wall. Also, specimens are installed through the wall of a vessel or
duct by means of a 2—inch pipe coupling and a companion plug that supports
the spool of specimens. No specimens were installed inside pipelines or
fittings.
Figures 3 and k show the type of spool assemblies used for
mounting the corrosion test disks. Teflon insulators were used to prevent
contact of dissimilar test materials.
Each wear—bar specimen was mounted by clamping both ends to a
holder which was placed on one of four sliding guides at the venturi cone
nozzle. The test bars were not insulated from the Type 3l6 stainless
steel specimen holders. Specimens of pipe were welded to the holder and
those of sheet rubber were fastened with stainless steel wire.
L-8
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Test Exposures, Conditions, and Procedures
The alloys tested as disk—type specimen mounted on spools are
listed in Tables I, II, and III, The specimens were identified by numbers
corresponding to a test location in series 1000 for the venturi scrubber
system and 2000 for the TCA system as shown in Figures 1 and 2, respectively.
Table IV gives the analysis of each alloy tested either as disks, wear bars,
or erosion-corrosion coupons.
Plant Operation
The two scrubber systems were operated simultaneously during
much of the test period. Information pertinent to the current exposure
periods and to the accumulative operation time since the original starting
date for the two systems follows.
Third series of corrosion tests
Hours accumulative
Test period Runs, inclusive Operating Idle
Venturi 3/15/7^/2^/75 602-lA/62k-lA 7315 2581
TCA 10/2V73-V21/75 525-2A/5^5-2A 9^10 309^
Total operating time of system
since starting date
Date Hours (Days)
Venturi 9/5/72 13,669 (570)
TCA 9/17/72 1^,237 (593)
Plant Process Materials and Deposition
The coal used at Shawnee Power Plant contained an average of
k<$> sulfur (2.0 to 5-5$ S) and 0.2$ chlorides (trace to 0.1$ Cl). The
compositions of inlet and outlet gas at the scrubber systems are tabu-
lated on the following page.
L-9
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Component
S02, %
C02, %
02, %
H20, %
Fly ash, gr/std ft3
Stack
gasa
0.1-0.4
10-lB
5-15
8-15
2-7
Scrubbed
gas
0.04-0.16
11-19
6-16
9-16
0.01-0.04
£L
dust collectors.
Temperature of the inlet stack gas from unit 10 boiler was in the range
of 260° to 330°F and that of the exhaust gas after being reheated was
230° to 265°F.
Properties of liquor in the effluent and clarifier tanks of
the two scrubber systems are given in Tables I, II, and III.
Table V shows analyses of deposits removed from the venturi
and the TCA scrubber systems. The following tabulation shows the variation
in chemical composition of solid deposited in each of the scrubber towers.
TCA tower
Period sampled:
No. of samples:
Component, j> by
CaS04
CaS03
CaC03
Mg (as MgO)
CaCl2
Acid insoluble
Venturi tower
4/30-5/21/7^
31-82
8-39
0.3-9.6
0.03-0.6
Trace-0.2
8-20
Phase A
1/10-1/16/74
4
36-90
1-36
Trace-9.1
0.03-0.2
Trace-5.3
1-28
Phase B
5/21-9/9/74
15
40-82
Trace-21.6
Trace-6.4
0.06-6.9
Trace-1.2
8-58
Exposed Test Specimens
Photographs were made of the spools of disk—type specimens when
they were removed from the plant as shown in Figures 5 and 6. Then the
specimens were cleaned and their corrosion rates and physical conditions
were determined as given in Tables I through III which also contain the
properties of gas and liquor at various test points.
L-10
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Results of the tests of wear-bar specimens are given in the
section "Specimens Tested Below Venturi."
Inspections of Plant Equipment
Equipment in the plant systems was inspected during the period
May 28—31, 1975, for corrosion and erosion damage. More corrosion, wear,
and other types of damage to the equipment were apparent than was noted
during previous inspections, "but this is to be expected as the units age.
The test facility inspection engineer contributed information compiled
from his observations and inspection reports throughout the test periods.
Much of this information has "been included in this report.
Durometer A hardness values of rubber lining on equipment and
on test specimens were measured with a Shore instrument, Type A2, ASTM 22kO.
Unfortunately, hardness of most lined plant equipment was not determined
before plant operation; so data from the rubber vendors were ordinarily
used as reference values. Temperature of the atmosphere varied from 65°
to 82 °F as did the temperature of equipment during the plant inspection
made "by the authors May 28-31, 1975. A decrease in temperature would be
expected to increase rubber hardness. Values for the hardness of neoprene
linings in the plant equipment are summarized in Table VI. The current
hardness values range from lower to higher than those accepted as original
values (determined at 73 °Fj ASTM D224G-68). The neoprene linings showed
good resistance to deterioration in some areas "but repairs Had been made
on the lining in the flooded elbow "between the venturi and the spray tower.
Linings in the towers appeared to be in good condition.
Results of Plant Inspections and Corrosion Tests
In this section, plant inspections are described first for a
unit followed by the results of corrosion tests conducted in the same unit'.
All corrosion rates were calculated on the "basis of weight loss of speci-
mens during the period of plant operation, rather than the overall exposure
period. In the first and the second interim reports, a corrosion rate was
determined on the "basis of weight loss (negligible if very little or no
weight loss was found) regardless of whether localized corrosion 'occurred.
However, in the current report where penetration "by crevice corrosion and/or
pitting is more prominent, low corrosion rates determined by weight loss are
omitted.
Inlet Ducts For Flue Gas
Carbon Steel Ducts: The carbon steel inlet gas ducts were in good
condition. A thin rust-colored scale was noted in some areas. A sample of
the scale taken near a joint was analyzed as follows:
L-ll
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Composition, "jo
Mg
as MgO
0.31
CaS04
33-19
CaS03
1.18
CaCOa
1.72
CaClg
0.24
Acid
insoluble
58.59
Also, small quantities of flyash had "been deposited in the ducts where
the gas flow changed directions "but this caused no apparent problem.
Stainless Steel Ducts; A Type 3l6L stainless steel section
of the duct is located between the carbon steel inlet gas duct and the
scrubber unit of each system. The humidification sprays are located in
the stainless steel section of the duct. The sprays in the duct to the
TCA scrubber system were not used during the current test period; those
in the gas duct to the venturi system were used to cool the gas for pro-
tection of the neoprene lining downstream only when the tangential sprays
to the venturi failed to operate. The stainless steel ducts were in good
condition, and they were clean from impact of flyash. Pits that formed
under deposits of solids when the sprays were used in previous tests,
apparently did not increase in depth during the current tests.
The soot blowers were in good condition and were performing
satisfactorily on an operating schedule of blowing once per day for
cleaning the ducts during the latter part of the corrosion tests. Prior
to this schedule, the soot blower had been operated once per shift. In
the TCA system, the stainless steel duct in the immediate area of the
soot blower showed little or no erosion or corrosion. However, the walls
of the duct near the entrance to the scrubber tower were pitted to depths
of 22 to 60 mils. The pitting occurred slightly downstream of the slurry
cooling sprays (three nozzles) where the first wetting of the flue gas
occurred. Solids were deposited on the duct walls in this area, but the
deposits were removed periodically by the soot blower.
The three spray nozzles (Bete ST32FC1) were of Type 3l6 stain-
less steel. The diffuser of one nozzle was plugged; one was pitted; and the
other was worn but not pitted at the end of the test period. A diffuser of
Type 3l6 stainless steel has a life of about 3000 operating hours. Also,
the stainless steel support rod for the coiled temperature sensory probe
(TE-2007 located a short distance•from the sprays) was pitted severely.
Specimens Tested In Inlet Gas Ducts; The inlet flue gas to the
venturi system entered the stainless steel duct at 275 ° "to 330°F and that
to the TCA system at 260° to 310°F. Since the use of humidification sprays
in the inlet flue gas ducts has been practically abandoned, little corrosion
of the test specimens at locations 1002 and 2002 occurred as compared with
that of earlier tests during which time the humidification sprays were used.
In the duct to the venturi system, the rates were 1 mil per year or less with
shallow pitting of some alloys except for red brass and Cor-Ten B which had
rates of 6 and 9 mils, respectively (Test location 1002; see Fig. 1 and
Table l).
L-12
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In the TCA flue gas inlet duct, the greatest rates were for red
"brass and Cor-Ten B, 8 and 9 mils per year for Cor-Ten B, and 26 and 3
for red brass in test phases A and B, respectively (see Tables II and III).
Corrosion of the other alloys was either negligible or less than 1 mil per
year with moderate localized attack of some specimens in phase A. Note
that pitting did not occur in phase B (see 2002 of Table III); these were
new specimens. Most of the specimens in test phase A (see 2002 of Table II)
had been exposed in previous tests when the humidification sprays were used
part of the time.
Venturi Unit
Stainless Steel Equipment; The Type 3l6L stainless steel bull
nozzle that discharged lime process scrubbing slurry into the throat of
the venturi was a smooth bend elbow of 5—inch Schedule 10 pipe. The nozzle
failed after 265 days of operation. Figure 7 shows that failure occurred
on one side rather than on the periphery of the elbow. Impingement of fly
ash accounted for wear on the external surface and lime slurry on the
inside. The combined attacks gave a penetration rate of 185 mils per year.
Repairs have been required on the Type 3l6L shell of the venturi
section. These consisted mainly of rewelding joints and patching holes
with stainless steel sheet. A complete inspection could not be made of
the venturi internals, but the adjustable plug—and-«2one unit appeared to
be in fair condition as observed through openings in the top and the bottom.
Severe erosion and pitting of the guide vanes immediately below
the throat of the venturi continued as was reported previously. The
original four equally spaced Type JI.6 stainless steel bars that guide the
support for the adjustable plug had eroded to the following depths in inches:
north, 1-1/8; east, 1-1/2; south, 1/4; and west, 1/2. These differences in
wear rates show that channeling of the flue-gas lime—slurry .mixture occurs in
this section; the cause for the channeling is not obvious. Some protection
for the bars was provided by the installation of test bars, sacrificial wear
bars, and shields of rubber. This was done to evaluate materials of con-
struction as well as to prolong the life of the original bars. Test bars
of Type 201 stainless steel and of Inconel 625 failed in less than 90 days
with penetration rates > 0.5 inch per year. Sections of a 1-inch, Type Jl6
stainless steel pipe were fitted to shield the guide bars; these failed
with wear rates of 1.5 to 2.5 inches per year. In previous tests, Haynes 6B
alloy exposed on the north guide bar showed the greatest resistance to
wear of any alloy tested to date—l62 mils per year (see Second Interim
Report of Corrosion Studies—May 197*0-
The shield of I/k—inch-thick rubber sheet failed after a very
short exposure period on two of the four guide bars.
The stainless steel support shaft for the adjustable plug in the
venturi was pitted to a depth of 67 mils above the guide vanes. The shroud
for the support shaft was pitted and the flanges at each end of the shroud
were eroded badly.
L-13
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General corrosion and pitting to a depth of 20 to ?0 mils
deep was observed on the stainless steel shield of the access door
below the venturi (test location 1011). The attack was greatest on
the periphery of the shield.
Flooded Elbow; Minor mechanical damage had occurred to
the neoprene lining in the area of the flooded elbow. Also, blisters
about 5/l6 inch in diameter were noted on the wall above the pool of
water. The surface of a blister could be broken easily leaving a
smooth hemispherical pit. The blistering might have resulted from
overheating during momentary loss of spray to the venturi and before
the humidification sprays upstream were activated to cool the inlet
flue gas.
The neoprene—lined duct between the venturi and the spray
tower had required repair since completion of the second series of
corrosion tests. During the outage in May, a 7— by l6—inch section
of the liner was replaced overhead in the duct because of sagging.
New rubber (not identified) with a Durometer A hardness of 68° at 73 °F
was used for the patch. Small areas of the lining that failed earlier
during the current test period had been repaired by application of
Plyobond, and epoxy-i>ase cement. The Plyobond hardens upon curing,
and it has shown good resistance to operating conditions encountered
in the duct. The remainder of the neoprene lining originally installed
in the duct appears to be in good condition; it had a hardness of 56
determined at 73°F.
The stainless steel thermocouple probe in the flooded elbow
near the entrance to the spray tower was pitted to depths as great as
65 mils.
Specimens Tested Below Venturi; The specimens were installed
directly below the venturi as shown at location 1011 of Figure 1.
Exposure conditions are more severe at this test location than for all
others in the two scrubber systems. The stack gas containing flyash,
carbon dioxide, oxygen, and sulfur dioxide at 275° to 330°F is humidi-
fied by lime process scrubbing slurry as they mix and pass through the
venturi at a high velocity. Erosion and corrosion are both important
factors in the test at location 1011. Due to the high erosion-corrosion
rate, the spool containing the test specimens had partially failed after
4179 hours of operation. Two specimens, one each of Cor—Ten B and Type
kk6 stainless steel, were destroyed.
The first spool of specimens was replaced by another for
the remainder of the third series of corrosion tests. Makeup of the
second spool was not identical to the first; however, both contained
several common specimens. After the second spool of specimens was
installed, the unit was operated 3136 hours, this completed the third
series of tests. In reporting the results for the two spools that were
exposed at test location 1011, the higher rate is given in the case of
common specimens (see Table l). Penetration rates, on the basis of
weight loss, ranged from 2 mils per year for Haynes 6B alloy to > 872 for
Cor—Ten B. The alloys that had penetration rates of < 20 mils per year listed
L-14
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in the order of increasing attack were: Haynes 6B, Hastelloy C-276,
Inconel 625, Nitronic 50, Incoloy 825, E-Brite 26-1, and Type 31?
stainless steel. The rate for Type 316 was 21 mils per year. Five
alloys were pitted; the maximum depth of pits ranged from 5 mils for
Nitronic 50 to ko mils for Incoloy 800. Each specimen that was pitted
also had crevice corrosion except for that of alloy Nitronic 50.
The specimens exposed at location 1011 remained clean through-
out the test. Severe erosion of the Teflon insulators and of the spacer
rods was common to both spools.
Scrubber Towers
Neoprene Lining, Hardware, and Spheres; The neoprene linings
on the walls of the venturi and the TCA scrubber towers appeared to be
in good condition; no changes of importance had occurred since the inspec-
tion prior to the second interim report. Impingement of slurry from sprays
had caused minute erosion in a few small areas. Also, slight mechanical
damage, possibly due to impact when changing the internal components, had
occurred in a few areas mainly in or near manways. The original Durometer
A hardness (taken from the vendor's data) of the neoprene liners was 60 to
65. The current range of hardness values of the lining in the venturi end
the TCA towers were k-2 to 60 and kk to 56, respectively. All measurements
were not made at the same temperature (range was 65°—7^°F) because of
weather changes. The hardness of the neoprene is expected to increase
with a decrease in temperature.
In general, the various pieces of stainless steel hardware, such
as manway deflector plates, header pipes for water and slurry, temperature
probes, overflow weirs, sampling equipment and suspension brackets were
pitted in both systems. Spot checks for alloy identification were made on
some of the hardware in the venturi system. This information revealed that
equipment of Type 304 stainless steel was less resistant to pitting than
that of Type "*>l6. The pits were more numerous and about twice as deep on
the Type 304 components. Figure 8 shows the comparative attack of Type 304
and Type 316 stainless steel components joined by weldi-ng in a common slurry
header in the venturi spray tower. Also, Figure 9 shows pitting at the
bottom of a Type 316 weir box outlet in the TCA tower.
Carbon steel clamps and brackets that fasten and support headers
for the slurry sprays were broken probably due to stress-corrosion cracking
(see Fig. 10).
Many of the spray nozzles in the venturi system were in excellent
condition, a few were pitted, and others showed moderate wear. The slurry
contained about 8% solids. Accelerated attack of threaded components caused
loosening of some nozzles. The life of the components could be increased
greatly by fully annealing after threading to remove the effect of cold-
working. Bete nozzles of Stellite No. 6 alloy have proven to be more durable
L-15
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than the original stainless steel nozzles for spraying lime slurry in the
venturi spray tower. In the TCA tower, four Type 3l6 stainless steel
nozzles (Spraco No. 1969 full-cone free—flowing) were used to spray lime-
stone slurry that contained about 15fo solids. After about 4200 hours of
service, the discharge throat (about 2.9—in dia.) of the nozzles showed
little if any wear, but the swirl vanes had several erosion grooves.
The original stainless steel wire grids which showed pitting
and crevice corrosion in the TCA tower were replaced October 24, 1973, with
3/8-inch-diameter rods of Type 3l6 stainless steel. By May 1975, the rod
grids had been in service about 9100 operating hours. Slight pitting was
noted on some rods and crevice corrosion occurred where the rubber grommets
on the ends made contact with the rods. Movement of TCA spheres wore a
flat surface in two planes on the top half of the grid rods. A decrease
in diameter of 8 to 15 mils was measured on the flat surfaces except on
the uppermost (fourth) grid which did not support spheres.
Two types of spheres were used during the corrosion test
period. High-density polyethylene spheres (HDPE, 6 gram) were used on
the bottom grid, and many of them failed by developing holes during I04l
hours of service. After the walls wore thin, these spheres often formed
single or double dimples. The beds on the second and third grids were of
thermoplastic rubber (TPR, 5-gram) spheres. Some of the TPR spheres were
used 3784 hours without failure, but others split -in half at the mold line
after short periods of service. The dimpled and the half spheres often
passed between the grid bars to a lower level. Strainers were installed
in the slurry lines to prevent the failed spheres from plugging spray
nozzles and/or damaging other equipment in the system.
The original mist eliminators in both the venturi and the TCA
scrubber systems were constructed of Type 31&L stainless steel; the vanes
were of l6-gage sheet (about 0.062—in thick).
The mist eliminator in the venturi system was a horizontal,
three—vane, open-pass unit that remained in service for 8700 operating
hours. It was corroded badly. The vanes were perforated in some areas
at penetration rates > 62 mils per year. Subsequently, a four—vane
closed-pass, conical—type mist eliminator with a 30-degree. slope was
installed in the venturi tower. It was used only 1219 hours during which
time the vanes were pitted to depths up to 45 mils. Plugging of the
bottom with solids was the major problem with the conical—type unit.
A new mist eliminator of the same design as the first, had
been in service in the venturi scrubber tower 823 hours at the time of
the present outage. No damage of the unit due to corrosion was noted.
A system of spraying the unit by automatically controlled cycles appar-
ently has improved the efficiency of the mist eliminator.
The original mist eliminator in the TCA system was in service
from the startup in August 1972 until the outage in April 1975. The
L-16
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estimated total hours of service for this unit is 1^,000. It is a 6-pass,
closed-path, chevron—type horizontal unit. Some vanes, were in excellent
condition while others had numerous pits and perforations. Where failures
occurred, the rates of penetration were > 34 mils per year.
During the outage, a two—stage, fiberglass—reinforced polyester
(FRP) mist eliminator was installed in the TCA tower. The vanes were about
O.o6o—inch thick end the spacer plates were 0.120-inch thick. Only the
lower stage was provided with oversprays and underspreys.
Specimens Tested in Towers; The locations of the test specimens
in the scrubber towers are shown in Figures 1 and 2. The test conditions
and corrosion rates are given in Tebles I, II, and III.
Figures k and 5 show the spools of specimens as they appeared
when the tests were completed. The test medium at each location in the
two towers and the approximate amount of solids deposited on the spool at
the end of the test are given below.
Test
System location No. Test medium Amount of solids on spool
Venturi 1006 Gas and liquor Rone (clean)
1005 Gas and liquor Partially covered
10C4 Gas and droplets Covered
TCA (phase A) 2006 Gas and liquor None (clean)
2005 Gas and droplets Partially covered
20C& Gas and mist Lightly covered
TCA (phase B) 2006 Gas and liquor None (clean)
2005 Gas and droplets Partially covered
2004 Gas end mist None (clean)
In the venturi tower, the specimens tested at location 1006 (the
lowest test location) had the lowest corrosion rates—less than 1 to 55 mils
per year; and those at the highest elevation (location 100*0 had the widest
range of rates—negligible to > 82 mils per year. Carpenter 20Cb—3, Hastelloy
C-2T6, Haynes 6B, Inconel 625, and Type 3l6L had rates of < 1 mil per year
on the basis of weight loss at the three test locations. Pitting and/or
crevice corrosion occurred on 20 of the 48 specimens tested in the venturi
tower.
In the TCA tower, a spool of specimens was exposed at each of
three locations, 2006, 2005, and 2004 identified in the order of the lowest
to the highest test locations; their positions in the tower are shown in
Figure 2. As stated previously, the third series of tests in the TCA syston
consisted of two phases, A and B.
L-17
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The results for tests in phase A are given in Table II, and
for phase B in Table III. With one exception which will "be discussed
later, there was little difference in corrosion rates of an alloy tested
at a given location in both phase A and phase B. Usually the greatest
general corrosion, on the basis of weight loss, occurred at the test
location of highest elevation (20C4). However, this was not necessarily
true in cases of localized corrosion.
The exception mentioned above was at test location 2006 in
phase B where the specimens were damaged due to abrasion of the periphery
by movement of the plastic spheres. Corrosion rates could not be deter-
mined for these specimerBbut information on crevice corrosion and pitting
is given in Table III. Guard rods were attached on the spool to prevent
contact of the spheres with the specimens in the test at location 2006 of
phase A, but the guard rods were inadvertently left off the spool in
phase B.
To generalize on both phases of the tests in the TCA tower,
the corrosion rates ranged from negligible for severe! alloys to > 57
mils per year for Cor—Ten B (specimen was consumed). The alloys with
corrosion rates of 1 mil per year or less were: Carpenter 20Cb—3,
Crucible 26-1, Hastelloy C-2j6, Haynes 6B, Inconel 625, Type 3l6L, and
Type 317 stainless steel. Some form of localized attack occurred on 57$
of the specimens tested in the tower. These specimens are identified in
Tables II and III.
Exhaust Gas System
Equipment for Reheating Scrubbed Gases; The inside area of
the Type 316L stainless steel stack between the venturi afterscrubber and
the reheater was pitted. About 18 inches above the uppermost neoprene
lining (or about 4 feet below the old inline reheater), pitting had
occurred to depths up to 37 mils. In the TCA system, the area between
the top of the scrubber tower and the reheater was not accessible for
inspection because the new plastic mist eliminator had been installed.
During operation, the scrubbed flue gases were reheated to 235 °
to ^65°F by oil—fired reheaters. The original reheaters were the inline-
type manufactured by Hauck. Before the third series of corrosion tests
was begun, an external reheater manufactured by Bloom Engineering Company
was installed in the venturi scrubbing system. Hot combustion gases from
the Bloom heater discharge into the cavity of the old Hauck unit for mixing
with and reheating of the scrubbed gas. The monolithic refractory lining
in the old inline unit was in good condition. However, the area of the
lining onto which the hot gases from the new Bloom unit impinged at a riglit
angle, had been repaired once after the Bloom unit was put in operation.
Also, moderate chemical attack had occurred due to acid in the condensate
that drained from the Type 3l6 stainless steel stack onto the lining at the
top of the unit.
L-18
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In the Bloom unit, the refractory lining and the insulating
materials have a combined thickness of 7 inches in the combustion chamber
and 14 inches in the discharge zone. The innermost monolithic lining was
discolored yellow-^brown and was cracked to depths of up to about 2 inches.
Although the lining was in good working condition, the discolored, cracked
material was removed "by chipping and was replaced with Kruzite, also a
monolithic refractory produced "by A. P. Green Company who recommends it
for service temperatures to 3200°F.
Operation of the Bloom reheater was reported to have been much
"better than that of the inline reheater previously used in the venturi
system. Frequent flameouts had made operation difficult with the inline
Hauck reheater. However, in the current inspection, there were more
deposits of flyash, oil, etc., in the venturi stack than in the TCA stack.
The Hauck inline reheater was used in the TCA system throughout
the third series of corrosion tests. During the May 1975 outage, a Bloom
external reheater identical to the one in the venturi scrubber system was
installed in the TCA system. The 3/l6—inch—thick carbon steel shell of
the old Hauck unit was stripped to permit relining. In general, the shell
was in good condition. Only moderate scaling had occurred inside except
around the burners where the insulation had failed.
During previous tests, the frequency of flameouts in the original
inline oil—fired reheaters was reduced by the use of burner nozzles with
better atomizing characteristics and by the installation of a sleeve 40
inches in diameter by 4 feet tall that improved combustion of the oil before
the scrubbed flue gas mixed with the hot combustion gases. Prior to this
installation, the scrubbed gas quenched the flames. The first sleeve
installed was of 10-gage Type 304 stainless steel because a heat—resistant
alloy was not immediately available; it had a service life of 3135 hours.
It was replaced by a 1/4—inch—thick sleeve of Type 310 stainless steel. Even
though the sleeve warped during 7930 hours of operation, its use was con-
tinued considerably longer. During the third series of corrosion tests in
the TCA system, frequent cleaning of the burner nozzles and ending steam
sparging for cleaning the mist eliminator further reduced the frequency of
reheater flameouts. Consequently, the deposition of soot in the stack and
fan was reduced; also, as a result of fewer flameouts, less oil was deposited
on the wall of the stack. In fact, no oil was found in the stack above the
reheater of the TCA system. This indicates that good combustion was obtained
in the Hauck reheater during the latter part of the corrosion test period.
There was a deposit of dry solid ranging from 1/16- to 1-inch thick on the
inside walls of the stack.
Pitting and general corrosion occurred on the inside wall of the
Type 316 stainless steel stacks. Because the Bloom reheater for the TCA
system was being installed and tested, only a limited inspection could be
made of areas above the reheater. However, in the stack of the venturi
L-19
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system, pitting to depths of as much as 78 mils had occurred a~bout 6
inches a"bove the refractory of the old inline reheater. About 2 feet
further up the stack pits were 30 mils deep. Apparently, the depth of
pits decreases as the elevation of the cylindrical sections of the
stacks increases.
Transition sections of duct (cylindrical to rectangular)
connect the inlet and outlet of the I.D. fan to the stacks. The
inlet section ("below the fan) divides the gas stream before it enters
the fan through two parallel sets of dampers. Green liquid dripping
from the divider "below the dampers indicates that the Type Jl6 stainless
steel had "been corroded at that elevation or above. Pits as deep as 13
mils were measured on the plates in this area.
I.D. Fans: During the corrosion test period, a crack devel-
oped on the east shroud of the Type 3l6L stainless steel I.D. fan in the
venturi system. The crack originated on the periphery of the shroud in
the heat—affected zone of a weld that joined a blade to the shroud. It
progressed parallel with the weld 2—1/2 inches, then deviated gradually
from the weld for a total length of about k inches as shown in Figure 11.
The crack was repaired by grinding out and welding from both sides. The
filler metal was Type 3^-7 and/or Type 31^L stainless steel.
The average thickness of the fan blades was 0.270 inch;
however, the values ranged from 0.2^7 to 0.282 inch. Apparently, the
blades in the I.D. fan of the venturi system were cut from plates of
different thickness. The current measurements were in fair agreement with
those made when the first series of tests was completed. Four of these
blades were bent slightly on the periphery; one blade had two bends. Some
of these bends have occurred since the first tests were completed. Reportedly,
a thermocouple weld fell from the stack above while the fan was in operation.
The following observations were noted on, the I.D. fan for the
TCA system:
• A small bend on each of three blades
• A small crack on the periphery of the west shroud near
a counterweight attached by welding to balance the fan
• A small cut on the periphery of one blade
• Pits on the periphery of a shroud near one blade
In the future, consideration should be given to welding counter-
weights on the spider (center rib of blade) rather than on the shroud to
balance the I.D. fan. The thickness of blades in the TCA fan ranged from
0.260 to 0.275 (avg. 0.269) inch.
The liners in the fans are spot welded only. Continuous welds
would reduce the extent of vibration of the liners and thereby decrease
the possibility of failure due to fatigue.
L-20
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Expansion Joints; Repairs have been required on the expansion
joints above the I.D. fan in both the venturi and TCA scrubber systems.
Corrosion, as shown in Figure 12, is believed to be the greatest factor
in damage to these joints; however, severe cold-working of the Type Jl6L
stainless steel during fabrication and fatigue caused by vibration from
operating equipment could have contributed to the failures. Small holes
were plugged by spot welding. Cracks were sealed by welding a strip of
metal over them.
The expansion joints are rectangular in shape with only a few
corrugations to absorb changes that accompany expansion and contraction.
If the design were cylindrical with a longer bellows section to absorb
the changes in dimension, a longer life could be expected. Also, fully
annealing the expansion joint after forming would increase its resistance
to corrosion. The use of a more corrosion—resistant alloy, such as
Inconel 625, in this service should be considered.
Specimens Tested in Exhaust Stacks; The Type Jl6 stainless steel
exhaust gas stacks for both scrubber systems were insulated externally
during the summer of 197^ so the minimum heat required to prevent forma-
tion of condensate in the stacks could be determined. New test locations
1014 and 2COA were provided in the stacks below the I.D. fans, and loca-
tions 1015 and 2015 above the fans in the venturi and TCA systems,
respectively (Figs. 1 and 2). Corrosion test specimens were installed
in the new locations in October 197^- for exposure during the remainder
of the third series of tests. The corrosion tests at locations 1007 and
2007 had been in progress several months before the stacks were insulated;
these tests were discontinued when the third series was completed. The
test conditions at locations 10l4 and 20l4 (only a few feet downstream) are
very similar to those at locations 1007 and 2007, respectively. The tempera-
ture of gases in these tests was usually 235° to 265°F.
Tables I, II, and III give pertinent information about exposure
conditions and results of the tests. When the specimens were removed for
evaluation, more solids were on the specimens in the venturi stack than on
those in the TCA stack, probably because of the presence of a small amount
of fuel oil in the venturi stack.
The specimens tested at location 1007 in the venturi stack were
exposed during 7315 hours of operation. General corrosion rates ranged
froa 1 mil per year for Cupro-Nickel 70-30 and Hastelloy C-276 to 11 mils
for Cor-Ten B (Table l). These and four other alloys that had intermediate
rates did not show evidence of localized attack. However, seven alloys
experienced crevice corrosion and/or pitting which was more severe than
the low rates determined by weight loss. The depth of pits ranged from
minute to 28 mils.
L-21
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Tests at location 2007 in the TCA stack during phases A and B
•were for exposure periods of 2954 and 6^56 operating hours, respectively.
Corrosion was negligible on three specimens in phase A and on seven in
phase B (Tables II and III). In the two test phases combined, 11 specimens
were corroded at rates of < 1 to 3 mils per year and 11 others were attacked
"by crevice corrosion and/or pitting. For Type 3l6L stainless steel, attack
of one specimen was negligible, "but crevice corrosion and shallow pitting
occurred on the other.
After the stacks were insulated, the test period for specimens
at locations 10l4 and 1015 in the venturi system was klfk operating hours
and for those at 2014 and 2015 in the TCA system, 3892 hours (the latter
part of phase B). In the venturi stack, corrosion rates at location 1014
(below fan) ranged from 1 to 6 mils per year and at 1015 (above fan), the
rates were 1 to 2 mils (Table I) with no evidence of localized attack.
Cor—Ten A had rates of 6 and 2 mils per year and mild steel had rates of
5 and 2 mils per year in the tests below and above the fan, respectively.
Corrosion was even less on specimens at the new test locations
in the TCA stack; the rates ranged from negligible for most alloys to 1 mil
per year for Cor—Ten A and mild steel. Crevice corrosion occurred on
stainless steel Type 201, 2l6, and 3l6L at test location 2015 (above fan)
but not at location 2014.
In general, the data indicate a slight decrease in corrosion of
specimens in the stacks after the insulation was applied.
U—shaped stressed, specimens of six alloys were installed
recently in the inlet gas cavity of each fan in an effort to identify
the cause of cracking of the I.D. fan and expansion joints. If static
stresses are detrimental in this environment, the U-shaped stressed
specimens could reveal this. However, if cyclic stresses caused by vibra-
tion are the main cause, the U—shaped specimens now being tested will not
reveal this. Earlier in the test program, stressed specimens had been
exposed at several locations, but none were installed in the housing of
the I.D. fans, lone of the stressed specimens failed in the earlier
tests, but those tests were for comparatively short periods.
Tanks
Effluent Hold Tanks; An EHT 20 feet in diameter and 21 feet
tall is located directly under each scrubber tower: D—101 for the
venturi and D-201 for the TCA. The shells are made of A-283 carbon steel
coated inside (80 mils minimum thickness) with Flakeline 103 manufactured
by the Ceilcote Company. This coating is a Bisphenol—A type of polyester
resin filled with flake glass (25-35$).
In general, the Flakeline 103 coating on the baffles and tank
walls appeared to be in good condition in both EHT's. The small cracks
with iron rust bleeding through at the junction of baffles with the walls
L-22
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which were noted in previous inspections were not visible currently due
to a deposit of scale which apparently provides protection.
In the venturi EHT, the Flakeline 103 coating was removed
from a small area of the wall (north side) near the tank "bottom for
installation of a stilling well for a level—sensing element. Near the
tank top, a l6-inch-diameter pipe had been installed from the scrubber
downcomer through the walls of the tank on the east and south sides.
The bare steel in the areas affected at these installations was coated
with blue epoxy paint. There is concern that undercutting of the frac-
tured Flakeline coating might cause "flaking off" of the coating. An
application of new Flakeline 103 in the affected area would demonstrate
the repairability of the old coating. To date, no onsite repairs have
been made using the Flakeline materials. Most repairs have been made
with epoxy paint.
The 8—inch—diameter pipe of Bondstrand (FRP, resin not
identified) supplied by Ameron, Brea, California, in each EHT was in
good condition. The pipe in D-101 for the venturi system has never
been used for conveying slurry but has served as a guide tube for
measuring liquid level. The Type 31&L stainless steel downcomers
(4—ft dia.) were pitted under the tightly adhering, hard scale. A
4—inch carbon steel pipe that extends from the top to near the bottom
on the west side of D-201 (TCA system) for returning wash tray liquor
is corroded severely; it had been in this service about 1—1/2 years.
The neoprene—covered agitator blades in D-201 are in good
condition; they show moderate wear on the leading edges and some damage
due to impact with foreign materials. During the test period, the
agitator had been lowered to within 2 feet of the tank bottom. The
agitator blades in D—101 of the venturi system have required appreciable
repairs. The stabilizer on each of two blades broke; these were repaired
by welding the broken pieces in place and then coating the metal core with
Epoxylite No. 203- Some erosion of the hard coating has occurred, but it
appears to resist abrasion fairly well. Another area of one repaired
blade had a large blister on the covering. The neoprene covering on the
third blade of the agitator had failed at the bottom corner on the end.
This damage appeared to be recent (corrosion of steel core was not apparent)
and was probably due to impact by a hard object. The hardness of the neo—
prene coverings on the agitators is given in Table VI; these values have
not changed appreciably from the original values.
Specimens Tested in EHT's; A spool of corrosion test specimens
was mounted in the EEC of the venturi and the TCA systems about 7 feet and
2 feet above the tank bottoms, respectively. Figures 1 and 2 show the test
location, and Figures 4 and 5 are photographs of the spools identified by
test location numbers. Tables I, II, and III give the test results. The
corrosion rate in the venturi EHT which handled lime slurry that usually con-
tained about 8% (range 7 to l6$) solids with pH 4.5 to 6.3 was negligible for
eight alloys, about 1 mil per year for Cor-Ten A and Cuprc—Nickel 70-30, and
L-23
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localized attack occurred on five specimens. Crevices were not measured,
tut pits penetrated in depth from minute to 15 mils during the test periods
of 7315 operating hours. The alloys that had negligible corrosion rates
were: Carpenter 20Cb-3, Hastelloy C-276, Haynes 6B, Incoloy 825, Incoloy
625, Mtronic 50, and Type 3l6L stainless steel. The list is practically
the same for materials that had negligible corrosion rates in the TCA EHT,
although the spools were not identical.
For the specimens exposed in the TCA EHT in test phase A,
corrosion was negligible for six alloys; < 1 mil per year for red "brass,
Cupro-flickel 70-30, and Monel k-00; 2 mils for Cor-Ten B; and localized
attack (crevice and/or pitting) occurred on seven specimens. Five of
these had only minute pits, but some pits on Type 201 stainless steel were
8 mils deep. In test phase B, 12 specimens had negligible corrosion rates,
four had rates of about 1 mil per year, only one (USS 18—18-2) showed crevice
corrosion, and no pitting occurred.
The reason for less localized corrosion in test phase B than in
phase A is not obvious. The exposure period (operating time) for test phase B
was more than twice that for phase A. Long exposure periods are desired for
identifying the susceptibility of metals to pitting. Therefore, it appears
that the chemical conditions and/or other factors affecting the limestone
slurry in the TCA EHT during test phase A (runs 525—2A through 530-2A) were
different from those during test phase B (runs 551—2A through 5^5-2A).
Magnesium oxide was added to the slurry during 26% of the exposure period
for test phase B.
Limestone slurry was used in both test phases A and B. The
temperature and pH of the slurries in the two tanks were comparable. The
ionic composition as tabulated below shows that the Cl~ and Ca"1^ ionic con-
centrations were highest in the venturi tank, and the S03=, C0s~, S04=, and
Mg4"*" ionic concentrations were highest in the TCA tank during phase B which
was the least corrosive.
Ionic Composition of Effluent in System, ppm
TCA
Ion Venturi Phase A Phase B
so3~ 35-1050 30-290 70-5000
C03~ 5-200 40-380 30-1000
so4~ 300-1600 200-2700 300-39,000
Ca** 100-W-OO 1100-2600 100-2000
Mg""" 50-6400 200-500 260-12,000
Na+ 25-90 30-120 35-60
£*"__ 50-330 50-520 4o-ii5
ci 4oo-84oo 1500-5000 800-4500
L-24
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A comparison of the results of the three series of tests
shows that corrosion rates were lower during the third series of tests
than in the first or second. However, many of the less promising alloys
had been eliminated during tihe first two series of tests.
In October 1973 a hole was discovered in the Flakeline 103
coating on the bottom of the TCA EHT and was assumed to have resulted
from erosion by the limestone slurry. In order to define the severity of
erosion on the tank bottom, under operating conditions, specimens of nine
alloys were tested in the area that had been damaged. The specimens were
approximately 1/8-inch thick by 2 inches wide by 6 inches long and were
positioned in a circle on the tank bottom directly under and about 2 feet
below the agitator. The specimens were mounted at a 15-degree incline to
amplify the effect of erosion on a carbon steel plate placed under the
agitator to protect the Flakeline floor from possible excessive erosion
resulting from lowering the agitator. The bottom end of the specimen was
insulated from the horizontal plate by sheet rubber and the upper end from
the steel bracket and bolt with Teflon tubing and washers. A list of the
alloys tested and the results of the tests after an exposure period of 392
operating days and 129 idle days are given in the following tabulation.
Alloys
Haynes 6B
Incoloy 800
Incoloy 825
Inconel 600
Inconel 601
Inconel 702
Mild steel
Type 3l6L stainless steel
USS 100
Erosion-corrosion
rate, mils/yra
Negligible
Negligible
Negligible
Negligible
Negligible
Negligible
Negligible
Negligible
Negligible
Other types of attack
None
Negligible
None
Minor crevice corrosion
P5, minor crevice corrosion
Negligible
P6, severe crevice corrosion
(50 mils)
None
P5, moderate crevice corrosion
Negligible indicates corrosion rates of < 0.05 niil per year; the specimens
had tightly adhering deposited coating that protected them from erosion.
"P" preceding a number indicates pitting during the exposure period to the
depth in mils indicated by the number.
Although a tightly adhering, deposited coating on the specimens
prevented erosion, four alloys did suffer localized attack. Corrosion was
negligible for: Haynes 6B; Inconel 702, Incoloy 800, Incoloy 825, and Type
3l6 stainless steel. Minor crevice corrosion occurred on Inconel alloys 600
and 601, USS 100 showed moderate crevice corrosion and pits 5 mils deep, and
L-25
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mild steel had pits 6 mils deep and a crevice 50 mils deep. Apparently,
the damage to the Flakeline coating on the tank "bottom was not due to
erosion so the tests were discontinued.
Clarifier Tanks; The clarifier tanks for both scnib"ber
systems are 15 feet tall. The diameter of tank D-102 for the venturi
system is 20 feet and that for D-202 for the TCA system is 30 feet. Each
tank has a cone—shaped "bottom that is positioned 3 to 5 feet above the
foundation elevation. The tanks are constructed of A-283 carbon steel
coated inside with Flakeline 103 and the mechanical equipment inside the
clarifiers is made of Type 3l6L stainless steel.
In general, the Flakeline 103 coating in the tanks was in
good condition. Rust bleeding through hairline cracks in the coating at
the junction of the effluent launder with tank walls had changed little
since the second series of tests. This was true also at the junction of
the walls with the bottom in D—102, but the corresponding area in B-202
had been sealed with an epoxy coating. The scratches through the top coat
on the walls of D-202 inflicted by the stainless steel plows (noticed Sept.
1973) have resisted corrosion equally as well as the undisturbed areas of
Flakeline 103.
The paint underneath the flange at the top of both tanks
failed in the area immediately above the overflow box for clarified liquor.
Also, outside and about 2 feet below the top of tank D-202, the paint had
blistered in a horizontal band. Apparently, this is a welded joint that
was painted without sandblasting.
Failure in April 19?4 (Run 530-2A) of the main shaft that
drives the plows in D-202 apparently occurred during a startup following
an idle period that allowed heavy deposits of solids to overload the equip-
ment. The shaft was replaced with the one from clarifier tank D—302 of the
marble—bed system which was not in use. The stainless steel mechanical
equipment in both clarifier units appeared to be in good condition.
Specimens Tested in Clarifier Tanks; A spool of corrosion test
specimens was suspended in the slurry 5 feet below the launder in each
clarifier tank, D—102 and D-202. These tanks are not shown in Figures 1
and 2. Items 1013 and 2013 in Figures k and 5 are photographs of specimens
after exposure. Tables I through III give the corrosion data.
The corrosion rates were negligible or < 1 mil per year for
most of the alloys tested in the clarifier tanks. The highest rate was
3 mils per year for Cor—Ten B in the TCA system during test phase A. The
following alloys were attacked by crevice corrosion and/or pitting:
Cor-Ten B, Hastelloy B, Type 201, and USS 18-18-2. Alloy USS 18-18-2 had
the most severe localized attack; each specimen had crevice attack and pits
were 8 to 23 mils deep. Pitting and crevice corrosion had progressed less
L-26
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on the specimens in the TCA clarifier tank during phase A than on those
during phase B or on those in the venturi clarifier tank. This was
expected because the operating period was much shorter for phase A
(295lf vs. 6^58 and 7315 hours, respectively).
Clarified Process Water Storage Tanks; The clarified process
water storage tank D-103 for the venturi system is 10 feet in diameter
and 9 feet tall. The tank D-203 for the TCA system is 13 feet in diameter
and 9 feet tall. Each tank has four verticle "baffles welded to a shell of
carbon steel and lined with 1/4 inch of neoprene. Each tank has a three-
blade agitator with diameters of 14 inches in D-103 and about k2 inches in
D-203. The agitators and shafts were covered with neoprene.
The neoprene lining in the D—103 tank was in good condition,
but the lining in the D-203 tank contained several hard blisters in the
area that was immersed when in operation. The blisters were about 3/4 inch
in diameter and protruded about 3/l6 inch. The agitator blades showed some
evidence of wear on the leading edges, but no failures. The carbon steel
pipe that discharges clarified water into D-203 was rusty.
The hardness of the neoprene tank linings and agitator covers
is given in Table VI. The hardness values for the two tank linings vary
less than those for the covers on the agitators, but these variations are
moderate.
Reslurry Tank; Tank D-401 is used for reslurrying waste
solids removed by the clarifier of both the venturi and the TCA systems.
It is identical in size and construction to tank D—103 already described.
The linings and agitator equipment appeared to be in good condition as
viewed from the top of the tank. The hardness of the lining above the
liquid level (see Table Vl) was comparable with the hardness of the
clarified process water storage tanks above the maximum liquid level.
Lime Slurry Preparation—Feed Tank; The lime slurry feed
tank D—521 is constructed of uncoated carbon steel. Also, the two
impellers (about 3 feet apart) and the shaft are of carbon steel. The
tank walls and agitator components were rusty, but showed no appreciable
deterioration.
Limestone Slurry Preparation—Feed Tank; The limestone slurry
feed tank D-$08 and tne 8 git e.t or "with dual impellers (one about 2 inches
above the bottom and the other 2 feet above the bottom) were constructed
of Type 3C4 stainless steel. The tank and the components were in good
condition.
L-27
-------
Pumps, Heoprene— Lined Centrifugal
Liners and Covered Impeller; Neoprene— lined Centriseal pumps
were used in both scrubber systems during the current test period. At
the time of the inspection (May 29-31, 1975), all the pumps had been
reassembled in preparation for subsequent operation; however, a casing
containing a worn neoprene lining that had been replaced in pump G— 201
was available for inspection. This lining and impeller were original
equipment in G— 201 used only in the TCA system during approximately 14,000
operating hours (Aug. 1972 to May 197&). Both the suction and the seal
side liners were worn badly in the area 6 to 10 inches from the center,
and the neoprene covering on the impeller was pitted and damaged from
impact with circulated debris. Durometer hardness measurements of the
impeller and liners (see Table VI) show that the hardness had not changed
appreciably.
Packing and Sleeves; The information available on maintenance
of the pumps shows that the most frequent problem is failure of packing.
Pumps G— 105, G-205, and G— 206 each were repacked five times during
October of 1971*-, and pumps G-105 and G-205 were repacked six times during
the previous month. The shaft sleeve is of Type 304 stainless steel, the
stuffing box and packing gland are of cast iron, and the packing is SEPCO
MIr402 and/or 502 that consists of graphite impregnated asbestos fibers
braided together by the braid-over-*raid method then calendered to a
square section. The reports indicate that the use of hardened sleeves
increases the life of the packing. The Strum Company of West Virginia
supplied Type 304 hard— faced sleeves. These were used only on small pumps.
The Second Interim Report of Corrosion Studies, .May 197^, listed
the pumps that had been converted from ffydroseal to Centriseal which has air
instead of water for a seal. The change was made because the Hydros eal
pumps added more water to the system than could be tolerated in closed— loop
operation. However, greater sleeve wear resulted when using air as a seal.
Piping
Only a few joints of the rubber— lined piping were opened for
inspection. One h- inch ell located just upstream of control valve 1047
had blisters in the neoprene lining, as shown in Figure 13- Also, the
pipe adjacent to the ell, both upstream and downstream, had a blister in
the lining. The piping had been in service about 1^,000 hours carrying
lime scrubbing process slurry to the venturi bull nozzle. A smell quantity
(0.8 mil) of clear liquid was withdrawn from the blisters with a syringe
and analyzed. Analysis of the liquid is shown below.
Calcium 113
Magnesium 688 ppm
Sodium 21^ ppm
pH 5-6
L-28
-------
Calcium, magnesium, and sodium are present in the scrubbing
process slurry in moderate quantities. The relative high concentrations
of magnesium and sodium in the liquid are attributed to earlier tests
during which large quantities of these elements were added to the slurry.
Currently, the cause is not known for blistering of the lining in the ell
or whether it is occurring at mid-length in long, straight sections of
pipe. Turbulence in the ell and adjacent area could be a factor. Also,
there is the possibility of a defective lining in this pipe section.
Strainers
The Elliott Type R filters (flat dual filters) in the dis-
charge lines of the G-201 and G-2C4 pumps were replaced by vertical-type
Hayward strainers. The cast iron housing of the Elliott strainers had
eroded and corroded to failure; however, the threaded copper-base shaft
that extends through the unit for diverting the flow of slurry from one
chamber to the other showed good resistance to attack. Also, the stainless
steel baskets showed negligible attack. Two single element Hayward strainers
used in parallel were installed in May 1975 to replace each dual-element
Elliott strainer. The materials of construction of the Hayward strainers
are: body, cast steel; trim, malleable iron; basket, Type ?l6 stainless
steel plate 20 mils thick perforated with 3/8-inch-diameter holes; and
cover gasket, neoprene.
Valves
Gate Valves; Fabri knife-gate valves were installed in the
slurry line upstream and downstream from the Hayward strainers for diverting
the slurry flow frcsn one stra.iner to the other. The wetted part of the
valves is Type Jl6 stainless steel; all other parts are cast or fabricated
carbon steel. Since installation of the valves, problems have been reported
with leakage at the O-ring,seal around the valve stem. Also, leakage through
the valve has occurred because a buildup of solids in the seat prevents com-
plete closing of the knife gate.
Check Valve; The stainless steel check valve in the pipeline
on the suction side of pump G—103 has been removed from the venturi system.
The spring that closes the valve had failed due to erosion and the hinges
were worn badly. The body of the valve was of cast stainless steel ASTM
A-351, Grade CF-8M. The plate (hinged vertically at the center of-the
cavity) was of Type 3l6 stainless steel, and it seated on a neoprene ring.
The check valves have not been needed, and others will probably be removed
as opportunity permits.
General Information
Table VII is a compilation of data for all alloys tested in the
two scrubber systems without identifying the test conditions. This table
summarizes information on pitting, crevice corrosion, and general corrosion
(on basis of weight loss). For convenience in comparing approximate costs
of alloys the information received is given in Table VIII.
L-29
-------
Current Work
For many years molybdenum has teen considered a valuable
alloying element to inhibit pitting attack of stainless steels. The
American Iron and Steel Institute (AISl) appointed a committee of
stainless steel producers to investigate further the role of molyb-
denum in providing resistance of stainless steel to pitting. In May
1975, the committee visited TVA at Muscle Shoals to discuss the
results of corrosion tests conducted in the sulfur dioxide removal
test programs at Colbert and Shawnee power plants. The committee
invited TVA to participate in this study. Consequently, the following
stainless steels containing the quantities of molybdenum indicated
were included in the fourth series of corrosion tests now in progress:
Stainless steel "jo Mo
Climax 18-2 2.1
Type 216 2.3
Type 316L 2.3
Type 316L • 2.8
Type 317 3-2
AL 29-4 4.0
AL 6X 6.4
The corrosion study is being continued on materials of con-
struction for the sulfur dioxide removal test facility at Shawnee Power
Plant.
Acknowledgment s
The onsite employees that contributed much to the corrosion
test program were: J. K. Metcalfe, Test Facility Supervisor, R. C. Tulis,
Inspection Engineer, and J. B. Barkley, Chief Chemist.
The following firms supplied alloys (sheet and filler metal)
for use in preparing welded corrosion test specimens:
Airco Vacuum Metals
Allegheny Ludlum Steel Corporation
Armco Steel Corporation
Carpenter Technology Corporation
Colt Industries
Huntington Alloys
Jessop Steel Company
Revere Copper and Brass, Incorporated
Stellite Division of Cabot Corporation
United States Steel Corporation
L-30
-------
The cost of materials was kindly provided "by Joe Martin of
Huntington Alloys, Atlanta, Georgia, and David Pratt of Metal Goods,
Incorporated, Memphis, Tennessee.
L-31
-------
Table I
Corrosion Testa Conducted jr.. the Venturi System of the limestone — Wet-Scrubbing Process
for Sulfur Dioxide Removal from Stack Gas at Shavnee Power Plant
/Test period— 3/15/T1* to k/ek/T5 (runs 602-1A through 62l»-lA); operating tine — 7515 hours
or JtA.8 days; and idle time — 2j8l hour a or 99.2
Corrosion specimens
Exposed in
Gas and
spray
Gas and
liquor
Exhaust
gas
Locations (See Fig. 1 ), Ref. No.
Gas
1002
Temperature, T 275-330
Velocity, ft/sec W3-64
Flow rate, 1000's acfm at 330°F 25-50
Composition, * by volume
S0r 0.1-0.1*
CO 10-lB
O, 5-15
H~0 S-15
F.ly ash, gr/std ft3 2-7
1011"
80-170
19-23
1006
80-160
6-8
19-23
1005
80-150
6-8
19-23
IOC*
8o-li*0
6-8
19-23
1007
S8-64
25-30
0.02-0.16
11-19
6-16
9-16
0.01-0.*
1015
1006
25!
25-50
25-50
0.02-O.16 0.02-0.16
11-19 11-19
6-16 6-16
9-16 9-16
0.01-O.Oi* 0.01-0.04
1013
Tenper.'Uure, r
-olids. unJii ssolved, "t by vt
ot'lids. .iisje-lve-,!, •£ by wt
J'K
nio_OvTHT?cri t-ion, ppm
- "
Corrosion rate of metals^ mils/yr
90-130
7-16
0.5-^.1
14.5-6.3
55-1050
5-200
300-1600
loo-Moo
50-61*00
25-90
50-330
ii-oo-8i*oo
70-1'- 872
1*9
ge P10
71*
8
2
17l*e, Pl*0
9
S
—
—
61*
8, P5
32e, pj.7
—
53e, PI1*
21
16
> (&
26e, P17
5
55
6
18
< 1
< 1
< 1
< 1
-
—
9
< i
e, P18
—
-
< ?
*-
e, Pl6
" 3d
e
~36e
k
' 12e
< 1
Neg.
S Pli
< 1
-
— d
9
-
-
—
, P13
< 1
—
e, P3fl
> 82
«, Pm
-62f
~26S
e, P10.
12d
Neg.
Neg.
Neg.
_
—
26
20
—
23
e, Pm
e, pi*o
5
«,P19
11
1
e, P28
-
1
e' ^
1
-
—
2
-
3
—
e, Pm
—
3, P6
1
1
6
-
—
_
-
—
1
5
—
-
1
1
-
1
—
-
< i
< 1
2
-
-
_
-
—
< 1
2
—
-
< 1
< 1
-
< 1
—
-
. Neg.
1
< 1
e
Pm
Neg.
Keg.
Pl5
Neg.
Neg.
-
—
Neg.
Neg.
-
—
'-', Jti
Neg.
—
e, F6
< 1
Neg.
~ Po
< 1
Neg.
Neg.
Neg.
Neg.
Neg.
Neg.
-
—
—
Neg.
Neg.
—
NeC.
Neg.
—
«;ni
a Alter 1*179 UvAii1:'. of operation, partial failure oi' a sportl (specijaen holder) occurred; a replacement spool of specimens ves exposed during the remaining
31 jo hours. The tvo spools did not contain identical specimens; the higher corrosion rate Is given in cases of duplicate tests.
k Test period VTOK from October T5, 1971*,'to April ;''*, 1975 (runs 611-1A to 62l*-lA), 3136 operating hours.
0 Negligible (Neg.) indicates corrosion rates of less than 0.05 "H Per year, and < 1 indicate* corrosion rates from 0.05 to 0.1*9 mil per year; "P" preceding
s number indicates pitting during the exposure period to the depth in nils shovn by the number; and "Pa" indicatei minute pits. Where lociilizod nttnck u-
more severe thun the rate determined by weight loss, no rate is given for general corrosion.
d Attack of veld.
f Crevice corrosion at Teflon insulator.
* Knife—line attack (groove adjacent to weld).
8 D,3lickelificatlon.
h Previously identified as Araco 22-13-5.
L-32
-------
Table II
Corrosion Tests Conducted in the TCA System of the Limestone - Wet-Scrubbing Process
for Sulfur Dioxide Removal from Stack Gas at Shawnee Power Plant •
/Test period—10/24/73 to 4/17/7% (runs 525-2A through 530-2A); operating time—2954 hours
or 123 days; and idle time—1246 hours or 52 days/
Test Phase A
Corrosion specimens
Exposed in
Locations (See Fig. 2 ), Ref. No.
Gas
Temperature, °F
Velocity, ft/sec
Flow rate, 1000's acfm at 300°F
Composition, % by volume
SO?
C0r
Oe'
Fly ash, gr/std ft3
Inlet
gas
2002
260-310
33-50
20-25
0.1-0.4
10-18
5-15
8-15
2-7
Gas and
liquor
2006
70-125
8-10
15-16
Gas and
droplets
2005
70-120
8-10
15-16
Gas and
mist
2004
70-120
8-10
15-16
Exhaust
gas
(heated)
2007
235-265
33-50
20-25
0.04-0.1
11-19
6-16
9-16
0.01-0.04
Effluent
liquor
2003
Liquor in
clarifier
2013
Solids, undissolved, % by wt
Solids, dissolved, % by wt .
pH
Ionic_composition, ppm
Corrosion rate of metals^ mils/yr
110-125
14-16
0.4-0.8
5.1-5.8
30-290
, 40-380
200-2700
1100-2600
200-500
30-120
50-520
1500-5000
85-100
o-4o
0.4-1.2
5-5-9.5
30-290
4o-38 o
200-2700
1100-2600
200-500
30-120
50-520
1500-5000
Brass, red, weld Oxweld 25M ....
Carpenter 20Cb— 3, weld Carpenter
20Cb-3
Cor Ten B, weld B80lB-C3
Crucible 26-1, weld E-Brite 26-1 . .
Cupro-Nickel 70-30, weld B259 RCuNi
Hastelloy B, weld Hastelloy B . . .
Hastelloy C-276, weld Hastelloy C-276
Incoloy 800, weld Inconel 82 ....
Incoloy 825, weld Incoloy 65 . . • •
Inconel 625, weld Inconel 625 . • •
Monel 400, weld Monel 60
Nitronic 50, weld Nitronic 50d . . .
Type 201, weld Type 3l6
Type 3l6L, weld Type 3l6L
Type 317, weld Type 317
USS 18-18-2, weld Inconel 82 ....
8b
< 1, P5
< 1, Pm
?.6
< 1, P?
—
—
Neg.
—
Neg.
Neg.
—
< 1, Pm
e, P2
< 1, Pm
< 1
c, Pm
8*
< 1
P
, Pm
56°
< lc
9
31
< 1
—
< 1
Neg.i
15
< 1, Pm
C,CP28
< 1 , Pm
< 1
"""
c i
, &
C*
c, Pm
2i|
c
, PI
4
8
Neg.
—
c, K:
Neg.
5
—
c, P25
c Pm
c, P3
_
9b
< 1, Pm
C
56c
\,
10
10
Neg.c
c
Neg.v
11
—
c, P12
c
, P10
e
Neg.
P4
3
Neg.
1
1
Neg.
Pm
Pm
1
—
Pm
c, PI
Pm
< 1
< 1
Neg.
Neg.
2
p
, Pm
< lt
Neg.
°, Pm
Neg.
Neg.
< 1
Neg.
P3
c, Pm
Pm
c, Pm
1
Neg.
Neg.
3
Neg.
< 1
1
Neg.
Neg.
Neg.
Neg.
< 1
—
Neg.
Neg.
Neg.
c, P8
a Negligible (Neg.) indicates corrosion rates of less than 0.05 mil per year and < 1 indicates corrosion rates
from 0.05 to 0.49 mil per year; "P" preceding a number indicates pitting during the exposure period to the depth
in mils shown by the number; nml "Pm" indicates minute pits. Where localized attack is more severe than the rate
. determined by weight loss, no rate Is given for general corrosion.
Attack of weld,
Crevice corrosion at Teflon insulator.
Previously identified as Armco 22—13-5.
6 Knife—line attack (groove adjacent to weld).
L-33
-------
Table III
Corrosion Tests Conducted in the TCA System of the Limestone — Wet-Scrubbing Process
for Sulfur Dioxide Removal from Stack Gas at Shawnee Power Plant
/Test period—5/10/74 to 4/21/75 (runs 531-2A through 545-SA); operating time—64$6 hours
or 269 days; and idle time—U348 hours or 77 days/
Corrosion specimens
Exposed in
locations (See Fig. 2 ), Ref. No.
Gas
CO.-
0.-
H-0
Fly ash, gr/std ft3
2002
Temperature, °F .......... 260-310
Velocity, ft/sec
Flow rate, 1000' s acfm at JOO°F .
Composition, % by volume
0.1-0.4
10-lfl
5-15
8-15
2-7
2006
70-130
8-11
15-24
Test Phase B
Gas and
mist
2005
2004
70-125 70-125
7-9 6-8
15-24 15-24
2007
235-265
35-56
20-32
2014°
2015
235-265 230-260
35-56 35-56
20-32 20-32
0.04-0.1 0.04-0.1 0.04-0.1
11-19 11-19 11-19
6-16 6-16 6-16
9-16 9-16 9-16
0.01-O.04 0.01-0.04 0.01-0.04
Effluent
liquor
2003
Liquor in
clarifier
2013
Temperature, °F
odids. undissolved, ,t by wt
Solids, dissolved, i by wt .
pH
Ionic_eomposition, ppm
504
C?.++
„,++
Cl
Corrosion rate of metals, mils/yr
AL 6X, weld AL 6X
AL 29-4, weld AL 29-4
Brass, red, weld Oxweld 25M ....
Carpenter 7-Mo, weld 316
Carpenter 20Cb-3, weld Carpenter
L'CCb-5
Cor-Ten A, weld E8018-C3
Cor-Ten B, weld E8018-C3
Cupro-Nickel 70-30, weld BL'59 RCuNi
B-Brite 26-1, weld E-Brite 26-1 . .
Hastelloy B, weld Hustelloy B . . ,
Hastelloy C-i??6, weld Hustelloy C-2T6
Hayncs 6B, weld Haynes No.25 ....
Incoloy 800, weld Inconel 82 ....
Ineoloy 8P5, weld Incoloy 65 ....
Inconel 6. '5, weld Inconel 6,°5 • • •
Jessop 7OO, weld Ciaiote i".'
Mild steel A-:'05, we.ld WiOl.' ....
Monel 'lOO, we.ht Monel oO
Nltronic 50, we.ld Nitronic 50f . . .
Type' ;'0l, w,-ld 'i-yi)e 310
Tyix- ;'10, weld 'Type ."Id
Type 3iVil,, weJd Type 3O8h
•Type JluJ,, weld Type 3l6l
Type 317, weld Type 317
UJC j8-lil-', welvl InconcJ !*.' ....
.. .1
c, d
d
> 57
d, e
d, e
d, e
d, e,
----- 110-130 85-100
_____ 7-lfi o-4o
----- 0.3-6.0 0.3-6.0
----- 4-. 7-5- 9 5-5-9-5
----- 70-5,000 70-5,000
----- 30-1,000 30-1,000
_____ 300-39,000 300-44,000
__--- 100-2,600 100-2,600
----- 260-12,000 260-a.2,000
_____ 35-50 35-60
----- 40-115 4o-ll5
----- 800-4,500 800-4,500
_
2
-
Neg.
lle
.-)6
Pu6
o
Neg.
Neg.
P10
Neg.
Neg.
—
_
3
Meg.
, P15
, p2;>
Neg.
e
—
_
9C
Neg.
51
9
e
1C'C
Neg'.
Neg.
Pll
e
Neg.
—
_
.1.'°
—
e, P6
_
°> PI;'
e
e
i;
' ric
_
i
-
Neg.
_
1
e
e
< 1
Neg.
Neg.
P3
-
Neg.
—
—
< 1
—
Neg.
—
U, P7
Neg.
Neg.
< 1
Neg. Neg. -
UA_ KTorr
iieg. jueg. —
- - < 1
Neg.
Neg.
1 < 1
— — 1
_ _ < 1
_ _ Neg.
Neg.
Neg.
Neg.
— — - —
Neg.
Neg.
Neg . Neg . —
1 < 1
< 1
Neg.
Nep. e Nee.
Neg. e
_ _ —
Neg. e Neg.
Neg.e
— —
-
1
—
Neg.
— .
1, P5
1
Neg.
e
Neg.
Neg.
Neg.
Neg.
Neg.
—
—
1
Neg.
P9
—
—
Neg.
Neg.
e, K3
11 Ti-at period wu;-. from October lo, .i'.'7'i, to April ,-'1, ,\<-r('j (runs 535-."A to ?45-iiA), 389- hours operating time.
k Negligible (Ne^.) indicates corrouiini rateu oi' less than 0.05 mil, and < 1 indicates corrosion rates from 0.05 to 0.49 mil per year;
"P" preceding a number indicates pitting diu-'uic, the exposxire period to the depth in milu shown by the number; and "Pm" indicates
Minute pits. Wliere loca.1 i/oil attucK i:; mon- Hi-von; than the rate determined by weight .Ions, no rate is given for gencruj corrosion.
c Attack of w< hi.
li Hprr-ijnen worn by movement of p]astir ba.lHc; corroyion on tin1 bnois oi' weight J.OUB could nut. be detennirii'd.
'I Crevice corrosion ut Tel'.ion in::ujiiltir.
L Previously identified ac Armco 22—1J—5.
L-34
-------
Table IV
00
U1
Composition of Alloys Tested in the Limestone - Wet-Scrubbing Systems
for oulfur Dioxide Removal from citack Gas at Shawnee Power Plant
Chemical analysis, £
Alleys
Al 'j'f.
Ai. £>— -"
Erass, ?.ed
Carpenter 7-"o°
Carpenter 2CCb-
Cor-Ien A&
Cor -Ten E£
Crucible 26 -la
Cupro-;;ic
-------
TABLE V
Analyses* of Deposits in Limestone — Wet-Scrubbing Systems for Sulfur Dioxide Removal from Stack Gas at Shawnee Power Plant
Identification of sample
Composition, % by weight
r
•
u>
Date
Number
Location
CaS03
CaS04
Venturi System
10/15/74
10/15/74
10/15/74
10/15/74
10/18/74
10/27/74
11/5/74
11/18/74
ll/lS/74
1/3/75
TCA System
H/15/73
H/15/73
H/20/73
1/24/74
1/25/74
1/25/74
1/28/74
TCA System
6/20/74
6/26/74
6/26/74
6/26/74
6/27/74
5/29/74
7/29/74
7/29/74
8/23/74
8/30/74
VD-4
V&-3
VD-2D
VD-1C
VB-2
TO-1
VD-1
VD-e
VD-3
VD-2
, Test
TCAB-2
TCAD-1
TCAD-1
TCAD-1
TCAD-1
TCAD-2
TCAD-1
, Test
TCAD-1
TCAD-1
TCAD-2
TCAD-2
TCAD-1
TCAD-5
TCAD-2
TCAD-4
TCAD-2
TCAD-1
Multilayerea scale from second door of afters crabber
Solids from duct at reheater outlet
Mud with green under layer from ID fan casing
Solids from rear faces of the ID fan blades
Scale from D-101 walls
Scale from "bottom of (inlet) mist eliminator vanes
Scale from underside of top mist eliminator vanes
Scale from top of mist eliminator
Multilayered scale from flooded elbow
Scale from under spray headers
Phase A
Solids from various locations on wash tray inlet
Crystalline solids from inlet tips of mist eliminator vanes
Composite scale from top of specimens on floor D-201
Solids from inlet vanes of mist eliminator
Solids 13 inches upstream, inlet duct spray nozzle
Solids from wash tray inlet
Scale from G— 201 discharge pipe
Phase B
Scale from underside of wash tray
Scale from "bottom sphere "bed grid
Scale from top of wash tray bubble caps
Scale from wash tray overflow weir
Scale from south wall under bottom grid
Solids from corroded area in expansion joint above ID fan
Scale from wall above top grid
Dry, tan— colored solids from ID fan casing
Solids in inlet duct 2 inches upstream from cooling sprays
Solids from inlet damper to ID fan
10.58
0.82
0.97
0.17
9-79
21.35
0.49
Trace
0.27
8.71
24.54
0.88
26.17
2.29
4.32
30.09
13.03
10.52
0.84
0.65
0.67
5.80
1.21
1.64
1.79
23.01
6.45
79.12
65-58
84.24
71.66
74.15
67.23
60. 04
57.41
66.14
68.30
34.87
67.42
61.00
66.08
8.11
34.04
69.40
69.40
94.81
68.78
39.95
55.46
33-03
90.15
22.89
37.54
30.65
CaC03
2.23
Trace
0.12
Trace
12.04
3.33
0.53
0.44
Trace
2.96
3.62
1.89
4.37
1.48
4.73
14.45
7.73
0.15
Trace
1.14
0.62
5-50
0.91
0.88
0.90
0.26
3-35
CaClg
Trace
Trace
Trace
Trace
Trace
Trace
1.44
Trace
Trace
0.52
1.92
4.53
0.14
2.21
Trace
Trace
1.15
Trace
3.13
1.15
0.10
1.03
0.85
2.66
3.53
1.76
Trace
MgO Acid insoluble
0.09
0.35
0.6l
9.40
0.97
0.33
0.45
0.30
0.27
0.13
0.10
0.30
0.06
0.05
O.lB
0.26
0.13
0.38
0.22
0.30
0.40
0.79
0.19
0.32
0.42
5.80
2.4
7.97
33.25
14.09
18.77
3.04
7-76
37.04
41.85
33.32
19.38
35-04
25.57
8.26
27.90
82.66
2l.l6
8.56
19. 51*
1.00
29.00
58.26
31.42
63.81
4.36
73-5^
31.64
57.15
Information taken from reports by J. B. Barkley to J. K. Metcalfe during the period 11/15/73 to 1/3/75.
" There was 16.72$ by weight free acidic material as sulfuric acid before the sample was normalized to 100$ dry solids.
c There was 26.31$ by weight free acidic material as sulfuric acid before the sample was normalized to 100$ dry solids.
-------
TABLE VI
Hardness of Neopreoe Linings of Equipment in the Limestone - Me-|>-Scrubbing Systans
for Sulfur Dioxide Removal from Stack Gas at Bhawnee Power Plant
(Exposure period: 8/12/72 to 4/S8/75)
Location of hardness test
Venturi System (Operating hours: aecumulated^-13,669; since last inspection—9468)d
Crossover Pact from Flooded Elbow to After Scrubber. Patched Area:
Barometer "A" hardness
Original8 Current" At""fc
Sew material, patch . _ 66_?0 _
Old material, near patch go^j 5!t_g0 ?j
After-Scrubber Tower:
Eight inches below Type 5l6L stainless steel at venturi section 60-65 53-58 73
Sidewalls near cone-shaped bottom (approx, elevation, 371 ft) 60-65 50-60 73
At approximate elevation, 587 feet 60-65 51-55 72
At approximate elevation, 392 feet 60-65 51-59 72
Three inches below mist eliminator (approx. elevation, 398 ft) 60-65 47-57 73
Three inches above mist eliminator (approx. elevation, 1*01 ft) 60-65 42-1*7 73
Six inches below the stainless steel duct (approx. elevation, 406 ft) .... 60-65 45-48 73
Clarified Process Water Storage Tank, D-J.Q3:
Above liquid level 55-60 63-65 82
Below liquid level 55-60 65-71 82
Agitator blades - 58-60 82
Reslurry Tank, D-401:
Above liquid level 55-60 60-66 82
Blades of Agitator In:
Effluent hold tank, D-101 60-70 57-62 82
TCA System (Operating hours; accumulated—Ik,237; since last inspection—9410)
Scrubber Tower:
Four inches above inlet gas duct (approx. elevation, 376 ft) 60-65 46-g2 65
Six inches above bottom grid (approx. elevation, 380 ft) 60-65 51-55 65
Three feet above the second grid, near Test 2006 (approx. elevation, 386 ft) . 60-65 52-56 65
Four feet below Koch tray (approx. elevation, 398 feet) 60-65 48-54 74
Two feet above the Koch tray (approx. elevation, 4o4 ft) 60-65 44-46 74
Clarified Process Hater Storage Tank, D-a03:
Above liquid level 55-60 61-66 82
Below liquid level 55-60 72-75 82
.Agitator blades - 64-67 82
Blades of Agitator In;
Effluent hold tank, D-201 • • • 60-70 57-62 70
Q
Heoprene Lining irom Centrifugal Pump, 0-201 :
Suction side of casing 54-56 62-66 ~4
Seal side of casing 54-56 65-69 74
Impeller 54-56 66-68 74
!1 Values not determined by OTA but were taken from information supplied to contractors for bidding on con-
struction. The ASTM standard K?24o-68 specifies that tests for hardness of rubber be made at 75 "F.
b The instrument used to determine the durometer hardness of neoprene linings during inspection of the plants
(May 29-31, 1975) was Shore "A.;1," ASTM D2240. Note that the measurements were made over a wide rangrj of
temperatures; therefore, an exact comparison of hardness values is not possible. Usually three or wore
tests were made in an arm.
c The atmospheric temperature varied from about 65° to 82°F while tests for hardness were being made.
J The previous'inspection was September lfl-£0, 1973-
e The impeller and liners were removed because of impact and abrasion damage. The service .life of the
impeller and liners is not available.
L-37
-------
Table VII
Compilation of Corrosion Data of Metals in the Two Limestone — Wet-Scrubbing Systems for
Sulfur Dioxide Removal from Stack Gas at Shawnee Power Plant
(Test period—10/24/73 to V2VT5)
Corrosion
Alloy
AL 6X
AL 29-4
Brass, Red
Carpenter 7-Mo
Carpenter 2CCb— 3
Cor— Ten A
Cor-Ten B
Crucible 26—1
Cupro-Nickel 70-30
E-Brite 26-1
Hastelloy B
Hastelloy C-276
Haynes 6B
Incoloy 800
Iiicoloy 825
Inconel 625
Jessop 700
Mild Steel A-285
Monel 400
Nitronic 50
Type 201
Type 2l6
Type 304L
Type 316L
Type 317
Type 446
uss 18-18-2
No. of
specimens
tested
k
4
20
8
22
k
22
8
21
13
20
22
15
111.
21
22
4
4
20
14
23
k
9
26
3B
l
18
On basis
of
wt. loss,0
mils/yr
Neg. - 1
Neg. - 1
< 1 - > 82
Neg. - < 1
Neg. - 86
< 1-6
1 - > 872
Neg. -< 1
< 1 - 49
Neg. -9
Neg. - 74
Neg. -8
Neg. - 2
Neg. - 174
Neg. - 9
Neg. - 8
Neg. - 1
< 1 -5
Neg. —'64
Neg. - 8
Neg., - 32
Neg. - 1
Neg. - 33
Neg. - 21
Neg. - 16
> 68
< 1 - 26
>i
Specimens pitted"
No.
0
0
0
3
8
0
3
3
0
7
1
0
1
8
3
1
0
0
0
4
12
0
7
7
4
0
14
Depth,
Min.
0
0
0
M
M
0
M
M
0
4
0
0
0
M
M
0
0
0
0
M
M
0
M
M
M
0
M
mils
Max.
0
0
0
8
19
0
6
2
0
28
M
0
7
40
5
M
0
0
0
5
26
0
22
1
3
0
40
Specimens
with crevice
attack, No.
0
0
0
2
7
0
5
4
3
9
4
0
1
8
5
1
0
0
1
2
9
1
7
9
9
0
14
Specimens with other
types
of attack
No. Identification
0
0
8
0
0
0
1
0
1
0
2
0
0
0
0
0
0
0
4
0
1
0
0
0
0
0
0
0
°d
8d
0
0
0
le
o.
lf
0
2d
0
0
0
0
0
0
?d
4d
0
le
0
0
o «
0
0
0
Tables i , u , and in give coruosion data for the materials tested in the venturl and TCA scrubber
systems. Because the number of specimens tested of each alloy ranged from 1 to 26, an order of
decreasing corrosion resistance could not be established.
M, minute pit; the numerical values show the actual depth of penetration in mils during test period.
0 The range of corrosion rates does not include severe abrasion caused by spheres rubbing the specimen
in test 20C6.
d Attack of weld.
e Knife—line attack (groove adjacent to weld).
f Denickelification.
L-38
-------
Table VIII
Cost of Alloys Tested in the Experimental Facilities for the Removal of
Sulfur Dioxide from Stack Gases at the Shawnee Power Plant
(Test period inclusive: 10/24/73 to 4/24/75)
Source of information:
Alloys tested
AL 6X
AL 29-4
Brass, red
Carpenter 7—Mo
Carpenter 20Cb—3
Cost for commercial quantities
3/4-inch tubing,
0.065—inch wall
$/ft Ratio based
B on Type 304
0.74
0.6
Sheet, 0.120-inch
$/lbRatio based
B on Type 304
2.65
2.65
3-4
Cor-Ten A
Cor— Ten B
Crucible 26-1
Cupro-rNickel 70-30
E-Brite 26-1
Hastelloy B
Hastelloy C-276
Haynes 6B
Incoloy 800
Incoloy 825
Inconel 601
Inconel 625
Inconel 702
Jess op 700
Mild Steel, A-285
Monel 400
Nitronic 50
Type 201
Type 2l6c
Type 304
Type 304L
Type 3l6L
Type 317
Type 446
uss 18-18-2
1.01
6.86
6.72
1.85
2.79
2.29
4.8l
2.08
1.17
1.18
1.47
1.90
0.9
5-9
5-7
1.6
2.4
2.0
4.11
1.8
1.0
1.0
1.26
1.62
0.20
1.23
7.16
7.16
13.42
2.38
3.14
3.13
4.8l
4.91
0.17
3.09
1.69
0.76
0.79
0.86
1.26
1.80
0.3
1.6
9.1
9-1
17.0
3.0
4.0
4.0
6.1
6.2
0.2
3.9
2.1
1.0
1.0
1.1
1.6
2.3
Details concerning ^ne jjreya.j.a.u-n.'j.i «uu. ^W^^-A.—^^ ~- a
numerous to list. Definite information can be obtained from manufacturer or
supplier. ,-
b A Metal Goods, Incorporated, Memphis, Tennessee, January 197o.
B' Huntington Alloy Products Division, The International Nickel Company,
Incorporated, Atlanta, Georgia, December 1975•
c Type 304 was not tested but is used as the basis ($1.17/ft for 3/4-in tubing
and $0.79/lb for 0.120-in sheet) for approximate cost ratios.
L-39
-------
TOP OF STACK
(MEL
LEGEND:
GEZi LOCATION OF TEST
^—T—1 SPECIMENS
O (SPOOL)
o CARBON STEEL ASTM A- 283 rr;
6. TEST 1013 WAS CONDUCTED IN
CLARIFIER TANK D-102 NOT SHOWN
QSDEX^
CHAMBER FOR MIXING
HOT GAS WITH SCRUBBER ^_
GAS, 73 J O.D. , 6?i. |. D. r~>.
8 H ^^^^^
8'-0"
CATWALK , 1
f TO PAUtf F 19 \ 1
BUILDING) \
— Nl/\i/\l/\ '
GAS INLET DUCT(40"DIA., IOGA. 0
CARBON STEEL0) \ W
EL. 397.'- 10" y
-------
LEGEND:
QDs. LOCATION OF TEST
*• 7- "SPECIMENS.
0 (SPOOL)
0 CARBON STEEL ASTM A-283
b TEST 2013»RS CONDUCTED IN
CLARtFIER TANK D-202 NOT SHOWN
EL
REHEATER (F- 201, REFRACTORY
LINED CARBON STEEL
SHELL,INSULATED)
73VO.D.,67'/2HI.D.
MIST ELIMINATOR (CHEVRON)
FLEXITRAY
GAS INLET DUCT(40"
DIA., 10 GA. CARBON ~\ »
STEEL) «"
397 '- 10" --^
TYPE 316 L S.S
(A TO B)
ACCESS DOOR
SPOOL'
RECIRCUL ATION -
TANK (D-204,
NEOPRENE LINED
CARBON STEEL)
I.D.FAN
(TYPE 316 LSS)
DUCT-40" DIA
(TYPE 316 LSS)
OOL
(TYPE 316LSS)
Vi
6-It"SO. INSIDE
UBBER LINING
SCRUBBER
STRUCTURE
SCRUBBER TOWER
5-7"Stt INSIDE
(NEOPRENE LINED ,.
CARBON STEEL)
POOL
GRIDS
(BALL SUPPORT)
DOWNCOMER(4'DIA.,
TYPE3I6LSS)
HOLD TANK
0-201 FOR
SCRUBBER
EFFLUENT,
FLAKELINE
103 COATIN6
ON CARBON
STEEL0)
TOP OF STACK
AGROUND LEVEL
EL. 348'-0
FIGURE 2
TURBULENT CONTACT SCRUBBER SYSTEM, TCA-CC-201)
(MOBILE BED)
L-41
-------
FIGURE 3
Spool assembly of Corrosion Test Specimens (2 in. Disk)
MwwsviRtt
FIGURE A
Probe Assembly of Corrosion Test Specimens (2 in. Disk)
L-42
-------
it
1002 1004 1005 1006
INLET GAS GAS AND DROPLETS GAS AND LIQUOR GAS AND LIQUOR
f
i
4^
CO
1007
EXHAUST GAS (HEATED)
1008
EFFLUENT LIQUOR
1011
GAS AND SPRAY
1013
LIQUOR INCLARIFIER
1014
EXHAUST GAS (HEATED)
1015
EXHAUST GAS (HEATED)
FIGURE 5. DISK SPECIMENS AFTER : XSURE IN VENTURI SYSTEM (MARCH 15, 1974
APRIL 24, 1975)
-------
2002
INLET GAS
2004
GAS AND MIST
2005
GAS AND DROPLETS
2006
GAS AND LIQUOR
r
i
2007
EXHAUST GAS (HEATED)
2008
EFFLUENT LIQUOR
2013
LIQUOR INCLARIFIER
2014
EXHAUST GAS (HEATED)
2015
EXHAUST GAS (HEATED)
FIGURE 6. DISK SPECIMENS AFTER EXPOSURE IN TCA SYSTEM (TEST PHASE B, MAY 10, 1974
APRIL 21, 1975)
-------
FIGURE 7
i! 111 ^ Nozzle Abo ye Venturl Section, Eroded Inside By
S |iii- r y and Outside By Flyash - 185 Mils Per Year
FIGURE 8
Spray Header in Venturi Afterscrubber, Type 316 Tee
and Type 304 Reducer, Pitted
L-45
-------
FIGURE 9
Pitting ii f Type 316 Weir Box Outlet In the TCA Tower
FIGURE 10
Stress Corrosion of Carbon Steel Clamp in Venturi Afterscrubber
L-46
-------
FIGURE 11
CRACK ABOUT 4 INCHES LONG IN SHROUD OF I.D. FAN
IN THE VENTURI SYSTEM
FIGURE 12
Type 316 Expansion Joint Above ID Fan
in Venturi System - Corroded and Cracked
L-47
-------
FIGURE 13
Blisters in Neoprene Lining of 4 in. Slurry Line
in Service 623 Days
L-48
-------
TECHNICAL REPORT DATA
(Please read Inunctions on the reverse before completing)
REPORT NO.
EPA-600/7-76-008
2.
3. RECIPIENT'S ACCESSION NO.
4.T.TLE ANDSUBT.TLE
SCRUBBING TEST
FACILITY: ADVANCED PROGRAM
Second Progress Report
5. REPORT DATE
September 1976
6. PERFORMING ORGANIZATION CODE
, AUTHOR(S)
8. PERFORMING ORGANIZATION REPORT NO.
Harlan N. Head, Project Manager
9. PERFORMING ORGANIZATION NAME AND ADDRESS
Bechtel Corporation
50 Be ale Street
San Francisco, California 94119
10. PROGRAM ELEMENT NO.
EHE624
11. CONTRACT/GRANT NO.
68-02-1814
12. SPONSORING AGENCY NAME AND ADDRESS
EPA, Office of Research and Development i
Industrial Environmental Research Laboratory
Research Triangle Park, NC 27711
13. TYPE OF REPORT AND PERIOD COVERED
Progress; 6/75-2/76
14. SPONSORING AGENCY CODE
EPA-ORD
16. SUPPLEMENTARY NOTES projeqt pfgcier {Qr ^ report Jg J
Ext 2915, Mail Drop 61. Previous report in this series
E. Williams, 919/549-8411
was EPA-600/2-75-050.
16. ABSTRACT
The report giVQS results of advanced testing (from June 1975 to February
1976) of 30,000 acfm (10 MW equivalent) lime /limes tone wet scrubbers for SO2 and
particulate removal at TVA's Shawnee Power Station. No reliability problems were
experienced in 1143 hours of lime testing with cycling gas rate to simulate variable
load operation in the venturi/spray tower. Clean operation of the mist eliminator
(M.E.) system (3-pass, open- vane chevron M. E. with intermittent top and bottom
wash) was achieved using lime in the venturi/spray tower system, but plugging
occurred with a similar M. E. system using limestone in the Turbulent Contact
Absorber. In tests to improve limestone utilization, M.E. reliability was found to be
a strong function of alkali utilization. In both scrubber systems , intermittent top and
bottom wash kept the M. E. clean at alkali utilization greater than 85%. Below 85%
alkali utilization, a continuous bottom wash was required. Limestone utilization was
correlated with scrubber inlet pH, hold tank residence time, and hold tank design.
17.
KEY WORDS AND DOCUMENT ANALYSIS
DESCRIPTORS
b.IDENTIFIERS/OPEN ENDED TERMS
c. COSATI Field/Group
Air Pollution
Alkalies
Scrubbers
Calcium Oxides
Limestone
Sulfur Dioxide
Dust
Air Pollution Control
Stationary Sources
Alkali Scrubbing
Particulate
Venturi/Spray Tower
Mist Eliminators
13B
07D
07A
07B
07G
11G
13. DISTRIBUTION STATEMENT
Unlimited
19. SECURITY CLASS (ThisReport)
Unclassified
21. NO: OF PAGES
376
20. SECURITY CLASS (This page)
Unclassified
22. PRICE
EPA Form 2220-1 (9-73)
L-49
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|