EPA-650/2-73-015
4653
Babcock&Wilcox
EQUIMOLAR NO-NC>2 ABSORPTION
INTO MAGNESIA SLURRY--A
PILOT FEASIBI ITY STUDY
RESEARCH AND DEVELOPMENT DIVISION
ALLIANCE RESEARCH CENTER
SPONSORED BY
ENVIRONMENTAL PROTECTION AGENCY
-------
EQUIM3LAR NO-N02 ABSORPTION INTO MAGNESIA SLURRY -
A PILOT FEASIBILITY STUDY
PROJECT SPONSORED BY ENVIRONMENTAL PROTECTION AGENCY
ORDER 4193-01
RESEARCH CENTER REPORT 4653
BY: W. DOWNS
NOVEMBER 29, 1971
THE BABCOCK & WILCOX COMPANY
RESEARCH AND DEVELOPMENT DIVISION
ALLIANCE RESEARCH CENTER
ALLIANCE, OHIO
COPY NO.
-------
THE BABCOCK § WILCOX COMPANY
RESEARCH AND DEVELOPMENT DIVISION
ALLIANCE RESEARCH CENTER
ALLIANCE, OHIO
EQUIM3LAR NO-NQz ABSORPTION INTO MAGNESIA SLURRY-
A PILOT FEASIBILITY STUDY
BylW. Downs
ABSTRACT
Purpose
The purpose of this project was to investigate the feasibility of
absorption of equimolar concentrations of NOx into MgO slurry on a 1500 cfm
wet scrubbing pilot plant.
Summary
A wet scrubbing pilot plant consisting of several scrubbers was modified
by the inclusion of an additional scrubber to enable series scrubbing of fly
ash, sulfur dioxide, and finally nitrogen oxides. Gaseous nitrogen dioxide
was injected into the flue gas following the S02 scrubber but before the NOx
scrubber. Seventeen tests were performed to evaluate parameters including the
liquid-to-gas ratio, the ratio of N02 to NO, slurry concentration, stoichiometry,
and gas flow rate.
Results
NOx absorption was very poor for all conditions tested. The absorption is
estimated to be less than 10%. The results are obscured by large variance in
the NOx measuring techniques. SOz absorption in the NOx scrubber was dependent
upon the liquid-to-gas ratio and varied from 86%jto 98.3%. Deposition on the
underside of the first tray of the S02 scrubber was observed. '
Conclusions
NOx absorption with equimolar concentrations of NO and N02 into MgO slurry
is not feasible in the apparatus tested. It is probably unfeasible in any
practical gas-slurry contacting apparatus.
NOx absorption into soluble alkalis may be feasible and would best be done
in packed towers.
Recommendations
MgO slurry should be removed from those bases being considered for aqueous
NOx absorption.
Work should continue on the feasibility evaluation of soluble bases for
this system.
Research Center Report 4653
Order 4193-01
November 29, 1971
Equimolar NOx-MgO Absorption
Project Sponsored by Environmental
Protection Agency
-------
TABLE OF CONTENTS
Page
1.0 INTRODUCTION 1-1
2.0 PILOT PLANT EQUIPMENT 2-1
2.1 Coal Preparation -- 2-1
2.2 Burner and Furnace 2-1
2.3 Fuel - 2-2
2.4 Wet Scrubbing Apparatus 2-2
2.4.1 Particulate Scrubbing System 2-2
2.4.2 Floating Bed Absorber 2-3
2.5 Induced Draft Fan Section 2-4
2.6 NOX Scrubber and Components 2-4
2.6.1 N02 Injection System - 2-4
2.6.2 NOX Scrubber 2-5
2.7 Overall Pilot Plant Schematic 2-6
3.0 TEST APPARATUS AND PROCEDURES - - - 3-1
3.1 Plant Operating Test Procedure - 3-1
3.2 Flue Gas Analysis - - 3-2
3.2.1 General Analysis 3-2
3.2.2 NOjj Analysis — 3-2
3.3 Liquid Analyzer - 3-7
4.0 RESULTS 4-1
4.1 Overall Results - 4-1
4.1.1 Particulate Scrubber 4-1
4.1.2 FBA 4-1
4.2 NOx Scrubber Results 4-2
4.2.1 NOjj Absorption 4-2
4.2.2 S02 Absorption 4-3
5.0 DISCUSSION - - 5-1
6.0 CONCLUSIONS 6-1
7.0 RECOMMENDATIONS -- - - 7-1
REFERENCES R-l
APPENDIX A, SALTZMAN ANALYTICAL PROCEDURE A-l
APPENDIX B, COMPUTER OUTPUT B-l
111
-------
TABLE OF CONTENTS
List of Tables
Table Page
2.1 Fuel Analysis --- 2-7
3.1 Sodium Nitrite Equivalence for Mixtures of NO and N02 --- 3-8
4.1 Analysis of Deposit Sanples 4-4
4.2 Parameter Study Specifications - 4-5
4.3 Summary of Results 4-6
List of Figures
Figure Page
•~"^~a ' • -. i *•
2.1 Magnesia Base Slurry Scrubbing Pilot Plant - — 2-8
2.2 Basic Combustion Test Furnace - --- 2-9
2.3 Particulate Scrubbing System 2-10
2.4 Particulate Scrubbing System -- -- 2-11
2.5 Floating Bed Absorber -- 2-12
2.6 Floating Bed Absorber - -- 2-13
2.7 Slurry Entrainment Separator Section 2-14
2.8 NO, Injection System --- 2-15
2.9 NOX Scrubber Dimensions 2-16
2.10 NOX Scrubber - 2-17
2.11 NOX Scrubber and Leach Bed 2-18
2.12 Pilot Plant Flow Schematic - — 2-19
3.1 S02 Sampling System - - 3-9
3.2 NC^ Sampling System - -- 3-10
3.3 NO Oxidation Rate in Air 3-11
3.4 NO Oxidation Rate in Flue Gas 3-12
3.5 Equilibrium HN02 Concentrations 3-13
4.1 Deposition on Underside of First FBA Stage — 4-7
4.2 S02 Absorption in NC^ Scrubber 4-8
5.1 Geometry Assumed for NO^ Absorption - 5-8
5.2 Predicted NOy Absorption in Test Apparatus 5-9
5.3 Process Flow Schematic - - - 5-10
IV
-------
1.0 INTRODUCTION
removal from power plant effluents by wet scrubbing is one of the
approaches being considered by the Office of Research and Monitoring (ORM)
of the Environmental Protection Agency (EPA) in its overall NOj, program.
In response to the suggestion from several sources including the recommendation
submitted to ORM by The Babcock § Wilcox Company under Contract CPA-22-69-162,
the feasibility of absorbing equimolar concentrations of NO and NO- into
magnesia slurry was undertaken. This work is the outgrowth of a study of wet
scrubbing of pulverized coal generated flue gas for the purpose of removing
particulate matter and sulfur dioxide in a 1500 cfm pilot plant. As part
of that study it was shown to be unfeasible to absorb equimolar NCL and
S02 simultaneously. However, it was suggested that possible nitrogen
oxides could be absorbed into magnesia in the scrubber following the SO.
scrubber. This report presents the results of that work under Contract
68-02-0022.
1-1
-------
2.0 PILOT PLANT EQUIPMENT
The pilot plant equipment used for these tests is a self-contained facility
which includes coal preparation equipment, a coal-fired furnace, and a wet
scrubbing pilot plant. Most of this equipment has been previously described/
Only the modifications and additions will be discussed in detail. A pictorial
drawing of the pilot facility is shown in Figure 2.1.
2.1 COAL PREPARATION
Coal preparation involves transporting 1/2" mesh coal from the storage
bunker to the pulverizer, pulverizing the coal, and transporting it to a storage
hopper at the pilot plant. From there the coal is removed by a screw and con-
veyed to the furnace by the primary air.
The storage bunker is used primarily to supply the heating plant for the
Research Center. The pulverizer used during this test program differs from the
used on previous tests. ^ A Schutz-O'Neill Air Swept pulverizer Model 22-WJ
superfine pulverizer was installed in early 1971 and was used exclusively for
these tests.
2.2 BURNER AND FURNACE
The pulverized coal burner is a B$W cell-type circular burner with a
natural gas lighter. This lighter is operated continuously during coal firing
to help maintain stable ignition.
The furnace, Figure 2.2, consists of a horizontal cylinder 8 feet in length
by 4-1/2 feet in diameter. This forms the actual combustion chamber. The walls
of the furnace are formed by a water jacket, which dissipates heat by the produc-
tion of nonpressurized steam. The inside walls are not covered with refractory.
To maintain stable ignition, the pulverized coal must be fired with preheated
air. This air is supplied by a forced draft fan and preheated by two gas-fired
air heaters capable of heating 10,000 Ib/hr air to a temperature of 1000°F. The
heat release of the furnace averages about six million Btu/hr.
Combustion gases pass from the furnace proper through three tube banks that
cool the flue gas to approximately 450°F. All tubes are 1-1/2-inch O.D. on
2-1/2-inch centers with exception of the first six rows of tubes which are on
5-inch centers. Behind each tube bank is a duct permitting flue gas recirculation
2-1
-------
to the burner. See Figure 2.2. This feature, however, was not used during the
tests. Flue gas leaving the tube bank passes through a transition piece to a
15-inch-diameter vertical stack. Gas flow to the scrubbing system is taken from
the side of this stack. The vertical stack ends at a relief valve. The relief
valve is pneumatically operated and is automatically activated during a test if
furnace pressure becomes too great. The relief valve can also be operated
manually from the control panel and is used during startup and shutdown operations.
The furnace control panel is fully equipped to monitor and control the fur-
nace pressures. A 12-point Speedomax recorder provides a continuous check of the
temperatures within the furnace and ancillary components. Oxygen concentration
of the flue gas is continuously monitored by a Bailey 02 Analyzer Model A57.
Located on top of the furnace (Figure 2.2) is the steam drum, a steel cylinder
4-foot diameter by 6-foot long. This drum supplies water to the furnace water
jacket and acts as a steam-water separator for venting the steam to atmosphere.
2.3 FUEL
Two fuels were used cocurrently during the tests, pulverized coal and natural
gas. Pulverized coal was the main fuel while natural gas was used in the lighter
and accounted for about 4% (thermal) of the fuel used. A number of coal analyses
were run and the results reported in Table 2.1. A typical natural gas analysis
obtained from the Ohio Fuel Company is also shown in Table 2.1.
2.4 WET SCRUBBING APPARATUS
2.4.1 Particulate Scrubbing System
Flue gas leaving the furnace passed through the water tube section to the
particulate venturi and cyclone, see Figures 2.3 and 2.4. As the gas entered
the venturi throat, its velocity was greatly increased. It is here that the
fly ash slurry spray was introduced, just slightly ahead of the throat. The
fly ash particles traveling at high velocity impacted upon the slower moving
slurry droplets.
The fly ash slurry was separated from the flue gas in the cyclone
separator. The flue gas and slurry entered the cyclone tangentially, spinning
the slurry to the walls while the gases moved toward the center and out the
top. The slurry moved from the cyclone into the sump located immediately below.
The slurry was pumped from the sump and recirculated back to the venturi
spray nozzle. To maintain the desired composition, part of the slurry was
2-2
-------
discarded. Fresh water previously treated by a zeolite bed was added directly
to the sump and through the pump seal. Approximately 25 gal/min of slurry were
recirculated through the spray nozzle, and about 9 Ib/min were discarded as
particulate product.
The particulate venturi spray nozzle flow was controlled by the pump and
pinch valve. A pneumatically controlled pinch valve (Red Valve Company)
regulated the amount of "short circuit" recirculation through the pump and valve
loop. Closing the pinch valve forced more slurry through the spray nozzle.
This arrangement was used instead of the normal control method via a gate or
glove valve, because solids tend to collect behind the seat, thereby restricting
flow. The product flow rate was controlled by an overflow weir in the sump which
dumped slurry into a 55-gallon drum.
At the gas outlet from the particulate cyclone, the vortex spin was elimi-
nated by a flow straightener. This cross-shaped member 10 inches long by 10
inches in diameter was placed in the cyclone gas exit duct.
A gas sampling probe used for both NCL sampling and SO- sampling is positioned
4 inches downstream from the dust sampling connection. The probe includes a
6-inch long 1-3/4-inch pipe welded flush to the duct wall and a I/8-inch glass
tube located concentrically in this pipe. The pipe provides a "quiescent" zone
in which the gas flow to the glass probe is relatively slow. This minimizes
the possibility of slurry carryover from the cyclone entering into the glass
tubing which in turn could result in S02 and NOX sampling errors due to scrubbing
of the gas by the slurry in the probe.
2.4.2 Floating Bed Absorber
The floating bed absorber (hereafter referred to as the FBA) includes a
sump, two contact stages, and a liquid disengagement section. The FBA is depicted
in Figures 2.5 and 2.6. This countercurrent device admits the flue gas through
the sump. Ancillary components of the FBA sump include the following: a liquid
level controller, sump observation window, and level indicator.
Above the sump the FBA consists of two stages. Each tray has an effective
flow area of 2 square feet and consists of a 1/8-inch thick stainless steel plate
perforated with 3/8-inch-diameter holes on staggered 1/2-inch centers. Each
stage is packed with 6 to 8 inches of "wiffle balls."
2-3
-------
Hie spray nozzle located above the top tray directs the spray of absorbing
slurry onto the top tray. Since the gas rises countercurrent through the slurry,
it comes into intimate contact with the absorbing slurry. Gas leaving the top
tray flows through an angle iron baffle section which serves to trap large water
drops, then through a York Demister to ensure that all remaining droplets are
removed. The Demister is located at the very top of the FBA and consists of
about 6 inches of Teflon mesh fibers. See Figure 2.7.
Flow to the spray nozzle is controlled by the aforementioned pinch valve
arrangement, and the slurry composition in the sump is controlled by the product
flow rate and MgO makeup rates.
2.5 INDUCED DRAFT FAN SECTION
The cleansed flue gas leaving the FBA passes downward through a vertical
length containing an orifice meter, a gas sampling probe, and a particulate
sampling port with slide valve. The vertical duct ends at a blank flange.
Approximately 3 feet up from the flange is the takeoff for the induced draft
fan. The purpose of this length of pipe is to trap any large liquid or solid
particles before the gas enters the I.D. fan. A pneumatically operated damper
was located at the fan inlet.
2.6 NOx SCRUBBER AND COMPONENTS
2.6.1 N02 Injection System
The flue gas leaving the I.D. fan contained only small concentrations of
fly ash and SO-. However, the nitric oxide concentration (NO) was still at the
same level as in the furnace exhaust gases. The flue gas left the I.D. fan
through a horizontal 10-inch stainless steel (316) duct to the NOy scrubber.
At a distance of 6 feet from the I.D. fan, gaseous N02 was injected into the
duct through a multi-orificed dispersion tube. The purpose behind the dispers-
ion tube design was to disperse the gases as rapidly as possible to minimize
the probability of extraneous reactions occurring with the momentarily concen-
trated N0~ gas as it left the orifices of the dispersion tube. The NO, injec-
tion system is shown schematically in Figure 2.8 and consists of bottled liquid
NO- provided with an eductor tube so that the NO- could be withdrawn as a liquid,
a rotometer to monitor the liquid NO,, a steam-heated boiler to vaporize the NO-,
and the dispersion tube. Placed immediately after the dispersion tube, a
2-4
-------
6-1/2-inch inside diameter orifice was placed for the dual purpose of monitoring
the total flue gas flow and to act as a means for mixing the N02 with the flue
gas prior to entry into the NOX scrubber.
The boiling point for N02 is 70°F. Thus, the tendency to form gas bubbles
in the line ahead of the rotometer was an operating problem. This problem was
solved by packing the valve at the N02 bottle in ice thereby substantially sub-
cooling the NO-.
2.6.2 NOx Scrubber
The NCL scrubber was placed approximately 12 feet from the I.D. fan. A
dimensional drawing of the scrubber is shown in Figure 2.9. The basic criteria
for the design and location of this scrubber are as follows:
1. Provide maximum practical gas contact time.
2. Sufficient mass transfer surface area to maximize the probability
that the system would be chemical reaction rate controlling.
3. Open gas flow path.
4. Locate sufficiently far from the N0_ injection point to provide
good mixing before entry into the scrubber.
5. Locate out-of-doors as a safety precaution.
The scrubber was designed for a total gas contact time of approximately
two seconds. This is about three times the maximum gas qontact time employed
in the FBA. If the process still proves to be chemical reaction rate controlling,
then it shall be deemed as being commercially unfeasible.
The mass transfer area consisted of parallel fiber glass window screens which
were irrigated with MgO slurry by four Spraying Systems 2H560WSQ stainless steel
square-pattern spray nozzles. A screen material was selected because of its
superior wetting characteristics. The parallel arrangement provides for an open
free flow path for the gas.
Locating the scrubber out-of-doors helped insure that no personnel in the
test building would inadvertently be exposed to noxious levels of N02 which
might leak from the slightly pressurized scrubber. Views of the scrubber, both
internal and overall are shown in Figures 2.10 and 2.11.
2-5
-------
2.7 OVERALL PILOT PLANT SCHEMATIC
Figure 2.12 shows in schematic form the overall arrangement and the
approximate nominal flow rates of the various streams.
2-6
-------
TABLE 2.1. FUEL ANALYSIS
PULVERIZED COAL ANALYSES
Lab. Serial No.
Sample Description
Ash (Dry) t
Sulphur (Dry) t
Carbon (Ult.)$
C-13425
C-13426
Coal from
BCTU Hopper
3-9-70
2200 hrs.
9.6
3.8
Coal from
BCTU Hopper
3-10-70
1000 hrs.
9.2
4.1
C-13427
Coal
4.5
Lab. Serial No.
Sample Description
Total Moisture, %
Ash, %
Sulphur, %
Btu per Ib. (Dry)
Btu per Ib. (M§A Free)
C-13260
Pulv. Coal Sample
N. Industry Strip
3.0
8.1
4.1
12730
13850
C-13386
Pulverized Coal
Ohio Seam
4.2
3.8
12700
C-13377
Pulverized Coal
Ohio Seam
7.4
3.7
NATURAL GAS ANALYSES
Sulphur Compounds
Hydrogen Sulfide, gr/100 cf 0.017
H2S Sulphur Equiv., gr/100 cf 0.018
Mercaptans - S - Equiv. 0.007
Sulfide Sulphur, gr/100 cf 0.007
Residual Sulphur, gr/100 cf 0.004
Total Sulphur, gr/100 cf 0.034
Date of Sample
Components:
Nitrogen
Carbon Dioxide
Methane
Ethane
Propane
Iso-Butane
N-Butane
Iso-Pentane
N-Pentane
Total
Tennessee
Guernsey
2/12/69
Mol %
0.44
0.65
95.40
2.86
0.49
0.07
0.06
0.02
0.01
100.00
2-7
-------
FIGURE 2.1. MAGNESIA BASE SLURRY SCRUBBING PILOT PLANT
ts>
I
oo
NOX SCRUBBER
-------
FIGURE 2.2. BASIC COMBUSTION TEST FURNACE
to
I
to
STEAM LANCE
LOCATIONS
SAMPLE
LOCATION
DUST
SAMPLING
LOCATION
GAS
RECIRCULATION
DUCTS
-------
FIGURE 2.3. PARTICULATE SCRUBBING SYSTEM
PRODUCT
OISQiARGE
PARTICULATE
VENTURI
SCRUBBER
DUST SAMPLING
LOCATION
N02 INJECTION
TESTS ONLY)
OBSERVATION
WINDOW
PINCH VALVE
MAKE-UP
WATER
RECIRCULATION
PUMP
DRAIN
2-10
-------
FIGURE 2.4. PARTICULATE SCRUBBING SYSTEM
2-11
-------
FIGURE 2.5. FLOATING BED ABSORBER
MAKE-UP
WATER
DEMISTER SECTION
ANGLE IRON BAFFLE
SECTION
SPRAY NOZZLE
FLOATING BED
ABSORBER
SUMP LEVEL
CONTROLLERS,
SUMP
PROBE
DUST SAMPLING
LOCATION
» - OBSERVATION
WINDOW
PINCH VALVE
RECIRCULATION
PUMP
DRAIN
2-12
-------
FIGURE 2.6. FLOATING BED ABSORBER
2-13
-------
FIGURE 2.7. SLURRY ENTRAINMENT SEPARATOR SECTION
10" SCHD.
10 Pipe
V V V V V V
York Demister
2-14
-------
FIGURE 2.8. NQ2 INJECTION SYSTB1
Flue
Gas
N02 Liquid
Supply
NO
Gas Disper-
sion lube
Steam-
Heated Boiler
2-15
-------
FIGURE 2.9. NOx SCRUBBER DIMENSIONS
10" Duct
Four Nozzles
Each Covering
One Quadrant
Fiberglass Screen
12 on 3" Centers
Three 6" Ducts
10" Duct .
Distribution
Box
2-16
-------
FIGURE 2.10. NOx SCRUBBER
2-17
-------
FIGURE 2.11. NOx SCRUBBER AND LEACH BED
C-O
I
M
oo
-------
FIGURE 2.12. PILOT PLANT FLOW SCHEMATIC
PARTICULATE
SCRUBBER
S02
ABSORBER
ABSORBER
Stream
1 Makeup Water
2 Seal Water
3 Recirculated Spray
4 Product Fly Ash Slurry
S Flue Gas
6 Flue Gas
7 Makeup MgO Slurry
8 Seal Water
9 Product Slurry
Nominal
Flow Rates
Ib/hr
750
120
11,500
540
4,400
4,600
286
120
498
Stream
10 Recirculated Spray
11 Flue Gas
12 Makeup MgO
13 Seal Water
14 Recirculated Spray
15 Product Slurry
16 Flue Gas
17 Fly Ash Slurry Bleed
18 NO2 Injection
Nominal
Flow Rates
Ib/hr
2-19
-------
3.0 TEST APPARATUS AND PROCEDURES
3.1 PLANT OPERATING TEST PROCEDURE
A day's testing began with the startup of the furnace. First, the air
heaters were fired and allowed to reach temperature (^750°F). This usually
took an hour. The coal feed was then ignited. The furnace gases at this time
were vented directly to the atmosphere via the stack relief. A waiting period
of approximately 1 to 2 hours followed until the furnace ignition was stable.
While waiting for the desired furnace conditions, the particulate scrubbing
system and the FBA were being readied for operation. During this time the MgO
makeup slurry was prepared to the proper concentration. When the furnace was
ready, the relief valve was closed, thereby directing the flue gas to the
scrubbing systems.
After the transfer of gas was made, it usually took an hour after the MgO
makeup was started before the chemical composition of the FBA reached steady-
state. Steady-state was assumed when two or three Palmrose analyses taken at
10-minute intervals showed that the system had reached the desired operating
conditions and also when the S02 concentration at the pilot plant exit was
constant and less than 50 ppm.
The N02 scrubber was started by filling the sump with MgO slurry and re-
circulating the slurry. During the startup period no slurry was added nor
withdrawn. The N02 flow was set as soon as the NO concentration was known.
The liquid level was maintained at as low a level as was consistent with good
pump operation. This insured a more rapid approach towards steady-state. It
took at least one hour to reach steady-state in the MX, scrubber. A typical
test lasted for about an hour, during which a complete set of data was taken.
During a test several samples were taken and put into storage in the event
that they were needed at a later date. If certain data were found to be unusual,
an analysis of the stored samples could provide a means for determining what
occurred. Samples collected and stored in 8-ounce bottles consisted of the
following: MgO makeup slurry, particulate cyclone slurry, FBA slurry,
scrubber slurry, and a makeup water sample.
3-1
-------
After a test was completed, the operating conditions were changed for the
next test. Depending upon the operating parameter changed, there was usually
a waiting period of about 1/2 to 1 hour before steady-state was again reached
and the next test could begin.
3.2 FLUE GAS ANALYSIS
3.2.1 General Analysis
The method employed for S09 analysis was primarily the Barton coulometric
f3l
titrator as previously described.1 J The sampling arrangement is shown in
Figure 3.1. At the beginning of these tests a second approach for S02 analysis
was attempted. This involved the use of a DuPont 460 S02/N02 Analyzer. This
UV analyzer has been used successfully on in-plant experiments on a particulate
free synthetic flue gas. However, during this test the DuPont continuously
registered S02 concentration 150 to 250 ppm higher than the Barton. The dis-
crepancy was investigated by measuring the S02 concentration with the Reich
iodine titration method.^ The Reich method was found to agree with the Barton
titrator. The possibility that particulate matter was causing an S02 interference
on the DuPont 460 was then explored analytically. It was deducted that flue gas
containing 0.015 grains/DSCF and a IL- of 0.25 micron could produce the observed
discrepancy. These values are certainly within the range of possibility. Thus,
the DuPont was dropped as an S02 monitor.
Fly ash and SO, concentrations were not measured during this test program.
3.2.2 NQx Analysis
It is generally recognized that the measurement of the oxides of nitrogen
is a difficult task. The circumstance here was even more so since the split
between nitric oxide (NO) and nitrogen dioxide (N02) was required. To accomplish
this the following methods were specified:
1. Phenoldisulfonic acid (PDS) for NO + N02-
2. Saltzman for N02 only.
3. Dynasciences "Fuel Cell" for NO only.
It became evident, however, that neither of the latter two methods were
selective. The result of this situation was, therefore, to obscure the analysis
of the data. The application of these methods are described below.
3-2
-------
The PDS method was the primary means employed for determining overall
performance.
PDS analyses were taken at three points: the FBA exit, the NCL scrubber
inlet, and the NQ^ scrubber • exit. Figure 3.2 depicts the sampling locations
for all three locations.
A typical PDS sampling and analysis consists of the following. To a
1000 ml flask is added an absorbing solution consisting of hydrogen peroxide
and dilute sulfuric acid. The flask is then evacuated; a gas sample is now
ready to be taken. The line to the other analyzers is pinched off, and one
arm of the three-way stopcock is connected to the tee. The stopcock is opened,
and the gas sample is drawn into the flask.
The nitrogen oxides are converted to nitric acid by the absorbent solution
and are then reacted with phenoldisulfonic acid to produce a yellow compound,
which is measured colorimetrically. The color is measured with a photometer
and compared with calibration curves made with a solution containing a known
amount of nitrate.
A more complete and descriptive explanation of the phenoldisulfonic acid
method used in these tests is given in the American Society for Testing and
Materials, Standard Method of Test for OXIDES OF NITROGEN IN GASEOUS COMBUSTION
PRODUCTS (PHENOL-DISULFONIC ACID PROCEDURE), ASTM Designation: D1608-60. With
the exception of the following modifications, the ASTM Method was followed as
written:
Modifications to ASTM Method:
1. Absorbent Solution - 2 ml of Hfy (3%) was added to 50 ml of
0.1N H2S04. This is about four times the peroxide concentration
called for in the ASTM Standard.
2. In place of IN sodium hydroxide solution, IN potassium hydroxide
solution was used.
The Saltzman method of analysis employed for these tests is a modification
by Strom1- J which permits the use of the Saltzman method for high concentrations
of N02. A detailed description of the method is attached in Appendix A. The
3-3
-------
intent of the Saltzman method was to analyze for N02 only in the flue gas.
However, it became evident during the tests that both NO and N02 were being
analyzed. This observation was made in spite of the fact that Saltzman points
to the observation that NO does not interfere substantially with the analysis.
However, he did not perform his analysis with an NO-N02-N2 gas mixture but
rather with an NO-N2 mixture.
The Saltzman analysis for samples containing only N02 depends upon the
following two reactions proceeding at approximately the same rate:
NH, HON=N
2N02 + II +HN03 + K'Jl (3-1)
2N02 + 2 () -»• H20 + 1/202 + 2 ) (3-2)
SOjH SOjH
where the aromatic on the left is sulfonilic acid and the aromatic on the right
is the diazosulfonilic acid.
If the disproportionating reaction (3-1) was much faster than the
oxidation reaction (3-2), then one mole of N02 would produce only one half
the color as one mole of sodium nitrite. If the reverse were true; i.e., if
reaction (3-2) was faster, then one mole of NO- would develop the same color
as one mole of NaNO_. As Saltzman reports, however, both reactions are
significant and one mole of NO- yields only as much color as 0.73 moles NaNO—
Now in the present system with mixtures of NO and N02, a third reaction is
possible which makes it quite difficult to determine the sodium nitrite equiva-
lency for the mixture; namely,
H20
NO + N02 - N203 -* 2HN02 (3-3)
3-4
-------
Both nitrous acid anhydride (N20,) and nitrous acid (HNO,) are at the same
oxidation state. The extent to which reaction (3-3) takes place will affect
that equivalence between MX^ (NO + N02) and the sodium nitrite. For instance,
if equimolar quantities of NO and N02 were present in the sample when taken
and if reaction (3-3) predominated, then the NOx-NaN02 equivalence would, of
course, be unity. Since reaction (3-3) is a gas-phase reaction while reactions
(3-1) and (3-2) are aqueous reactions, it is quite possible that reaction (3-3)
does indeed predominate. Table 3.1 summarizes the expected sodium nitrite
equivalence for various ratios of N02/N0 assuming reaction (3-3) is far faster
than the other two reactions. For example, if 15 minutes elapsed between the
time that a sample containing 600 ppm NO is drawn and the time that the sample
is analyzed, 84% of the original NO can be oxidized to N02. See Figure 3.3.
It is apparent from Table 3.1 that unless some aleternate means is avail-
able to determine the NO-/NO ratio, the correct equivalence, C , cannot be
L eq
assigned. There are fortunately means available by which the ratio can at
times be estimated as will be shown later.
Finally, since the gas sample is injected into the septum bottle, which is
filled with air, significant oxidation of the NO can take place by the time the
sample was analyzed.
The Dynasciences NX-130 monitor was employed with the hope of being able
to monitor only NO from the MX, mixture. Refer to Figure 3.2 for a description
of the sampling arrangement. Although this monitor is designed to measure both
NO and N02, it was hoped that by passing the flue gas through Mallcosorb the N02
could be quantitatively removed. As was evident from the tests, this was not
the case. Specifically, when monitoring flue gas at the FBA exit and the MX,
scrubber inlet with N02 being injected in between, the apparent NOy concentration
increased substantially. With a bias voltage of 0.4 volts across the fuel cell,
the relationship between monitor response and gas composition is as follows:
H 0.53
where y^~ = apparent NOy concentration, ppm by volume
yNO = N0 concentrati°n» PPm ty volume
= N02 concentration, ppm by volume
3-5
-------
Thus, unless the ratio of NO to N02 is known the NX- 130 monitor output is
difficult to translate. It is known, however, from combustion kinetics that the
NOX split at the furnace exit is essentially all NO. However, given sufficient
time and oxygen within the flue gas, the NO will partially oxidize to N02. Like-
wise as N02 forms it can further react with NO to form N203 and/or HN02, the
latter constituent very likely being removed in the Mallcosorb.
To investigate the above question the following analysis is presented.
Since the N203 formation is probably much faster than the NO oxidation, an
equilibrium conversion of N203 (HN02) can probably be assumed. It would follow
then that if we started with 600 ppm NO (at furnace exit) and assumed also that
the flue gas contains 3% oxygen, then by the time the flue gas passed to the
FBA exit sampling point and through the sample line to the Mallcosorb at the
NX-130 monitor, a period of ^ 60 seconds, ^ 20 ppm N02 could have formed (see
Figure 3.4). At 80°F about 16 ppm HN02 could also have formed (see Figure 3.5).
The HN02 would most likely be removed in the Mallcosorb. Thus, the NX-130 would
have registered as follows:
" 20) + (°-53)C21 • 16/2) = 587
This is an error of only 2%. However, when the NX-130 is monitoring the NO, NO,,
H20 mixture at the NC^ scrubber inlet and exit, the potential for erroneous
answers is substantially increased. For instance, assume the following typical
condition :
[NO] = 600 ppm
[N02] = 600 ppm
[H20] = 15.11 at 130°F
= 6.5% at 100°F
TEMP. BULK GAS = 130°F
TEMP. SAMPLED GAS = 100°F
3-6
-------
From Figure 3.5 the equilibrating HN02 is 106 ppm and 148 ppm at 100°F and 130°F
respectively. Since the HN02 will be absorbed into the Mallcosorb at 100°F, the
apparent NOY on the NX- 130 will be:
A.
£ = (600 - 106/2) + (0.53) (600 - 106/2) = 573.5 + 303.5 = 837 ppm
This amounts to an error of 30%.
The net result of the discussion presented above is that because of several
measuring problems, a significant uncertainty exists in all the NO,, values with
the possible exception of the PDS method. That is, there is no interpretive
problems with the PDS method except for its usual characteristic scatter.
In summary, the NO analyses will be interpreted in this report as follows:
1. PDS: Standard Procedure.
2. Saltzman: The nitrite equivalence (C ) will be assumed to equal 1.0.
eq
3. Dynasciences NX-130: Valid only on NO- free samples.
3.3 LIQUID ANALYZER
The sulfite, MgO, and suspended solids analysis procedures performed on all
three process streams were identical to those used during the previous work. ^
No sulfate analyses were performed on the FEA product. However, sulfate, nitrite,
and nitrate analyses were all performed upon the MX, scrubber recirculated slurry.
The sulfate analysis used was the standard gravimetric analysis of precipitated
barium sulfate. The nitrite analysis was the ASTM method D-1254-67. Finally,
the Brucine Alkaloid Method was used for the nitrate analysis.
3-7
-------
TABLE 3.1. SODIUM NITRITE EQUIVALENCE
FOR MIXTURES OF NO AND N02
N02/N0 Ceq
> 1.0 (excess NO) 1.0 (excess NO will be missed)
1.0 1.0
1.2 0.975
1.4 0.955
» (no NO) 0.73
3-8
-------
FIGURE 3.1. S02 SAMPLING SYSTEM
O-J
i
vo
NOv SAMPLLS'G
LOCATION
NOX SAMPLING
LOCATION
S02 PROBE
AT PILOT PLANT
EXIT
S02 PROBE
iT PARTICULATE
'CLONE EXIT
EXCESS SAMPLE
i GAS VENT
f!
SOT PROBE
AT FURNACE
EXIT
BUBBLE
TUBh
BARTON
TITRATOR
CONDENSATE TRAPS
-------
FIGURE 3.2. NOy SAMPLING SYSTEM
04
I
I-"
o
r
Fuel I R U
Cell [—' |J ]__
n
D
-\ DuPont
t
Saltzman Sampling Location
Fuel Cell Sampling Location
Control Valve
-------
FIGURE 3.3. NO OXIDATION RATE IN AIR
T=130°F 100°F 70°F 40°F
1000
900
800
I
o
•-j
OJ
in
t
8
0)
700
600
500
O-
S =>
O •
0.2
0.4 0.6
Fractional NO Conversion
0.8
1.0
3-11
-------
FIGURE 3.4. NO OXIDATION RATE IN FLUE GAS
T = 130°F
100'
S!
i
H
I
H «
0?
t- u
O?
"" o
Ox
yu
oU
-
/u
in °° T
•3
C
0
o
2
4j
•H 50 — --£-
iz
01 IL
"7
C '
•8 .- j~ . --
rH ^ 2
m y ^ 131
« : "ti tt
12 in " t Z 10
/ /i
" ?I tl
i if J 1
i / J
if f
30 ?--? -2
-i r -±f-
i-~j- ' z
' i E: :z_:
' j_i?-iijj_niii?
_j / £_ \ A
i j z rx^i
, r . >r
">A /. J J > . ,
ZU- — "-r- -f jf
it Zi! :ii _
1:7 /
~ t f j 2-1
j.j .f 2 i
2 f 2 "? J
3 j j ^
in ' L _^ ^
2 ^
[ j y j ^
I 5 j j
I \Af 4
\ jy X /
| Jy V
JHr
^Pr
£ ^ 1
1
.
/
/ i/
_j_j
4 t
j
/ r
' j
2 "L
2
2 .
j / .
/ r
V 7 . .
- ^
-J -
- / -- 71
T- t ? ::___>
J ^
/
y
i/
^
-t -t - (I ^
t f /!;,.,
_L J J J _J [_
. [ - _ ? _U
, / /
7 ^^ y
:_ t -,
t -^Tv 2 _-
j i _L > ; i
t / >
j ' r
: ? ::? ,2 ;iji
It
A
* ' _.f j :_____.,
:2 ::;: : :-?!
/ x r
J _L ,-J - - , --
/ i / - ?-
^ / ^
M~ X " ?
Z T - ??
""j ' r
/ r
j " /
/ X
^ ^^
X
/
r
r
"L ^ '
Re
_+_ — _ _ jn;
n
II - 2
^~ IT NO
E
^
, '
J
r^
7
y
r
V
^i
ference 12
Ltial Cond.
= 3%
= 600 ppm
±H±tt ± lii
I
/
^
^
^
^-
|
1 1 1
/
--
_-
0°F
0°F
1.0
2.0 3.0 4.
NO Conversion
5.0
6.0
3-12
-------
FIGURE 5.5. EQUILIBRIUM HN02 CONCENTRATIONS
n .
O-
r- =.
O •
51
i 8
U I
Pi i
l-u J
o? 5
"° !
X - *
O*
=190°F
160°F
:. 130°F
Reference 10
Initial NO Cone. = 600 ppm
Gas Saturated with
600
Initial N02
800 . - 1000
Concentration
3-13
-------
4.0 RESULTS
Since the singular purpose of these tests was to evaluate the feasibility
of NOX absorption in flue gas containing dilute concentrations of S02, the NCL
scrubber system was the only equipment which was subjected to variable control.
The remainder of the pilot plant was maintained under constant operating condi-
tions. However, some pertinent observations were made with regards to the rest
of the system. Therefore, before reporting on the results of the NO^ scrubber,
the operation and observation of the particulate scrubber and FBA will be reported.
All of the computerized data and results are included in Appendix B.
4.1 OVERALL RESULTS
4.1.1 Particulate Scrubber
The particulate venturi scrubber was operated at about 5 to 6 inches w.g.
over the entire course of these tests. The liquid spray rate amounted to 20
f71
gal/MCF. These conditions are comparable to the previous tests.L J S02 per-
formance was also similar. The only difference observed was that while previously
the slurry pH varied from 2.0 to 3.5, during these tests the pH varied from 4.0
to 5.5. This is probably due to the presence of an alkaline constituent in the
ash.
4.1.2 FBA
(81
During the previous work*- J the FBA was the major subject of study. During
the present program its sole function was to reduce the SO- concentration to be-
low 50 ppm. To accomplish this a set of operating conditions were specified as
follows:
Slurry pH Greater than 7.0
Liquid-to-Gas Ratio Greater than 4.0 Ib/lb
Unslaked MgO was used exclusively and at a sufficient rate that the pH was
maintained at about 8.0. Fly ash slurry from the particulate scrubber was
added intermittently. This was done because during the previous work the presence
of fly ash in the slurry prevented the formation of deposits in the sump and
piping of the FBA. The results of operation of the FBA in this fashion are as
follows:
4-1
-------
1. Exit SO- concentrations were at all times less than 50 ppm. The
nominal value was 14.2 ppm.
2. Although no deposition problems were experienced in the FBA piping,
for the first time deposition occurred on the underside of the bottom
tray. This condition was severe enough to completely close the tray
holes. To a lesser extent deposition also began on the underside of
the top tray. This material was analyzed by X-Ray diffraction analysis
and the results given in Table 4.1. The only identifiable operating
difference is the continuous operation at elevated pH's (MJ.O).
Only intermittent operation under these conditions was covered in the
previous tests. A photograph of the deposit is shown in Figure 4.3.
4.2 NO SCRUBBER RESULTS
4.2.1 NO Absorption
Because of the analytical problems described in Section 3.2.2, discrimina-
tion of the data and evaluation of the degree to which NO^ was absorbed is quite
limited. Table 4.2 shows the parameters which were tested and also depicts the
run number designation used here. That is, the tests were numbered successively
but were assigned a letter which depicts the condition which was to be set up.
For instance, Run 10-G was the tenth test and was specified to evaluate NO^
absorption at test condition G in Table 4.2.
The primary results can be summarized as follows:
1. Under none of the conditions tested was any significantly observable
reduction in NOy concentration experienced across the NO,, absorber.
2. The NOL scrubber operated without difficulty except for a consider-
able degree of carryover leaving the top of the scrubber. For a
period, this carryover affected the analysis by creating a difficult
sampling situation.
All of the major results are summarized in Table 4.3. The most interesting
factor to note is the NO^ measurements by the NX -130 and the PDS. The former
analysis depicts a reduction in NO^ concentration in several tests. Significantly
the PDS method not only does not indicate the same reduction but in fact indicates
an increase NO^ concentration across the scrubber in several instances. This
probably is due to the variance in the PDS method.
4-2
-------
4.2.2 S02 Absorption
After several of the scheduled tests were completed and the lack of
performance was evident, the suitability of the design of the NO^ scrubber became
a concern. To evaluate the scrubber design a test was run whereby the scrubber
could be evaluated as a sulfur dioxide absorber. This was accomplished by
operating the FBA deficient of MgO. Flue gas containing 1350 ppm S02 entered
the NOy scrubber. No N02 was added to the flue gas. The results are shown
in Figure 4.2. These results reveal several facts. First, the K a for S02
absorption although only about one third as great as for the FBA is still
adequate to produce large and measurable changes in SO- concentration. Secondly,
the fact that SO- absorption changed significantly with changes in the liquid
spray rate means that either the wetted area changes significantly with the
liquid spray rate or that a significant liquid-phase effect is present. This
liquid-phase dependence could be either the liquid-phase diffusion coefficient
k- or a reaction rate effect such as the following:
MgO, , + H-0 -»• Mg+* + 20H~ (4-1)
V.SJ L
SO-'H-O + 20H~ ->• SO-= + 2H-0 (4-2)
Reaction (4-1) represents the dissolution of MgO which could be the
limiting step in either the S02 absorption or NOX absorption systems.
Although no data exists with regards to the diffusivity of HN02 in the
gas phase, if it does not differ greatly from S02 (by a factor of 2 to 3),
then the SO- results will be useful in interpreting the NOjj results as will be
shown in the following section.
4-3
-------
TABLE 4.1. ANALYSIS OF DEPOSIT SAMPLES
Chem Lab No. M-24801 M-24802 M-24803
Sample Description Soft Sample Incipient Bulk Sample
from Center Deposit from from Edge
Corner
X-Ray Diffraction
(Crystalline Constituent)
Major MgS03-6H20 MgS03-6H20 MgS03-6H20
4-4
-------
TABLE 4.2. PARAMETER STUDY SPECIFICATIONS
Recirc.
Test Slurry
Condition N02/NO L/G Stoich. Cone. Load Number Tests
A 1.
0 15 1.
B 0.7
C 0.0
D 1.3
E 1.0 10
F
G
H
I
J
K
5
i
15 2.
i
5 2.5% 100% 4
0
3.0
1.5 5
i
10
1
2
1
1
1
1
1
1
1
2.5 50 2
16 Two Tests/Day
4-5
-------
TABLE 4.3. SUMMARY OF RESULTS
I
O\
Test Nunber
NOx by PDS
FBAExit
NOx Scrubber Inlet
NOx Scrubber Exit
NOx by Saltzman
NOx Scrubber Inlet
NOx Scrubber Exit
NOx by Fuel Cell
Furnace Exit
FBA Exit
NOx Scrubber Inlet
NOx Scrubber Exit
Ratio N02/N0
PDS
F.C. 5 Rotameter
SOZ by Barton
Furnace Exit
Paniculate Scrubber Exit
FBA Exit
K>X Scrubber Exit
Gas Residence Time, sec
Gas Velocity, fps
L/C, Ib/lb
Ratio Nitrite/Nitrate (LioJ
Flue Gas Flow Rate, Ib/hr
1-C
124.8
233.4
209.1
870.3
902.0
6S6.0
635.2
0.87
0.00
1007.6
1138.6
10.3
6.0
Z.22
1.8
21.4
11.739
5508.0
2-A
420.7
1122.1
901.3
876.9
485.8
485.8
803.4
308. 3
1.67
2.29
1862.4
1720.0
3.S
2.10
1.9
19.2
O.S34
3913.0
3-E
969.3
1180.9
930.3
986.7
485.6
504.3
644.4
SS1.1
2.24
1649.6
9.4
2.22
1.8
13.6
1.632
3748 0
4-F
502.4
759.5
855. 0
613.9
7S1.1
561.9
486.9
580.6
299.7
0.51
1.55
1538.4
1431.0
10.3
2.32
1.7
8.5
3.857
3S41.0
5-K
589.4
671.3
920.6
901.6
1226.1
588.1
559.6
777.8
398.4
0.14
1.45
2.50
1.6
12.5
6.000
3260.0
6-L 7-C
S63.4
504.1
550.4
324.2
311.1
733.2
695.6
714.4
629.8
-0.11
0.00
1799.0
1614.5
1308.8 21.2
22.8 8.3
2.10 2.22
1.9 1.8
19.1 19.9
0.000
3927.0 3772.0
8-B
580 .4
906.0
947.5
802.1
566.9
759.6
873.6
1688 7
1557.1
13.2
2. 22
1.8
20.2
6.533
3719.0
9-D
1026.2
717.5
937.1
857.8
773.6
698.0
698.0
4.2
2.22
1.8
20.2
41.333
3715.0 '
10-G
608.8
766.0
1709. S
680.8
491.6
692.4
645.6
729.9
6SS.O
0.26
0.65
1783.4
1595.7
4.1
2.22
1.8
19.9
9.167
3761.0
11-H
469.5
913.9
274.1
696.2
509. 7
748.7
664.4
786.1
505.3
0.95
0.65
1801.2
1479.5
30.9
2.22
1.8
20.3
4.407
3688.0
12-A
501.6
762.0
442.0
748.6
655.0
842.2
617.6
0.67
1741. S
1479.5
30.9
2.22
1.8
20.4
4.321
3684.0
13-A
580.9
525.8
580.3
662.5
256.4
674.2
730.4
664.8
725.7
-0.09
0.63
1713. S
1116.7
8.5
2.32
1.7
22.0
5.889
3466.0
14-1
528.6
1310.9
1076.8
689.1
492.4
648.7
614.9
1.48
0.76
1704.6
1587.7
2.0
2.32
1.7
22.0
5.750
3460.0
15-A
547.5
971.8 '
1136.4
694.9
471.8
785.5
835.8
795.6
84S.9
0.78
0.59
1675.5
1369.9
18.4
2.32
1.7
21.5
6.833
3518.0
16-K
627.7
866.3
886.4
642.5
449.4
715.7
403.2
846.8
514 1
0.33
0.92
1643.2
14.2
3.08
1.3
17.6
6.000
2726.0
17-J
576.6
1194.6
1223.1
609.6
451.1
815.7
704.9
856. 0
916.4
1.07
0.70
1951.5
1692.4
18.9
2.32
1.7
21.8
4.674
3466.0
-------
FIGURE 4.1. DEPOSITION ON UNDERSIDE OF FIRST FBA STAGE
-------
FIGURE 4.2. S02 ABSORPTION IN NOx SCRUBBER
Inlet S02 Cone: 1350 ppm
Gas Flow = 4200
-------
5.0 DISCUSSION
The purpose of the program was to experimentally study the feasibility of
absorbing NOj^ into magnesia slurry. Since the results were largely negative,
the task remaining is to establish the degree to which these results reflect
upon the general feasibility of NO^ absorption by wet scrubbing. That is, it
can certainly be concluded that NO^ absorption into MgO in the apparatus tested
is unsatisfactory and is therefore not a feasible approach. However, to what
extent does the equipment design and the choice of alkali affect the feasibility
of NO^ absorption by alkali scrubbing?
To approach this question a mechanism for this absorption must first be
postulated. The model for which this research work was based and which is still
felt to be valid is presented here.
It is well known that NO absorption into any aqueous medium is very slow
owing to its extremely low solubility in water. Secondly, several people have
studied N02 absorption, particularly with respect to nitric acid manufacture.
Absorption is known to diminish rapidly with decreasing NO- partial pressure.
N02 absorption efficiency greater than 50% is difficult to attain when inlet
NO 2 concentrations are less than 1000 ppm. However, several experimenters
have noted that NQ^ absorption is enhanced when equimolar concentrations of NO
and N02 are present in the gas phase. Quite obviously any absorption enhance-
ment must be the result of a reaction between NO and N02 forming a substance
more readily absorbed than either of the two reactants. That reaction is
believed to be the following:
NO + N02 + H20 ->• HN02 + HN02 (5-1)
In the wet scrubbing environment water vapor is present at very substantial
levels. The above reaction probably takes place in two steps:
NO + N02 + N203 (5-2)
N203 + H20 ->• HN02 + HN02 (5-3)
5-1
-------
Little is known of the kinetics of reaction (5-1) except for the work done
by Wayne. ^ ' He studied the formation of HN09 at 25°C and found the forward
/I O 1 ™
rate to be k£ = 7.4 x 10 atm sec . Therefore, equimolar concentrations of
NO and N02 initially at 1000 ppm each in a flue gas saturated with water vapor
at 130°F and assuming that kf equals its 25°C value, it would take 1.6 seconds
to reduce the NO + N02 concentration to 200 ppm total. This conversion time is
the first clue as to the contact time required for an NO^ scrubber relying on
reaction (5-1).
However, gas-phase kinetics are not the only factor of importance in this
system. First, it should be noted that chemical thermodynamics show that reac-
tion (5-1) is reversible and in fact in the conditions under question conversion
is relatively low (5 to 151) . This means that the HNO- concentration driving force
for mass transfer will be severely limited. Finally, the gas absorption mass
transfer rate of HN02 into the alkali solution can easily be limiting by this
system for any one of several reasons. The first is quite obviously the small
gas-phase driving force available; the second is the possible N?gO dissolution
lags; and the third follows from the long gas side residence times required
which necessitates low gas Reynolds numbers which in turn create poor gas side
mixing and mass transfer conditions.
The material balances for NO, N02, and HN02 across an element of volume
as shown in Figure 5.1 lead to the following set of equations:
For HN02,
dy, , f k, a
• ri - T*- <*i - »
5 \ o
ar i
\
For NO,
For N02,
(5-6)
g
5-2
-------
where y, = HNCL molar concentration = P-i/PT
y, = NO molar concentration = P2/PT
X3 = NO. molar concentration = P3/PT
v = gas velocity, ft/sec
r, = kinetic rate of formation of HN02
p = molar density of bulk flue gas
g 73
a = specific mass transfer surface area, ft surface/ft scrubber volume
k, = gas-phase mass transfer coefficient for HN02
2
= gas -phase mass transfer coefficient for
y? = HNO- gas concentration at the gas-liquid interface
y* = NO, gas concentration at the gas -liquid interface
Now the kinetic rate of formation of HN07 is developed as follows :
Forward reaction:
ar
= k
Forward
H
(5-7)
Reverse reaction:
ar
Reverse
(5-8)
where K = .-=- = equilibrium constant
k = reverse reaction rate constant
H = molar water vapor concentration
H - - yi2
eq
(5-9)
5-3
-------
Several factors are significant from these equations (5-4) through (5-9).
From equations (5-4) and (5-9) it is seen that if kf is fast enough to maintain
instantaneous equilibrium then the limiting factor will surely be the mass trans-
fer rate. The maximum value of y, will be the equilibrium value.
From equation (5-5) it is seen that the only mechanism for reducing the NO
concentration is to form HN02 which means, of course, that it is dependent on
both the reaction rate and the mass transfer rate of HN02-
Equation (5-6) accounts for the fact that N02 can absorb directly in alkali
solution. N02 absorption would be detrimental to the process in question since
it would defeat the purpose of injecting N02 into the flue gas in the first place.
Since experience has shown equimolar N0-N02 absorption to be superior to N02
absorption alone, it is evident that N02 absorption must be substantially greater
than k, . It would seem more likely that since N02 is substantially less soluble
in water than HNCL, then it follows that y2 - y£ must be small compared to
yT - y* (in spite of the small value of y^. The relative degree to which these
two constituents were absorbed in the present experiment can be examined from the
product liquid analysis. N02 absorption will produce equimolar quantities of
nitrite (N02) and nitrate (NO^) in solution while HN02 absorption will produce
only nitrite. See Table 4.2 for this ratio (NO^/NOJ). These results confirm
that HNCL was the predominant species absorbed.
To apply the above model to the present experimental situation, the following
simplifying assumptions were made:
1. N02 absorption was negligible relative to HN02 absorption (supported
by liquid analysis).
2. y? = 0 (no liquid film or reaction effects). This is a weak assump-
tion but will provide a limiting solution to the present case.
3. The geometry depicted in Figure 5.1 was used.
4. The surfaces were assumed to be fully wetted.
The model was applied to typical operating conditions as follows:
5-4
-------
v = 2 ft/sec
T = 130°F
H = 0.151 moles water vapor/mole wet gas
p = 0.00232 Ib moles/ft3
Kg = 0.465 atnf1
a = 10 ft2/ft3
Hie mass transfer coefficient k, was determined from the Sherwood equation
where:
v n n97 v °-8 N °'44 = ^
WSH " u'u" wRe WSC Df
NRe ' 248°
Nsc = 0.94
.'. NSH = 10.6
D = 0.25 ft
eq 2,
D = 0.2 cm /sec
kc = 4.56 x 15"3 ft/sec
kx = 0.0764 Ib mole/hr ft2
Equations (5-4) through (5-9) were solved by numerical integration on an
IBM 360 computer and showed that NCX, absorption would only be 2% for this case.
The calculated k a is only 0.764. This is an extremely low mass transfer
coefficient. However, from the single S02 absorption experiment it is possible
to obtain a measured value of k a for this device. For comparable liquid recir-
culation rates the S02 experiment demonstrated a k a equal to 15.8 Ib moles/
hr ft3. Adjusting for differences in the expected diffusivities, the kga for
HNO. absorption would be as follows:
5-5
-------
D,
'S02
15.8
0.20
0.138
= 23.0 Ib moles/hr ft
3
This k a is nearly 30 times larger than that calculated from theory. This is
obviously a better measure of k a than the theoretical value. However, for this
condition the NOy absorption should have been 331. For this magnitude of
reduction, the measured change in total NCX, concentration across the scrubber
would surely have been apparent in spite of the analysis difficulties. The
conclusion to be drawn here is that a significant liquid film resistance must
be present in the HNO, absorption situation. That is equivalent to saying that
y? is not negligible. To include y? as a system variable would greatly increase
the complexity of this model because it would require the coupling on liquid side
material balances, liquid side diffusion equations, and liquid side chemical
reaction kinetics. If it can be assumed that y? is a linear function of y, for
a fixed set of liquid and gas flow rates, then the k a in equation (5-4) will be
reduced by a constant and the solution to these equations will still be valid.
To evaluate the expected NOjj absorption performance over a broad range of
k a's and k^s, this model was applied to the subject scrubber geometry and the
results plotted in Figure 5.2. From this figure and from some facts regarding
the process material balance, the potential feasibility of NO*, absorption in
the subject apparatus can be established. First, consider the flow sheet in
Figure 5.3 which depicts the minimum unit operations required of the process.
The process design established the criterion that the N02 flow to the flue gas is
just sufficient (no excess N02) to produce an equimolar quantity of NO and N02.
Then the minimum NO^ absorption efficiency which will produce a self -sustained
supply of NO- is 75%. This, however, will produce an overall NO^ efficient of
only 50%. The NOjj concentration leaving the scrubber which will be acceptable
to regulating agencies in light of the fact that 50% of the N02 would leave as
N02, is highly questionable. Deferring the above question and addressing the
question to technical feasibility only, the 75% absorption efficiency is the
minimum acceptable scrubber performance. Then from Figure 5.2 it is seen that
A *} T
for kf = 7.3 x 10 atm sec , the k a will have to be in excess of 72 Ib moles/
hr ft3. This is as much as 100 times the apparent k a. There appears to be no
o
5-6
-------
physical manner in which sufficient contact surface area could be packed into
a scrubber of this type to increase the k a appreciably. It would appear that
o
the system is liquid film mass transfer or chemical reaction rate limiting and
at least for the MgO base, would probably not perform even under very extreme
design changes. If the MgO dissolution step is the limiting factor, then for a
soluble base such as sodium carbonate the apparent k a would only need to be
increased from 23 Ib mole/hr ft to 72 Ib mole/hr ft*. This is certainly a
feasible physical possibility. For a soluble base, a packed tower seems to be
the most appropriate device for this function.
Summarizing, it is concluded that NOy absorption into a slurry of MgO is
not a technically feasible approach for power plant application within the con-
fines of reasonable equipment design. However, based upon the arguments presented
above, it is quite possible that NO^ absorption into a soluble alkali base may
be feasible. The appropriate apparatus would seem to be a conventional packed
tower.
A final factor which can be drawn from the above analysis is that the absorp-
tion process can be highly temperature dependent. Increasing temperature will
increase the water vapor concentration, the forward reaction rate constant, the
equilibrium conversion of HN02, and finally the gas-phase diffusion coefficient.
All of the above, of course, will increase HNO- absorption.
5-7
-------
FIGURE 5.1. GEOMETRY ASSUMED FOR NOx ABSORPTION
Z = ZT
Z = 0
t
I
Gas Flow
Spray Nozzles
' / Parallel
( Falling
Films
\
' )
dZ
5-8
-------
K
^ SEMI-LOGARITHMIC 46 5893
* CYCLES X 60 DIVISIONS MADE IN u S.K.
l/i
atnf sec
FIGURE 5.2. PREDICTED NOx ABSORPTION IN TEST APPARATUS
Gas-Phase
Diffusion
Limiting
Gas-Phase
Reaction Rate
Limiting
m 14.6 xlO4
JJ1L
Total Height = 4 ft
Temp. = 130°F (saturated to H20] -j!
Initial NO: 600 ppm
Initial N02: 600 ppm
Initial HN02: 84 ppm
Minimum Self Sustaining
Absorption Rate
Maximum
Probable
for This
Apparatus
Apparent
MgO-NOx
Range
"I'D So. o
k a, Ib moles/hr ft'
O
-------
FIGURE 5.3. PROCESS FLOW SCHEMATIC
Absorber
NO, N02
Absorber: NO + N02 + MgO -»• Mg(N02)2
Nitrator: 3Mg(N02)2 + 2H20 •*• 4NO
ZMg(OH)
Absorber Efficiency
Process Efficiency
75*
50
80
60
85
70
90
80
95
90
99
98
* Minimum acceptable performance for self sustaining N02 supply.
5-10
-------
6.0 CONCLUSIONS
1. NOX absorption with equimolar concentration of NO and N02 into MgO slurry
is unfeasible in the apparatus tested. It is probably unfeasible in any
practical gas-slurry contacting apparatus.
2. N0y absorption into soluble alkalis may be feasible and would best be done
in packed towers.
6-1
-------
7.0 RECOMMENDATIONS
1. MgO slurry should be removed from those bases being considered for aqueous
NOy absorption.
2. Work should continue on the feasibility evaluation of soluble bases for
this system.
jlz Submitted by: W^lCj&VTW/&,
W. Downs I* v
Approved by:
H. P. Markant
7-1
-------
REFERENCES
1. W. Downs and A. J. Kubasco, "Magnesia Base Wet Scrubbing of Pulverized
Coal Generated Flue Gas - Pilot Demonstration," Final Report to NAPCA
under Contract CPA-22-69-162, Alliance Research Center Report 5153,
pp. 2-1 through 2-17, September'28, 1970.
2. Ibid., p. 2-1.
3. Ibid., p. 3-3 through 3-5.
4. Ibid., p. 3-5 through 3-6.
5. S. S. Strom, "Catalytic Reduction of Nitrogen Dioxide with Ammonia," MS
Thesis, University of Cincinnati, June, 1966, pp. 18-22.
6. W. Downs, op. cit., pp. 3-11 through 3-15.
7. Ibid., p. 4-1, pp. 4-13 through 4-14.
8. Ibid.
9. Ibid., p. 4-8.
10. L. G. Wayne and D. M. Yost, J. Chem. Phys. 18, pp. 767-768, 1950.
11. B. E. Saltzman, Anal. Chem., 26, No. 12, pp. 1949-1955, December 1954.
12. U. S. Department of Health, Education, and Welfare, Public Health Service,
Selected Methods for the Measurement of Air Pollutants, PAS Publication
No. 999-AP-ll, 1965, pp. C1-C7.
R-l
-------
APPENDIX A
DETERMINATION OF NOX: SALTZMAN METHOD
-------
APPENDIX A
DETERMINATION OF NO^ SALTZMAN METHOD
Introduction
The Saltzman method is intended for the manual determination of nitrogen
dioxide in the atmosphere in the range of a few parts per billion (ppb) to
about 5 ppm by changing the sample size, though the range can be increased to
about 10,000 ppm. This method is also applicable to the determination of nitric
oxide after it is oxidized to nitrogen dioxide. The nitrogen dioxide is absorbed
in Griess-Saltzman reagent. A stable pink color is produced within 15 minutes
and may be read visually or in an appropriate instrument. Only slight interfer-
ing effects occur from other gases.
Reagents
All reagents are made from analytical-grade chemicals in nitrite-free water
prepared, if necessary, by redistilling distilled water in an all-glass still
after adding a crystal of potassium permanganate and barium hydroxide. They are
stable for several months if kept well stoppered in brown bottles in a refrig-
erator. Ihe absorbing reagent should be allowed to warm to room temperature
before use.
N-(l-Naphthyl) - Ethylenediamine Dihydrochloride. 0.1%
Dissolve 0.1 g of the reagent in 100 ml of water. This is a stock solution.
Sulfanilic Acid, 0.5%
Dissolve 5 g of sulfanilic acid in almost a liter of water containing 140
ml of glacial acetic acid. Gentle heating is permissible, if desired, to speed
up the process. Cool and dilute to 1 liter with water.
Absorbing Reagent
Add 10 ml of the N-ethylenediamine dihydrochloride stock solution to a
500-ml volumetric flask and dilute to mark with the 0.5% sulfanilic acid. Mix
just before use and discard at end of each day!
A-l
-------
Standard Sodium Nitrite Solution. 0.0203 g/Liter
One ml of this working solution produces a color equivalent to that of 10
ml of nitrogen dioxide (10 ppm in 1 liter of air at 760 mm of mercury and 25°C).
Prepare fresh just before use by dilution from a stronger stock solution con-
taining 2.03 g of the reagent grade granular solid (drying is unnecessary) per
liter. The stock solution should be stable for 90 days.
Apparatus
Spectrophotometer or Colorimeter
A laboratory instrument suitable for measuring the pink color at 550 mm,
with stoppered tubes or cuvettes, is recommended.
10 or 20 ml Gas Tight Syringe
Hamilton type, for measuring gas samples.
100-ml Serum Bottle
Needle-puncture rubber stoppers, sleeve type, for serum bottles.
Analytical Procedure for Nitrogen Dioxide
Sampling Procedure
Pipet exactly 10 ml of absorbing reagent into a serum bottle and stopper
bottle with rubber stopper. Inject 10 ml of the sample gas with the syringe
and shake bottle vigorously. If the gas sample has an expected concentration
of about 500 ppm, a 10-ml gas sample will yield an absorbance very near the
standard. If the concentration is higher, use a smaller sample proportionally.
If the gas sample temperature and pressure deviate greatly from 25°C and 760 mm
Hg, measure and record the values.
Determination
After collection and absorption of the sample a pink color appears. Color
development is complete within 15 minutes at ordinary temperatures. Transfer
A-2
-------
to cuvettes and read in a spectrophotometer at 550 mm using unexposed absorbing
reagent as a blank. Colors may be preserved, if well stoppered, with only 3 to
4% loss in absorbance per day; however, if strong oxidizing or reducing gases
are present in the sample in concentrations considerably exceeding that of the
nitrogen dioxide, the absorbance should be determined as soon as possible to
minimize any bleaching.
Standard!zation
Add graduated amounts of the working standard sodium nitrite solution up
to 1 ml (measured accurately in a graduated pipet or small buret) to a series
of the serum bottle containing 10 ml of the absorbing reagent. Mix, allow 15
minutes for complete color development, and read the absorbance.
A-3
-------
APPENDIX B
COMPUTER OUTPUT
-------
MAGNESIUM BASE SLURRY SCRUBBING PRUGRAM-OUT^UT DATA PAGE 1
RUN NUMBER 1-C
FLUE GAS DATA
PRIMARY AIR
SECONDARY AIR
FURNACE EXIT
PART.SCRB.INLFT
PART.CYC.EXIT
VENT ABS.INLET
ABS CYC.EXIT
FLOATING BED IN
FLOATING BED EX
P.P. EXIT ORTF.
SCRUBBER STREAM DATA
PARTICULATE
MAKbUP WATER
PRODUCT LIW.
RECIRCULATED LIO.
FURNACE PERFORMANCE
MEAT RbLE^SEtBTU/HR
% FUEL AS COAL
COAL FLOW RA1E,#/HR
NAT. GAS FLOrt,#/HP
% EXCESS AIR
DATE 9-11-71
TIME Of DAY 1530
FLOW
#/HP
454.
4b95.
545?.
5452.
3274.
*****
*****
3274.
3686.
36 R6.
TF.MP.
F
160.0
690.0
680.0
505.0
148.0
******
******
150.0
0.0
138.0
S02
PPM
1007.6
******
113R.6
******
******
******
******
10.3
SCn
PPM
*****
*****
*****
*****
*****
*****
*****
*****
NUX
PPM
*****
*****
*****
*****
*****
*****
*****
125.
FI.YASH
GR/DSCF
*******
*******
*******
*******
*******
*******
*******
*******
HUP.
tt/ti
0.016
0.016
0.050
0.050
0. IS9
******
******
0. 159
0.196
0.196
DEW
POINT
F
74. «
75.6
116.9
116.9
147.9
*****
*****
147.9
153.4
153.4
DRY
FLOW
¥/HR
447.
4522.
5150.
2825.
3081 .
STAT
PRES
IN.H20
8.1
6.3
2; 6
2.7
-6.8
*****
*****
81
--16. 3
-16.3
TEMP.I-
60.0
142.0
142.0
FLC1W,GPM
0.0
0.0
19.78
C.535E 07
96.5
423.7
8.6
14.8
3.10
15.39
0.059
C02,*DRY-CALC.
HUMI01TY,#/# - CALC.
S02 ABSORPTION PARAMETERS
VENTIJRI ABSORBER
KGA,9MOL£/HR-FT3» = ******
SUIFITE/S02-MOL/MOL = ******
SUMP RESin.TIME,MIN = ******
***** Mf-ANS ITEM NOT MEASURED
S02 ABS
FLYASH
S03 ABS
NOX ABS
GAS VEL
LIQ/GAS
LIQ/tiAS,fl/#
P3ES.DRUP,IN.WG
VENTUKI ARSDRBFR
GAS ABSORBER TEMP,F FLOWt^/M
MAKEUP WATER ***** *****
MAKEUP MGO SL . ***** 3.1
PRODUCT LIQ. ***** *****
REC. (SPRAY NOZ) ***** *****
REC.(FLCW NOZ.) *****
ORMANCE PArtT. VENT ABS.
..EFF -13.01 ******
.FFf- ****** ******
,.EFF ****** ******
,.ErF ****** ******
TY.FPS 91. R ******
L/MCF 21.7 ******
# 3.0 ******
FBA
TEMPtF FLOWtrf/
60.0 0.6
92.0 3.1
142.0 0.0
142.0 5?0.0
355.0
FLOAT. BED
9^.09
******
******
******
6.3
5?. 6
5. R
FLOATING BED ABSORBER
KGA,«MOLE/HR-FT3
SULFITE/S02-MOL/MOL
SUMP RfcSIO.TIME.MIN
30.0
27.98
******
5.3
SULFATE FORMATION PARAMETERS
CONC.,GM-MOLF/L= ******
MULS TOTAL SULF- *****
02 AT FURN. EX.= 3.10
n? AT ABSORB.IN= *****
Ll? AT ABSORB.EX= *****
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM - OUTPUT DATA PAGE 2
RUN NUMBER
MATERIAL BALANCES
FURNACE
INPUT,r/HR
OUTPUT, S/HR
PART. SCRUBBER
' INPUT, #/HR
OUTPUT, #/HR
S02 ABSORBERS
INPUT , #/HR
OUTPUT, #/HR
*
*S02 ABSORBER S-
-PRQDUCT COMPi
TOTAL,
COMBINED
FREE
MONOITOTAL)
MONOCDI-SSOLVEDI
MONO (SOL ID)
— BTSurFiTE-
MGO
SULFATE
MAGNESIUM
'FLYA'SH
SOL I OS, MG
l-C
SULFUR
1 5.6 8
5.41
5.4-1
3.35
0.03
GM S02/
1'OOML
• 4.'12
4.12
0.0
4.12
0.-96 —
3.16
'OVO '
1.23
*****
5.36
DATE 9-11-71 TIME OF DAY 1530
M-AGNFSIUM
W^»^ MM
7.53
******
GM-MOLE/
~L TTER "
0.6440
0.6440
-o.o
0.6440
a; 1 500
0.4940
0.0
0.1929
******
0.8369
FLYASH
31.36
******
******
******
****** •
******
GRAM/
IOOML
U560
10.473
0.0
0.771
******
- ******
18.457
INPUT FOR EO. - KIN.PROG.
WATER 'DRY GAS
INPUT FLOWS, 4ATOMS/1000FEED
284.0 " 5142i " CARBON 0.'477223
302.4 5150. HYDROGEN 0.62O751
" OXYGEN 1.3930T4
NITROGEN 5.046655
345. 5150. SULFUR 0.009072
449. 2825.
FEED RATE,#/SEC= 1.50 ~ ~
658. 2825. ENTHALPYtBTU/W = —4412.
605. 3081.
MAKEUP MGO COMPOSITION
- -SttlRRY CONC.- GM MGO/1OOML = 6.75
MGO PRESLAKEO, N0=0, YES=1 • 0
MG(OH)2 t MEAS. = ******
PRODUCT MG BASE PHYSICAL PROPERTIES
ACID STRENGTH, PH = 8.00
*P. GRAVITY, HYDROM. = - lr.0700 ~ "
PARTICULATE SCRUBBER PRODUCT ~ "
nr w r\ CTDCM/~TI4 DM — K AH
AOIU oIKCOIuin , rrl — J»t\J
FLYASH CONC. GM/100ML = 6i50
COAL COMPOSITION-MASS
CARBON 0.7150
HYDROGEN 0.0485 - _ - -
OXY+NIT 0.0817
ASH 0.
VATER ~ o;
U3 ru
0740
0438 ~ '
_. . _ _ . - _ . — —
*SOLIDS FREE BASIS, MASS/VCLUME SOLUTION
-------
RUN NUMBER l-C
FLUE GAS DATA FLOW
FURNACE EXIT 5452.
FLOAT. BED EX 3686.
NOX SCRUB IN 3508.
NOX SCRUB EX 3554.
NOX SCRUB. DATA TF:MP.
F
MAKEUP WATER 60.0
MAKEUP MGO 60.0
PRODUCT LIO. 138.0
NU2 FLOW DATA
N02 FLOWRATE,#/MIN
N02/NO( PDS BASIS!
N02/NO(FC £ ROTOI
0.
TEMI
6*80
138
176
136
&TE 9-11-71 TIME OF DAY 1530
P. S02 NOX NOX*1 NOX*2 HUM. DEW STAT
• -p?M P-PM-- PPM
.0 1007.6 ****** ******
.0 10.3 124. B ******
.0 10.3 233.4 ******
.0 6.0 209.1 ******
PPM " V79 1MTTWT-" PKFb -"
F IN.WG
870.3 0.059 116.9 2.6
902.0 0.196 153.4 -16.3
686.0 - O.t96 153.4 2.7
635.2 0.212 157.4 0.0
FLOW SCRUB. PERFORMANCE SPRAY SLURRY ANALYSIS
#/MIN S02 ABSORB. 41.70
1.71 NOX ABSORP. 10.45 MGO»GM/100ML 2.850
0.-76 NOX1 ABSQRP ****** MGS03( SOL IDI ,M O.0094
3.10 NOX2 ABSORP 7.41 MGS03 ( TOTAL \ ,M 0.0097
1-2WJ-. - G-A-S VE-tTf^S- t.-8 MGSO4, MGt AR' - ' OJTO0T5
L/G,GAL/MCF 147.0 MGIN02J2, MOLAR 0.0270
L/G,#/* 21.4 MGCNC3I2, MOLAR 0.0023
0.0 PRES.DROP.WG 0.1 T$S,GM/IOOML 11.677
0.87 NITRITF/NITRATE 11.739
0.0
MATERIAL BALANCE
SULFUR
NOX SCRUBBER
INPUT, #/HR 0.03
OUTPUT, #/HR 0.12
**
MAGNESIUM WATER NITROGEN
0.0 723.8 0.31
3.39 624.3 0.43
MAKEUP MGO COMPOSITION
SLURRY CONC.,GM MGO/IOOML= 0
PHYSICAL PROPfcRTIfcS OF
RECYCLED SLURRY
PH
CONDUCT.MlCROMHOS
9.30
0.
rvcr~
NOX
= POS ANALYSIS
=s~SALTSMAN ANAI
NOX*2 = FUEL CELL ANALYSIS
** OXIDIZED NITROGEN ONLY
-------
MAGNESIUM BASF SLURRY SCRUBBING PROGRAM-OUTPUT DATA PAGE I
RUN NUMBfcR 2-A
FLUE GAS DATA
PRIMARY AIR
SECONDARY AIR
FURNACE EXIT
PART. SCRB. INLET
PART. CYC. EXIT
VENT ABS. INLET
ABS CYC. EXIT
FLOATING BED IN
'-FT-OtnTNG-BED EX"
P.P. EXIT ORIF.
SCRUBBER STREAM DATA
^ARTICULATE
MAKEUP MATER
DATE 9-15-71
TIME OF DAY 1745
FLOW
#/HR
487 .
4523.
54D1.
5401.
3494.
*****
3494.
3*47 .
3847.
TEMP.
F
1 10. 0
635. 0
- 6VO.O
570. 0
143.0
******
******
143.0
" ~ ~0".0
135.0
502
PPM
186.2.4
1720.0
******
******
******
-***-***
3.5
503
PPM
*****
*****
*****
*****
*****
*****
******
*****
NOX
PPM
*****
*****
*****
*****
*****
*****
*****
421.
FLYASH
GR/DSCF
******* •
*******
*******
*******
*******
*******
*******-
*******
HUM.
#/#
O.O14
n o 17
. 058
0.161
******
******
.161
0^191
OEM
POINT
F
71.8
76. 4
1 16. 3
I4fl.2
*****
*****
148.2
152.8
DRY
FLOW
480.
4449.
-5r°*».
3010.
3230.
STAT
PRES
IN.H2Q
13.5
4.0
O.O
2-1
-6.8
*****
*****
— *. a
— 1 j. 5
-13.5
REC1RCULATED L1Q.
FURNACE PERFORMANCE
TEMP,F
60.0
14?.0 "
J42.0
FLOH.GPM
0.0
Ovt) "
20.02
GAS ABSORBER
MAKEUP HATER
MAK'EtfP WGO-SL—-
PRODUCT L10.
REC.(SPRAY NOZ)
RFC.(FLOW NOZ.I
VENTURI ABSORBER FBA
TEMP»F FLOH,-#7N TEMP,F FLOW,#/M
0.8
0.0
0.0
380.0
***** ***** 60.0
***** — -3v2 " "-fr.-C
***** ***** 141.0
***** ***** 141.0
*****
HtAT kt LEAbC i BTU/HR 0.5L9E OT
FUEL AS COAL
FfOH RflTE v #7HR
NAT. GAS FLOH,#/HR
f TKC^SS ATR
OXYGEN, ^DRYyHEAS.
HUMIDITY,#/# - CALC.
S02 ABSORPTION PARAMETERS
VENTURI ABSORBER
96.2
410.3
8.8
16.7
3.50
0.058
SCRUBBER PERFORMANCE
--- SXT2 ABSORBTEFF-
FLYASH COL.EFF
503 ABSORB. EFF
NOX ABSORB. EFF
GAS VELOCITY ,FPS
LIO/GAS*GAL/MCF
PART,
VENT ABS.
FLOAT. BED
PRES. DROP, 1N.WG
******
******
******
97.5
20.7
3.0
******
******
******
******
******
******
******
******
******
******
6.6
54.3
---•*-. 9'
4.6
FLOATING BED ABSORBER
ICGAVffHOL-b/HK-l-T3l = ******
SULFITE/S02-MOL/MOL = ******
- SUMP RESTD.TIMETMIN = ******
***** MtANS ITEM NOT MEASURED
SULFITE/S02-MOL/MOL
SUMP RESID.TtME,M-IN
20.86
******
SULFATE FORMATION PARAMETERS
CONC. ,GM-MOLE/L= ******
1WL? TOTAlr -StJLF-= *****
02 AT FURN. EX.= 3.50
02 AT ABSORB. IN= *****
02 AT ABSORB. EX= *****
-------
MAGNF.-SIUM BASE SLURRY SCRUBBING PROGRAM - UUTPUT DATA PAGE 2
RUN NUMBER 2-A
MATERIAL BALANCES
FURNACE
DATE 9-15-71
SULFUR MAGNESIUM FLYASH
TIME OF DAY 1745
WATER
DRY GAS
INPUT FOR EQ. - KIN.PROG.
INPUT FLOWS,#ATQMS/lOO#FtEO
-I-NI»UT,*/HR
OUTPUT, S/HR
PART. SCRUBBER
INPUT, #/HR
OUTPUT, J»/HR
S02 ABSORBERS
INPUT, #/ttR
OUTPUT, #/HR
*
*S02 ABSORBERS-
PRODUCT COMP.
TOTftt »
COMBINED
FREE
MONO! TOTAL)
MONO(OISSOLVED)
MONO(SOLID)
•BtStJtFlTF
MGO
SULFATE
MAGNESIUM
FLYASH
SUL IDS-MG
COAL COMPOSITin
CARBON 0.
HYnROGEN 0.
OXY+NIT 0.
- -SOtFtJR ' "0.
ASH 0.
HATER 0.
rs-. is
9.93
9.91
5.41
0.01
GM SO2/
100ML
2.40
0.0
2.40
1.06
1.34
- o;o
4.56
*****
6.97
N-MASS
7150
0485
0817
t)370 -
0740
0438
_-;-«_
7. 72
******
GM-MOL
LITER
Or3755
0.3755
0.0
0.3755
0.1656
0.2099
er.o -
0.7131
******
1.0886
30.36
******
******
******
E/ GRAM/
100ML
1.722
4.449
0.0
2.852
******
******
20.411
278.1 5097. CARBON 0.467256
297.1 5104. HYDROGEN 0.595881
• — - uXYGcW 1.39418*?
NITROGEN 5.055843
360. 5104. 'SULFUR O.OORP70
494. 3010.
FEED RATE,#/SEC= 1.49 -
712. 3010. -eNTHALPYiBTW* -' •**&&>.
617. 3230.
MAKEUP MGO COMPOSITION
SLURRY CONC.- GM MGD/100ML = 6.70
HGO PRESLAKED, N0=0, YES=1 0
? SLAKED TO MG(OH )2 .MEAS". = ******
PRODUCT MG BASE PHYSICAL PROPERTIES
ACID STRENGTH, PH = 8.10
SP.GRAVITY.HYDROM. = 1.0750
PARTICULATE SCRUBBER PRODUCT
ACID STRENGTH , PH * 5.55
FLYASH CONC. GMMOOML = 5.50
- —
. _ _
SSOLIDS FREE BASIS, MASS/VGLUME SOLUTION
-------
RUN NUMBbR 2-A
• DATE 9-15-71
TIME GF DAY 1745
FLUE GAS DATA
FURNACE EXIT
FLOAT.BED EX
NOX SCRUB IN
NOX SCRUB EX
FLOW TEMP.
SD2
PPM
NOX
PPM
NOX*1
'PPM
NOX*2
PPM
HUM.
5401.
3847.
3913.
3924.
640.0 1R62.4
135.0 3.5
136.0 ******
12B.O ******
******
420.7
1122.1
901.3
******
******
B76.9
******
485.8
485.8
803.4
308.3
0.058
0.191
0.194
DEW
POINT
F
116
152
152
154
STAT
IN.WG
0.0
-13.5
1.4
0.0
NQX SCRUB.DATA TFMP. FLOW
F 4/MIN
60.0 0.81
60.0 2.00
133.0 2.35
-133.tr—125 Ov
MAKEUP WATER
MAKEUP MGO
PRODUCT LIO.
-R-CCTRC-. -tio;-
SCRUB. PERFORMANCE
S02 ABSORB. ******
NOX ABSORP. 19.67
NOX1 ABSORP ******
NGX2 ABSORP 61.63
SPRAY SLURRY ANALYSIS
MGO,GM/100ML
MGS03ISULID),M
MGS03(TOTAL),M
1.787
0.0156
0.0157
N02 FLOW DATA
N02 FLOWRATE,#/MIN
N02/NOI PDS BASIS)
N02/NO(FC £ ROTO)
0.09
1.-&7
L/G,GAL/MCF 140.5
L/Gt#/# 19.2
PRES.DROP,WG 0.0
MG(N02)2i MOLAR
MG(N03l2t MOLAR
TSS,GM/100ML
NITRITE/NITRATE
0.0055
0.0103
10.677
0.534
MATERIAL BALANCE
SULFUR MAGNESIUM WATER
NOX SCRUBBER
INPUT,#/HR 0.01
OUTPUT,#/HR 0.10
PHYSICAL PROPERTIES OF
RECYCLED SLURRY
PH
CONDUCT.MICROMHOS
0.0
1.64
796.2
640.5
**
NITROGEN
1.68
1.42
MAKEUP MGO COMPOSITION
SLURRY CONC.,GM MGO/IOOML=
0.0
7.90
5170.
—rvtrrs
NOX » PDS ANALYSIS
= "~S ATTSWAN flNAL'VS TS
NOX*2 = FUEL CELL ANALYSIS
** OXIDIZED NITROGEN ONLY
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM-OUTPUT DATA PAGE 1
RUN NUMBER 3-E
FLUE GAS DATA
PRIMARY AIR
SECONDARY AIR
DATE 9-15-71
TIME OF DAY 2000
PART. SCRB. INLET
PART. CYC. EXIT
VENT ABS. INLET
ABS CYC. EXIT
FLOATING BED IN
P.P. EXIT
SCRUBBER STREAM DATA
PARTICULME
MAKEUP WATER
PRQ6UCT LHJ.
HECIRCULATED LIO.
FURNACE PFRJ-ORMANCE
H-F.A-T RELEASE, BTV/HR
? FUEL AS COAL
COAL FLOW RATE,#/HR
NAT. GAS FLOWt#/HR
1 EXCESS AIR
OXYGEN, *DRYfMEAS.
HUMIOITV,#/# - CALC.
S02 ABSORPTION PARAMETERS
VENTURI ABSORBER
FLOW TEMP. SO? S03 NUX FLYASH HUM. DEH
#/HR F PPM PPM PPM GR/DSCF #/# POINT
F
*n-* * i *» *» r* nl c 1 1 O
487 . 1 10
5128. 672
• u "«
5_ __„__ __ _ _ _ n
— — - (j ,
i \J I J » -* • V
,014 71.2
*G-55. — 6"50 .'0 t*4-«3.6 ***** -***** ******* 0.056 ~114.V
6055. 540.0 ****** ***** ***** ******* 0.056 114.9
3397. 144.0 ****** ***** ***** ******* 0.150 146.0
***** ****** ****** ***** ***** ******* ****** *****
***** ****** ****** ***** ***** ******* ******- *****
3397. 146.0 ****** ***** ***** ******* 0.150 146.0
3T61. 0.0 ****** ***** ***** ******* 0.181 151.2
3761. 136.0 9.4 ***** ***** ******* 0.181 151.2
TEMP,F
60.0
143.0
143.0
VENTUR1
FLUHiGPM GAS ABSORBER TEMP,F
0.0 MAKEUP WATER *****
0.0 MAKEUP MGO SL . *****
20.02 PRODUCT LIQ. *****
REC. (SPRAY NUZ) *****
REC.IFLOW NOZ.)
[ ABSORBER
DRY STAT
FLOW PRES
#/HR IN.H20
5057. 4.7
5"73fr." 0.0
__ _— 2 7
2954. -6.8
*****
-.———- *****— --
.._."__.
3185. -13.5
FBA
FLOW,#/M TtMP.F FLOW,#/M
*****
2-.-8-
*****
*****
*****
60.0 0.8
— O;0" - ~ ?;**"
140.0 0.0
140.0 0.0 —
3BO.O
SCRUBBER PERFORMANCE PART. VENT ABS. FLOAT. BED
0."S83E ~O7
96.6
462.8
8.8
16.7
3.50
- 1-5.05
0.056
so 2 A-BSORH.FFF ******
FLYASH COl .fcFF ******
S03 ABSORB. t^F ******
NOX ABSORB. HF ******
GAS VELOCITY, FPS 94.4
LIQ/GAS,GAL/MCF 21.4
trt-Q/GftSrU/f 2-Q
PRES.OROP,1N.WG 3.0
****-**
******
******
******
******
******
******
******
IS SULFATE FORMATI
—--******
- ******
= ******
FLOATING BED ABSORBER
KGA-»"#MOLE'/HRiiSf:T3" = ******
SULFITE/S02-MOL/MOL = ******
SUMP RESID.TIMETMIN = ******
- vvww —
******
******
******
6.4
55.9
"6'."!
5.5
ON PARAMETERS
_
CONC.,GM-MOLE/L= ******
MQLf •TOT-ftl 'St>tF-= ***** ••
02 AT FURN.
0? AT ABSORB
0? AT ABSORB
EX.= 3.50
,IN= *****
,FX= *****
***** MEANS ITEM NOT MEASURED
-------
RUN NUMBER 3-E
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM - OUTPUT DATA PAGE 2
DATE 9-15-71 TIME OF DAY 200O
MATERIAL BALANCES
FURNACE
SULFUR MAGNESIUM FLYASH
******
i in ru > » tf I nn
OUTPUT, #/HR
PART. SCRUBBER
I NPtlT . fl/HR
ll^rwl ffr^lflA
OUTPUT, 0/HR
S02 ABSORBERS
- --I-NPUT, r/Htt "
OUTPUT, #/HR
*
*S02 ABSORBERS-
PRODUCT COMP.
TOTAL-, -
COMBINED
FREE
MONO(TOTAL)
MONO(DISSOLVEO)
MONO(SOLID)
BISULFITE
MGD
SULFATE
MAGNESIUM
FLYASH
SOLIDStMG
i 1 . L£
9.88
900
. O o
******
******
0.03
GM S02/
100ML
3-. 13
3.13
0.0
3.13
1.18
1.95
"0^0
4.23
*****
7.42
...
-6; 25
******
GM-MOLE/
LITER
-0.4892
0.4892
0.0
0.4892
0.1844
0.3049
'0.0 '
0.6695
******
1.1587
.
COAL COMPOSITION-MASS
CARBON 0.
HYDROGEN 0.
OXY+NIT 0.
SULFUR 0.
ASH 0.
WATER 0.
7150
0485
0817
U3 ru
0740
043"8
******
******
******
GRAM/
100ML
WATER
300.3
382.
442.
-6-49 ;
577.
DRY GAS
572ft.
5736.
5736.
2954,
2954,
3185,
INPUT FOR EQ. - KIN.PROG.
INPUT FLOWS, #ATOMS/100#Ftt-D
CARBUN 0.467918
HYDROGEN 0.603335
(JXYGFN 1.194246
NITROGEN 5.055199
SULFUR 0.00*905
1-hED RATE,#/SEC= 1.67
ENTHALPY,BTU/# = -3592.
MAKEUP MGO COMPOSITION
SLURRY CONC.- GM MGO/IOOML = 6.20
MGCJ PRESLAKED, N0=0, YES=l 0
« SLAKE-D TO MG(OH)2,MEAS. = ******
1.917
6.463
- -Q-. 0 - '
2.678
******
******
19.612
PRODUCT MG BASE PHYSICAL
ACID STRENGTH, PH
SP.GRAVITY.HYDROM.
OROPFRTIFS
8.05
1.0780
PARTICULATE SCKUBBER PRODUCT
AC 10 STRENGTH , PH = 5.50
FLYASH CONC. GM/100ML = *****
*SOLIDS FREE BASIS, MASS/VOLUME SOLUTION
-------
RUN NUMBtR 3-E
DATE 9-15-71
TIME OF DAY 2000
FLUE GAS DATA FLOW
TEMP.
SO?
FURNACE EXIT 6055.
FLOAT. BED EX 3761.
NGX- SCRUB IN 3-748.
NOX SCRUB EX 3781.
650.0 1649.6
136.0 9.4
162.0 ******
130.0 ******
NOX
-PPM- -
******
******
969.3
1180.9
NOX*]
PPM
******
******
930.3
986.7
NOX*2
- PPM
485,6
504.3
644.4
551.0
HUM.
#7* -
0.056
0.181
0.181
0.192
OEM
POINT-
F
114.9
151.2
151r.2
154.3
STAT
PRES
IN.WG
0.0
-13.5
1.4
0.0
NOX SCRUB.DATA TEMP. FLOW
F
MAKEUP WATER 60.0
-MAKFUP MGO 60.0
PRODUCT LIQ. 134.0
LIQ.
0.81
2.00
2.35
-850.
N02 FLOW DATA
N02 FLOWRAT£t#/MIN 0.09
N02/NCK PDS BASIS) *****
N02/NO(FC £ ROTO) 2.24
SCRUB.PERFORMANCE
S02 ABSORB. ******
NOX AEtSORP. -21.83
NOXi AfrSORP -6.07
NOX2 ABSORP 14.49
1.8
96.1
13.6
0.0
SPRAY SLURRY ANALYSIS
MGO.GM/100ML
MGS03(S01ID) tM
MGS03(TOTAL),M
1.462
OvO
0.0
L/G,GAL/MCF
L/Gt#/#
PRES.DROP.WG
MG(NO?I2, MOLAR
MG(NO3)2t MOL-AR
TSStGM/lOOML
NITRITF/NITRATE
0.0155
0.0095
8.398
1.632
MATERIAL BALANCE
NOX SCRUBBER
lNPUTt#/HR
OUTPUT,#/HR
SULFUR MAGNESIUM WATfcR
0.03
0.02
2.88
1.34
738.5
610.2
**
NITROGEN
1.40
1.81
MAKEUP MGO COMPOSITION
SLURRY CONC.tGM MGO/100ML'
4iOO
PHYSICAL PROPERTIES OF
RECYCLED SLURRY
PH
CONDUCT.MICROMHOS
8.05
0.
~l:.0t"8 ~ '
NOX = POS ANALYSIS
1ttT>C*l-= SlttTSWftN-ttNMr
NOX*2 = FUEL CELL ANALYSIS
** OXIDIZED NITROGEN ONLY
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM-OUTPUT DATA PAGE I
RUN NUMBER 4-F
DATE 9-16-71
TIME OF DAY 1200
FLUE GAS DATA
PRIMARY AIR
SECONDARY AIR
-FURTnTCTT "ETIT
PART.SCRB. INLF.T
PART.CYC.EXIT
VENT ABS.INLET
ABS CYC.fcXIT
FLOATING BED IN
F1GATING BED EX
P.P. EXIT ORIF.
SCRUBBER STREAM DATA
PARTICULATE
MAKEUP WATER
"--PROTTOCT-tlO.
REClRCULftTED LIO.
FURNACE PERFORMANCE
-HEAT RITL-E-A-SEVBTU/HR-
% FUEL AS COAL
COAL FLOW RATE,*/HR
NAT. GAS FLOW,#/HR
% EXCESS AIR
OXYGEN, SDRY.MEAS.
CO2,~*DRY-CALt.
HUMIDITY,*/*) - CALC.
502 ABSORPTION PARAMETERS
VENTURl ABSORBER
FLOW
»/HR
462.
4454.
5294V"
5294.
3323.
*****
*****
3323.
36C4.
3604.
TEMP.
F
110.0
685. C
- 5-40.0
450.0
142.0
******
******
143.0
- o.o
128.0
S02
PPM
153 8-. 4
******
1431.0
******
******
******
******
10.3
S03
PPM
- *****
*****
*****
*****
- *****
*****
-*****
*****
NQX
PPM
-*****-
*****
*****
*****
*****
*****
*****
502.
FLYASH
GR/DSCF
*******
*******
*******
*******
*******
*******
*******
*******
HUM.
*/*
0.012
0.010
• -0.0-52
0.052
0.125
******
******
0.125
0. 156
0.156
DEW
POINT
F
65.6
60.6
- 1 1 2 .-a
112.8
140.6
*****
*****
140.6
146.4
146.4
DRY
FLOW
#/HR
456.
4408.
5-073 .
2954.
3118.
STAT
PRES
IN.H20
-14.9
5.0
• - ~ovo
2.7
-6.8
*****
*****
-6.8
^l7;-6 -
-17.6
FEMP.F
60.0
135.0
FLOWtGPM
0.0
o.-o
20.02
GAS ABSORBER
MAKEUP WATER
MAKEUP MGO SL.
PRODUCT LIQ.
VENTURl ABSORBER FBA
TEMP,F FLOW,#/M TEMP.F FLOW,#/M
SCRUBBER PERFORMANCE
0.504E 07 ' -S02 "ABSORB.EFF
96.1 FLYASH COL.EFF
397.5 S03 ABSORB.EFF
0.9 NOX ABSORB.FKF
18.1 GAS VELOCITY,FPS
3.80 LIQ/GAStGAL/MCF
14.77 LTO/GAS,»/#
0.052 PRES.DROP,IN.WG
R *****
SL. -*****
i. *****
NOZJ *****
OZ. 1
PART.
~ BV9S
******
******
******
90.4
22.3
3.0
2.3
*****
3.2
*****
*****
*****
VENT ABS.
******
******
******
******
******
******
******
******
60.0 0.6
0.0 3 . 2 " '
133.0 0.0
133.0 380.0
380.0
FLOAT. BED
99.28 "
******
******
******
6.1
58.7
6.3
12.8
' =-***-***
SULFITE/S02-MOL/MOL = ******
SUMP RFSIO.TIME,M1N = ******
***** MEANS ITEM NOT MEASURED
FLOATING BED ABSORBER
KGA,8MOLEAHR-FT3
SULFITE/S02-MOL/MOL
SUMP R£SID.TIME,MIN
SULFATE FORMATION PARAMETERS
CONC.»GM-MOLE/L= ******
-3r.9 -— -MOt* TOT-Ar "SUVFs— *****
****** 02 AT FURN. EX.= 3.80
****** 02 AT ABSORB. IN= *****—
02 AT ABSORB.EX= *****
-------
RUN NUMBER 4-F
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM - OUTPUT DATA PAGE 2
DATE 9-16-71 T1MF OF DAY 1200
MATERIAL BALANCES
FURNACE
SULFUR MAGNESIUM FLYASH
29.42
******
imr-ui , tff rm i *t « r 1
OUTPUT, #/HR 8.09
PART. SCRUBBER
IMPIIT . tf /HP ft HO
OUTPUT, #/HR 4.42
S02 ABSORBERS
INPUT, r/HR -4.42
OUTPUT, #/HR 0.03
*
*S02 ABSORBERS- GM S02/
PRODUCT COMP. 100ML
TUT-AL, 1.45
COMBINED 1.45
FREE 0.0
MONO(TOTAL) 1.45
-MONOI DISSOLVED) *****
MONO(SOLID) *****
BISULFITE *****
MGO 1.71
SULFATE *****
MAGNESIUM 3.16
EI V-ACU i._i -_^
cm i nc MT _____
COAL COMPOSITION-MASS
CARBON 0.7150
HYDROGEN 0.0485
OXY+NIT 0.0817
•SULFUR 0.0370
ASH 0.0740
WATER 0.0438
—————
7.14
******
GM-MOLE/
LITER
O.P2-63
0.2263
0.0
0.2263
*******
******
******
0.2672
******
0 . 49 34
******
******
******
GRAM/
100ML
WATER
242.5
261.6
324.
370.
586.
486.
DRY GAS
5026.
5033.
5033.
2954.
2954.
3118.
INPUT FOR EQ. - KIN.PROG.
INPUT FLOWS,#ATOMS/100#FEEO
CARBON 0.459826
HYDROGEN 0.570051
OXYGEN -lT-3^5035—
NITROGEN 5.062690
SULFUR 0.008723
FEfO RATE,#/SEC= 1 ,~46 —
ENTHALPY*BTU/# =- -14T7; "
MAKEUP MGO COMPOSITION
SLURRY CONC.- GM MGO/IO&ML
MGO PRESLAKEDt N0=0, YES=1
% SLAKED TO MG (OH ) 2 r
6.20
0
******
******
******
*•***•**
1.069
******
******
1.690
PRODUCT MG BASE PHYSICAL
ACID STRENGTH, PH
SP.GRAVITY-,HYOROM. =
PROPERTIES
7.80
1.0200 -
PARTICULATE SCRUBBER PRODUCT
ACID STRENGTH , PH = 6.10
FLYASH CONC. GM/100ML =- *****
*SOLIDS FREE BASIS, MASS/VOLUME SOLUTION
-------
RUN NUMBER 4-F
DATE 9-16-71
TIME OF DAY 1200
FLUE GAS DATA
FURNACE EXIT
FLOAT.8EO EX
NOX SCRUB IN
NOX SCRUB EX
FLOW
#/HR
5294.
3604.
3541.
3581.
TEMP.
F '
540.0
128.0
160.0
122.0
S02
PPM
1538.4
10.3
******
******
NOX
PPM
******
502.4
759.5
855.0
NOX*1
PPM
******
******
613.9
751 .1
NOX*2
"PPM-
561.9
486.9
580.6
299.7
HUM.
#/r
0.052
0.156
- 0~.156
0.169
DEW
POTNT
F
112.8
146.4
146.4
150.7
STAT
PRES
1N.WG
0.0
-17.6
1.4
0.0
NUX SCRUB.DATA TEMP. FLOW
F «/MIN
MAKEUP WATER 60.0 0.71
MAKEUP MGO 60.0 2.00
PRODUCT LIO. 124.0 2.95
LIQ. 124.0 - 5-00.
N02 FLOW DATA
N02 FLOHRATt,#/HIN 0.06
N02/NOI PDS BASIS) 0.51
NO?/NOJFC L ROTO) 1.55
SCRUB.PERFORMANCE
S02 ABSORB. ******
NUX ABSORP. -12.57
NOXi ABSORP -22.35
NOX2 ABSORP 48.39
— «AS VEL.FPS" "1-T7 -
L/G,GAL/MCF 61.0
L/G,#/# 8.5
PRES.DROPtWG 0.0
SPRAY SLURRY ANALYSIS
MGO,GM/100ML
MGS03(SOLID)tM
MGS03(TOTAL) ,M
MG(N02)2, MOLAR
MG(N03)2f MOLAR
TSS,GM/100ML
NITRITE/N1TRATF
3.031
0.0
O.0008
0.-QOT6
0.0054
0.0014
7.519
3.857
rERIAL BALANCE
NOX SCRUBBER
INPUT, a/HR
OUTPUT, #/HR
SULFUR
0.03
0.05
MAGNESIUM
2. 88
3.28
WATER
635.5
520.3
**
NITROGEN
1.06
1.23
MAKEUP MGO COMPOSITION
SLURRY CONC.,GM MGO/ 100
4.00
PHYSICAL PROPERTIES OF
RECYCLED SLURRY
PH 9.20
CONDUCT.MICROMHOS 2280.
SPECIFIC GRAVITY 1.015
NOX = PDS ANALYSIS
NOX*1 = SALTSWAN" ANALYSIS
NOX*2 = FUEL CELL ANALYSIS
** OXIDIZED NITROGEN CNLY
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM-OUTPUT DATA PAGE 1
RUN NUMBER 5-K
FLUE GAS DATA
PRIMARY AIR
SECONDARY AIR
-FURNA-CT EXIT
PART.SCRB.INLET
pART-.-tYC.EXIT
VENT ABS.INLET
ABS CYC.EXIT
FLOATING BED IN
-F-tOATlNG -8€0 EX
P.P. EXIT ORIF.
DATE 9- 16-71
TIMF OF DAY 1530
FLOW
U/HR
487.
5146.
6D-73.
6073.
3188.
*****
*****
3188.
T4-O9-. -
3409.
TFMP.
F
115.0
687.5
600.0
510.0
142.0
******
******
140.0
~ O.tf
128.0
S02
PPM
******-
******
******
******
******
******
******
******
S03
PPM
*****
*****
*****
*****
*****
*****
*****
*****
NOX
t>PM
*****
*****
*****
*****
*****
*****
*****
589.
FLYASH
GR/nSCF
*******
*******
*******
*******
*******
*******
*******
*******
HUM.
#/#
0.015
0.011
OV053
0.053
0.140
******
******
0. 140
&. 173
0. 173
DEW
POINT
F
74.2
64.9
113.5
113.5
143.7
*****
*****
143.7
150.1
150.1
DRY
FLOW
#/HR
480'.
5089.
-5767V
2797.
2907.
STAT
PRES
IN.H20
14.9^
5.3
over
1.4
-9.5
*****
*****
In o
u . o
-12. Z
-12.2
SCRUBBER STREAM DATA
PARTICULATE
MAKEUP WATER
-— PW3OUCT LIQ.
RECIRCULATED LIQ.
FURNACE PERFORMANCE
TEMP.F
60.0
132.0
132.0
FLOW,GPM
0.0
0.0
20.02
GAS ABSORBER
MAKEUP WATER
MAKEUP MGO SL.
PRODUCT LIQ.
REC.tSPR'AY NOZ) *****-
REC.1FLOW NOZ.)
VENTURI ABSORBER
TEMP,F FLOW,#/M
***** *****
***** ;>.q
***** *****
*****
*****
FBA
TEMP.F FLOWf#/M
0.0
60.0
80.0
132.0
132;0
0.0
0.0
367.0
% FUEL AS COAL
COAL FLOW RATE,#/HR
NAT. GAS FLOW,#/HR
x- excess- AIR
OXYGEN, ?DRY,MEAS.
- C02,*DRY-CALCV
HUMIDITY, #/# - CALC.
S02 ABSORPTION PARAMETERS
ABSORBER
SCRUBBER PERFORMANCE
0.-583E 07 S02 AUSOR'B.EFF
96.6 FLYASH COL.EFF
462.7 S03 ABSORB.EFF
8.9 NOX ABSORB.EFF
17.1 GAS VE-LOCITY.FPS
3.60 LIQ/GAStGAL/MCF
14.96 1_ig/GAS,-#/# -
0.053 PRES.DROP,IN.WG
PART.
**"* * **~ •
******
******
******
88.0
22.9
3.1
4.5
VENT ABS.
-******
******
******
******
******
******
******
******
FLOAT.BED
-•*«****
******
******
******
5 i 7
60.3
5.5
FLOATING BED ABSORBER
-rTMOL E / HR- FT 3 T ' =-•******
SULFITE/S02-MOL/MOL = ******
SUMP RESI'D.TIME,MIN = ******
SULFITE/S02-MOL/MOL
SUMP RESIDiTIME.MIN
******
******
******
SULFATE FORMATION PARAMETERS
CONC. ,GM-MOLE/L= ******
-MOt? -TOfAt - S-OtF— - ***** -
02 AT FURIM. EX.= 3.60
02 AT ABSORB. IN= *****
02 AT ABSORB. EX= *****
-*****
ITEM NOT MEASURED
-------
_ __RUN NUMBER 5-K
MATERIAL BALANCES
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM - OUTPUT DATA PAGE 2
DATE 9-16-71 TIME GF DAY 1530
INPUT FOR EO. - KIN.PROG.
SULFUR
17 1 ?
******
GM S02/
100ML
i 5n
o. n
1 . 5O
1.08
0.42
t).0
I. 10
*****
? . 60
-
MAGNESIUM
6?K —
******
GM-MOLE/
LITER
— ~fi ~*?"^ SfV —
0 23 SO
On
fl ? "H so
0.1687
0.0663
0.0
0.1715
******
*
. —
FLYASH
34 .ZH
******
*
******
GRAM/
IOOML
1.755
1.405
070
0.686
******
.442
WATER DRY GAS
INPUT FLOWS, *ATOMS/100#FEEO
286.7 5758. CARBON 0.465489
305.8 5767. HYDROGEN 0.601821
JXYGEN 1.394532
NITROGEN 5.057435
306. 5767. SULFUR 0.008858 - — -
391. 2797.
FEED RATE,#/SEC= 1.68 - -
502. 2907.
MAKEUP MGO COMPOSITION
SLURRY CONC.- GM MGO/100ML--= " ~ '6.-20 — -
MGO PRESLAKEO, N0=0, YE S= 1 0
? SLAKED TO MG( OH) 2 , MFAS . - ******
PRODUCT MG BASE PHYSICAL PROPERTIES
AC 1 U STRENGTH, PH = 7.85
SP.GRAVITY,HYDROM. = 1.020O - — .
PARTICULATE SCRUBBER PRODUCT
ATTnCTDCKIPTl-f nu c c f
AL1U oIKfclNbTH , PH = 5.55
FLYASH CONC. GM/100ML = *****
... _
*SOLIDS FREE BASIS, MASS/VOLUME SOLUTION
-------
RUN NUMBER 5-K
DATE 9-16-71
TIME OF DAY 1530
FLUE GAS DATA FLOW
FURNACE EXIT
FLOAT.PFD EX
NOX -SCRU8 IN
NOX SCRUB EX
TEMP. S02
----- PPM-
NOX
—PPM-
NOX*1
'PPM '
NOX*2
PPM
6073.
3409.
326-0.
3291.
600.0 ******
128.0 ******
16?. 0 ******
128.0 ******
******
589.4
671.3
920.6
******
******
901.6
1226.1
588.1
559.6
777;8
398.4
NOX SCRUB.DATA TfcMP. FLOW
F #/MIN
60.0 0.48
60-. 0 1-.20
132.0 1.70
-1-32.0 -6 80-.
MAKEUP WATER
HAKEtfP MGO
PRODUCT LIQ.
N02 FLOW DATA
N02 FIOWRATE,#/MIN 0.06
N02/NO( PDS BASIS! 0.14
NU2/NO(FC C ROTO) 1.45
SCRUB.PERFORMANCE
S02 ABSORB. ******
NOX ABSORP. -37.13
NOX1 AB-SORP -35-. 991
NOX2 ABSORP 48.78
- 6A-S- VEtvFRS 1.6
L/G.GAL/MCF 89.2
L/G,#/# 12.5
PRES.DRHP.WG 0.1
HUM. DEW STAT
#/-« - -POI-NT PR-ES
F IN . WG
0.053 113.5 0.0
0.173 150.1 -12.2
0.173 150.1 1.4
0.184 153.2 0.0
SPRAY SLURRY ANALYSIS
MGO,GM/100ML 1.662
-MGSO3(SOLtD),M - 0.0125
MGS03(TOTAL),M 0.0133
- MGS-O4,MQtAR OvO04-8
MG(N02)2, MOLAR 0.0060
MG(N03)2, MOLAR 0.0010
TSS,GM/100ML 16.373
NITRITE/NITRATE 6.000
MATERIAL BALANCE
NOX SCRUBBER
INPUT,#/HR
OUTPUT,#/HR
SULFUR MAGNFSIUM WATFR
*****
0.06
1.73
1.08
578.3
512.3
**
NITROGEN
0.85
1.19
MAKEUP MGO COMPOSITION
SLURRY CONC.,GM MGU/100ML'
4.00
PHYSICAL PROPERTIES OF
RECYCLED SLURRY
PH 7.90
CONDUCT.MICROMHOS 3600.
-— SPECIFrc-iJKiwrTY- - -tvote
NOX = POS ANALYSIS
MOX»1 g-^fttTSHAtl -AWA
NOX*2 = FUEL CELL ANALYSIS
** OXIDIZED NITROGEN ONLY
IHC210I PROGRAM INTERRUPT(P) OLD PSW IS
IHr.210I PROGRAM INTERRUPT (P» OLD PSW IS
FF15000 F 82015C58
FF15000 F 82015C68
-------
RUN
FLUE GAS DATA
6-L
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM-OUTPUT DATA PAGE 1
DATE 9-22-71 TIMfc OF DAY
PRIMARY AIR
SECONDARY A[R
FURNACE EXIT
PART.SCRB.INLET
PART.CYC.EXIT
VENT ABS.INLET
ABS CYC.EXIT
FLOATING BED IN
F-t"QAT-T"NG "BE'D EX
P.P. EXIT QRIF.
SCRUBBER STREAM DATA
PARTICULATE
MAKEUP WATER
PITOOXTCT LIQ. - -
RECIRCULATED LIQ.
FURNACE PERFORMANCE
HEAT RELEASE fBTU7HR
% FUEL AS COAL
COAL FLOW RATE.S/HR
NAT. GAS FLOW,#/HR
% EXCESS AIR
OXYGEN, ?URY,MEAS.
------ CO2TZDRY-CALC." "
HUMIDITY, #/# - CALC.
S02 ABSORPTION PARAMETERS
VENTURI ABSORBER
FLOW
#/HR
451.
5027.
5947.
5947.
3721.
*****
*****
3721.
-4-124V
4124.
TEMP.
F
110. 0
708. R
430.0
410.0
114.0
******
******
136.0
O.t)
125.0
S02
PPM
******
******
******
******
******
******
— ******—
1308.8
S03
PPM
*****
*****
*****
*****
*****-
*****
***** •
*****
NOX
PPM
*****
*****
*****
*****
*****
*****
-*****--
*****
FLYASH
GR/DSCF
*******
*******
*******
*******
*******
*******
*******
*******
HUM.
#/1t
0.010
0.015
0.056
0.056
0.12?
******
******
0.122
-QV15-1--
0.151
DEW
POINT
F
61.2
74.3
irs.6
115.6
139.8
*****
*****
139.8
14"8.7'
148.7
DRY
FLOW
#/HR
486.
4951.
5630.
3316.
3582.
STAT
PRES '-
IN.H20
13.5
4.8
-Q.-0
2.7
-a. I
*****
&&&&•&- — • —
-8.1
13.5
13.5
TEMP.F
60.0
13&-.0
13ft.0
0.0
- -CYO
20.02
V/EIMTURI ABSORBER FBA
GAS ABSORBER TEMP.F FLOW,r/M TEMP.F FLOW,#/M
MAKEUP WATER ***** ***** 60.0 1.0
- MAKEUP- WGtT "Str. ***** 3V? Ovt) 3T2"-
PRODUCT LIQ. ***** ***** 132.0 0.0
REC.{SPRAY NOZ) ***** ***** 132.0 0.0
REC.JFLOW NOZ.) ***** 380.0
S&9E 07
96.5
451.4
8.9
17.1
3.60
14. W
0.056
SCRUBBER PERFORMANCE
- -S02 ABSORB.EFF
FLYASH COL.EFF
S03 ABSORB. EFF
NOX ABSORB.EFF
GAS VELOCITY, FPS
LIO/GAS.GAL/MCF
PRES. DROP, IN. WG
PART.
******
******
******
******
99.6
20.3
2VT
3.3
VENT ABS.
- ******
******
******
******
******
******
FLOAT.BED
- ***-***-
******
******
******
6.4
55.Q
FLOATING- BED ABSORBER
****** 3.3
SULFATE FORMATION PARAMETERS
SULFITE/SC12-MOL/MOL = ******
SUMP RESID.TIME.MIN = ******
***** MEANS ITfcM NOT MEASURE.')
=FT3
SULFITE/S02-MOL/MOL
SUMP RESID.TIME.MIN
******
******
******
CONC.,GM-MOLE/L=
MOL? TOTAL SULr-
02 AT FURN. EX.=
02 AT ABSORB. IN=
02 AT ABSORB. EX=
******
*****
3.60
*****
*****
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM - OUTPUT DATA PAGE 2
RUN NUMBER 6-L
MATERIAL BALANCES
FURNACE
- INPUT,#/HR
OUTPUT,#/HR
PART.SCRUBBER
INPUT,#/HR
OUTPUT,#/HR
S02 ABSORBERS
l1MPOT-,-*/HR
OUTPUT,#/HR
*
*S02 ABSORBERS-
PRODUCT COMP.
SULFUR
16.70
******
******
******
DATE P-22-71
MAGNESIUM FLYASH
TIME OF DAY 1545
****** -
******
GM S02/
100ML
TOTAL,
COMBINED *****
FREE *****
MONO(TOTAL) *****
MONO(DISSOLVED) *****
MONO(SOLID) *****
BISUtFl-fE *****
MGO *****
SULFATE *****
MAGNESIUM *****
FLYASH
SOLIDSfMG
COAL COMPOSITION-MASS
******
******
GM-MOLE/
LITER
******
******
******
******
******
******
-****** -
******
******
******
33.40
******
******
******
******
******
GRAM/
100ML
WATER
2^7.6
316.8
379.
405,
660,
541,
******
******
******
******
******
******
******
CARBON
HYDROGEN
OXY+NIT
SULF~Ufr~
ASH
WATER
0.7150
0.0485
0.0817
0.0370
0.0740
0.0438
DRY GAS
5622.
5630.
5630.
3316.
3316.
3582.
INPUT FOR EO. - KIN.PROG.
INPUT FLOWS,#ATOMS/100#FEED
CARBON 0.46534-7
HYDROGEN 0.545518
[JXYGEN 1.394-5-21D
NITROGEN 5.057571
SULFUR 0.008851
FEED RATE,#/SEC= 1.64
ENTHALf>Y,-B-TU/1¥- -
MAKEUP MGO COMPOSITION
SLURRY CONC.- GM MGO/100ML
MGO PRESLAKEL), N0=0, YES=1
5? SLAKFD TO MG(OH) 2, MEA3.
******
0
******
PRODUCT MG BASE PHYSICAL
ACID STRENGTH, PH
SP.GRAVITY.HYDROM.
PROPERTIES
*****
*******
PARTICULATE SCRUBBER PRODUCT
ACID STRENGTH , PH = *****
FLYASH CONC. GM/100ML = *****
-------
RUN NUMBER 6-L
DATE 9-22-71
TIME OF DAY 1545
FLUE GAS DATA FLOW
S02
FURNACE FXIT 5947.
FLOAT.BFO EX 4124.
NOX SCRUB IN 3927.
NOX SCRUB EX 39RO.
TEMP.
480.0 -******
125.0 1308.8
L64.0 1308.8
120.0 22.8
NOX
NOX*l
NOX*2
HUM,
rPM"
******
******
******
******
- PFM
******
******
******
******
******
******
******
******
~ VTW ' ' '
0.056
0.151
0.151
0.167
POUT! —
F
115.6
148. 7
146.7
150.4
PRES
IN.HG
0.0
13.5
1.4
0.0'
NOX SCRUB.DATA TEMP. FLOW
MAKEUP MATER
MAKEUP MGO
PRODUCT LIO.
REC IRC. LIO.
F
60.0
60.0
124.0
124.0
0.48
3,40
4.25
125CT;-
N02 FLOW DATA
N02 FLOWRATE.0/M1N 0.0
NQ2/NOC POS BASIS) *****
N02/NO(FC L ROTO) *****
SCRUB.PERFORMANCE
S02 ABSORB. 98.26
NOX ABSORP. -37.13
NOX1 ABSORP -35.99
NOX2 ABSORP 48.78
~ GAS VEL'.FPS • 1.9
L/GtGAL/MCF 137.7
L/GV«y# ~ -19.1
PRES.DROP,WG O.I
SPRAY SLURRY ANALYSIS
MGOfGM/lOOML -0.0
MGS03(SOLrD)»M 0.0
MGS03(TOTAL)*M 0.0
MGS04,MOLAR -" 0.0
MG(N02)2, MOLAR 0.0
HG(NO3)2~f~ MOLAR 0.0
TSS.GM/100ML 0.0
NITRITE/NITRATE 0.0
MATERIAL OALAMCF
NOX SCRUBBER
INPUT,#/HR
OUTPUT,#/HR
SULFUR MAGNESIUM WATER
4.90
0.08
0.0
0.0
748.3
572.8
**
NITROGEN
*****
*****
MAKEUP MGO COMPOSITION
SLURRY CONC.,GM MGO/100ML-
0.0
PHYSICAL PROPERTIES OF
RECYCLED SLURRY
PH 0.0
CONDUCT.MICROMHOS 0.
SPECIFIC GRAVITY 0.0 "
NOX = PDS ANALYSIS
= -SA1TSMAN ANALrSIS
NOX*2 = FUEL CELL ANALYSIS
** OXIDIZED NITROGEN ONLY
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM-OUTPUT DATA PAGE 1
RUN NUMBFR 7-C
FLUE GAS DATA
-PRTM'ARY AIR
SECONDARY AIR
-FURNACE EXIT -
PART. SCKB. INLET
PART. CYC. EXIT
VfcNT ABS. INLET
ABS CYC. EXIT
FLOATING BED IN
DATE 9-23-71
TIME OF DAY 1130
P.P. EXIT ORIF.
SCRUBBER STREAM DATA
PARTICULATF
MAKEUP WATER
" PRODUCT LIQ.
RECIRCULATED LIQ.
FURNACF PERFORMANCE
-FfE-AT- RELEASE-.BTUAHR "
1 FUEL AS COAL
COAL FLOW RATE,#/HR
NAT. GAS FLOW,#/HR
* EXCESS AIR
OXYGEN, %DRY,MEAS.
FLOW
#/HR
491.
4608.
5-4-82.
5482.
3546.
*****
*****
3546.
3715.
TEMP.
F
110.0
10. 0
- -560.0
470.0
138.0
-******
138.0
"""lj »\J
130.0
S02
PPM
1799-;0
***.***
1614.5
******
******
21.2
S03
PPM
--**-***
*****
*****
*****
*****
*****
-- »**«» •
*****
NOX
PPM
***** —
*** **
*****
*****
*****
*****
—*•**•*-* —
563.
FLYASH
GR/DSCF
***-**-**•-
*******
*******
*******
*******-
*******
*******
HUM.
#/#
Om y-
0 0 12
O» 052
. Q5Z
0.131
******
-***•***-
0.131
0.160
DEW
POINT
F
L-r p-
66.5
•~tT3".0" '
11 •> f\
1.3 . U
142.0
*****
—***** -
142.0
1^47.7
147.7
DRY
FLOW
#/HR
4554.
5210.
3136.
3202.
STAT
TOES ~
IN.H20
5.3
27
-6"i8
*****
• •• *****
-6.8
— 1 J« 3
-13.5
TEMP,F
60.0
138.0 -
138.0
FLOW,GPM
0.0
Ov0
20.02
VENTURI ABSORBER FBA
GAS ABSORBER TFMP,F FLOW,#/M TEMP,F FLOW,#/M
***** ***** 60.0 0.6
MAKEUP WATER ***** *****
MAX-F-UP MGO SL. •*•**** -3.6~
PPODUCT LIQ. ***** *****
REC. (SPRAY NUZ) ***** *****
REC.CFLOW NOZ.) *****
60.0
••o.-o- --
136.0
136.0
0.6
3-.tr
0.0
0.0
380.0
SCRUBBER PERFORMANCE
-0.-510E- O7 -
96.1
402.6
8.9
20.0
4.20
— SO-2
FLYASH COL.EFF
S03 ABSORB. EFF
NOX ABSORB. EFF
GAS VELOCITY, FPS
LIQ/GAS.GAL/MCF
HUMIDITY, V/lt - CALC.
S02 ABSORPTION PARAMETERS
VENTURI ABSORBER
0.052
PRES.DROP, IN.WG
PART.
- 1-O.-26'
******
******
******
96.0
21.0
2~sU '
3.1
VENT ABS.
****** - -
******
******
******
******
******
.*.....
**•* *«V ^
******
FLOAT. BED
^a.-6-9-
******
******
******
6.2
57.5
6-.t
4.4
FLOATING BED ABSORBER
SULF1TE/S02-MOL/MOL = ******
SUMP RESID.TIME.MIN = ******
***** ME&NS IJEM NOT MEASURED
SULF I TE/S02-MOL/MOL
SUMP RESID.TI'MEtMIN
32.06
******
SULFATE FORMATION PARAMETERS
CONC.,GM-MOLE/L= ******
«Ot?--TOTftt:-SUt^= -- ***** ---
02 AT FURN. EX.= 4.20
02 AT ABSORB. I N= *****
02 AT ABSORB. EX= *****
-------
MAGN€SIUM BASE SLURRY SCRUBBING PROGRAM - OUTPUT DATA PAGE 2
RUN NUMBER 7-C
DATE 9-23-71
TIME OF DAY 1130
MATERIAL BALANCES
SULFUR
FURNACE
INPUT, #/HR 14.90
niiTDiiT it i MO a 01
uu i r\j i , iff nr< 7 . *5 1
PART. SCRUBBER
IMP) IT 4/UP O Q 1
m IT Pi IT tf/MQ f\ "an
S02 ABSORBERS
INPuT,#/flR 5.30
OUTPUT, &/HR 0.07
*
*S02 ABSORBERS- GM S02/
PRODUCT COMP. 100ML
TOTAL t 1 • HI
CD cc n n
Mf iMfl 1 TflT Al \ 1 A 1
MONO(DISSOLVED) 1.52
MONO(SOLID) -0.11
BISULFITE 0.0
MGU 0.79
SULFATE *****
MAGNESIUM 2.20
FLYA5H — — —
cm T nc Mf* ___
COAL COMPOSITION-MASS
CARBON 0.7150
HYDROGEN 0.0485
OXY+NIT 0.0817
SULFUR 0.0370
ASH 0.0740
WATER 0.0438
MAGNESIUM
******
GM-MOLE/
LITER
0. 22Ov
On
• U
Oo 5 no
• C.C. U7
-0.2375
-.0166
0 .0
0.1230
******
0.3439
INPUT FOR EQ. - KIN. PROG.
FLYASH WATER DRY GAS " ' ~ '
INPUT FLOWS, #ATOMS/100#FEED
29.80 253.1 5203. CARBON 0.450212
www tr/«3 7clU« n YUKUl>tN U« DOv"**^
OXYGEN 1.-396I97 '
NITROGEN 5.071530
ftdcdcAAA A.1 I ^1 1 A
V9WW *tl 1 • 3 1 JO •
-._- _ ,.-.- .--.. FEED RAJE ,-#/ SEC = 1«~51
****** 663. 3136. ENTHALPY,BTU/# = -1315.
****** 513. 3202.
GRAM/ MAKEUP MGO COMPOSITION
IOOML "SLURRY CONCi- GM MGO/ 100 ML = ******
MGO PRESLAKED, N0=0, YES=1 0
1 SLAKED TO MG ( OH) 2 » MEAS . = *•**«*.*
ODnmi^T Hi/* DACC D UV CffAt DDOOCDTfCC -- - -
— — — KKIJUUU I PH» BAor rnYoILAL "KUPtKl Itb
__-*_ APfnCTDCMPTU OU Q1A
2.-470 SP.GRAVTTYiHYDROM. = ******* -
-0.353
0. 0
0.492
****** PARTICULATE SCRUBBER PRODUCT - - -
ACID STRENGTH , PH = 5.50
www rLYAbH LUNL . OM/ IOOML = *****
2.0S3
- - - _ ---- . . _
*SOLIDS FREE BASTS, MASS/VOLUME SOLUTION
-------
RUN NUMBER 7-C
DATE 9-23-71
TIMF OF DAY 1130
FLUE GAS DATA
FURNACE EXIT
FLOAT.BED EX
Nt3X SCRUB IN
NOX SCRUB EX
NOX SCRUB.DATA TEMP. FLOW
— - -•- F -#-/MTN
MAKEUP WATER 60.0 0.81
MAK€U P - MGO - 6'0 . 0 ~t^t)5
PRODUCT LIQ. 130.0 2.90
FLOW
~ 87HR' ' ""
5482.
3715.
3772.
3816.
TEMP.
— -e- —
560.0
130.0
164.0
128.0
S02
- P1»M
1799.0
21.2
******
8.3
NOX
•ppw
******
563.4
504.1
550.4
NOX*1
' " PPM
******
******
324.2
311 .1
NOX*2
PPM
733.2
695.6
714.4
629.8
HUM.
#'/#
0.052
0.160
0.160
0.174
DEW
PtJINT'
F
113.0
147.7
147.7
151.6
STAT
-~PR^S '
IN.WG
-0.1
-13.5
1.4
0.0
N02 FLOW DATA
NO? FLOWRATE,#/MIN
N02/N0< PDS BASIS)
N02/NO(FC I ROTO)
0.0
-0.11
0.0
SCRUB.PERFLIRMANCE
S02 ABSORB. 61.02
NOX ABSORP. -9.17
- 1MO*1 ABSORP -4^0S
NOX2 ABSORP 11.84
- G-A-S- -vet :f-ps i-;n •-
L/G,GAL/MCF 142.2
L/G,#/# 19.9
PRES.DROP,WG 0.1
SPRAY SLURRY ANAIYSIS
MGO,GM/100ML 0.587
MGSQ3|-SOtI15)-,M- — OvO03-t
MGS03(TOTAL) ,M 0.0137
MATERIAL BALANCE
NOX SCRUBBER
lN1>UTf #/HR
OUTPUTf#/HR
PHYSICAL PROPERTIES OF
RECYCLED SLURRY
PH
CONDUCT.MICROMHOS
SPECIFIC
8.15
6870.
-1.01:2
MG(N02)2» MOLAR
MG(tJO:»)2, MOLAP
TSS,GM/100ML
NITRITE/NITRATt
0.0096
0.0000
3.326
******
SULFUR
0.07
0.24
MAGNtSlUM
1.51
0.81
WATER
629.7
567.6
**
NITROGEN
0.75
0.87
MAKEUP MGO COMPOSITION
SLUPRY CONC.,GM MGO/100ML=
4.00
NOX = PDS ANALYSIS
*1-— SALTSHAN
NOX*2 = FUEL CELL ANALYSIS
** OXIDIZED NITROGEN ONLY
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM-OUTPUT DATA PAGE 1
RUN NUMBER 8-B
FLUE GAS DATA
PRIMARY AIR
SECONDARY AIR
FUSNACf: EXIT
PART. SCRB. INLET
PART. CYC. EXIT
VENT ABS. INLET
ABS CYC. EXIT
FLOATING BED IN
-PLWTING 8E-0 EX
P.P. EXIT ORIF.
DATE 9-23-71 TIME OF
FLOW
#/HR
486.
4602.
5485.
5485.
3535.
*****
*****
3535.
-3^t»;
3703.
TEMP.
F
115.0
710.0
590.0
485.0
138.0
******
******
138.0
-0.0
130.0
S02
PPM
1688.7
******
1557.1
******
******
******
- — ***-***—
13.2
S03
PPM
*****
*****
*****
*****
*****
*****
- ******
*****
DAY 1345
NOX
PPM
*****
*****
*****
*****
*****
*****
*****
580.
FLYASH
GR/nSCF
*******
*******
*******
*******
*******
*******
*******
*******
HUM.
#/*
0.011
0.014
0.055
0.055
0.137
******
******
0.137
' 0". 167"'
0.167
DEW DRY
POINT FLOW
F #/HR
64.7 483.
70.4 4541.
114.5 5200.
11 A 1 — — —
143.3 3109.
*****
*****
143.3
'1^4'8v7- ' ' - — ---••-
148.7 3174.
STAT
PRES
IN.H20
\~&' ft' —
5.6
• o~« o
2.7
-8.1
*****
*****
-8.1
— 14.9
-14.9
SCRUBBER STREAM DATA
PARTICIPATE
MAKEUP WATER
---- TOODOCT 'tlQ;-
RECIRCULATED 1.10.
VENTURI ABSORBER
FBA
TEMP,F FLOW.GPM
60.0 0.0
GAS ABSORBER
TEMP,F FLOW,*/M TEMP.F FLOW,#/M
140.0
19.78
MAKEUP WATER *****
"MAKEUP MGO—St. -*****
PRODUCT LEO. *****
REC.(SPRAY NOZ) *****
REC.tFLflW NOZ.)
*****
3". 2
*****
*****
*****
60.0
0« V
137.0
137.0
1.0
-O ~i
3.2
0.0
0.0
385.0
FURNACE PERFORMANCE
HEAT RELCASE.BTU/HP
* FUEL AS COAL
COAL FLOW RATE.0/HR
NAT.GAS FLOW,#/HR
X EXCESS AIR
OXYGEN,%DRY,MEAS.
C02tZDRY-CArC.
HUMIDITY,#/# - CALC.
S02 ABSORPTION PARAMETERS
VENTURI ABSORBER
SCRUBBER PERFORMANCE
0
.«523E 07-
96.2
413.5
8.9
17.6
3.70
14.'ff6 ~
0.055
"-SO 2 ABSORBiEFF
FLYASH COL. EFF
SD3 ABSORB. EFF
NOX ABSORB. EFF
GAS VELOCITY, FPS
LIO/GAS,GAL/MCF
PRES.DROP»IN.WG
-FLOATING BED ABSORBER
SULFITE/S02-MOL/MOL = ******
SUMP RES1D.TIME.MIN = ******
***** MEANS ITEM NOT MEASURED
SULFITE/S02-MOL/MOL
SUMP-RES1D.TIME,-MIN
PART.
7.79
******
******
******
96.3
20.7
2.~B"
3.3
25.08
******
VFNT ABS.
******
******
******
******
******
******
******
******
FLOAT.BED
99Y15
******
******
******
6.2
58.1
-6-V2-
4.7
SULFATE FORMATION PARAMETERS
CONC.,GM-MOLE/L= ******
— MOL? TOT"A~C SUL"F'= *****
02 AT FURN. EX.= 3.70
02 AT ABSORB.IK= *****
02 AT ABSORB.FX= *****
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM - OUTPUT DATA PAGE 2
RUN NUMBER 8-B
MATERIAL BALANCES
FURNACE
INPUT,»/HR
OUTPUT,#/HR
PART.SCRUBBED
INPUT,#/HR
OUTPUT,#/HR
S02 ABSORBERS
INPUT,#/HR —
OUTPUT,#/HR
*
*S02 ABSORBERS-
PRODUCT COMP.
" TOTAL ,"
COMBINED
FRE-E
MONO (TOTAL)
MONtJ(DISSOLVED)
MONO(SOLID)
- "BtJUtPTTE
MGO
SULFATE
MAGNESIUM
FtrYASH
SOLIDS,MG
DATE 9-23-71
SULFUR MAGNESIUM FLYASH
TIME C1F DAY 1345
15.30
9.1R
9.18
5.06
30.60
******
0.04
GM S02/
100ML
******
GM-MOLE/
LITER
******
**-****-
******
GRAM/
IOOML
WATER
265.5
284.7
321.
426.
-—6-73".
529.
DRY GAS
5193.
5200.
5200.
3109.
INPUT FOR EO. - KIN.PROG.
INPUT FLOWS,#ATOMS/100*FEED
CARBON 0.462460
HYDROGEN 0.558342
NITROGEN
SULFUR
5.060255
0.008780
FE-EO RATEff/SCC> t-
-8N TttALPY,BTtr/-T -=• — -
3174.
2.23
0.0
2.23
1.12
1.11
— 0;t) "
0.85
3.08
0.3480
0.0
0.3480
0.1750
0.1710
0.0
0.1329
0.4809
COAL COMPOSITION-MASS
CARBON
HYCROGEN
OXY+NIT
SULFUR
ASH
- WATER
0.7150
0.0485
0.0817
.0370
0.0740
-0.0438
1.820
3.669
0.0
0.532
******
******
2.640
MAKEUP MGO COMPOSITION
SLURRY CQNC.- GM MGO/IOOML =
MGO PRESLAKED, N0=0, YES=1
S - S L AK-EO-TG -
4.00
0
PRODUCT MG BASE PHYSICAL PROPERTIES
ACID STRENGTH, PH = 8.05
SP.GRAVITYjHYDROM. = -*******
PARTICULATE SCRUBBER PRODUCT
ACID STRENGTH , PH = 6.35
FtYASH CONC. GM/IOOML = *****
*SOLIDS FREE BASIS, MASS/VOLUME SOLUTION
-------
RUN NUMBER 8-B
DATE 9-23-71
TIME OF DAY 1345
FLUE GAS OATA FLOW TEMP
FURNACE EXIT 5485. 590.
FLOAT. BED EX 3703. 130.
NOX SCRUB IN 3719. 164.
NOX SCRUB EX 3759. 12P.
NOX SCRUB. DATA TEMP. FLOW
F #/MlN
MAKEUP WATER 60.0 0.81
MAKEUP MGO 60.0 2.00
PRODUCT LIQ. 130.0 2.90
"ftEC'l R C .• 1_ TO". 13 0 ; 0 1"? 5tt: ~
N02 FLOW OATA
N02 FLOWRATE,#/MIN 0.03
N02/N01 PITS' BASIS) 0.56
N02/N01FC £ ROTO) 0.46
MATERIAL BALANCE
SULFUR
NOX SCRUBBER
INPUT, #/HR 0.04
OUTPUT, #/HR 0.14
S02 NQX
NOX*1
PPM PPM PKM
0 1688.7 ****** ******
0 13.2 580.4 ******
0 ****** 906.0 802.1
0 ****** 947.5 566.9
NOX*2 HUM.
PPM #/#
759.6 0.055
873.6 0.167
****** 0.167
****** 0.179
DEW STAT
POINT PRES
F IN.WG
114.5 0.0
148.7 -14.9
148i 7 1.4
152.5 0.0
SCRUB. PERFORMANCE SPRAY SLURRY ANALYSIS
S02 ABSORB.
NOX ABSORP.
-NOXI A-BSORP
NQX2 ABSORP
GAS VfcL.rPS
L/G,GAL/MCF
L~/Gl#/
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM-OUTPUT DATA PAGE 1
RUN NUMBER 9-D
FLUE GAS DATA
- PRIMARY AIR
SECONDARY AIK
-FOR1MACE- EXIT
PART.SCRB.INLbT
PART.CYC.EXIT
VENT ABS.INLET
A8S CYC.EXIT
FLOATING BED IN
- FtOATING BED EX
P.P. FX1T ORIF.
SCRUBBFR STREAM DATA
PARTICULATE
MAKEUP WATER
PRCTOUCT LIQ.
RECIRCULATED LIO.
FURNACE PERFORMANCE
M&AT KbLEASE,BTU/HR
1 FUEL AS CUAL
COAL FLOW RATE,#/HR
NAT. GAS Fl.OW,0/HR
« EXCESS AIR
OXYGEN, *DRY,MEAS.
DATE 9-23-71
TIME OF DAY 1500
FLOW
#/HR
486 .
T1 j n I •
54-6-4-.
5464.
3543.
*****
*****
3543.
3 7-05 i
37C5.
TEMP.
F
1 20 . 0
"7 1 "7 K
71 7. ">
590.0
490.0
138.0
******
******
138.0
0.0
130.0
S02
PPM
698.0
******
698.0
******
****** -
******
*******
4.2
S03
PPM
*****
*****
*****
*****
*****
*****
*****
*****
NOX
p-pw
*****
*****
*****
*****
-*****-
*****
*****
0.
FLYASH
GR/OSCF
*******
*******
*******
*******
- *******
*******
*******
*******
HUM.
#/*
OO1 ?
. w 1. c.
0 012
\s • W L £_
0.053
0. 053
0.137
******
******
0.137
0.166
0.166
DEW
POINT
F
66. 0
U t7 • W
67.4
113.8
113. R
143.5
*****
*****
143.5
148.7
14R. 7
URY STAT
FLOW PRES
#/HR IN.H20
481. 14.<»
4531. 5.7
2.7
-6.8
*****
TEMP.F
60.0
138.0 - '
138.0
FLCWtGPM
0.0
OiO-
20.02
GAS ABSORBER
MAKEUP WATER
-MAKEUP MGO SL .
PRODUCT LIQ.
REC. (SPRAY NOZ)
REC.(FLOW NOZ.)
VENTU&I ABSORBER
TEMPtF FLOW,#/M
***** *****
***** 3.2
***** *****
3116.
4
4
-fl.l
3177. -14.9
FBA
TEMP,F FLOW.0/M
*****
*****
*****
60.0
O-.-O
137.0
137.0
0.6
- - 3-i2
0.0
0.0
380.0
HUMIDITY, #/# - CALC.
>02 ABSORPTION PARAMETERS
VFNTURI ABSORBER
519E "7
96.2
410.1
8.9
- 18.1
3.80
W-'TT-
0.053
SCRUBBER PERFORMANCE
S02 ABSORfl;EF-F
FLYASH COL.EFF
S03 ABSORB.FFF
NOX ABSORB.EFF
GAS VELOCITY,FPS
LIQ/GAS,GAL/MCF
PRES.DROP,IN.WG
PART.
-0.0
******
******
******
96.1
21.0
3.3
VENT ABS.
- --- ****** -
******
******
******
******
******
*** **•*"
******
FLOAT. BED
******
******
******
6.2
57.3
FLOATING BED ABSORBER
• —«- ******
SULFITE/S02-MOL/MOL = ******
-SUMP RES-ID.TIME,MIN = ******
***** MFANS ITEiv NC'T MEASURED
SULFITE/S02-MOL/MOL
SUMP RESID. TIME, MIN
- - 3-3-s 7 -
******
******
4.7
SULFATE FORMATION PARAMETERS
CONC.,GM-MOLE/L= ******
- - -MOt? -TOT*t- SULF- -*****- -
02 AT FURN. FX.= 3.80
02 AT-ABSORB.IN= *****
02 AT ABSORB.EX= *****
-------
RUN NUMBER 9-D
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM - OUTPUT DATA PAGE 2
DATE 9-23-71 TIME OF DAY 1500
MATERIAL BALANCES
FURNACE
INPUT,*/HR
OUTPUT,#/HR
PART.SCRUBBER
INPUT,#/HR
OUTPUT,#/HR
S02 ABSORBERS
rNPUT-v-f7fffl
OUTPUT,#/HR
*
*S02 ABSORBERS-
PRODUCT COMP.
SULFUR MAGNESIUM F1YASH
TO1
COMBINED
FREE
MUNO(TOTAL)
MONCK DISSOLVED)
MONO(SOL ID)
BISULFITE
MGO
SULFATE
MAGNESIUM
FLYASH
SOLIDStMG
15. 17
3.78
3.78
2.27
2 ^27
******
GM S02/
100ML
--*«»»*
*****
*****
*****
*****
*****
*****
*****
*****
*****
"**** ** -----
******
GM-MOLE/
-tTTER-
-~****** ----
«*«*«*
30.35
******
******
******
-**•
******
GRAM/
TOOM1.-
WATER
^57.9
277.1
340.
426.
DRY GAS
SlflO.
5137.
5187.
3116.
INPUT FOR EQ. - KIN.PROG.
INPUT FLOWS,#ATOMS/100#FEED
C'ARBON- ~ Oi 4-5999B ~
HYDROGEN 0.56-1502
OXYGE-N- •• i.39505^ — -
NITROGEN 5.062521
SULFUR 0.008732
FEE-D RATE,*/SEC*
527.
3177.
MAKEUP MGO COMPOSITION
" SLURRY CONC.- GM MGO/10t)ML = ******
MGO PRESLAKED, N0=0, YES=1 0
—r-SLAKED "re-tt€(OH)2fMEift-S-.-—= —-*-*****
-******-
#*»*«*
******
******
******
-*-***•**
******
-*•*****
******
PRODUCT MG BASE PHYSICAL
ACID STRENGTH, PH
SP .-GR AVI TYfHYDROM.
PROPERTIES
*****
*******
******
******
PARTICULATE SCRUBBER PRODUCT
ACID STRENGTH , PH = *****
FLYASH CONC. GM/IOOWL = *****
COAL COMPOSITION-MASS
CARBON
HYDROGEN
OXY+NIT
-SULFOR- - *
ASH
WATER
0.7150
0.0485
0.0817
0. 0370
0.0740
0.0438
-------
RUN NUMBER 9-0
DATE 9-23-71
TIME OF DAY 1500
FLUE GAS DATA
-FURNACE" EXIT
FLOAT.BED EX
-NU* SCRUB IN
NOX SCRUB EX
FLOW
~#/HR~ *
5464.
3705.
3715.
3758.
TEMP.
- —p-
590.0
130.0
166.0
128.0
502
• "PPM
698.0-
4.2
******
******
NOX
PPM
-******
0.0
1026.2
717.5
NOX* I
PPM-
******
******
937. I
857.8
NOX*2
PPM
******
******
******
773.6
HUM.
#/#
O.G53
0.166
0 . 166
0. 179
DEW
POINT
F
113.8
148.7
- 148.7
152.6
STAT
PRfS
IN.WG
0.0
-14.9
I. A
0.0
NOX SCRUB.DATA TEMP.
F
MAKEUP WATER 60.0
MAKrEttP "MGO" 60vO~
PRODUCT LIQ. 130.0
FLOW
fl/MIN
0.81
2-. 30
3.20
N02 FLOW DATA
N02 F-LOWRATE,#/MIN
N02/N0( PDS BASIS)
N02/NO(FC L ROTO)
0.06
*****
*****
SCRUB.PERFORMANCE
S02 ABSORB.
NOX ABSORP.
NOX1 -ABSORP
NOX2 ABSORP
G-AS -v&trvf-ps- •
L/G.GAL/MCF
L/G,#/#
PRES.DROP,WG
30.08
8.46
11.84
- IT. 8
143.7
20.2
0.1
SPRAY SLURRY ANALYSIS
MGO,GM/100ML
MGS03(SOLI-D),M
MGS03(TOTAL),M
MG(N02)2, MOLAR
MG(N03)2f MOLAR
TSStGM/iOOML
0.900
0;0031
0.0037
G;0134
0.0124
0.0003
3.373
MATERIAL BALANCE
NOX SCRUBBER
INPUT,#/HR
OUTPUT,#/HR
SULFUR MAGNESIUM WATER NITROGEN
NITRITE/NITRATE 41.333
MAKEUP MGO COMPOSITION
SLURRY CONC.,GM MGCJ/100ML'
4.00
0.01
0.11
3.31
1.17
709.9
575.0
1.50
l.ll
PHYSICAL PROPERTIES OF
RECYCLED SLURRY
PH
CONDUCT. MICROMHOS
8.20
6080.
NOX = PDS ANALYSIS
NOX»1 = SALr
NOX*2 = FUEL CELL ANALYSIS
** OXIDIZED NITROGEN ONLY
-------
RUN NUMBER 10-G
FLUE GAS DATA
PRIMARY AIR
SECONDARY AIR
FURNACE EXIT
PART.SCRB.INLET
PART.CYC.EXIT
VENT ABS.INLET
ABS CYC.EXIT
FLOATING BED IN
—FtQ-A-T-ING BED E'X' ' '
P.P. EXIT ORIF.
SCRUBBER STREAM DATA
PARTICULATE
MAKEUP WATER
PRODtJCT lrIO.
RECIRCULATED LIQ.
FURNACF PERFORMANCE
HEAT RELEASE, BTUAHR
* FUEL AS COAL
COAL FLOW RATEt#/HR
NAT. GAS FLOW,#/HR
% EXCESS AIR
OXYGEN, SDRY.MEAS.
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM-OUTPUT DATA PAGE 1
DATE 9-24-71 TIME OF DAY 1200
FLOW
#/HR
482.
4640.
5516.
5516.
3639.
*****
*****
3639.
3 r So •
3798.
TEMP.
F
110.0
690.0
490.0
410.0
130.0
******
******
130.0
0.0
125.0
S02
PPM
17B3.4
******
1595.7
******
******
******
V W V W
4.1
S03
PPM
*****
*****
*****
*****
- *****
*****
»•**»*
*****
NOX
PPM
*****
*****
*****
*****
-'*****
*****
£$.?JP9
609.
FLYASH
GR/DSCF
*******
*******
*******
*******
*******
*******
*******
*******
HUM.
#/»
0.008
0.012
0.-053
0.053
0.119
******
******
0.119
. 147
0.147
DEW
POINT
F
56.9
66.9
113.7
113.7
139.2
*****
*****
139.2
145.0
145.0
DRY
FLOW
#/HR
478.
45.85.
5239.
3251.
3312.
STAT
PRES
IN.H20
14.9
5.2
OTO
2.7
-8.1
*****
-8.1
-14.9
-14.9
VENTURI ABSORBER
FRA
HUMIDITY, it/It - CALC.
S02 ABSORPTION PARAMETERS
VENTURI ABSORBER
"KG A r, ITMOCE 7HR~F T3 , ='
SULFTTE/S02-MOL/MOL = ******
SUMP RESID.TIME,MIN = ******
MCANS ITFM NOT MEASURED
TEMP.F FLOW,GPM
60.0 0.0
r52TO- ~ OTO
132.0 19.78
SCRUBBER PERFORMANCE
, 524E 07 'SO2- ABSORB.rEFF
96.2 FLYASH COL.EFF
414.1 S03 ABSORB.EFF
9.1 NOX ABSORB.EFF
18.1 -GAS VEtTOCITY.FPS
3.80 LIO/GAS,GAL/MCF
0.053
iAi AB5TJKUEK ltl"IP»l- 1
MAKEUP WATER *****
MAKEUP MGO SL . *****
PRODUCT LIQ. *****
REC.C SPRAY NOZ) *****
REG. (FLOW NOZ.)
"L.UW t w/ n
*****
.5
*****
*****
*****
60.0
0.0
130.0
130.0
0.6
. 5
0.0
- o.o
385.0
PART. VENT ABS. FL
ro~.53 ******
****** ******
****** ******
****** ******
96.3' ****** .
20.7 ******
2.7
******
OAT. BED
99.'74
******
****** " ~ ~
******
6.3
57.5
6.1
PRES.DROP,IN.WG
3.5
******
5.2
FLOATING BED ABSORBER
SULFITE/S02-MOL/MOL
SUMP RESlD.TrME.MIN
28.05
****-**
SULFATE FORMATION PARAMETERS
CONC.tGM-MOLE/L= ******
-HOtT TOTAL SULF= -**Krv*
02 AT FURN. EX.= 3.80
02 AT 'ABSORB. I N= -*****
02 AT ABSORB.EX= *****
-------
MAGNESIUM BASE
RUN NUMBER 10-G
MATERIAL BALANCES
SULFUR
FURNACE
INPUT»B/HR 15.32
OUTPUT, #/HR 9.77
PART. SCRUBBER
INPUT ,#/HR 9«77
OUTPUT, #/HR 5.42
S02 ABSORBERS
IIMPUTfff/HR 9.42
OUTPUT, #/HR 0.01
*S02 ABSORBERS- GN S02/
PRODUCT COMP. -t-00«t-
__ TfVT^rt • ^ AC
I U 1 AL « -3« U5
COMBINED 3.05
FRE E OvO
MONO( TOTAL) 3.05
-Mnun-j-n-T-c-cni uEfvt-- i-^-»& •
nuraui L» i 33UL vcui i«?*t
MONO(SOLIO) 1.71
BISULFITE 0.0
MGO 0.59
- SULFATE --*****
MAGNESIUM 3.64
fLYASH «.---
cm tnc nr _
COAL COMPOSITION-MASS
CARBON 0.7150
HYDROGEN 0.0485
OXY+NIT 0.0817
-— . -o-i-ti <= i fA- -A., rtO^-ri ...»
bULrUK U • Udru
ASH 0.0740
WATER 0.0-438
SLURRY
DATE 9-24-71 T
•
MAGNESIUM
7.41
******
GM-MOLE/
1.ITE-R
• 4764
0.4764
0.0 -
0.4764
-A — O-A-QA- —
U* ^UM«t
0.2670
.0
0.0921
-*#«***-
0.5684
.
.
FLY-ASH
' '30.&4"
******
******
******
******
******
GRAM/
-teoMt -
- ^;»-.»w
•O t ^"^
£.177
5.660
.0
0.368
- ******
—******
3.161
— —
.
SCRUBS mG PROGRAM - OUTPUT DATA PAGE 2
IME OF DAY 1200
INPUT FOR EQ. - KIN. PROG.
• ttATER" ORY"t51»rS -- . . _. . .
INPUT FLOMS,#ATOMS/100#FEED
25J.fr —52-32. "CftfrBOW^ ~ O~. 4-59919- -
277.2 5239. HYDROGEN 0.528744
1 OXYGEN 1.3950*3'
NITROGEN 5.062600
340. 5239; SULFUR O.O08727
388. 3251.
•;- — •- - - - Pf€O--RATEt #y^~EC»- 1.52
625. ' 3251. ENTHAfPY,-enjy-#--= -1857.
486. 3312.
MAKEUP MGO COMPOSITION
SLWHV -CONCi — GM M©G/H5OML - 5^80
MGO PRESLAKED, N0=0, YES=1 0
SLAKED TO MGl OH|2 , MEAS . = — ******
rKUDUCT MG BlVSc rnYSICAL KKDPER rIES
AC lO STRENGTMf PM — 7»95
SP .GR AVI TY,HYDROM. = 1.O200 . . . .
- — — -o -A-CK7- T-fM-tl A T- C- t^F-OI-i-Q-Q-Cf* -Oflf*fMt*~T - - ... - -. .- .
TAICI rUULAit StKtltyocK TRuDUCT
ACID STRENGTH , PH = *****
rLTASH CONC* GM/1OOML — ***** — - - —
- — - — - — . _.
.
"SOLIDS FREE BASIS, MASS/VOLUME SOLUTION
-------
RUN NUMBER LO-G
DATE 9-24-71
TIME OF DAY 1200
FLUE GAS DATA
FURNACE EXIT
FLOAT.BED EX
NOX SCRUB IN
NOX SCRUB EX
FLOW
"S71HR--
5516.
3798.
3761.
3807.
TEMP.
— F
490.0
125.0
160.0
122.0
S02
- -ppM
1783.4
4.1
******
******
NOX
PPM "
******
608.8
766.0
1709.5
NOX*1 NOX*2
—-PPW PPM' '-•
HUM
******
******
680.8
491.6
692.4
645.6
729.9
655.0
0.053
0.147
0.-147
0.161
DEW
POINT
F
113.7
145.0
145.0
149.4
STAT
"PR'ES
IN.WG
0.0 "" '
-14.9
1.4 - - -
0.0 '
NOX SCRUB.DATA TEMP. FLOW
F */MIN
60.0 0.81
60.0 2.90
123.0 4.00
V23TO 125-0.
MAKEUP WATER
M-AKEUP MGO
PRODUCT LIO.
SCRUB. PERFORMANCE
S02 ABSORB. ******
NOX ABSORP. *****,*
NOX I A'BSORP ' 27^79-
NOX2 ABSORP 10.26
NO2 FLOW DATA
N02 FLOWRATE,#/M1N 0.03
N07/NOI PDS BASIS) 0.26
N02/NOCFC 6 ROTO) 0.65
L/GtGAL/MCF 145.4
L7GT«/# 19.9
PRES.OROP«WG 0.1
SPRAY SLURRY ANALYSIS
MGOtGM/lOOML 0.562
MGS03IS01IDI ,-M 0.0031
MGS03-
MG(N02I2, MOLAR 0.0055
-MGIN03»21 MOLAR 0.-Q006
TSStGM/lOOML 1.576
NITRITE/NITRATE 9.167
MATERIAL BALANCE
NOX SCRUBBER
INPUT,#/HR
OUTPUT,#/HR
SULFUR MAGNESIUM WATER
0.01
0.08
5.22
0.91
"6-95.-0
530.8
**
NITROGEN
2.60
MAKEUP MGO COMPOSITION
SLURRY CONC..GM MGO/100ML-
5.00
PHYSICAL PROPERTIES OF
RECYCLED SLURRY
PH
CONDUCT.MICROMHOS
GRAVITY-
8.'25
660.
" TTOTtT
NOX = PDS ANALYSIS
= -S7STTS1WN
NOX*2 = FUEL CELL ANALYSIS
** OX1DTZFD NITROGEN CKLY
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM-OUTPUT DATA PAGE I
RUN NUMBER 11-H
DATE 9-24-71
TIME OF DAY 1330
FLUE GAS DATA
PR IMAR Y AIR
CCfnKinADV ATD
dCLUnUMKT A1K
eiin»*-«r>g es v i T
FLOW
»/HR
48O.
tf. "7 f\1
*r f Ut .
0-B-A-4
TEMP.
TtO.T)
f*Q 1 Tl
oy i . j
SG2
PPM
S03
— PPtl-"
* * * * * —
NOX
•~PPM
^ Jh Jh * *
FLYASH
GR/DSCF
A A ft * * * A
HUM.
tf /#
0 .009
On l A.
. O 1H
DEW
POINT
F
58.4
T> n
r^.u
— « « * a —
DRY
"FllOW
#/HR
476.
CO t. v. •
3.80
*****
*****
***** MEANS ITEM NOT MEASURED
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM - OUTPUT DATA PAGE 2
RUN NUMBER 11-H
MATERIAL BALANCES
FURNACE
INHUT,#/HR
OUTPUT,#/HR
PART.SCRUBBER
I-NPUT,»/HR
OUTPUT,#/HR
S02 ABSORBERS
INPUT,#AHK - -
OUTPUT,#/HR
*
*S02 ABSORBERS-
PRODUCT COMP.
COMBINED
FREE
MONO(TQTAL)
-MONOIDISSOLVFD)
KONO(SOLin)
-BISULFITE
MGO
SULFATE
MAGNESIUM
FLYASH
SOL I OS,MG
SULFUR
15.4M
9.96
9.96
DATE 9-24-71
MAGNESIUM FLYASH
TIME OF DAY 1330
30.95
******
******
******
WATER
271.0
290.5
354.
4O6.
DRY GAS
5283.
5290.
5290.
3143.
INPUT FOR EQ. - KIN.PROG.
INPUT FLOWS,#ATOMS/100*FEED
CARBON 0.459979
HYDROGEN 0.533.617
OK Y GEN 1.39504-8 ' "
NITROGEN 5.062540
SULFUR 0.008731
FEED RATE,-0/SEC= 1.54 -
~ •4V'82"~ " ~
0.10
GM S02/
100ML
4.06
IM. CIA
t . uo
0.0
l^ flA
H . UO
1.38
2.68
OiO
1.25
*****
3Tt 1
. 31
6-.-6'8-
******
GM-MOLE/
LITER
n " f^T
L. • O j H *t
0.0
f\ f*. "3 A A.
\J m O O*T*#
0.2156
0.4188
OVO
0.1960
******
OQI nt
. so UJ
-*«r**** 6-2-2.-
****** 506.
GRAM/ MAKI
- rODML-"— SLl
MG(
* •
--*»*=.»- PR 01
___ AT '
2.242 SP
8.878
OTO -
0.784
****** PAR'
______ Af"
11 ACC
L • Ov J
3214.
MAKEUP MGO COMPOSITION
SLURRY CONC.- GM MGO/100ML
MGO PRESLAKED, N0=0, YES=l
5.80
0
PRODUCT MG BASE PHYSICAL PROPERTIES
ACID STRENGTH, PH = 8.00
SP.GRAVITY,HYDROM. = *******
PARTICULATE SCRUBBER PRODUCT
ACID STRENGTH , PH = 6.70
FLYASH CONC. GM/100ML = *****
COAL COMPOSITION-MASS
CARBON
~ HYDROGEN
OXY+NIT
SULf-UK
ASH
— WATER
0.7150
0.0485
0.0817
0.03/0
0.0740
0.04'38
*SOLIDS FREE BASIS, MASS/VGLUME SOLUTION
-------
RUN NUMBER ll-H
DATE 9-24-71
TIME OF DAY 1330
FLUE GAS DATA
- F-URNA-C-E- EX
FLOAT. BED
NOX SCRUB
NOX SCRUB
rr
EX
tN
EX
FLOW
#/HR
-5531-.-
3721.
368^.-
3736.
TEMP.
F
130*0
164.0
126.0
SQ2
PPM
-i-eois-2 —
30.9
******
NOX
PPM
469.5
-~91r3v9
274. 1
NOX*1
PPM
******-
******
509^7
NOX*2 HUM.
DEM
PPM #/# PU1NI
F
743 -TT — 0.055 H4.8
664.4 0.157 147.2
-Tfr6ri-t O-i-157- -t*7v2—
505.3 0.172 151.5
STAT
PRES
IN.WG
-14l9
T..4
0.0
NOX SCRUB.DATA TEMP. FLOW
SCRUB.PERFORMANCE
SPRAY SLURRY ANALYSIS
MAKEUP WATER 60.0
MAKEUP MGO 60.0
PRODUCT L 10. 128.0
RECIRC. LIO. 128*0
N02 FLOW DATA
N02 FLOWRATE,#/MIN
- N02/N01 PDS BAS-1-S-)
N02/NO(FC & ROTO)
ft SHIN
0.81
4.15
4.80
• ^Crt
129O.
0.03
O.^5
0.65
suz ABSORB; •
NOX ABSORP.
NOX1 ABSORP
NOX2 ABSORP
GAS VEL.PPS
L/GtGAL/MCF
PRES.OROP,WG
MATERIAL BALANCE
- — - — - - C-4H-- CUP —M-A-PMg.C-T-1-Ha I.I » T g O •
»»****
70.00
26.79
35.71
• 8
146.4
0.1
MGO*GM/100ML
MGS03( SOL IDI «M
MGS03 (TOTAL) ,M
MG(N02)2, MOLAR
TSS,GM/100ML
NI TRITc/NI TRATt
0.450
0.0031
0.0033
• 0056
0.0119
O.OO27
1.409
4s 40 7
** MAKEUP MGO COMPOSITION
NOX SCRUBBER
- fNf>UTt#/MR
OUTPUT,«/HR
---- 7-;-4r7
0.08 0.94
787. a
554.0
0.52
PHYSICAL PROPERTIES OF
R-ECYCLED SLURRY
-PM
CONDUCT.MICROMHOS
SI^ECtf^C GRAVITY
535.
1.050
NOX = PDS ANALYSIS
- t»CX*r g"SALTSHAN" ANALYSIS
NOX*2 = FUEL CELL ANALYSIS
** OXiniZFD NITROGEN ONLY
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM-OUTPUT DATA PAGE 1
RUN NUMBER 12-A
FLUE GAS DATA
PRIMARY AIR
SECONDARY AIR
FURNACE EXIT
PART.SCRB.INLET
PART.CYC.EXIT
VENT ABS.INLET
ABS CYC.EXIT
FLOATING BED IN
FLOATING - BED~ E*
P.P. EXIT ORIF.
DATE 9-24-71
TIME OF DAY 1430
SCRUBBER STREAM DATA
PARTICULATE
MAKtUP WATER
PRODUCT-riOT
RECIRCULATED LIQ.
FURNACE PERFORMANCE
FfEAT RELEASE,BTU7HR
% FUEL AS COAL
COAL FLOW RATE,#/HR
NAT.GAS FLOW.&/HR
% EXCESS AIR
OXYGEN,?DRY,MEAS.
C02 * yDRY=T7AUCT
HUMIDITY. ,1/lt - CALC.
SQ2 ABSORPTION PARAMETERS
VENTURI ABSORBER
FLOW
#/HR
481.
4704.
5583.
5583.
3550.
***** *
3550.
3713.
TEMP,F
60.0
I38TO"
138.0
TEMP.
110.0
692.5
560.U
460
138
***
.0
.0-
**
S02
PPM
741.8
******
1479.5
******
S03 NUX FLYASH HUM. DEW
PPM PPM GR/DSCF #
•_.• —. — n
u
/ff KU1NI
F
.010 62.7
.014 72.0
DRY
#/HR
476
4638
***** ***** -*-****** O.ua^j i j.«».'* "arz^
***** ***** ******* o
***** ***** ******* o
.055 114.
.132 142.
9
3
3137
***** ***** ******* ****** *****
^^ .^^.A ^ * «. •.«*•• *'*•..•.- • •. .«_ .A. .*. .1. •_ .*_.».*._••.•. _•..«..•_.•_•.
135
132
»» ****** ***** ***** ******* **
.0 ****** ***** ***** ******* o
. 0
.0
FLOW
0.
0.
19.
*»**•*»
30.9
iGPM- ~
0
0
78
***** ***** *****¥4> U
***** 502. ******* o
VENTUR
XJAS ABSORBER TEMP.F
MAKEUP WATER *****
MAKEUP MGO SL. *****
PRODUCT LIO. *****
REC. JSPRAY NOZ1 *****
REC.CFLOW NOZ.)
**** ****
.132 142.
. 160 147.
.160 147.
I ABSORBER
FUOW.3/M
*****
3.2
*****
*****
*****
*
3
7
7
3201
FBA
TEMP.F
60.0
0.0
136.0
136.0
STAT
PRES
IN.H20
14.9
5.8
. 0.
2.
. isr8v
u
7
.j. _.
- *****
^
-8.
- -14.
-14.
t
1
9
9
Ftouiir/fi
0.6
3.2
0.0
0.0
385.0
-
E SCRUBBER PERFORMANCE PART. VENT ABS. FLOAT. BED
'HR 0.-529E 07 ~
96.2
'HR 418.4
^ 9.1
18.1
3.80
14. 77
\LC. 0.055
so 2" A-B-SOR B-.'EF F
FLYASH COL.EFF
S03 ABSORB. EFF
NOX ABSORB. EFF
- GAS VELOCITY, FPS
LIQ/GAS,GAL/MCF
Llu/bAS? #/#
PRES. DROP, IN. WG
__. 15T06— -
******
******
******
95.9
20.8
2.8
3.3
-- ****tr?
******
******
******
******
******
******
' -97;9X
******
****** —
******
6.2 -~
58.4
6. 2
6.0
FLOAT ING-
SULFATE FORMATION PARAMETERS
******
SULFITE/S02-MOL/MOL = ******
SUMP RE SID.TTMEiMIN~=******
***** MEANS ITEM NUT MEASURED
-XbA,#HOLE/HK-M J
SULFITE/S02-MOL/MOL
fM IN
25TT
31.77
CONC.,GM-MOLE/L=
HOL^ TOTAL SULF-^
02 AT FURN. EX.= 3.80
—02' AT ABSORBVIN^" *****-
02 AT ABSORB.EX= *****
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM - OUTPUT DATA PAGE 2
RUN NUMBER 12-A
DATE 9-24-71
TIME OF DAY 1430
MATERIAL BALANCES
SULFUR MAGNESIUM" FtY-ASH WATER
FURNACE
I-NPUT,#/HR 15-.48 -
OUTPUT,#/HR 9.63
PART. SCRUBBER
INPUT, #/HR 9.6-3 -
OUTPUT,#/HR 4.85
S02 ABSORBERS
INPUT, #/HR ' 4.85
OUTPUT, #/HR 0.10
*
*S02 ABSORBERS- GM S02/
PRODUCT COMP. 100ML
•"* 1 !f A • * — *
TuiALi *t » 54
COMBINED 4.54
COC c - n -n
MONO {TOTAL) 4.54
MONO (DISSOLVED) Iv36 —
MONO(SOLID) 3.18
"B I SUL-f5"! TE • • " -QrQ —
MGO 1.52
SULFATE *****
MAGNESIUM 6.06
FtTYASH =-^_^ -
cni i nc ttr _____
COAL COMPOSITION-MASS
CARBON 0.7150
HYDROGEN 0.0485
OXY+NIT 0.0817
SULFUR 0.t)J70
ASH 0.0740
WATER 0.0438
*
— «--- - 3t)^J6 - 2 71-. 7
-— — — - ****** -J5*.
****** 413.
O*o8 VV**** o 3"O •
****** *****# 512.
—
GM-MOLE/ GRAM/ MAKE
-LITER- - I-OOML sn
MGC
0"7DQQ _ __
0-n— • — — _==-^=.-^.- -- -oonr
OTOftQ ____ AT 1
Q-.2125 — -2^21X) SP.
0.4964 10.523
OvO ~ OvO — ' ~
0.2375 0.950
****** -*-*****- - - PARI
OQA.AA ____ AT 1
«_=.=»*--- -****** - - Ft^l
^^.._.. 5 Tf 1 c i
______ ^ r • 1 5 1
.
* SOL I OS FREE BASIS, MASS/VOLUME SOLUTION
52&5.
5292.
5292
3137
INPUT FOR EQ. - KIN.PROG.
INPUT FLOWS,0ATOMS/1000FEED
C1VRBON 0-. 4 5998-1
HYDROGEN 0.548169
- ' OXYGEN rv39504B
NITROGEN 5.062539
SUL-FUfr- -O-iOt)8T3-l-
-3-13-Tv
3201.
1 MGO COMPOSITION
SLURRY CONCi^ GM MGO/10t)ML -= 5'. 80
PRESLAKED, N0=0, YES=1 0
-S-t-A-K-EO—TQ-MG( OH I 2 , MEA S. = ******
PRODUCT- MG BAS-E- PHYSItiAL—PROPE-RT-TES
ACID STRENGTH, PH = 7.95
SP.GR-AVI TY,HYOROM. - =
ULATE SCRUfrBER PRODUCT
STRENGTH , PH = 6.50
FL^ASH CONC. -6M/IOOML = *****
-------
RUN NUMBER 12-A
DATE 9-24-71
TIME OF DAY 1430
FLUE GAS DATA
FURNACE FXIT
FLOAT. BED EX
NOX SCRUB IN
NOX SCRUB EX
NOX SCRUB. DATA
MAKEUP WATER
MAKEUP MGQ-
PRODUCT LIQ.
R"t"t* I K C • L 1 0 •
N02 FlOW DATA
N02 FLOWRATE
N02/NO( PDS
N02/NO(FC £
MATERIAL BALANCE
FLOW
T&7HP
5583.
3713.
3684.
3730.
TEMP.
F
60.
60.
0
0
130.6
130. 0
,#/M
BAS1
ROTO
IN
S)
)
TEMP
560.
132.
165.
126.
FLOW
S/MIN
0.81
2.00
3.35
1250.
0.03
*****
0.67
SULFUR
NQX SCRUBBER
INPUT,#/HR
OUTPUT,#/HR
0.
0.
10
05
S02
NOX
NOX*1
PPW HHH HFH
0 1741.8 ****** - ******
0 30.9 501.6 ******
0 ****** ****** 442.0
0 ****** 762.0 ******
SCRUB.
S02
NOX
NOX1
NOX2
L/G,
L/Gt
PRES
-
PERFORMANCE
ABSORB.
ABSQRP.
-AB'SORP-
ABSORP
GAL/MCF
ft/ft
.DROP.WG
— -
MAGNESIUM WATER
3.60
0.73
671.0
557.2
NOX*2 HUM. DEW
F
748.6 0.055 114
655.0 0.160 147
842.2 0.160 147
617.6 0.174 151
IM
•
•
•
•
1
9
7
7
9
STAT
IN.WG
0.0
-14.9
1.4
0.0
SPRAY SLURRY ANALYSIS
******
70.
00 .
-******- - -
26.
.
146.
20.
0.
-
NI
67
~~
2
4
1
**
TROGEN
MGO,GM/IOOML
MGS03-(SOLID),M
MGS03(TOTAL» ,M
MG(N02)2* MOLAR
MG(N03)2, MOLAR
TSS,GM/100ML
NITRITE/NITRATE
0
0
0
0
4
0
•
•
•
•
1
•
.512
0031 - —
0033
0121
0028
.500
321
MAKEUP MGO COMPOSITION
SLURKY CONC
•
t
GM MGO/IOOML= 5.00
***** -
1
.19
PHYSICAL PROPERTIbS OF
RECYCLED SLURRY
PH
CONDUCT.MICROMHOS
S Prt I'Fl C ~GR~K VTT Y
7.95
824.
1TOTO
NOX
= PDS ANALYSIS
NOX*2 = FUEL CELL ANALYSIS
** OXIDIZED NITROGEN ONLY
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM-OUTPUT DATA PAGE 1
RUN NUMBER 13-A
DATE 9-27-71
TIME OF DAY 1600
FLUE GAS DATA
—PittMARY
SECONDARY AIR
FURNACE
PART.SCRB.INLET
PART.CYC. EXIT
VENT ABS.INLET
A-BS-CYC.rXIT
FLOATING BED IN
P.P. EXIT ORI
SCRUBBER STREAM DATA
PARTICULATE
MAKEUP WATER
PRODUCT L-fg;
RECIRCULATED LIQ.
FURNACF PERFORMANCE
- KtEUT RE'L-BASEf 8TU/HR'"
% FUEL AS COAL
COAL FLOW RATE,#/HR
NAT.GAS FLOW.O/HR
f EXCESS AIR
OXYGENt*DRY,MEAS.
C02,8DRY-CALC;
HUMIDITY,/*/* - CALC.
FLOW
- -#/HR~
. ._ . . - ^^Q___
4822 .
5696.
.ET 5696.
r 3381.
:j *****
- *****
IN 3381.
-f-X- — 3547. —
IF. 3547.
TEMP.
F- —
-1-tOvO —
690* 0
' 570« 0
460.0
138.0
******
******
139.0
11 "0 '^0 "
132.0
S02
•--PPfl
:^_ — _ — •.
1713. 51
******
1116.7
******
******
******
****** -
8.5
S03
— PPM "
~-^=.-i — s.
—*****
a
*****
*****
*****
*****
*****
** ***
*****
NOX
— PPM—
- - -=.-=-^=-
*****
**** *
*****
*****
*****
**** *
• ••*•** * *
581.
FLYASH
— GR-AOS'C'F—
=r=^=.-== -
*******
*******
*******
*******
*******
HUM.
#/#
- Oi017
Oni 7
IT. O!>8
f\ rt c o
\J m U t> O
0.135
******
. 13?
0 • 164"
0.164
DEW
POINT-'
F
^6.9
7f% 2
*
1 1 o . 1
11 A 1
lo. 1
142.8
*****
1 H/l . O
148. e.
148.2
DRY
FtOW
#/HR
- 460.
4744.
53 oo •
2980.
— — — — —
~*
3047.
STAT
IN.H20
-14.
5.
u.
-•=6.
****
*r**:k
—i n
1 *t •
-14.
___„-.___ — — * ™
9
7
*
fl - —
*
9
TEMP.F
60.0
-t3Tre~
137.0
FLOW,GPM
0.0
19.78
VENTURI ABSORBER FBA
TEMP.F FLOW,#/M TEMP.F FLOWi#/M
***** ***** 60.0 0.6
*»*** 3v3 O^O 5r3—
PRODUCT LIQ. ***** ***** 137.0 0.0
REC r( SPRAY NOZ )-***** ***** 13-7.-Q -;-Q^O—
REC.(FLCW NOZ.) ***** 385.0
- GAS ABSORBER
MAKEUP MATER
SL.
SCRUBBER PERFORMANCE
0-7-
96.4
426.4
8.9
18;1-
3.80
FLYASH COL.EFF
SO 3 A B SOR B . EF F
NOX ABSORB. EFF
GA-S- VE-LOC-fTY,FPS
LIQ/GAS.GAL/MCF
PART.
3-4-V83-
******
******
******
9U9
21.7
VENT ABS.
******
******
******
******
******
0.058
PRES.DROP,IN.WG
2.8
02 ABSORPTION PARAMETERS
~ VENTURI ABSORBER
-FLOATING 'BED-ABSORBER
KGAt*MOLE/HR-FT-3-V ******
SULFITE/S02-MOL/MOL = ******
St)MP RESID.T-IME,MIN =-******
***** MEANS ITEM NOT MEASURED
SULFITE/S02-MOL/MOL
SUMP RE-S-K>-.-Tf-METM-IN-
40.32
*«»»»«
******
SULFATE FORMATION PARAMETERS
CONC.,GM-MOLE/L= ******
MOLf TOTAL SULF=—*****-—
02 AT FURN. EX.= 3.80
- 02 AT ABSORB.IN=-'*****
02 AT ABSORB.EX= *****
-------
MAGNES-IUM BASE SLURRY SCRUBBING PROGRAM - OUTPUT DATA PAGE 2
RUN NUMBER 13-A
MATERIAL BALANCES
DATE 9-27-71
TIME OF DAY 1600
FURNACE
SULFUR MAGNESIUM FLYASH
WATER
DRY GAS
INPUT FOR EO. - KIN.PROG.
INPUT FLOWS,#ATOMS/100#FEED
1 IS'-tJ 1 f
-------
RUN NUMBER 13-A
DATE: 9-27-71
TIME OF DAY 1600
FLUE GAS DATA FLOW
S02
NOX
NOX*1
FURNACE EXIT 5696.
FLOAT.BED EX 3547.
NOX 'SCRUB IN 3-466.
NOX SCRUB EX 3509.
TEMP.
—F
570.0 17T3.5 -******
132.0 8.5 580.9 ******
-166iO ****** - 525 ;-8 662.5
128.0 ****** 580.3 256.4
NOX*?
PPM
674.2
730.4
"664. 8"—
725.7
HUM.
-0.058—
0.164
-0.1-6-4
0.179
DEW
POINT
F
tt6.1
148.2
14-8i2
152.3
STAT
PRES
IN.WG
=0.1 - - - —
-14.9
1.4 ~
0.0
NOX SCRUB.DATA TEMP. FLOW
MAKEUP WATER
-MAKEUP MGO
PRODUCT LIQ.
±1-9.-
F
60.0 0.81
60.0- -2.00
132.0 3.35
-13±-.e t-2i
SCRUB. PERFORMANCE
S02 ABSORB. ******
NOX ABSORP. -10.36
- N1DX1-- ABSORP — 6iv3-o-
NOX2 ABSORP -9.15
SPRAY SLURRY ANALYSIS
MGO,GM/100ML
---- -WSOS-l-SOttDTyfl
MGS03(TOTAL)iM
0.975
-Qv0312
0.0332
N02 FLOW DATA
N02 FLOWRATE,#/MIN
N02/N0( PDS BASIS)
N02/NO(FC L ROTOI
0.03
-0.09
0.63
L/G,GAL/MCF 156.2
L/Gt#/« 22.0
PRES.DROP.WG 0.1
MATERIAL BALANCE
NOX SCRUBBER
INPUT ,#/HR
OUTPUT,#/HR
SULFUR MAGNESIUM WATER
0.03
0.40
4.18
1.54
650.0
535.0
PHYSICAL PROPERTIES OF
RECYCLED SLURRY
PH
CONDUCT.MICROMHOS
GRAVITY
8.15
397.
MG(N02)2, MOLAR
MG(N03)2f MOLAR
TSStGM/lOOML
NITRITE/NITRATE
0.0106
0^0018
11.783
5.889
NITROGEN
0.72
0.86
MAKEUP MGO COMPOSITION
SLURRY CONC.tGM MGO/100ML'
5-sSO
NOX
= PDS ANALYSIS
NOX*2 = FUEL CELL ANALYSIS
** OXIDIZED NITROGEN ONLY
-------
RUN NUMBER
FLUE GAS DATA
PRIMARY AIR
SECONDARY AIR
FUR1MACE EXIT
PART. SCRB. INLET
PART. CYC. EXIT
VENT ABS. INLET
A BS CYC. EX IT
FLOATING BED IN
PtQ-ATI-NG -BED ^X
P.P. EXIT ORIF.
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM-OUTPUT DATA PAGE 1
DATE 9-27-71 TIME OF DAY 1700
FLOW
«/HR
474.
4575.
5434.
5434.
33H.
*****
*****
3311.
3480V--
3480.
TEMP.
F
120.0
691.3
59tr.-o--
490.0
139.0
******
******
140.0
n - n —
S02
PPM
170^-6
******
1587.7
******
******
******
133.0 2.0
S03
PPM
*****
*****
*****
*****
-**«**
*****
*****
NOX
PPM
---*****-
*****
*****
**..***
*****
*****
- ****-*-
529.
FLYASH
GR/DSCF
- *****-**
*******
*******
*******
*******
*******
---*•**•*•***
****£**
HUM.
#/#
0.016
0.017
' ~X);T)58
0.058
0. 142
******
******
0. 142
0.1 71™
0.171
DEW
POINT
F
76.1
77.0
116-.2
116.2
144.3
*****
*****
144.3
149.4
149.4
DRY
FLOW
0/HR
467.
4499.
5T38^
2900.
2971.
STAT
PRES
IN.H20
14.9
6.0
SCRUBBER STREAM
PARTICULATE
MAKEUP MATER
DATA
REC1RCULATED LIQ.
FURNACE PERFORMANCE
HOT RELEASE,BTU/HR
58 FUEL AS COAL
~ COAL FLOW RATE«#/HR
NAT.GAS FLOW,ff/HR
" ? EXCESS AIR
OXYGEN,SDRY.MEAS.
CTJ2 , SDR Y-CATC ^
HUMIDITY,#/# - CALC.
502 ABSORPTION PARAMETERS
VENTURI ABSORBER
TEMP,F
60.0
FLOWtGPM
0.0
4.1
-8.1
*****
*****
-8.1
-16.3
-16.3
VENTURI ABSORBER FBA
GAS ABSORBER TEMP,F FLOWir/M TEMP.F FLOW/ff/M
MAKEUP WATER ***** ***** 60.0 0.6
rsu • IT "
138.0
0 ; 5 1 re 07
96.2
403.8
8.9
18.6
3.90
I*». bO
0.058
— OVO- MWCEtTP-MGO- Sir; — »»»«* TT3
19.78 PRODUCT LIO. ***** *****
REC. (SPRAY NOZ1 ***** *****
REC.(FLGW NOZ.K. *****
SCRUBBER PERFORMANCE PART.
SO2 "ttffSOR B . E-F F - ' - -«Vff6-
FLYASH COL.EFF ******
S03- ABSORB ;EFF ******
NOX ABSORB. EFF ******
(TA~S-VELOCITYfFPS -90V8~
LIQ/GAStGAL/MCF 22.0
l\J/\3A^tWfV
PRES. DROP, IN.WG
J.U
2.5
VENT ABS.
******
****** -
******
******-
******
**«tr*r«
******
Olt) 3V3
138.0 0.0
138.0 OVO ~- - - —
3.8
FLOAT. BED
99"; 88" ----- -
******
****** -—- . _
******
5.9
0.6
— o-;t
-15.0
SULFITE/S02-MOL/MOL = ******
SUMP RESID.TIME,MIN = ******
***** MEANS ITEM NOT MEASURED
F iTOttTTNG -BED-frBSOR BE R
KGA t #MOL t AHK— h I 3
SULFITE/S02-MOL/MOL
SUMP RESID.TlMEiMfN
SULFATE FORMATION PARAMETERS
CONC.tGM-MOLE/L= ******
^ ~ *****
0.23
****-**
02 AT FURN. EX.=
~ 02 AT ABSORB. IN-
02 AT ABSORB.EX=
3.90
*****
*****
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM - OUTPUT DATA PAGE 2
DATE 9-27-71
TIME OF DAY 1700
MATERIAL BALANCES
SULFtm -
FURNACE
INPUT, #/HR 14.94 -
nilTDMT Jt/MD O 1 A
PART. SCRUBBER
IM O1 1 T *l / U O Q 1 A
INKU 1 ,ff/f1K V.lo
nilTPIIT fl/HR & fil
S02 ABSORBERS
INPUT»#/HK 4.8L
OUTPUT, #/HR 0.01
*
*S02 ABSORBERS- GM S02/
PRODUCT COMP. 100ML
rnuR I M£n 7 IS
FREE 0 0
MONO(TOTAL) 2.15
MON01D1-SSOLVED) 0;96
MONO(SOLID) 1.19
MGO 3.44
SULFATE *****
MAGNESIUM 5.59
Ct VACU .3.
cni fncup _ — — —
COAL COMPOSITION-MASS
CARBON 0.7150
HYDROGEN 0.0485
OXY+NIT 0.0817
SULFUR 0.0370
ASH 0.0740
WATER 0.0438
MAGNESIUM
5.67
******
GM-MOLE/
L i T-E-R
A --1O-«O- •
U. j 3:jri
O1 'XRO
. 3 ^3^»
On
0.3359
0.1500
0.1859
0.0
0.5368
******
0.8728
.
FLYASH
- 29.88
A A A A-&-A
******
******
GRAM/
100ML
1.560
3.942
0.0
2.147
******
11 ?T)
1*2 JZ
INPUT FOR EQ. - KIN. PROG.
WATER DRY GAS -- ~
INPUT FLOWS,#ATOMS/100#FEED
^96.*? ?13n. HYDROGEN 0.608727
OXYGEN 1.395331
NITROGEN 5.064827
360. 5138. SULFUR O.TJOooHTT
A. 1 1 O Of\ A
Hi 1. . ^SUO.
' "' FEED RATE,#/SEC^ 1.49
638. 2900. ' ' ENTHALPY»BTU/# = "Jr4-itt"3 •; ' —
509. 2971.
MAKEUP MGO COMPOSITION
SLURRY CONC.- GM MGO/IOOML = 4.70 -
MGO PRESLAKED, N0=0f YES=1 0
* 5L AlvcD 1 u Mb 1 OH f 2 t HfcAS* = ******
ODnniirT Mf* DACC DU v c-r-r= Ai--DonocoTtcc- - — - • — -
PKUUUL- 1 MU BAbt rnYS iCAL rHOrcRT 1 E5
ACIO STRENGTH, PH = 8.10
SP. GRAVITY, HYDROM. = *******
PARTICULATE SCRUBBER PRODUCT
ACID STRENGTH , PH = 5.30
FLYASH CUIML. GM/iOOML = ***** --
-
_
*SOLIl)S FREh BASIS, MASS/VOLUME SOLUTION
-------
RUN NUMBER 14-1
DATE 9-27-71
TIME OF DAY 1700
FLUE GAS DATA
FURNACE EXIT
FLOAT.BED EX
NUX SCRUB IN
NOX SCRUB EX
FLOW
ff/HR
5434.
3480.
3460.
3502.
TEMP.
S02
PFM
NGX
PPM
NOX* I
NOX*2
PPM" "
590.0 1704.6
133.0 2.0
166.0 ******
129.0 ******
******
528.6
1310.9
1076. B
******
******
689.1
492.4
648.7
614.9
*«**«*
******
NGX SCRUB.DATA TEMP. FLOW
MAKEUP WATER
MAKEUP MGO "
PRODUCT LIO.
F
60.0
6'0.0
133.0
ff/MIN
0.81
l;20
3.00
SCRUB. PERFORMANCE
S02 ABSORB. ******
NOX ABSORP. 17.86
NOXl- -AB'SORP 28.55'
NQX2 ABSORP -9.15
ttOV -133-.O—t2TO. - - —i
N02 FLOW DATA
N02 FLOWRATE,#/MIN 0.03
N02/N0( PDS BASIS) 1.48
N02/NO(FC & ROTO) 0.76
L/G,GAL/MCF 155.9
L/G,#7# --22.0
PRES.DROP,WG O.I
HUM. DEW STAT
*rw POINT- --pRrs -
F 1N.WG
0.058 116.2 0.0
0,171 149.4 -16.3
0.171 149.4 1.4
0.186 153.5 0.0
SPRAY SLURRY ANALYSIS
MGO.GM/100ML 3.350
--HGS031SOL1D)tM 0.0031
MGS03(TOTAL1,M 0.0041
- WGSO4> MOLAR - Q-;01ff5
MG(N0212» MOLAR 0.0115
MG(N03)2, MOLAR 0.0020
TSS,GM/100ML 16.356
NITRITE/NITRATE 5.750
MATERIAL BALANCE
NOX SCRUBBEK
" - INPUT,#/HR
OUTPUT,#/HR
SULFUR MAGNESIUM WATER
3^77
o.o
O.L3
551.2
**
NITROGEN
—1.77
1.52
MAKEUP MGO COMPOSITION
SLURRY CONC..GM MGO/100ML= 10.20
PHYSICAL PROPERTIES OF
RECYCLED SLURRY
PH • -
CONDUCT. MI CROMHOS
S P^'CT FTC GTTAVTTY"
310.
NOX
NUX* l"
NOX*2
PDS ANALYSIS
STfLTS1WN"7iWff
FUEL CELL ANALYSIS
** OXIDIZED NITROGEN ONLY
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM-OUTPUT DATA PAGE I
RUN NUMBER I 5-A
FLUE GAS DATA
PRIMARY AIR
SECONDARY AIR
FORNACE EXTT
PART.SCRB.INLET
P-ART.CYC.EXIT
VENT ABS.INLET
ABS CYC.EXTT
FLOATING BED
-—FtOftTtNG-
P.P. EXIT
SCRUBBER STREAM DATA
PARTICULATE
MAKEUP WATER
-PRODUCT -L-I-Q-;
RECIRCULATED LIQ.
FURNACE PERFORMANCE
DATE 9-28-71
TIME OF DAY 1325
FLOW
- ~1»/HR
- 471.
Rf. C 31 O
*r3 J O.
• "9396;
1 C T C^ QA.
Lh 1 !> 3 9o •
T -3432.
ET *****
*****
IN 3432.
EX 3560.
IF. 3560.
TEMP.
F
130.0
/. 07 a
<3O 1 • J
• 5-W.O
A AA n
440. O
1-39. 0
******
- ******--
135.0
— "OvO
130.0
S02
- ' P-PM
1675.5
A&ft & A A
1369.9
**«*#*
#**•***
««****
******
18.4
SO 3
PPM
•#4c«^#
AA A&A
*****
*****
*****
*****
*****
*****
NOX
PPM'
•' *****
^A & A A
-*****-
*****
*****
*****
*****
547.
FLYASH
GH/DSCF -
********
^ && A A A A
*******"-
*******
*******
*******
*******
*******
HUM.
#'/'#
•0.'01-8~
Oo?n
0'. 06 1
OnA i
. UO i
Oil34
******
******
0.134
0. 162
0.162
DEW
POINT
F
79.*
pi a
118.1
UQ 1
D. L
142.6
*****
*****
142.6
14 r« 9
147.9
DRY
~FL~OW
#/HR
• ' 462. "
A, A en
5085.
30?7— -
3063.
STAT
-PfrE~S~ " "
IN.H20
14.9
5C
0.0
27
• f
=8-. 1
*****
*****
-8.1
-^14.^?
-14.9
VENTURI ABSORBER FBA
TEMP,F PLOW.GPM GAS ABSORBER TEMP.F FLOW,#/M TEHP.F
60.0 0.0 MAKEUP WATER ***** ***** 60.0
-t3tr;0 —fl-re MAKEttP - MGG ~SLs •--***** 3^ - e^rQ-
136.0 19.78 PRODUCT LIQ. ***** ***** 135.0
- - REC. (SPRAY NOZ1 ***** ***** 135-.0
REC.IFLOW NOZ.) *****
0.7
0.0
0.0
385.0
SCRUBBER PERFORMANCE
1^E*SE-?BTWHR Or5-14€ - 07
* FUEL AS COAL
COAL FLOW RATE,#/HR
NAT. GAS FLOWtl/HR
% EXCESS AIR
OXYGEN, ZDRY,MEAS.
96.2
406.4
8.9
17.1
3.60
FLYASH COL.EFF
SO3 ABSORB.EFF
NOX ABSORB.EFF
GAS VEtOCITY-.FPS
LIQ/GAS.GAL/MCF
PART.
ltT.24
******
******
******
93.4
21.4
HUMIDITY, #/# - CALC.
102 ABSORPTION PARAMETERS
VENTURI ABSORBER
0.061
PRES.DROP,IN.WG
3.0
VENT ABS.
******
******
******
******
******
******
- - *»*»-»*
******
FLOAT. BED
******
******
******
6.0
60.6
6-^-
7.2
FLOATING BED ABSORBER
- *»*«**—
SULFITE/S02-MOL/MOL = ******
SUMP RESID.TIME,MIN = ******
***** MEANS ITEM NOT MEASURED
SULFITE/S02-MOL/MOL
SUMP RESIDiTlMEfMIN
22.69
******
SULFATE FORMATION PARAMETERS
CONC.,GM-MOLE/L= ******
- -MOtX-fQTM; -Stft^=—*****
02 AT FURN. EX.= 3.60
02 AT ABSORB.IN= *****
02 AT ABSORB.EX= *****
-------
RUN NUMBER 15-A
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM - OUTPUT DATA PAGE 2
DATE 9-28-71 TIME OF DAY 1325
MATERIAL BALANCES
FURNACE
SULFUR MAGNESIUM FLYASH
30.07
******
******
******
i mru i , if/ rm
OUTPUT, #/HR
PART. SCRUBBER
INPUT, #/HR
OUTPUT, #/HR
S02 ABSORBERS
"INPUT, #WR -
OUTPUT, #/HR
*-
*S02 ABSORBERS-
PRODUCT COMP.
TOrAtTi
COMBINED
FRFE
MONU(TOTAL)
MONO(DTSSnLVED)
MONO(SnLID)
-BISULFITE
MGO
SULFATE
MAGNESIUM
FLYASH
SOL IOS,MG
13. VJ«t
8.90
8.90
4.33
4.33
0.06
GM SU2/
100ML
- 2V88- -
2.88
0.0
2.88
0.86
2.02
- o.o
3.5«5
*****
6.43
5-; 63
******
GM-MOLE/
LITER .
07^495-
0.4495
0.0
0.4495
0.1344
0.3151
o.o -
0.5552
******
1.0047
_
COAL COMPOSITION-MASS
CARBON 0.
HYDROGEN 0.
OXY+NIT 0.
7150
0485
0817
SULFUR O.O37O "
ASH 0.
WATER 0.
0740
0438
WATER
291.5
310.6
374,
404.
******
GRAM/
100ML
496,
DRY GAS
5078.
50R5.
5085,
3027,
302T;
3063.
INPUT FOR EO. - KIN.PROG.
INPUT FLOWS,#ATOMS/100#FEED
CARBON 0.4-64768
HYDROGEN 0.634411
- OXYGEN 1 .-3-94-4-69 - —
NITROGEN 5.058137
SULFUR 0.008820
FEED RATE-,#/SEC= 1.48
' -E N T HAL-PY ;-8Ttt/* - = -6030T~
MAKEUP MGO COMPOSITION
SLURRY CONC.- GM MGO/100ML =
MGO PRESLAKEO, N0=0, YES=1
4.60
0
1. 397
6.680
-o.o —
2.221
******
******
11.985
PRODUCT MG BASE PHYSICAL PROPERTIES
ACID STRENGTH, PH = 8.05
SP.GRAVITY,HYDROM. = *******
PARTICULATE SCRUBBER PRODUCT
ACID STRENGTH , PH = *****
FLYASH CONC.-GM/IOOHL = *****
*SOLIDS FRfcE BASIS, MASS/VULUME SOLUTION
-------
RUN NUMBER 15-A
DATE 9-28-71
TIME OF DAY 1325
FLUE GAS DATA
FURNACE EXIT
FLOAT. BED EX
NOX SCRUB IN
NOX SCRUB EX
NOX SCRUB. DATA
MAKEUP WATER
MA1CEUP- MGO
PRODUCT LIQ.
R-&Ct~R-C. -L~fO. —
FLOW
"ff/HR-
5396.
3560.
3518.
3560.
TEMP.
F
60.0
^0". 0"
130.0
l-*OvO-
TEMP
'- * ~F
540.
130.
168.
128.
FLOW
#/MIN
0.81
2; 00
3.00
- IgftQ.-
•
0
0
0
0
S02 NOX
— -PPM- — PPM-
1675.
13.
5 ******
4 547.5
****** 9-71 rg
****** H36.4
SCRUB.
S02
NOX
• -NOX1
NOX2
— fi*<5-
NOX*l
- ******
******
- -694 i 9
471.8
PERFORMANCE
ABSORB. -
ABSORP.
ftBSORP-
ABSORP
Mfl -F-fr<5
******
-16.93
-32 .-10 *-
-6.33
NOX*2
785.5
835.8
795.6
845.9
HUM.
- 0.061
0.162
0.162
0.176
DEW STAT
-potirr — PRES --- -- - —
F
118.1
147.9
-1-^7 ; 9
152.1
IN.WG
0.
-14.
1.
0.
0
9
4 "
0
SPRAY SLURRY ANALYSIS
-
MGO,GM/100ML
-- "M&S133-
MGS03
t c r\t ¥f\t
1 jUL. I U 1 9 M
( TOTAL), M
-
-0.0
0.0
- - -
_ _
0.0003
N02 FLOW DATA
N02 FLOWRATE,#/MIN
N02/N0( POS BASIS)
N02/NO(FC € ROTO)
0.04
0.78
0.59
L/G.GAL/MCF 152.8
- -L/GT#A# 21-. 5
PRES.DROP.WG 0.2
MG(N02)2, MOLAR 0.0082
- MG{NG3-f2-f -MOLAR- OvOOl'2
TSStGM/lOOML 12.929
I TRAT€ - 6 .-833
MATERIAL BALANCE
NGX SCRUBBER
INPUT,»/HR
OUTPUT,0/HR
SULFUR MAGNESIUM
0.06-
0.04
4-. 46
0.07
651.8
536.5
**
NITROGEN
1-.34
1.62
MAKEUP MGO COMPOSITION
CONC.,GM MGO/TOOM1'
PHYSICAL PROPERTIES OF
RECYCLED SLURRY
PH - - -
CONDUC T.MICROMHOS
«C GRAVITY
8 . 1-0
208.
1 .040""
NOX = PDS ANALYSIS
WOX*1 ^—S"A-LTSHAN-ANAL YS 1"S-
NOX*2 = FUEL CELL ANALYSIS
** OXIDIZED NITROGEN ONLY
-------
MAGNESIUM BASE SLURRY SCRUBBING PRUG*AM-OUTPUT DATA PAGE 1
RUN NUMBER 16-K
FLUE GAS DATA
PRIMARY AIR
SECONDARY AIR
FURNACE EXIT
PART.SCRB.INLET
PART.CYC.EXIT
VENT ABS.INLET
ABS CYC.EXIT
FLOATING BED IN
FtOAT ING BED EX
P.P. EXIT OR IF.
SCRUBBER STREAM DATA
PARTICIPATE TEMP,F
MAKEUP WATER 60.0
PRODUCT LIQ. - 135.0
RECIRC .LATEIJ LIO. 135.0
DATE 9-28-71
TIME OF DAY 1500
FLOW
#/HR
471.
4532.
5387.
5387.
2580.
*****
*****
2580.
2 759 .
2759.
TEMP.
F
130.0
687.5
570.-0
460.0
139.0
******
******
135.0
- o.o
128.0
S02
PPM
1643.2
******
******
******
****** -
******
******-
14.2
S03
PPM
*****
*****
*****
*****
*****
*****
*****--
*****
NOX
PPM
*****
*****
*****
*****
-*****
*****
*****
628.
FLYASH
GR/DSCF
*******
*******
*******
*******
*******
*******
~ ******** "
*******
HUM.
#/#
0.019
0.019
0.0*0 -
0.060
0.137
******
******
0.137
~ ~0vl~6~6~
0.166
DEW
POINT
F
80.3
79.9
117.5
117.5
143.6
*****
*****
143.6
-r*8v6-
148.6
DRY
FLOW
462.
4449.
2?69.
2367.
STAT
PRES
IN.H20
14.9
6.1
-O-TO-
2.7
-5.4
*****
*****-
-5.4
-14.9-
-14.9
FLOWtGPM
0.0
OVO
19.78
GAS ABSORBER
MAKEUP WATER ***** *****
•MAKEUP" WGO SL. ***** --3;-$
PRODUCT LIO. ***** *****
REC.(SPRAY NOZ) ***** *****
REC.iFLOW NOZ.) *****
VENTURI ABSURBER FBA
TEMP,F FLOW,#/M TEMP.F FLOW,»7M
60.0
0.0
133.0
133.0
0.8
..3_5
0.0
0.0
385.0
FURNACE PERFORMANCE
HEAT RELEASE,BTU/HR 0.511E 07
* FUEL AS COAL 96.2
COAL FLOW RATE,#/HR 403.9
NAT.GAS FLOW,#/HR 8.9
% EXCFSS AIR 17.6
OXYGEN,?DRY,MEAS. 3.70
C02,lDRY-CAtC. -' -' 14.86
HUMIDITY, H/tl - CALC. 0.060
SO2 ABSORPTION PARAMETERS
VENTURI ABSORBER
~ KGA,*MOLE/HR-FT3, = ******
SULFITF/S02-MOL/MOL = ******
SUMP RESID.TIME.MIN = ******
("EAiMS ITEM NUT MEASURED
SCRUBBER PERFORMANCE
S02 ABSORB.EFF
FLYASH COL.EFF
SQ3 ABSORB.EFF
NOX ABSORB.EFF
GAS VELOCITY,FPS
LIQ/GAS,GAL/MCF
••- LTQ/GTTSfS/S ™
PRES.OROP,IN.WG
FLOATING BED ABSORBER
KGA,»MOLE/HR-FT3-
SULFITE/S02-MOL/MOL
SUMP RESID.TIME.MIN
VENT ABS.
******
******
******
******
******
******
- ******
******
FLOAT.BED
******
******
******
******
4.6
78.0
-«.r
15.7
******
******
******
SULFATE FORMATION PARAMETERS
CONC.,GM-MOLE/L= ******
~ HOL* -TOT*t"SULTw ***** —
02 AT FURN. EX.= 3.70
02 AT ABSORB.IN= *****
02 AT ABSORB.EX= *****
-------
RUN NUMBER 16-K
MATERIAl BALANCES
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM - OUTPUT DATA PAGE 2
DATE 9-28-71 TIME OF DAY 1500
INPUT FOR EQ. - KIN.PROG.
SULFUR
FURNACE
INPUT tt/MR 1 L. QA
nilTPIIT d/MR A 71
PART. SCRUBBER
OUTPUT, #/HR ******
S02 ABSORBERS
OUTPUT, #/HR 0.04
*
*S02 ABSORBERS- GM S02/
PRODUCT COMP. 100ML
— T^flT-A-fr — - - 9- Q1
COMBINED 2.91
FREE 0.0
MdlMfMTnTAI ) 7 Ql
-MQNO( DI SSOLVFO 1 — ?-7O"
MONOISOLIDI 5.61
-RtSULF-fTE — • - 2rfr$- ~
MGO ^ . R 1
SULFATE *****
MAGNF^ KIM A 7?
Cl VACLJ -_,i -
cni Tnc MP — _
COAL COMPOSITION-MASS
CARBON 0.7150
HYDROGEN 0.0485
OXY+NIT 0.0817
ASH 0.0740
WATER 0.0438
MAGNESIUM
5 .flfr
******
GM-MOLE/
LITER
0- -ArC=-A A .
• f J*tU
0;0
OA CAA
— s.- -& O IQ-
0.8759
---O.'/Ofi? -
******
-
FLYASH WATE-R DRY G"AS-
INPUT FLOWSt#ATOMS/100#FEED
29.89 285.6 5076. CARBON 0.462322
****** 304.7 5083. HYDROGEN 0.6377.65
Q-XYSErtr " - t~«3"94^53 — ' "
NITROGEN 5.060390
*4«t»£ 368. 5083. SULJ-Uk " O.-OOIT7T3 ~
****** 3H. 2269.
. _ ~FEBO R-A-Ttf-#rSEC= 1-=-*8- - -
****** 560. 22'69. E'NTflAL PY , BTU/# = 1-B3*93« —
****** 392. 236'.
GRAM/ MAKEUP MGO COMPOSITION
100ML SLURRY CONC . - GM MGO/100ML = 4.60
MGO PRESLAKED, N0=0, YES=1 0
— — -"- % S'LAKFO-Tfr MG(OM ) 2 » MEAS. -•- ****** —
— ^— — PRODUCT MG BASE PHYSICAL PROPER-TIES -
AU1U ol KciMG I Hf PH — 8 • 10
-^- A ~"1 P "?- * — - C-D — P Q-ft~\t f -T-V u vno n-M — A A *•* * ^-^
18.569
3- ft^-fr — - - - -- - - - .
-****** PARTICIPATE SCRURBER PRODUCT
~~ ACID STRENGTH , PH — *****
****** rLYAbH LUNG. GM/ IOOML — ***** -
11 1 C 1
I . i 53
*SOLIDS FREE BASIS, MASS/VCLUME SOLUTION
-------
RUN NUM8FK 16-K
DATE 9-28-71
TIME OF DAY 1500
FLUE GAS DATA
F URN ACT EXIT
FLOAT.BED FX
NUX SCrtUB IN
NOX SCRUB EX
NOX SCRUB.DATA TEMP. FLOW
FLOW
#/HR
5387.
2759.
2726.
2763.
TEMP.
F
570.0
12R.O
166.0
128.0
SO?
PPM
1643.?
14. 2
******
******
NOX
PPM
******
627.7
866.3
8R6.4
NOX*1
PPM
******
******
642.5
449.4
NOX*2
PPM
715.7
403.2
846.8
514.1
HUM.
Hf9
0.060
0.166
0.166
0.18?
DEW
POINT
F
117.5
148.6
148.6
153.0
STAT
PRES
IN.WG
0.0
-14.9
1.4
0.0
MAKEUP WAFER
MAKEUP MGO
PRODUCT LIO.
LTQ.
F
60.0
60.0
130.0
130.O
N02 FLOW DATA
NU2 FLOWRATF.
N02/NOI PDS BASIS)
NO?/NO(FC 6 'ROTO)
MATERIAL BALANCE
NUX SCRUBBER
INPUT,#/HR
OUTPUT,#/HR
PHYSICAL PROPERTIES OF
RECYCLED SLURRY
PH
CONDUCT.MICROMHOS
SPECIFIC GRAVITY
0.81
1.20
3.00
80O-;
0.0?
0.3R
0.<»2
SCRUB.PERFORMANCE
S02 ABSORB. ******
NOX ABSORP. -2.32
NOX1 ABSORP 30.06
NOX2 ABSORP 39.29
GAS Vft^FPS- •— lr3
L/CitGAL/MCF 125.3
L/G,*/# 17.6
PRES.DROP,WG 0.2
SULFUR
0.04
0.03
MAGNES IUM
2.68
0.09
WATER
503.9
427.6
**
NITROGEN
0.93
1.03
SPRAY SLURRY ANALYSIS
MGO,GM/IOOML -0.0
MGS03ISOLID)»M 0.0
MGS03
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM-OUTPUT DATA PAGE 1
RUN NUMBER 17-J
FLUE GAS DATA
PRIMARY AIR
SECONDARY AIP
- FURNACE exir-
PART.SCRB.INLET
P ART-; CYC. EXIT
VENT ABS.INLET
- A&S CYCVEX IT
FLOATING BED IN
P.P. EXIT ORIF.
SCRUBBER STREAM DATA
PARTICULATE
MAKEUP WATER
PRODtJCT-LI-Q. —
REC1RCULATED LIQ.
FURNACE PERFORMANCE
- HFAT -Rt LeASE fB TtT7 ftR—
% FUEL AS COAL
COAL FLOW RATE»#/HR
NAT.GAS FLOW,#/HR
% EXCESS AIR
OXYGEN,?ORY,MEAS.
C02TJ5DRY-CALC.
HUMIDITY,#/* - CALC.
DATE 9-28-71
TIME OF DAY 1600
FLOW
#/HR
L.tt
t If. .
A C-S7
53^*5.
5395.
"33^73.
*****
-*****-
3373.
3495.
3495.
TEMP.
• - F
I^n n
JU . U
AOO n
5 80. 0
475.0
•— T38.-0
******
- -******•
132.0
o.o
130.0
S02
PPM-
195 1.5
****#*
169 2. -4
******
******
******
******
18.9
S03
-PPM
*****
*****
-*****
*****
*****
*****
*****
*****
NOX
PPM
-****•*
*****
*****
*****
*****-
*****
**** *
577.
FLYASH
GR/DSCF
*******
*******
*******-
*******
ft******
*******
*******
*******
HUM.
TEMPtF
60.0
137.0-
137.0
FLOWtGPM
0.0
frO
GAS ABSORBER
MAKEUP WATER
0.018
0.021
t*v062
0.062
0. 14?
******
-******
0.143
-Ovl Tt
0. 171
VENTURI Ai
TEMPrF FLOW,#/M
***** <
19.78
PRODUCT LIO. *****
REC.C SPRAY NOZ >--*****
REC.IFLOW NOZ.)
DEW
POtNT
F
78.7
83.1
11 a A
14-4. 7
*****
*****
1 AA. "7
1 *»t-. r
149.4
RBER
#/M
**
**
**
**
DRY
FLOW
#/HR
463
4445
2951:
2986
FBA
TEMP^F
60.0
o«u
137.0
137. 0
STAT
PRE-S
IN.H20
16.3
6.1
•~ - t);0
27
• ~ o1» I
*****
^ a i
— —8. 1
— —16.3
-16.3
FtOlrfi#/M
0.8
0.0
.. QVQ
385.0
SCRUBBER PERFORMANCE
PART.
VENT ABS.
FLOAT.BED
-Ci-5-14E 07 - -
96.1
405.9
9.0
17 . 1
3.60
1-4V94
SO2
FLYASH COL.EFF
SO3 ABSOR8.EFF
NOX ABSORB.EFF
GAS VELOCITYfFPS
LIQ/GAStGAL/MCF
******
******
******
92. 1
21.7
0.062
PRES.DROP, IN.WG
2.8
******
******
******
******
******
******
******
******
******
******
5; 9
61.2
8.6
102 ABSORPTION PARAMETERS
VENTURI ABSORBER
FLOATING BED ABSORBER
' KGA. ffHOLEfHR-FT3-« TT--******-
SULFITE/S02-MOL/MOL = ******
SUMP RESID.TrMEvNIN =-******
***** MEANS ITEM NOT MEASURED
SULFITE/S02-MOL/MOL
-SUMP RES1DvriME,-MIN
SULFATE FORMATION PARAMETERS
CONC. ,GM-MOLE/L= ******
— -M0t%- TOTAL SULF= «****- ~
02 AT FURN. EX.= 3.60
t)2 AT ABSORB. I N= ***** —
02 AT ABSORB. EX= *****
-------
MAGNESIUM BASE SLURRY SCRUBBING PROGRAM - OUTPUT DATA PAGE 2
PUN NUMBER 17-J
MATERIAL BALANCES
DATE 9-2B-71
TIME OF DAY 1600
SULFIJK
FURNACE
1 M D 1 1 T U / UD 1 K f l O
I IM K U t f If / UK 1 " • U t
Mi IT DMT M / MD in :»**
UUIrUliff/nK L U # J t>
PART. SCRUBBER
1 M n i j T & / M ft in ^ A
1 \ F U 1 t Sr r n K L » 1 • J 1
rn i T D 1 1 T M y uu ci *5 *>
UUIrUl tff/ flK J • £./.
S02 ABSORBERS
INPUT, »/HR 5.22
OUTPUT, #/HR 0.06
*
*S02 ABSORBERS- GM S02/
PRODUCT COMP. IOOML
TOTAL, 2.86
COMBINED ?.B6
FREF 0.0
MONtH TOTAL) 2.86
MONO< DISSOLVED) 0.06
MONO (SOL ID) 2.80
BISULFITE 0.0
MGO 3.85
SULFATE *****
MAGNESIUM 6.72
cm i nc M c .....
COAL COMPOSITION-MASS
CARBON 0.7150
HYDROGEN 0.0485
OXY+NIT 0.0817
SULFUR OV0370
ASH 0.0740
WATER 0.0438
M AGNFS IU1*
5. 38
******
GM-MOLE/
LITER
-0.-4474
0.4474
0.0
0.4474
0.0094
0.4380
0.0
0.6020
******
1.0494
_ _
FLYASh
30.03
******
-******
******
GRAM/
100ML
WATfcR
295.1
377.
422.
509.
DRY GAS
5074.
50R1.
5081.
2951.
" 295U
2966.
INPUT FOR EO. - KIN. PROG.
INPUT FLOWS»#ATOMS/100#FEEO
CARBON
HYDROGEN
OXYGEN
NITROGFN
SULFUR
0.464699
0.679736
1.394463
5.058205
0.008817
FEED -RATE, #/SEC= 1.48
MAKEUP MGO COMPOSITION
SLURRY CONC.- GM MGO/100ML = 4.60
MGO PRESLAKED, N0=0, YES=1 0
* SLAKED TO MG (OW12TWEAS.- = ******
0.097
9.286
o-.o
2.408
******
PRODUCT MG OASE PHYSICAL
ACID STRENGTH, PH
SP.GRAVITY,HYDROM.
PROPERTIES
fl.05
*******
PARHCULATE SCRUBBER PRODUCT
ACID STRENGTH , PH = 5.25
FLYASH CONC. GM/100ML = *****
11.264
*SOL1US I-KEE BASIS, MASS/VCLUME SOLUTION
-------
RUN NUMBER 17-J
DATE 9-28-71
TIME OF DAY 1600
FLUE GAS DATA
FURNACE EXIT
FLOAT.RED EX
NOX SCRUB IN
NOX SCRUB EX
FLOW
' ff/HR"
5395;
3495.
34~6-6.
3503.
TEMP. S02
-~F PPW
NOX
58t).0 -:
130.0 18.9
16-6.0" -**-****
129.0 ****** 1223.1
NOX*1
PPM
*****
*****
6-9-9.6 "
451.1
NOX*2
PPM
815 .7
704.9
'85-6- . 0"
916.4
HUM.
»/»
0.062
0.171
— "G-.-tTl '
0.183
OFW
POINT
F
lT8-;6"
149.4
"1-^9 S'4
153.2
STAT
IN.WG
0.0 -
-16.3
l."4-
0.0 .
NOX SCRUB.DATA
MAKEUP WATER
MAKEUP MGO
PRODUCT LIQ.
RECIftC. LIQ.
TEMP.
F—
60.0
130.0
-reovo-
N02 FLOW DATA
N02 FLOWRATEf#/MIN
N02/N0( PDS BASIS)
NC2/NO(FC & ROTO)
FLOW
-r/Mi N
0.81
2.15
•^260;
0.04
1 i 07
0.70
SCRUB.PERFORMANCE
SO2-ABSORBS"-******
NOX ABSORP. -2.38
-- -N GX-lr-AfrS-GRP "25 .9^
NOX2 ABSORP -7.06
-&A^- VEL.F1>S- 1-.-7
L/G,GAL/MCF 155.0
L/Gi#/# 21.8
PRES.OROPtWG 0.2
SPRAY SLURRY ANALYSIS
MGO,GM/100ML
MGS03 (TOTAL )»M
MGSO4" i MOL A"R "
MG(N02)2, MOLAR
MGCN03)2, MOLAR
TSS,GM/100ML
NIT-RITE/NITRATE
-0.0
t). 0 -----
0.0
0.005-6-
0.0215
20.148
4.674
MATERIAL BALANCE
NOX SCRUBBER
INPUT,#/HR
OUTPUT,#/HR
SULFUR MAGNESIUM WATER
0^06-
0.02
4i22
0.10
597v6
544.6
**
NITROGEN
1.62
1.75
MAKEUP MGO COMPOSITION
SLURRY CONC.,GM MGO/IOOML-
PHYSICAL
RECYCLED
PH
PROPERTIES OF
SLURRY
CONDUC T,MICROMHOS
GRAVITY -
8.50
321.
NOX = PDS ANALYSIS
IMQX»1 -a—SArTSMAN ANALYSIS
NOX*2 = FUEL CELL ANALYSIS
** OXIDIZED NITROGEN ONLY
------- |