EMISSION TESTING REPORT
EPA REPORT NO. 74-KPM-15
ST. REGIS PAPER CO.
TACOMA, WASHINGTON
PEDCo ENVIRONMENTAL
-------
PEDCo- ENVIRONMENTAL
SUITE 8 • ATKINSON SQUARE
CINCINNATI. OHIO 45346
513 I ~7~7 1-433O
EMISSION TESTING REPORT
EPA REPORT NO. 74-KPM-15
ST. REGIS PAPER CO.
TACOMA, WASHINGTON
Contract No. 68-02-0237
Task 27
Prepared by:
R.S. Amick
W.G. DeWees
R.W. Gerstle, P.E,
Submitted by: PEDCo-Environmental Specialists, Inc.
Suite 13, Atkinson Square
Cincinnati, Ohio 45246
-------
I. TABLE OF CONTENTS
Page
II. INTRODUCTION 1
III. SUMMARY OF RESULTS . 4
IV. PROCESS. DESCRIPTION AND OPERATION 8
V. LOCATION OF SAMPLING POINTS . 18
VI. SAMPLING AND ANALYTICLA PROCEDURES 22
VII. APPENDIX
A. PARTICULATE RESULTS, CALCULATIONS AND
EXAMPLE CALCULATIONS
B. PROCESS DATA
a. FIELD DATA
D. LABORATORY REPORT
E. SAMPLING METHODS
F. TEST LOG
G. PROJECT PARTICIPANTS AND TITLES
-------
II. INTRODUCTION
Under the Clean Air Act of 1970, as amended, the Environ-
mental Protection Agency is charged with establishing
performance standards for stationary sources which may contribute
significantly to air pollution. A performance standard is based
on the best emission reduction systems which have been shown to
be technically and economically feasible.
In order to set realistic performance standards, accurate
data on pollutant emissions must be gathered from the stationary
source category under consideration.
St. -Regis Paper Co. in Tacoma, Washington was designated
as a well-controlled stationary source in the kraft pulp mill
industry and was thereby selected by GAP for an emission testing
program. The tests were conducted during the period of February 12
to February 19, 1974.
The specific processes under investigation in this test series
were the No. 2 lime kiln and the No. 4 recovery furnace. Emissions
from the lime kiln were controlled by a venturi scrubber followed
by a cyclone separator demister. Emissions from the recovery
furnace were controlled by an electrostatic precipitator (ESP). A
schematic diagram of the simplified Kraft process and the operations
sampled is shown in Figure 2.1.
Five particulate tests were conducted in the exit stack of
the recovery furnace to determine filterable and total particulate
-------
RECOVERY
FURNACE
SMELT
BLACK
LIQUOR
GAS FLOW
LIQUOR FLOW
AIR PRE-
HEATERS
RECOVERY
FURNACE
TEST SITE
ELECTROSTATIC
PRECIPITATOR
STACK
FUEL
VENTURI
SCRUBBER
LIME KILN
TEST SITE
CYCLONIC
SEPARATOR
DEMISTER
STACK
Figure 2.1. Schematic diagram of simplified Kraft process
and processes sampled.
-------
emissions. Simultaneous determination of moisture content and
dry molecular weight of the flue gases were also made. It was
originally intended that six runs be made; however, the sixth
test was cancelled due to a malfunction in the No. 4 recovery
furnace ESP. The duration of the recovery furnace tests varied
from 224 minutes to 336 minutes and averaged 315 minutes. These
relatively lengthy tests were necessary because the No. 4
recovery furnace ESP provided such a high particulate control
efficiency that the exit gas stream was extremely clean, ancj
a longer sampling period was required than normal in order to
obtain a measurable particulate sample.
Six particulate tests were conducted on the exit stack of
the lime kiln to determine filterable and total particulate
emissions. Simultaneous determination of moisture content and
dry molecular weight of the kiln flue gases were made.
During the period of testing the No. 4 Recovery Furnace,
the crew of another contractor, (Valentine, Fisher, and Tomlinson)
were conducting parallel, simultaneous particulate emission tests
of the recovery furnace with both an in-stack filter sampling
\
train and an out-of-stack heated filter sampling train. Their
tests were designed to permit a comparison of the two sampling
train methods. Results of this test are available in a separate
EPA Report 74-KPM-14.
-------
III. SUMMARY OF RESULTS
Recovery Furnace
A summary of particulate emission and flue gas data for
the five (5) particulate tests on the No. 4 Recovery Boiler
exhaust is presented in Table 3.1. The data is fairly consistent
when all the tests are considered simultaneously. Although
the particulate emission concentration varied from 0.00445
gr/DSCF (grains per dry standard cubic foot) (Test 1-3) to
0.01139 gr/DSCF (Test 1-5), this variation is not unexpected,
when ESP efficiencies of 99+ percent and the many possible
process variations are considered. The average particulate
emission results for the five tests were 11.22 Ib/hr and 0.0087
gr/DSCF.
Several problems were encountered during the recovery
furnace testing, resulting in the abortion of three tests;
however, none of the five tests shown in the summary tables were
effected. Twice during testing, the No. 4 Recovery Boiler ESP
malfunctioned, which necessitated a restart of the test since
the resulting uncontrolled recovery furnace emissions overloaded
the sampling trains before they could be shut off. The other
aborted test resulted from a break in the six foot glass probe
which was discovered during a leak test while changing ports.
Since it was not known when the break had occurred, a new test
was started.
-------
Table 3.1 SUMMARY OF PARTICULATE EMISSION RESULTS
NO. 4 RECOVERY FURNACE
Run Number
Date
Volume of Gas Sampled - DSCFa
- (Nm3)b
Average Stack Temperature - °F
- °C
Percent Moisture by Volume - %
Stack Volumetric Flow Rate - DSCFMC
- (Nm3/sec)d
Stack Volumetric Flow Rate - ACFM6
- m3/sec
Percent Isokinetic
Particulates - probe, and
filter catch
mg
gr/DSCFf
(mg/Nm3)9
gr/ACF
mg/irr
Ib/hr
Kg/hr
Particulates - total
mg
gr/DSCF
mg/Nm
gr/ACr
mg/m
Ib/hr
Kg/hr
1-1
2-12-74
176.861
5.01
338
170
21.5
141928
67.0
274310
139
111.0
30.4
0.00265
6.06
0.00137
3.19
3.226
1.46
92.4
0.00806
18.4
0.00417
9.71
9.808
4.45
1-2
2-13-74
182.949
5.18
349
177
22.8
148427
70.1
292782
149
109.8
37.3
0.00314
7.18
0.00159
3.70
4.002
1.82
127.8
0.01078
24.7
0.00545
12.7
13.715
6.23
1-3
2-14-74
388.718
11.0
361
182
23.1
159325
75.2
312178
158
108.7
61.2
0.00242
5.54
0.00126
2.93
3.358
•1.52
112.1
0.00445
10.2
0.00231
5.38
6.152
2.79
1-4
2-15-74
273.535
7.76
347
175
22.1
160461
75.7
299248
152
101.2
39.0
0.0022
5.03
0.00117
2.72
3.026
1.37
154.3
0.00870
19.9
0.00466
10.9
11.973
5.44
1-5
2-18-74
244.558
6.93
345
174
22.9
143142
69.9
294630
150
98.6
43.2
0.00273
6.25
0.00137
3.19
3.461
1.57
180.6
0.01139
26.1
0.00573
13.3
14.471
6.57
a Dry standard cubic feet at 70°F, 29.92 in. Hg.
Normal cubic meters at 21.1°C, and 760 mm Hg. - dry basis
c Dry standard cubic feet per minute at 70°F, 29.92 in. Hg.
d Normal cubic meters per second at 21.1°C, and 760 mm Hg. - dry basis
e Actual cubic feet per minute.
Grains per dry standard cubic foot.
9 Milligrams per dry normal cubic meter.
-------
Lime Kiln
A summary of particulate emission data from the six tests
on the No. 2 Lime, Kiln is presented in Table 3.2. The emission
results of the first three (3) particulate tests on the lime
kiln (Tests 2-1 through 2-3) were very similar, with an average
grain loading of 0.1113 gr/DSCF and average emission rate of
13.41 Ib/hr. The final three (3) test results were neither
similar when compared with one another or with the first three
tests. This probably occured because the fuel used to fire the
rotary lime kiln was changed from oil to natural gas about mid-
way through Test 2-4. The grain loading for Test 2-4 (0.0856
gr/DSCF) was about midway between the average grain loading for
the first three tests (0.1113 gr/DSCF) and that of Test 2-5
(0.05961 gr/DSCF), which supports the possibility that the fuel
switch to gas caused a decrease in particulate emissions. This.
rationale also is consistent with the fact that particulate
emissions from oil combustion are generally higher than those from
natural gas combustion. Test 2-6 yielded a grain loading of only
0.03699 gr/DSCF, but the volumetric flow rate (11,560 DSCFM) for
this test was well below the average flow rate for the other
five tests (13,467 DSCFM), which could account for this difference.
The production rate was somewhat lower during this run. (See
Chapter IV).
The average grain loading for the six kiln tests was
0.08604 gr/DSCF, while the emission rate averaged 11.2 Ib/hr.
There were no problems encountered with the actual testing which
should influence the results.
-------
Table 3.2 SUMMARY OF PARTICULATE EMISSION RESULTS
NO. 2 LIME KILN
Run Number
Date
Volume of Gas Sampled - DSCFa
- Nm3 b'
Average Stack Temperature - °F
- °C
Percent Moisture by Volume - %
Stack Volumetric Flow Rate - DSCFMC
- Nm3/sec d 6.97
Stack Volumetric Flow Rate - ACFM6
- m /sec
Percent Isokinetic
Particulates - probe, bypass, and
filter catch
mg
gr/DSCFf
mg/Nm3 ^
gr/ACF
mg/m3
Ib/hr
kg/hr
Particulates - total
mg
gr/DSCF
mg/Nm3
gr/ACF
mg/m
Ib/hr
kg/hr
2-1
2-12-74
59.589
1.68
151
66
25.2
14755
6.97
22844
11.6
101.0
416.8
0.10794
247
0.06962
162
13.651
6.18
435.3
0.11273
258
0.07271
.69
14.257
6.45
2-2
2-13-74
57.781
1.64
151
66
24.3
14292
6.75
21714
11.0
101.0
363.7
0.09713
222
0.06395
149
11.899
5.39
392.5
0.10483
240
0.06902
161
12.842
5.81
2-3
2-14-74
54.503-
1.54
151
66
25.5
13165
6.21
20357
10.3
103.5
361.5
0.10235
234
0.06632
154
11.550
5.23
411.4
0.11648
266
0.07548
176
13.144
5.94
2-4
2-14-74
56.300
1.59
154
68
30.6
12832
6.06
21337
10.8
109.7
312.3
0.08560
196
0.05152
.120
9.415
4.26
332.9
0.08560
196
0.05492
128
ao.ose
4.54
2-5
2-14-74
58.532
1.66
156
69
27.0
13896
6.56
22016
11.2
105.3
226.3.
0.05961
136
0.03762
87.6
7.100
3.21
336.5
O.C5961
136
0.05599
130
10.567
4.78
2-6
2-14-74
48.010
1.36
152
67
24.5
11560
5.46
17643
8.96
103.5
115.J
0.03C99
3-1. G
0.02-132
56.6
3.678
1.66
198.9
0.03099
B4.G
0.04203
98
6.356
2.88
a Dry standard cubic feet at 70°F, 29.92 in. Hg.
b Normal cubic meters at 21.1°C, and 760 mm Hg. - dry basis
c Dry standard cubic feet per minute st 70°F, 29.92 in. Hg.
Normal cubic meters per second at 21.1°C, and 760 mm Hg. - dry basis
g
Actual cubic feet per minute.
Grains per dry standard cubic foot.
" Milligrams per dry normal cubic meter.
-------
IV. PROCESS DESCRIPTION AND OPERATION
The St. Regis Paper Company mill at Tacoma, Washington pro-
duces 1000 tons of kraft pulp per day. About 15 percent of the
pulp is bleached and made into paper. The remaining pulp is made
into a variety of brown paper and paperboard products. The plant
has been operating since 1928. •
Process Description
A. General . ,
The process for making kraft pulp from wood is shown in
Figure 4.1. In the^process, wood is chipped into small pieces
and then cooked in digesters (five batch and two continuous) at
elevated pressure and temperature. The cooking chemicals, called
white liquor, are sodium hydroxide and sodium sulfide in water
solution. The white liquor chemically dissolves lignin, leaving
wood cellulose (pulp) which is filtered from the spent liquor and
washed. The pulp is made into paper.
The balance of the pulping process is designed to recover the
cooking chemicals. Spent cooking liquor and the pulp wash water
are combined for treatment to recover chemicals. The combined
stream, called weak black liquor, is concentrated, in steam heated
multiple-effect evaporators, including a special effect called a
concentrator. The strong black liquor leaving the evaporators
is burned in a recovery furnace.
Combustion of the organic matter in the black liquor provides
heat needed to generate process steam. Inorganic chemicals from
the black liquor are recovered as a molten smelt at the bottom
of the furnace. The smelt, consisting of sodium carbonate and sodium
sulfide, is dissolved in water and transferred to a causticizing
8
-------
WOOD
(NaOH +
IQLJOR
Na2S)
DIGESTER
SYSTEM
— U F fl k1
PULP
WASHERS
RI A r ic i T niir
"PULP
•WATER
RECOVERY
FURNACE
SYSTEM
STACK
n
AIR
HEAVY
BLACK •
LIQUOR
MULTIPLE
EFFECT
EVAPORATOR
SYSTEM
o
UJ
C£.
\
SMELT
(Na2C03 + Na2S)
WATER-
SMELT
DISSOLVING
TANK
GREEN LIQUOR
L
I WHITE LIQUOR
(RECYCLE TO
DIGESTER)
CAUSTICIZING
TANK
LIME
CALCIUM.
•CARBONATE
MUD
Figure 4.1. The Kraft pulping process at the St. Regis mill
in Tacoma, Washington.
-------
tank. Lime added to this tank converts sodium carbonate to sodium
hydroxide, completing the regeneration of white liquor, which is
then recycled to the digester. The calcium carbonate mud that .
precipitates from the causticizing tank, is recycled to a kiln
to regenerate lime.
B. Recovery Furnace
The Number 9 recovery furnace was designed by Combustion
Engineering to burn 108,000 pounds of black liquor solids per hour,
which corresponds to a pulp production rate of about 863 tons per
day. Auxiliary fuel oil is also burned.
The furnace is not equipped with direct contact evaporators.
Special steam heated evaporators, called concentrators, are used
instead. With this design, gases leaving the furnace are not
used to concentrate the incoming black liquor. Instead, the gases
preheat the combustion air in two parallel heat exchangers called
laminaire heaters, as shown in Figure 4.2.
Steam is generated in the recovery furnace to provide some
of the process heat requirements. A portion of the steam is used
within the furnace to blow soot from the boiler tubes. The soot
blowers operate one at a time, with each complete sequence taking
about 2 1/2 hours. A new cycle begins as soon as the previous
cycle ends, so that the soot blowers operate continually.
C. Electrostatic Precipitator
The exhaust gases from the Number 9 recovery furnace are
cleaned in an electrostatic precipitator. The precipitator was
installed in 1973 by Wheelabrator-Lurgi. The unit was designed
10
-------
RECOVERY
FURNACE
FURNACE
COMBUSTION
GASES
SAMPLING PORTS
ELECTROSTATIC
PRECIPITATOR
STACK
Figure 4.2. Recovery furnace and precipitator at the St. Regis Mill in Tacoma, Washington,
-------
to treat combustion gases at a rate of 400,000 ACFM, at a tempera-
ture of 350-475°F.
The precipitator has two parallel chambers with four sec-
tions in each chamber. The middle sections have independent power
supplies; the two inlet sections share one power supply and the
two outlet sections share one power supply.
The insulator compartment is heated to protect it from
corrosive condensation. Five fans blow hot air over the in-
sulators, with each fan supplying about 800 CFM. The total heat-
ing air is only 1 percent of the design capacity of the precipita-
tor, and does not lower the particulate concentration significantly.
Dust collecting on the precipitator electordes is shaken loose
by a system of rappers. The rappers operate in continual cycles,
with each cycle lasting 3 1/2 minutes. The collected dust falls
into dry hoppers and is removed by screw conveyors to a mix tank.
In the tank, the dust is dissolved in black liquor and recycled
to the process. If the conveyors are stopped by a malfunction,
the precipitator power is automatically shut off to prevent clogging
the conveyors. This happened twice during the test series.
Each time, the precipitator was off for only a few minutes but the
surge of particulate through the stack forced the cancellation
of both test runs.
The precipitator is located near ground level and the exhaust
gases discharge through a tall stack.
12
-------
D. Lime Kiln and Venturi Scrubber
The Number 2 lime kiln was designed by Traylor Company to
produce 80 tons of lime per day. This is equivalent to a pulp
production rate of about 320 tons per day. This rotary kiln is
170 feet long, with an inside diameter of 8 1/2 feet. It is fired
with either natural gas or No. 6 fuel oil.
The feed to the kiln is the calcium carbonate slurry that
precipitates from the causticizing tanks. The slurry is washed
and then dried on a rotary vacuum drum, as shown in Figure 4.3.
The dried cake is removed from the drum on a knife edge and con-
veyed to the kiln. In the kiln, the calcium carbonate mud is
roasted and carbon dioxide is driven off, leaving calcium oxide
(lime) as product.
Noncondensable gases from the multiple-effect evaporators
are burned to destroy odors. These gases are burned in either of
the two kilns operated at the plant. Dregs from the green liquor
clarifier are not burned in the kilns.
The combustion gases from the kiln are cleaned in an adjust-
able throat venturi scrubber. They then pass through a demister
and out a 100 foot stack. The scrubbing water is recycled from
the demister and blended with fresh water makeup. A portion of
the recycled water is purged to prevent fexcessive accumulation of
solids, and used elsewhere in the process.
Process Operation
A. General
The purpose of the tests was to measure emission levels during
13
-------
LIMESTONE
MUD —*
MUD
WASHER
VACUUM
FILTER
SAMPLING PORTS
EXHAUST
GAS
STACK
AIR
GAS OR
NO. 6 OIL
FRESH
WATER'
LIME
(PRODUCT)
VENTURI
\
DEMISTER
•RECYCLE-
-»-BLEED
Figure 4.3. Flow diagram of the No. 2 lime kiln at the St. Regis mill
in Tacoma, Washington.
-------
normal plant operation. Process conditions were carefully observed,
and testing was done only when the test facility appeared to be
operating normally.
The laminaire heaters on the furnace are cleaned daily.
During cleaning, the flow rate of black liquor to the furnace is
reduced. By arrangement with the plant, the heaters were cleaned
after the test periods, so that during the test the full charge
of black liquor would go to the furnace.
As previously mentioned the precipitator lost power twice
because of malfunctions to the screw conveyors under the hoppers.
Power was lost at 1130 hours on February 13, and at 1247 hours on
February 19. Particulate sampling was stopped on both occasions
and the test runs were aborted.
The plant has installed a Lear-Siegler transmissometer to
monitor the stack gas opacity. The chart record of this instrument
was very steady throughout the tests, indicating an opacity of
4.5 to 6 percent. The opacity readings were observed to increase
slightly when the black liquor charging rate increased by about
40 gpm. During both precipitator malfunctions mentioned above,
the opacity readings went off scale. The readings are recorded
on the process data sheets in Appendix B.
During the tests, important process conditions were monitored
and recorded on data sheets. Readings were taken about once every
half-hour. These data, and a key to the entries, are in Appen-
dix B. The readings made on the precipitator include voltage
and amperage of the primary and secondary circuits of all six
15
-------
control fields. Charging rate and other significant operating
variables were also recorded. Furnace temperatures cound not
be recorded because the monitors were not operational.
Based on available precess data and conversations with the
operators, the furnace and precipitator operated normally during
the tests, with the exception of the two precipitator power-outages,
The black liquor charging rate was in its normal range of 190 to
240 gpm. Soot blowers operatied continually during the testing,
as normal.
The gas flow rate through the precipitator during the tests
is compared to the design flow rate in Table 4.1 below. As shown,
the flow rate during the tests averaged 74 percent of the design
rate.
Table 4.1. Gas Flow Rates Through the Precipitator
Gas Flow Rate, ACFM
Run Number
Date, 1974 During Test
Design
% of Design
1-1
1-2
1-3
1-4
1-5
Feb.
Feb.
Feb.
Feb.
Feb.
12
13
14
15
18
274
292
312
299
294
,310
,782
,178
,248
,630
400
400
400
400
400
,000
,000
,000
,000
,000
69
73
78
75
74
7 4 Avg .
C. Lime Kiln
During the tests, important process conditions were monitored
and recorded on data sheets. Readings were taken about every half-
16
-------
hour. These records and a key to the entries are in Appendix B.
As far as known from the process information and conversations
with the operators, the kiln and scrubber operated normally during
the tests. The main process information is summarized in
Table 4.2 below.
As shown, the particulate emissions ranged from 0.04 to
0.11 gr/dscf. The three highest emissions occurred while the kiln
was fired with oil; the two lowest emissions occurred while the kiln
was fired with natural gas; an intermediate emission level occurred
when the kiln was fired with oil for half the sampling period, and
then switched to gas. It should also be noticed that the kiln
charging rate was lower during gas firing (50 compared to 60 gpm
of mud). The combination of gas firing and lower charging rate
apparently reduced particulate emissions about 50 percent.
Table 4.2. Summary of Lime Kiln Process Data
During Particulate Sampling
Mud. Venturi Fuel Fuel
Charging Pressure Gas Oil Particulate
Date Sampling Rate, Drop, Rate, Rate, Emissions,
Test 1974 Hours gpm in H20 mscfh Ib/hr gr/dscf (total)
2-1
2-2
2-3
' 2-4
2-5
2-6
Feb. 12
Feb. 13
Feb. 13
Feb. 14
Feb. 14
Feb. 14
1225-1555
1000-1225
1400-1628
0908-1213
1235-1538
1605-1834
60-61
60
60
0-60a
50-60
50
31-32.5
32-32.5
32-32.5
30-32
29.9-31
24.5-28
0 1650-1760
0 1660-1780
0 1680-1710
25-27b 0-1790b
22-26 0
22 0
0
0
0
0
0
0
.11
.10
.12
.09
.06
.04
a Feed was off briefly while the kiln was switched from oil to gas firing.
k Kiln was switched from oil to gas at 1025 hours.
17
-------
V. LOCATION OF SAMPLING POINTS
Recovery Furnace
Figure 5..1 illustrates the locations of the sampling ports
and points for Recovery Boiler No. 4. The sampling site was
located at a point approximately 70 ft. (5.0 stack diameters)
from the top of the stack and 74 ft. (6.7 diameters) from the
outlet of the ESP (also the closest upstream disturbance). The
diameter of the stack at the sampling site is 14.0 ft. Twenty,
eight (28) traverse points (14 along each of two perpendicular
diameters) were selected as prescribed by the Method 1 of the
Federal Register.
The sampling platform was especially constructed for
testing and consisted of a metal grating floor surrounding the
stack and enclosed on the top and sides by corrugated plastic.
Access to the sampling points was accomplished through four (4)
ports (at 90° separation), since the 14.0 ft. diameter stack
was too wide to traverse along one diameter through a single
port.
Lime Kiln
Locations of the sampling ports and points for Lime Kiln
No. 2 are shown in Figure 5.2. The sampling site was located
at a point approximately 30 ft. (7.5 stack diameters) from the
top of the stack and 10 ft. (2.5 stack diameters) from the
demister exit (also the nearest upstream restriction). The
diameter of the stack at the sampling site is 4.0 ft. Forty
1) Federal Register, Vol. 36, No. 247, December 23, 1971.
18
-------
SAMPLE POINT LOCATION FROM INNER STACK WALL
(inches)
N-l 3.0
E-l 3.0
S-l 3.0
W-l 3.0
9.5
16.75
24.5
33.75
47.5
61.5
9.5
16.75
24.5
33.75
47.5
61.5
9.5
16.75
24.5
3.75
47.5
61.5
14 ft ID
28 SAMPLING POINTS
3 5 7° 6 4 2
ooooooo ooooooo
246°753
9.5
16.75
24.5
33.75
47.5
61.5
70 *
74
RECOVERY
FURNACE
ESP
Figure 5.1 Sample port and point locations on Recovery
Furnace No. 4.
19
-------
SAMPLE POINT LOCATION FROM INNER STACK WALL
(inches)
S-l
2
3
4
5
6
7
8
9
10
1.0
2.0
3.25
4.5
6.5
8.0
9.75
12.0
14.25
18.25
S-ll
12
13
14
15
16
17
18
19
20
29.5
33.5
36.0
38.25
40.0
41.5
43.5
44.75
46.0
47.0
W-l
2
3
4
5
6
7
8
9
10
1.0
2.0
3.25
4.5
6.5
8.0
9.75
12.0
14.25
18.25
4 ft ID
40 SAMPLING POINTS
LIME
KILN
B-ll
12
13
14
15
16
17
18
19
20
29.5
33.5
36.0
38.25
40.0
41.5
43.5
44.75
46.0
47.0
VENTURI
SCRUBBER
30*'
10'
/
2-3"
Ports
6
DEMISTER
Figure 5.2 Sample port and point locations on Lime Kiln No. 2,
20
-------
(40) sampling points (20 along each of two perpendicular diam-
eters) were selected, as prescribed by Method 1 of the Federal
Register.
The sampling platform was especially constructed for
sampling and consisted of a metal grating floor around approxi-
mately 270° of the stack circumference enclosed on the top and
sides. Access to the sampling points was provided by two ports
at 90° separation..
1) Federal Register, Vol. 36, No. 247, December 23, 1971,
21
-------
VI. SAMPLING AND ANALYTICAL PROCEDURES
All sampling procedures were selected by EPA prior to
field sampling. All analyses of collected samples were
performed by PEDCo. Appendix E contains detailed descrip-
tions of the sampling and analytical procedures employed for
the tests. These procedures are described briefly below.
Velocity and Gas Temperature
All gas velocities were measured with a calibrated type
S pitot tube and inclined draft gage. In all cases veloc-
ities were measured at each sampling point across the stack
diameter to determine an average value according to pro-
cedures described in the Federal Register - Method 2.
Temperatures were measured with long stem dial thermometers.
Molecular Weight
An integrated sample of the stack gases was collected
daily throughout the testing periods by pumping the gas into
•p
a Tedlar plastic bag at the rate of approximately 0.015
CFM. This bag sample was then analyzed with an Orsat ana-
lyzer for C0~» Oy, and CO as described in the Federal
Register , Method 3.
Particulates
2
Method 5 as described in Federal Register , was used to
measure particulate matter. A rigid train consisting of a
heated glass lined probe, a 3" glass fiber filter, and a
series of Greenburg-Smith impingers was employed in all
particulate tests. A water wash of the probe and filter
portion of the train was made in addition to the acetone
rinse.
1) Federal Register, Vol. 36, No. 247, December 23, 1971
2) Federal Register, Vol. 36, No. 159, August 17, 1971
22
------- |