74-KPM-17
(REPORT NUMBER)
AIR POLLUTION EMISSION TEST
THE BUCKEYE CELLULOSE CORPORATION
(PLANT NAME)
FOLEY, FLORIDA
(PLANT ADDRESS)
U. S. ENVIRONMENTAL PROTECTION AGENCY
Office of Air and Water Programs
Office of Air Quality Planning and Standards
Emission Standards and Engineering Division
Emission Measurement Branch
Research Triangle Park, N. C. 27711
-------
STATIONARY SOURCE TESTING OF A KRAFT PULP MILL
at
The Buckeye Cellulose Corporation
Foley, Florida
EPA Project Report No. 74-KPM-17
by
William H. Maxwell
Midwest Research Institute
EPA Contract No. 68-02-0228
MRI Project No. 3585-C(41)
For
Office of Air Quality Planning and Standards
Envirqnmental Protection Agency
Research Triangle Park, North Carolina 27711
Attn: Mr. Lance S. Granger
-------
PREFACE
The work reported herein was conducted by Midwest Research In-
stitute (MRI) under Environmental Protection Agency (EPA) Contract No. 68-
02-0228, Task No. 37, Changes Nos. 2 and 5.
The project was under the technical supervision of Mr. Paul C.
Constant, Jr., Head, Environmental Measurements Section of the Physical
Sciences Division. Mr. William Maxwell served as crew chief and was as-
sisted by Messrs. George Cobb, Bruce DaRos, and John LaShelle. Ms. Christine
Guenther was responsible for the data reduction and computer analysis. The
analysis of the samples was done by Ms. Carol Green.
Approved for:
MIDWEST RESEARCH INSTITUTE
Paul C. Constant, Jr.
Program Manager
ii
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TABLE OF CONTENTS
I. Introduction 1
II. Summary and Discussion of Results. . . . 2
III. Process Description and Operation 7
A. Process Description. 7
B. Process Operation. 10
IV. Location of Sample Points. ....... 14
V. Sampling and Analytical Procedures 14
A. Mass Particulate 14
B. Flue Gas Composition 18
C. Opacity 18
Appendix A - Results of Analysis - Printout of Computer
Calculations 20
Appendix B - Sample Calculations 62
Appendix C - Process Data 67
Appendix D - Field Data. ........ 103
iii
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LIST OF TABLES
No. Title
I Summary of Particulate Results: No. 3 Lime Kiln ..... 3
II Summary of Particulate Results: No. 2 Recovery Furnace. . 4
III Summary of Opacity Readings: No. 3 Lime Kiln. ...... 5
IV Summary of Opacity Readings: No. 2 Recovery Furnace ... 6
V Summary of Lime Kiln Process Data During Particulate
Sampling 12
VI Summary of Recovery Furnace and Electrostatic Precipitator
Process Data During Particulate Sampling 13
VII Location of Sampling Points: No. 3 Lime Kiln Stack. ... 17
VIII Location of Sampling Points: No. 2 Recovery Furnace
Stack. . 17
LIST OF FIGURES
No. Title Page
1 The Kraft Pulping Process at the Buckeye Cellulose Mill
in Foley, Florida 8
2 Flow Diagram of the No. 3 Lime Kiln at the Buckeye
Cellulose Mill in Foley, Florida 9
3 No. 2 Recovery Furnace and Precipitator at the Buckeye
Cellulose Mill in Foley, Florida ............ 11
4 Schematic of Stack and Ports: No. 3 Lime Kiln ...... 15
5 Schematic of Stack and Ports: No. 2 Recovery Furnace. . . 16
iv
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I. INTRODUCTION
This report presents the results of source testing performed dur-
ing the period 28 April to 15 May 1974 by Midwest Research Institute on two
processes of the Buckeye Cellulose Corporation mill at Foley, Florida. Six
tests each for particulate emissions were conducted on the stacks of the
No. 3 lime kiln and the No. 2 black liquor recovery furnace during periods of
continuous process operation. The composition of the stack gas was deter-
mined by Orsat analysis. Plume opacity readings were taken for each test.
Process conditions were monitored by the Environmental Protection Agency.
All tests were conducted on the stacks following the control de-
vices, a wet scrubber for the lime kiln, and an electrostatic precipitator
for the recovery furnace. Tests were completed in accordance with the
Federal Register, Vol. 36, No. 159, Part II, 17 August 1971, except as may
be defined later in this report.
The scope of work for this project specified:
1. Three tests on the lime kiln when natural gas was the firing
fuel;
2. Three tests on the lime kiln when fuel oil was the firing
fuel; and
3. Six tests on the recovery furnace.
The following sections of this report present:
1. The summary and discussion of results;
2. The process description and operation;
3. The location of the sample points; and
A. The sampling and analytical procedures.
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II. SUMMARY AND DISCUSSION OF RESULTS
Tables I and II present a summary of the particulate load results
for the lime kiln tests and the recovery furnace tests, respectively. Data
are given for the front-half and total catch and presented as grains per dry
standard cubic foot (gr/dscf), milligrams per normal cubic meter (mg/ncm),
pounds per hour (Ib/hr), and kilograms per hour (kg/hr). Computer printouts
of the field data and reductions are found in Appendix A. Sample calcula-
tions are found in Appendix B.
The sampling volumes for the lime kiln tests ranged from 56.57 to
60.09 dscf, with only Run K-6 being over 60 dscf. A longer sampling time
would have increased the volume but as sufficient sample was collected, and
the maximum variation from the 60-dscf minimum volume required by the Fed-
eral Register was only 5.77o, it is not believed that the results will be
biased. Sampling volumes for the recovery furnace tests ran from 104.40 to
130.09 dscf. Values for the percent isokinetic sampling rate varied from
95.8 to 111.6, with only Run R-7 being out of the acceptable range. The
results for Run R-12 appear out of line with those of R-7 through R-ll but
subsequent checking has verified their accuracy.
As the lime kiln stack gas stream was saturated with water vapor
and contained water droplets, percent moisture determinations were obtained
from a psychrometric chart. The volume of water collected value needed for
entry into the computer program was back-calculated from this percent mois-
ture value using the standard equation. The moisture percentages for the
lime kiln tests ranged from 34.5 to 41.0. As the recovery furnace gas
stream was not saturated with water vapor, the normal procedure was followed.
Values of the percent moisture ranged from 29.6 to 32.6 for the recovery
furnace tests.
Tables III and IV present summaries of the plume opacity readings
for the lime kiln and recovery furnace tests, respectively. Data are given
for both observers on each test. Difficulty in reading the plumes was en-
countered due to intermingling plumes and attached steam plumes.
-------
TABLE I
SUMMARY OF PARTICULATE RESULTS: NO. 3 LIME KILN
Particulate Load
Front -Half Catch
Run
K-l
K-2
K-3
Average
K-4
K-5
K-6
Average
a/ gr/dscf =
mg/ncm =
Ib/hr =
kg/hr =
Fuel
Gas 30
Gas 1
Gas 1
Oil 2
Oil 2
Oil 3
grains per
milligrams
pounds per
kilograms
Date £gr/dscf)^7 (rag/ncm)-'
April
May
May
May
May
May
0
0
0
0
0
0
0
0
dry standard
per normal
hour
per hour
.0327
.0255
.0214
.0265
.2545
.2614
.2330
.2496
cubic foot
74.8
58.4
49.0
60.7
582
598
533
571
i Total .Catch
(gr/dscf)^ (rng/ncm)^7
0.0369
0
0
0
0
0
0
0
.0310
.0276
.0318
.259
.274
.237
.257
84.5
70.9
63.1
72.8
592
627
543
587
(Ib/hr)-7
4.80
4
3
4
32
35
30
32
.19
.42
.14
.5
.7
.5
.9
(kg/hr):
2.18
1.90
1.55
1.88
14.8
16.2
13.8
14.9
cubic meter
-------
Run Date
R-7 7 May
R-8 8 May
R-9 9 May
R-10 10 May
R-ll 13 May
R-12 14 May
Average
TABLE II
SUMMARY OF PARTICIPATE RESULTS: NO.2 RECOVERY FURNACE
Partlculate Load
Front -Half
(gr/dscf)
0.0144
0.0120
0.0132
0.0120
0.0159
0.0153
0.0138
Catch
(mg/hcm)
32.9
27.5
30.2
27.5
36.3
34.9
31.6
(gr/dscf)
0.046
0.048
0.044
0.034
0.063
0.102
0.056
Total
(mg/ncm)
106
111
102
78
144
232
129
Catch
(lb/hr)
45
49
43
33
62
105
56
(kg/hr)
20.2
22.3
19.6
15.1
28.0
47.6
25.5
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TABLE III
SUMMARY OF OPACITY READINGS: NO. 3 LIME KILN
Duration of
Total No. of
No. Readings
No. Readings
Run No.
Date
Observation (min)
Readings
Unobservable
0% Opacity
5
10
15
20
25
30-100
Percent Readings Unobservable
Percent Readings 0% Opacity
5
10
15
20 .
25
30-100
K-l
30 April
Obs. l2/<
123
492
0
0
488
4
0
0
0
0
0
0
99.19
0.81
0
0
0
0
100
K-2
1974
Dbs. 2-1
131
524
21
0
503
0
0
0
0
0
4.01
0
95.99
0
0
0
0
0
100
1 May
Obs. 1
121
484
0
0
484
0
0
0
0
0
0
0
100
0
0
0
0
0
100
1974
Obs. 2
130
520
484
Q
36
0
0
0
0
0
93.08
0
6.92
0
0
0
0
0
100
K-3
1 May
Obs. 1
130
520
146
0
374
0
0
0
0
0
28.08
0
71.92
0
0
0
0
0
100
1974
Obs. 2
130
520
399
0
121
0
0
0
0
0
76.73
0
23.27
0
0
0
0
0
100
K-4
2 May
Obs. 1
130
520
180
0
286
40
13
1
0
0
34.62
0
55.00
7.69
2.50
0.19
0
0
100
1974
Obs. 2
130
520
503
0
4
6
3
0
4
0
96.73
0
0.77
1.15
0.58
0
0.77
0
100
K-
2 May
Obs. 1
130
520
0
0
72
337
88
23
0
0
0
0
13.85
64.81
16.92
4.42
0
0
100
5
1974
Obs. 2
130
520
436
0
81
3
0
0
0
0
83.85
0
15.58
0.58
0
0
0
0
100.01
K-6
3 May
Obs. 1
131
524
0
0
0
314
198
12
0
0
0
0
0
59.92
37.79
2.29
0
0
100
1974
Obs. 2
130
520
520
0
0
0
0
0
0
0
100
0
0
0
0
0
0
0
100
Average Opacity =
Sum of Nos.
No. Readings Observable
5.04
5.00
5.00
5.00
5.00
5.00
6.01 13.24
10.60
5.19
12.12
a/ Obs. 1 = Observer 1. . Obs. 2 = Observer 2.
-------
TABLE IV
SUMMARY OF OPACITY READINGS: NO. 2 RECOVERY FURNACE
Run No.
Date
Duration of Observation (min)
Total No. of Readings
No. Readings Unobservable
No. Readings 07. Opacity
5
10
15
20
25
30
35
40
45
50
55-100
Percent Readings Unobservable
Percent Readings 07= Opacity
5
10
15
20
25
30
35
40
45
50
55-100
Avnrnen Orv.ci.-v Smn of Nos •
R-7
7 May
Obs. I3-
242
968
0
0
858
59
28
9
12
0
1
0
1
0
0
0
0
88.64
6.10
2.89
0.93
1.24
0
0.10
0
0.10
0
0
100
fi.ns
1974
/ Obs. Z*j
237
948
0
0
875
38
14
8
5
5
0
2
0
1
0
0
0
92.30
4.01
1.48
0.84
0.53
0.53
0
0.21
0
0.11
0
100.01
S.81
R-8
8 May
Obs. 1
233
932
0 .
0
867
35
26
2
2
0
0
0
0
0
0
0
0
93.03
3.76
2.79
0.21
0.21
0
0
0
0
0
0
100
5. 54
1974
Obs. 2
211.5
846
0
0
817
17
6
6
0
0
0
0
0
0
0
0
0
96.57
2.01
0.71
0.71
0
0
0
0
0
0
0
100
S.28
R-9
9 May
Obs. 1
252
1,008
252
0
688
45
11
11
1
0
0
0
0
0
0
25.00
0
68.25
4.46
1.09
1.09
0.10
0
0
0
0
0
0
99.99
S.fiQ
1974
Obs. 2
210
840
413
0
408
8
7
. 2
1
1
0
0
0
0
0
49.17
0
48.57
0.95
0.83
0.24
0.12
0.12
0
0
0
0
0
100
5.41
R-10
10 May
Obs. 1
281
1,124
198
0
873
22 .
22
8
1
0
0
0
0
0
0
17.62
0
77.67
1.96
1.96
0.71
0.09
0
0
0
0
0
0
100.01
=;. si
1974
Obs. 2
240
960
224
0
709
15
8
4
0
0
0
0
0
0
0
23.33
0
73.85
1.56
0.83
0.42
0
0
0
0
0
0
0
99.99
s ?q
R-ll
13 May
Obs. 1
281
1,124
74
0
985
21
33
10
1
0
0
0
0
0
0
6.58
0
87.63
1.87
2.94
0.89
0.09
0
0
0
0
0
0
100
S S8
1974
Obs. 2
239
956
219
0
709
13
9
4
i
1
0
0
0
0
0
22.91
0
74.16
1.36
0.94
0.42
0.10
0.10
0
0
0
0
0
99.99
s is
R-12
14 May
Obs. 1
278
1,112
0
0
1,022
32
47
9
2
0
0
0
0
0
0
0
0
91.91
2.88
4.23
0.81
0.18
0
0
0
0
0
0
100.01
S 7?
1974
Obs. 2
247
988
0
0
928
28
23
9
0
0
0
0
0
0
0
0
0
93.93
2.83
2.33
0.91
0
0
0
0
0
0
0
100
s si
a/ Obs. 1 = Observer 1. Ofas. 2 = Observer 2.
-------
a/
III. PROCESS DESCRIPTION AND OPERATION-
The Buckeye Cellulose Corporation mill at Foley, Florida, produces
about 900 tons of bleached kraft pulp per day. Buckeye Cellulose uses the
dissolving kraft pulping process. This process is similar to the normal
kraft process, but incorporates steam digestion of the wood before digestion
with the usual cooking liquor.
The EPA test program conducted at this mill included particulate
emission measurements on the recovery furnace and the lime kiln.
A. Process Description
1. General: Kraft pulp is produced from wood as shown in Figure 1.
In the process wood is chipped into small pieces, then cooked in 19 batch
digesters at elevated temperature and pressure. The wood is first cooked
with steam and then with the cooking chemicals, called white liquor. The
cooking chemicals 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 then
bleached and made into paper.
The balance of the process is designed to recover the cooking
chemicals. Spent cooking liquor and the pulp wash water are combined for
treatment. The combined stream, called weak black liquor, is concentrated
in multiple-effect evaporators. The black liquor receives its final concen-
tration in direct contact evaporators and is then fired to a recovery
furnace.
2. Lime kiln: The No. 3 limekiln was manufactured by Allis
Chalmers and installed in 1965. The kiln is designed to produce 125 tons
of lime per day. This is equivalent to a pulp production rate of about
500 tons per day. This rotary lime kiln is 181 ft long, with an inside
diameter of 10 ft. It is fired with either natural gas (principle fuel) or
No. 2 fuel oil (reserve fuel).
The feed to the kiln is the calcium carbonate slurry that precipi-
tates from the causticizing tanks. The slurry is washed and dried in a
centrifuge, as shown in Figure 2. The dried cake (calcium carbonate) is
conveyed to the kiln where it is roasted and carbon dioxide is driven off,
leaving lime (calcium oxide) as product.
A venturi scrubber is used to control the particulate emissions
from the lime kiln. The scrubber was manufactured by Chemico and installed
in 1971. The venturi scrubber has a design pressure drop of 20 in. of water.
Lime mud centrifuge centrate is used as makeup water to the scrubber system.
a/ This section-furnished by EPA.
-------
o
z
o.
0-
WOOD
WHITE LIQUOR
(NaOH+Na2S)
STACK
JOR — +>
2S)
DIGESTER
SYSTEM
— PU
LP-*-
— WE
PULP
WASHERS
AK BLACK L
•PULP
-WATER
t—I
RECOVERY
FURNACE
SYSTEM
HEAVY
-BLACK-
LIQUOR
AIR
LLJ
g
SMELT
WATER-
3
SMELT
DISSOLVING
TANK
L-
GREEN LIQUOR
WHITE LIQUOR
(RECYCLE TO-
DIGESTER)
CAUSTICIZING
TANK
MULTIPLE
EFFECT
EVAPORATOR
SYSTEM
-LIME
CALCIUM
•CARBONATE-
MUD
Figure 1 - The Kraft Pulping Process at the Buckeye
Cellulose Mill in Foley, Florida
-------
LIMESTONE
MUD ~
CENTRIFUGAL
FILTER
AIR •
GAS OR '
NO.2 OIL
SAMPLING PORTS-
—EXHAUST 1
GAS
i.
STACK
VENTURI
FRESH
WATER"
»1 ^
LIME
(PRODUCT)
DEMISTER
-RECYCLE-
•BLEED
Figure 2 - Flow Diagram of the No. 3 Lime Kiln at the Buckeye Cellulose Mill in Foley, Florida
-------
3. Recovery furnace: The No. 2 recovery furnace was designed
by Babcock and Wilcox to operate at an equivalent pulp production rate of
550 tons/day. The recovery furnace normally operates at 1670 overload, burn-
ing 125 to 140 gal. of black liquor per min and 2 to 10 gal. of No. 6
fuel oil per min. The furnace has.a conventional design with direct con-
tact evaporators. The furnace was installed in 1958.
Exhaust gases from the furnace are cleaned in an electrostatic
precipitator. The precipitator was manufactured by Western Precipitation,
and installed in 1972. The precipitator was designed to treat 300,000 actual
cubic feet of combustion gases per minute. As shown in Figure 3, the pre-
cipitator has two separate chambers in parallel; each chamber has four
electrical fields. The precipitator is situated near ground level and
exhaust through a tall stack.
Dust collecting on the precipitator electrodes is shaken loose
by a system of rappers. The rappers operate in a continuous cycle, with
each cycle lasting 3 min. The dust falls into hoppers and is recycled to
the process.
B. Process Operation
1. General: The purpose of the tests was to measure emission
levels during normal mill operation. Process conditions were carefully
observed, and testing was done only when the test facility appeared to be
operating normally. During the tests, important operating parameters
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 Appendix C.
The process data are summarized below.
2. Lime kiln: As far as is known from the process information
and conversations with the operators, the lime kiln and scrubber operated
normally during the tests. Lime mud feed rate to the centrifuge was
between 95 and 100 gal/min. The solids content of the lime mud ranged
between 34.7 and 39.57<>. The pressure drop across the venturi scrubber
ranged between 15 and 18 in. of water. The averages of the major process
parameters for each test are listed in Table V.
3. Recovery furnace: As far as is known from the process data
and conversationswith the operators, the recovery furnace was operating
normally during the tests. Black liquor feed rate was steady between 130
and 141 gal/min. The black liquor solids content ranged between 58.5 and
62.07o. Steam production was between 215,000 and 260,000 Ib/hour throughout
the testing. Supplemental oil was burned at about 5 to 10 gal/min. During
the fourth tests no supplemental oil was required for steam production.
10
-------
RECOVERY
FURNACE
FURNACE
COMBUSTION
GASES
I—
DIRECT
CONTACT
EVAPORATOR
ELECTROSTATIC
PRECIPITATOR
(East Chamber)
DIRECT
CONTACT
EVAPORATOR
ELECTROSTATIC
PRECIPITATOR
(West Chamber)
AIR
l-BLACK LIQUOR
SAMPLING'
PORTS
INDUCED
DRAFT
FAN
o
STACK
Figure 3 - No. 2 Recovery Furnace and Precipitator at the Buckeye
Cellulose Mill in Foley, Florida
-------
TABLE V
SUMMARY OF LIME KILN PROCESS DATA DURING PARTICIPATE SAMPLING
Run
K-l
K-2
K-3
K-4
K-5
K-6
Fuel
Type Flow
Gas 78^7
Gas 75&'
Gas 75^/
Oil 7.3^
Oil 7.2-/
Oil 7.4^
Mud Flow to
Centrifuge
(gpm)
96
100
99
100
98
107
Solids
Content
(%)
38.3
38.9
38.4
37.8
38.7
35.0
Scrubber
Pressure
Drop
(in. H20)
17
16
16
16
16
16
Lime
Production
(tons/day)
165
167
169
166
170
169
a/ 1,000 cu ft/hr
b/ Gallons per minute
The averages of major operating parameters for each test are listed in
Table VI. The furnace-induced draft fan was cleaned with steam at approxi-
mately 12-min intervals. Soot is blown from the boiler tubes continuously.
The operation of the electrostatic precipitator was also
monitored during the tests. As far as is known the precipitatpr operated
normally during the tests. The primary voltage and current drawn by each
of the four control sections were monitored. The average primary voltages
during each test are also summarized in Table VI.
12
-------
TABLE VI ' .
SUMMARY OF RECOVERY FURNACE AND ELECTROSTATIC PRECIPITATOR PROCESS DATA DURING PARTICULATE SAMPLING
Recovery Furnace • Precipitator
Run
R-7
R-8
R-9
R-10
R-ll
R-12
Black Liquor
Flowrate
(gpm)
130
132
136
138
137
140
Solids
Content
(%)
61.0
61.4
60.3
60.3
61.2
60.0
Supplemental
Fuel Flow
(gpm)
9.8
9.2
6.2
0.0
6.1
13.5
Steam
Production
(lb/hr.)
251,000
255,000
241,000
223,000
238,000
247,000
Field
A
270
270
261
269
273
265
Primary
Field
B
329
331
342
330
335
330
Voltage
Field
C
309
308
207
305
314
326
Field
D
284
287
274
265
265
274
u>
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IV. LOCATION OF SAMPLE POINTS
Figure 4 shows a schematic layout of the lime kiln stack. Exist-
ing 3-1/2 in. ID ports were used. Although not located in accordance with
the Federal Register. Vol. 36, No. 159, 17 August 1971, with regard to the
minimum number of stack diameters downstream from disturbances, they were
used with EPA approval.
Figure 5 shows a schematic diagram of the recovery furnace stack.
Existing 6-in. ID ports were used. Their location was in accordance with
EPA and Federal Register guidelines.
Tables VII and VIII show the sampling points used for particulate
sampling on the lime kiln and recovery furnace stacks, respectively. For
the lime kiln, 24 points per traverse were used, while for the recovery
furnace, three points per traverse were used.
Integrated gas sampling for flue gas composition was done from the
same ports as for particulate sampling.
V. SAMPLING AND ANALYTICAL PROCEDURES
A. Mass Particulate
Particulate samples were taken with Research Appliance Company
Model 2243 "Stacksamplr" equipment, modified by MRI. Sampling train speci-
fications were in compliance with the Federal Register, Vol. 36, No. 159,
17 August 1971.
A preliminary velocity and temperature profile was taken on each
stack. A preliminary moisture determination was made on the recovery fur-
nace stack. Pyrex glass probe liners were used for sampling in all tests.
Sampling time on the lime kiln stack was 3 min/point for a total
sample time of 144 min. This permitted two tests per day to be run. Sam-
pling time on the recovery furnace stack was 24 min/point for the first run
and 20 min/point thereafter.
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a. Elevation
Sampling
Ports
Sampling
Platform
~56'-0"
Roof
b. Plan
Sampling
Platform
Not to Scale
Figure 4 - Schematic of Stack and Ports: No. 3 Lime Kiln
15 _
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a. Elevation
85'-0
lo:
_j
I'-O"
I
i "
20'-0"
1
"7
i
7
1 x
LJ
•Sample Ports
Sampling
„ Platform
b. Plan
Steel
Stack
Sampling
Platform
Concrete
Shell
Sampling Ports
Figure 5 - Schematic of Stack and Ports: No. 2 Recovery Furnace
16
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TABLE VII
LOCATION OF SAMPLING POINTS: NO. 3 LIME KILN STACK
48 in.
dint
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
Fraction of Stack ID
tt>
1.1
3.2
5.5
7.9
10.5
13.2
16.1
19.4
23.0
27.2
32.3
39.8
60.2
67.7
72.8
77.0
80.6
83.9
86.8
89.5
92.1
94.5
96.8
98.9
Distance from Inside Wall
(in.)
1
1-1/2
2-5/8
3-3/4
5
6-3/8
7-3/4
9-1/4
11
13
15-1/2
19-1/8
28-7/8
32-1/2
35
37
38-3/4
40-1/4
41-5/8
43
44-1/4
45-3/8
46-1/2
47
TABLE VIII
LOCATION OF SAMPLING POINTS: NO. 2 RECOVERY FURNACE STACK
Stack ID = 132 in.
Fraction of Stack ID Distance from Inside Wall
Point £%) (in.)
1 4,4 5-3/4
2 14.7 19-3/8
3 29.5 39
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This yielded 288- and 240-min total sample times, respectively. Two ports
were sampled prior to a lunch break, and then the test was completed follow-
ing lunch.
Due to the volume of water collected during testing on both stacks,
the first impinger was replaced halfway through the test with a fresh impinger
containing 100 ml of distilled deionized water. This practice was begun with
Run K-5. For the lime kiln tests, the filter was also replaced, beginning
with Run K-5.
Problems were encountered on the lime kiln tests with water in the
pitot lines due to the saturated gas stream. An air line was obtained and
the lines were periodically purged to ensure proper readings.
For Run K-4, it was observed that water had been pulled over into
the silica gel impinger. It is not believed that this will affect the
results, as the catch should be contained on the filter and the first two
impingers. Also, the volume of water collected per se was not used for
moisture determinations on the lime kiln stacks as previously mentioned.
During Run R-7, a piece of glassware was observed to be broken. The piece
was replaced and the test restarted.
Analysis of the particulate samples was in compliance with the
Federal Register. Vol. 36, No. 159, 17 August 1971.
B. Flue Gas Composition
An integrated gas sample was obtained over the duration of the
mass-particulate sampling time. The sampling was adjusted such that the bag
would be full at approximately the same time as the end of the particulate
test.
Analysis of the gas for percent C02, 02, and CO was obtained by
Orsat analysis. For Runs K-l through K-3, the MRI Burrell instrument was
used. As the value of the C02 was such that the 02 read off-scale on this
instrument for Run K-4, the sample was lost attempting to obtain values.
A Hays instrument was borrowed from the mill for the remainder of the tests
and no further samples were lost. Values obtained for Run K-5, run the same
day and under the same conditions as K-4, were used for K-4 also.
C. Opacity
Opacity observations of the stack plumes were made by two observers
in accordance with the August 1971 Federal Register. Due to the length of
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the mass particulate tests, the observers were allowed to take periodic
breaks, as long as there was an overlapping period where both were observing
between breaks.
The plan was to begin opacity observations prior to the start of
the mass particulate run and continue them past its completion. However,
due to a gradual and continuing deterioration in radio communications between
stack and ground, it cannot be stated with assurance that the plan was car-
ried out for all tests. The total period of opacity observations was in-
creased, particularly for the recovery furnace, in an attempt to more closely
adhere to the plan.
The observers chose their own observation locations and timed the
readings using Kodak timers (Model 8239) synchronized at the start of each
test. Four readings per minute were taken. Problems were encountered with
intermingling plumes and saturated water vapor plumes on the lime kiln stack
and with intervening steam on the recovery furnace stack. Each observer
made his own determination as to when readings were observable.
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APPENDIX A
RESULTS OF ANALYSIS - PRINTOUT OF COMPUTER CALCULATIONS
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