74-KPM-12
(REPORT NUMBER)
AIR POLLUTION EMISSION TEST
BRUNSWICK PULP AND PAPER
(PLANT NAME)
COMPANY
BRUNSWICK, GEORGIA
(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
-------
EPA REPORT NUMBER 74-KPM-12
BRUNSWICK PULP AND PAPER COMPANY
BRUNSWICK, GEORGIA
FINAL REPORT
Submitted to
Environmental Protection Agency
Office of Air Programs
Contract No. 68-02-0225
Task No. 24
Submitted by
Engineering-Science, Inc.
7903 Westpark Drive
McLean, Virginia 22101
December 1974
-------
TABLE OF CONTENTS
Section Title Page
I INTRODUCTION l
II SUMMARY AND DISCUSSION OF RESULTS 2
III PROCESS DESCRIPTION AND OPERATION 9
A. Process Description *
B. Process Operation 10
IV SAMPLING AND ANALYTICAL PROCEDURES 16
A. Location of Sampling Points 16
B. Sampling Procedures *7
C. Analytical Procedures 17
(Appendices omitted from this copy.)
-------
LIST OF TABLES
Table Title Page
II-l Particulate Emission Summary 3
II-2 Particulate Emission Summary (Metric System) 4
II-3 System Performance 6
H-4 System Performance (Metric System) 7
III-l Summary of Calculations of Equivalent Pulp
Production Rate 15
LIST OF FIGURES
Number Title Page
III-l The Kraft Pulping Process 10
III-2 No. 5 Recovery Furnace and Electrostatic Precipitator 12
IV-1 General Layout, Brunswick Unit #5 Precipitators 17
IV-2 Stack Dimensions, Brunswick Pulp & Paper Company 18
IV-3 Cross Section Outlet Stack (One of Two) 19
ii
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I INTRODUCTION
Under Section 111 of the Clean Air Act of 1970, as amended, the Environ-
mental Protection Agency (EPA) is charged with the establishment of perfor-
mance standards for new stationary sources which may contribute significantly
to air pollution. A performance standard is based on the best emission systems
which have been shown to be technically and economically feasible. In order
to set realistic performance standards, accurate data on pollutant emissions
are normally gathered from the stationary source category under consideration.
The No. 5 black liquor recovery furnace at the Brunswick Pulp and Paper
Company in Brunswick, Georgia, was designated as a well-controlled stationary
source in the Kraft pulp industry and was thereby selected by the Office of
Air Quality Planning and Standards for an emission testing program. Tests
were conducted by Engineering-Science, Inc. personnel during January 22-25, 1974.
This facility processes about 1,500 tons of bleached Kraft pulp per day.
The No. 5 recovery furnace burns approximately 136,750 pounds/hour of black
liquor solids. Air pollution abatement equipment for this furnace consists
of an electrostatic precipitator with two parallel chambers.
A total of six particulate samples from each of the two chambers of the
electrostatic precipitator were collected. These samples were taken down-
stream of the respective chamber to determine filterable and total particu-
/
late emissions. As this process operated continuously with no known periods
of peak emissions, testing was conducted during normal operating conditions.
Opacity observations of the two outlet ducts were conducted during the
particulate testing by personnel from Environmental Science and Engineering,
Inc., Gainsville, Florida. This work was performed under a different contract
and was reported separately.
The test team and the EPA are greatly indebted to Mr. Andy Ryfun of Bruns-
wick Pulp and Paper Company for his cooperation in this sampling program.
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II SUMMARY AND DISCUSSION OF RESULTS
The purpose of this test was to establish emission levels from a well-con-
trolled black liquor recovery furnace. The twelve particulate runs conducted
provide a strong and consistent data base for the determination of emissions
from this unit.
Exhaust gases from the No. 5 recovery furnace are controlled by an electro-
static precipitator with two parallel chambers. The outlet of the north
chamber is designated the "A" stack while the "B" stack is the outlet of the
south chamber. Individual tests are specified by a letter and number corres-
ponding to the stack and test run number.
A summary of the individual test results is given in Tables II-l and II-2.
Each stack individually shows little variation but the south chamber (B stack)
emissions are about 3 times heavier than those of the north chamber (A stack).
An average of the particulate concentrations established by the sample train
3
front-half catches for the A stack is 0.013 gr/scf (29.0 mg/Nm ) while for
3
the B stack is 0.054 gr/scf (124.1 mg/Nm ). An average of concentrations
3
determined by total train catches yields values of 0.023 gr/scf (53.2 mg/Nm )
3
for A and 0.064 gr/scf (146.4 mg/Nm ) for B. Using these averages shows that
the front-half catch accounts for approximately 56% of A stack and 84% of
B stack total emissions. The data also reveals that the sample train back-half
catches are about the same for all the test runs in both the A and B stacks.
The average exhaust flow rates for the stacks were 94,930 scfm for A and
108,370 scfm for B. The maintenance histories for the two chambers are not the
same and could account for some of the differences. Approximately one month
prior to the testing, the north chamber was down for its periodic maintenance
and repair. The south chamber maintenance shutdown was about 3 months before
the testing.
-------
TABLE II-l
PARTI CULATE EMISSION SUMMARY
Run code
Test A-l
Test R-l
Test A-2
Test B-2
w Test A-3
Test B-3
Tost A-t*
Test B-l*
Test A-5
Test B-5
Test A-6
Test B-6
stop
sru's:2.7
i
Dry gas
vol ume
(scf)
17.05
111.10
85.77
97.31
?<5.06
100.50
01. OR
loi.oi
88.99
98.81
91.95
102.07
Mo! sture
(%>
27.17
27.87
30.71*
27.75
28.1*8
29.1*6
29.67
29. nit
29.61*
29.67
28.76
29.09
Orsat
C02
12.6
11*. 9
11*. 7
11*. 7
lit. 1
ll.i*
13.U
13.2
1U. 0
11*. 0
13.1
13.2
analysis
(S)
02 CO
6.8 .1
I*. 7 0.
1*.7 .1
«* . 7 .1
5.«* 0.
8.5 0.
6.n 0.
6.1 0.
5.2 .2
5.2 .2
6.6 .2
6.2 0.
Exhaust
flow rate
(scfm)
99113.
112163.
02668.
106305.
91296.
107637.
95835.
107018.
93029.
108315.
07637.
108768.
Stack
temp.
(F)
i*0i*. 9
it i»8. 5
1*1*5.0
«*02.5
1*32.5
1*01.1
1*31*. 0
1*0?. 0
1*30.1*
3"9.9
1*33.8
393.0
IsokJn-
etlc
(%>
105.6
106.9
101*. 5
18.7
101.7
10.0.7
102.5
101.8
103.2
98.1*
101.6
101.2
Part. cone.
Ur/scf)
front total
.011
.058
.018
.055
.013
.052
.010
.057
.010
.051
.Oil*
.052
.017
.067
.030
.063
.027
.062
.020
.061*
.021
.061
.025
.065
Emission rate
(Ib/hr)
front total
9.1*1
56.03
11*. 36
50.1*6
9.91
1*8.38
8.22
51.90
8.1«*
U7.03
11.80
1*8.59
11*. 02
6U.70
23.51
57.51
20.95
57.53
16.1*0
59.02
17.07
56.81*
21.01
61.00
-------
TABLE II-2
PARTICULATE EMISSION
(Metric System)
SUMMARY
Run code
Test A-l
Test R-\
Test A-2
Test B-2
Test A-3
Test 3-3
Test A-!*
Tost B-i*
Test A-5
Test B-5
Test A-5
Test B-6
Dry gas
vol ume
(Nm3)
2.75
3.15
2.51*
2.76
2.i»l*
2.85
2.58
2. 86
2.52
2.80
2.60
2.89
Mo! sture
U)
27.17
27.87
50.71*
27.75
28.1*8
29.1*6
29.67
29.01*
29.6it
29.67
28.76
29.09
Orsat
C02
12.6
11*. 9
1U. 7
U. 7
It*. 1
11. I*
13.1*
13.2
11*. 0
11*. 0
13.1
13.2
analysis Exhaust
(%) flow rate
02 CO (Nm3/m)
6.8 .1
i*.7 0.
i*.7 .1
it. 7 .1
5.1* 0.
8.5 0.
6.0 0.
6.1 0.
5.2 .2
5.2 .2
6.6 .2
6.2 0.
2806.
3176.
2621*.
3010.
2585.
301*8.
2711*.
3030.
2631*.
3067.
2765.
3080.
Stack
temp.
(C)
207.2
231.'*
229.5
205.3
222.5
205.1
223.3
208.9
221.3
201*. I*
223.2
200.6
Isokin- Part. cone.
etlc (mg/N'm3)
(%) front total
105.6
106.9
101*. 5
98.7
101.7
100.7
102.5
101.8
103.2
98.1*
101.6
101.2
25.31*5
133.376
U1.375
126.751*
28.993
120.030
22.906
129.502
23.365
115.91*3
32.272
119.289
37.763
151*. 025
68.029
11*1*. 1(63
61.261
11*2.718
1*5. G97
11*7.260
1*8.987
l'*0.123
57.1*53
11*9.71*2
Emission rate
(kg/hr)
front total
i*.27
25.1*1
6.51
22.89
i*.50
21.95
3.73
23.51*
3.59
21.33
5.35
22.01*
5.36
29.35
10.71
26.09
5.50
26.10
7.1*1*
26.77
7.7U
25. 7S
9.53
27.67
-------
Tables II-3 and II-4 provide a tabulation of system performance for the
No. 5 recovery furnace. The total furnace emission rates were obtained by
adding the emission rates from the individual chambers. Based on the front-
half catch, the average total furnace emission rate was 60.7 Ibs/hr (27.5
Kg/hr). The corresponding average total furnace emission rate, based on
total catch, was 78.3 Ibs/hr (35.5 Kg/hr). A weighted average concentration
was selected as an appropriate characterization of the particulate loading
of the effluent gas stream of the total system. The weighted average concen-
tration is defined by the following equation:
(gr/scf x SCFM) + (gr/scf x SCFM)_
Weighted Avg. Cone, (gr/scf) (SCFM) + (SCFM) ' ^ (II
A B
The mean value of the weighted average concentration for the six experimental
3
runs was 0.035 gr/scf (79.7 mg/Nm ), based on the front-half catch, and 0.045
o
gr/scf (103 mg/Nm ), based on the total catch.
Process emission rates (i.e., particulate emission rate/production rate)
were computed for each of the individual chambers and for the total system.
Based on the furnace production rates expressed in equivalent tons of
unbleached air dried pulp per hour, and on the particulate emission rates for
the total system, the following average process emission rates were determined
for the No. 5 recovery furnace:
3
Front-half catch =1.33 Ib/ton = 0.667 Kg/10 Kg
3
Total catch =1.72 Ib/ton = 0.860 Kg/10 Kg
Some minor equipment problems were encountered during the test program
that resulted in short time delays but had no adverse effect on test results.
During test run A-l, the heater element in the filter holding section of the
sample box malfunctioned and,resulted in the formation of condensate in the
cyclone prior to the filter. A total of 43 ml of condensate was collected
-------
TABLE II-3
PARTICULATE EMISSIONS SUMMARY
(English Units)
Production Rate, (tons/hr,
unbleached air-dried
pulp basis)
Front-Half Particulate :
Weighted Average Concen-
tration, (gr/dscf)
Total Furnace Emission
Rate, (Ib/hr)
Process Emission Rates:
Chamber A, (Ib/ton)
Chamber B, (Ib/ton)
Total System, (Ib/ton)
Total Particulate:
Weighted Average Concen-
tration, (gr/dscf)
Total Furnace Emission
Rate, (Ib/hr)
Process Emission Rates:
Chamber A, (Ib/ton)
Chamber B, (Ib/ton)
Total System, (Ib/ton)
1
45.8
0.036
65.4
0.21
1.22
1.43
0.044
78.7
0.31
1.41
1.72
2
45.7
0.038
64.8
0.31
1.10
1.41
0.048
81.1
0.52
1.26
1.78
Run Number
3 4
44.9
0.034
58.3
0.22
1.08
1.30
0.046
78.5
0.47
1.28
1.75
45.8
0.035
60.1
0.18
1.13
1.31
0.043
75.4
0.36
1.29
1.65
5
45.4
0.032
55.2
0.18
1.04
1.22
0.042
73.9
0.38
1.25
1.63
6
45.3
0.034
60.4
0.26
1.07
1.33
0.046
82.0
0.46
1.35
1.81
Avg.
45.5
0.035
60.7
0.23
1.11
1.33
0.045
78.3
0.42
1.31
1.72
-------
TABLE II-4
PARTICULATE EMISSIONS SUMMARY
(Metric Units)
3
Production Rate, (10 Kg/hr,
unbleached air-dried pulp
basis)
Front-Half Particulate:
Weighted Average Concen-
tration, (mg/Nm3)
Total Furnace Emission
Rate, (Kg/hr)
Process Emission Rates:
Chamber A, (Kg/103Kg)
Chamber B, (Kg/103Kgl
Total System, (Kg/103Kg)
Total Particulate:
Weighted Average Concen-
tration, (mg/Nm3)
Total Furnace Emission
Rate, (Kg/hr)
Process Emission Rates:
Chamber A, (Kg/10^Kg)
Chamber B, (Kg/103Kg)
Total System, (Kg/103Kg)
1
41.6
82.7
29.7
0.103
0.612
0.715
99.5
35.7
0.153
0.706
0.859
2
41.5
87.0
29.4
0.157
0.552
0.709
109
36.8
0.258
0.629
0.887
3
40.7
78.3
26.4
0.110
0.539
0.649
105
35.6
0.233
0.641
0.874
4
41.5
79.1
27.3
0.090
0.567
0.657
99.3
34.2
0.179
0.644
0.823
5
41.2
73.2
25.0
0.090
0.518
0.608
98.0
33.5
0.188
0.626
0.814
6
41.1
78.1
27.4
0.130
0.536
0.666
106
37.2
0.232
0.673
0.905
Avg.
41.3
79.7
27.5
0.113
0.554
0.667
103
35.5
0.207
0.653
0.860
-------
in the cyclone and this measured volume was included in the moisture deter-
mination. This liquid catch was added to the front-half wash for particulate
analysis. During this same test, it was noticed that arcing had occurred
between the stack port and the probe nozzle, resulting in a small section of
the knife edge being burned away. The nozzle was replaced for subsequent
tests and both probes were grounded to the stacks to prevent reoccurrence.
Temperatures on stack B were mostly taken with a long stem thermometer
generally positioned in one place. An inoperable pyrometer prevented
obtaining the temperature readings at the traverse points as is normally
done.
An integrated bag sample of exhaust gas was taken during each test at
both stacks for Orsat analysis. During the twelve test runs, two of the
sample results were not obtainable. A pump malfunctioned during test
run B-2 and no gas sample was obtained. The pump was repaired before the
next test proceeded. The bag sample obtained during test run B-5 was
voided because analysis showed that the sample was contaminated with ambient
air. Exhaust gases in both stacks originated in the same boiler thus
constituent concentrations should be the same for each test run. Because
of this, the data obtained from A-2 and A-5 were used for calculations
purposes for the missing B-2 and B-5.
-------
Ill PROCESS DESCRIPTION AND OPERATION
The Brunswick Pulp and Paper mill at Brunswick, Georgia, produces 1500
tons of bleached kraft pulp per day. The pulp is made into various paper and
board products.
The EPA test program at this mill consisted of six particulate tests on
both stacks of the No. 5 recovery furnace precipitator.
A. Process Description
1. General
Kraft pulp is produced from wood as shown in Figure III-l. In the process,
wood is chipped into small pieces, then cooked in 18 batch digesters at ele-
vated temperature and pressure. The cooking chemicals, called white liquor,
are sodium hydroxide and sodium sulfide in water solution. The white liquor
chemically dissolves lignin from the wood; the remaining cellulose (pulp) is
filtered from the spent liquor and washed. The pulp is then made into the
various paper products.
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 evaporators to
about 65 percent solids, and then fired in a recovery furnace.
Combustion of the organics in the black liquor provides most of the 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, con-
sisting of sodium carbonate and sodium sulfide, is dissolved in water and
transferred to a causticizing tank. Lime added to this tank converts sodium
carbonate to sodium hydroxide, completing the regeneration of white liquor,
which is then recycled to the digesters. The calcium carbonate mud, that pre-
cipitates from the causticizing tank, is recycled to a kiln to regenerate lime.
-------
FIGURE III-1
THE KRAFT PULPING PROCESS
Wood -
White Liquor
(NaOH + Na2S)
DIGESTER
SYSTEM
Pulp *
u
PULP
WASHERS
eak Black Lioun
Pulp
Water
RECOVERY
FURNACE
SYSTEM
Heavy
Black
Liquor
(Na2C03
•Water
o
CJ
Of.
Smelt
3
t
Air
I
Na2S)
MULTIPLE
EFFECT
EVAPORATOR
SYSTEM
SMELT
DISSOLVING
TANK
I
Green Liquor
t
White Liquor
(recycle to
digester)
CAUSTICIZING
TANK
.Lime
Calcium
Carbonate
Mud
10
ENGINEERING-SCIENCE, INC
-------
2. Recovery Furnace
The No. 5 recovery furnace was designed by the Babcock and Wilcox Company
to burn 338 gallons of black liquor per minute at a solids content of 64 per-
cent; this corresponds to a pulp production rate of 1100 air dried tons per
day. This direct fired (no direct contact evaporator) recovery furnace was
installed in 1972. Soot is continuously blown from the boiler tubes with
steam. Each soot blowing cycle takes about two hours and ten minutes.
3. Electrostatic Precipitator
Exhaust gases from the No. 5 recovery furnace are cleaned in an electro-
static precipitator. The precipitator was designed for a collection efficiency
of 99.8 percent and installed in 1972 by the Koppers Company. The unit was
designed to treat 415°F combustion gases at a rate of 393,000 ACFM. As shown
in Figure III-2, the precipitator has two separate chambers in parallel; each
chamber has five electrical fields. The precipitator is situated on the roof
of the recovery building. The gases from each chamber exhaust through a
separate stack.
Dust collecting on the precipitator electrodes is shaken loose by a sys-
tem of rappers. The rappers operate in a continuous cycle, with each cycle
lasting about 1 1/2 minutes. The dust falls to the bottom of the precipitator
where it is removed by drag conveyors to a mix tank. In the tank, the dust is
dissolved in the black liquor and recycled to the process.
B. Process Operation
1. Recovery Furnace and Electrostatic Precipitator
The purpose of the tests was to measure particulate emission levels during
normal furnace operation. The information was to help demonstrate actual con-
trol levels for recovery furnace operations.
11
-------
NO, 5 RECOVERY FURNACE AND ELECTROSTATIC PRECIPITATOR
10
AIR
tn
ESP
N Chamber
A
ESP
S Chamber
B
t
— SAMPLE
LOCATION
1
—SAMPLE
LOCATION
ŁT>
73
\
ro
-------
During the particulate tests, significant furnace and precipitator para-
meters were monitored. Readings were made every half hour and recorded on the
process data sheets contained in Appendix C.
As far as known from the process data and conversations with the operators,
the equipment operated normally during the tests. The black liquor charge rate
was 345 gallons per minute during each test. The percentage of solids in the
black liquor ranged between 59.8 and 61.8 percent. No auxiliary fuel was
fired during the tests.
2. Equivalent Pulp Production Rate
The operation of the recovery furnace is quantitatively related to the
pulp production rate in the digesters. As a result, pollutant emission rate
can be expressed on the basis of equivalent pulp production, as shown below:
(Emission Rate\ _ /Emission Rate\ / /Equivalent Pulp\
(lb/ton pulp)] ( (Ib/hr) I / (Production Rate) . Eq. (III-l)
/ \ // V (tons/hr) /
To use Equation III-l, the equivalent pulp production was calculated from
the black liquor charged during the tests, as shown below:
/Equivalent Pulp\ /Black Liquor\/ \ //Solids to Pulp\
I Production 1= I Charge )(% Solids)/1 Ratio ). Eq. (III-2)
\ (tons) / \ (Ibs) /\ 100 // \ (Ibs/ton) /
The solids-to-pulp ratio used in Equation III-2 was 3000 pounds of black
liquor per ton of unbleached air-dried pulp. This is based on the assumption
(used by the recovery furnace's manufacturer) that 3000 pounds of solids re-
sult for each ton of unbleached pulp produced.
Equation III-2 was used to calculate the equivalent pulp production during
each test on the recovery furnace. Dividing by the time elapsed while
charging the black liquor, gave the equivalent unbleached pulp production rate.
13
-------
The calculations are summarized in Table III-l. As shown, the average rate
was found to be 45.5 tons per hour. Substituting into Equation III-l gives the
following equation, which was used to calculate mass emission rates:
/Emission Rate
\ (Ib/ton)
>\ = /Emission Rate\ / / 45.5 \ > .
/ I (Ib/hr) j / (fcon/hr)) ' Eq.(III-3)
14
-------
TABLE III-l
SUMMARY OF CALCULATIONS OF EQUIVALENT PULP PRODUCTION RATE
Black
Hours (1)
Date T
Jan.
Jan,
Jan.
Jan.
Jan.
Jan.
1974
22
23
23
24
24
25
Start
1401
0935
1551
0909
1526
0804
Finish
1932
1337
1920
1311
1913
1134
Liquor Readings
Integrator (2)
Start
515,387,000
519,327,000
520,739,000
524,337,000
525,753,000
529,167,000
Finish
516,632,000
520,237,000
521,521,000
525,248,000
526,602,000
529,959,000
Avg. %
Solids
60.7
60.3
60.3
60.5
60.9
60.0
Black
Liquor
Charged
(Ibs)
1,245,000
910,000
782,000
911,000
849,000
792,000
Equivalent
Pulp Elapsed
Production (3) Time
(tons) (hrs)
251.9
182.9
157.2
183.1
172.4
158.4
5.5
4.0
3.5
4.0
3.8
3.5
Equivalent
Pulp
Production
Rate (4)
(tons/hr)
45.
45.
44.
45.
45.
45.
45.
8
7
9
8
4
3
5 (Avg.)
(1) Item 12 on the process data sheets.
(2) Item 11 on the process data sheets.
(3) Calculated from Equation 2.
(4) Calculated by dividing Equivalent Pulp Production by Elapsed Time.
-------
IV SAMPLING AND ANALYTICAL PROCEDURES
A. Location of Sampling Points
The two pricipltator outlet stacks are identical as far as dimensions and
port locations are concerned. They are rectangular and protrude from the
building roof about 10 feet with a cross section of 270" x 72". Each has six
4" pipe ports evenly spaced along the long dimension. From the centerline of
the sampling ports it is 7'-0" down stream to the stack outlet and an
estimated minimum distance of 7'-0" up stream to a flow disturbance in the
precipitators. The stacks have an equivalent diameter of about 113" thus
flow disturbances are less than one diameter from the sample points in both
directions. Because of the sampling location it was decided that nine sampling
points would be utilized along each traverse. This resulted in an elemental
sampling area of 8" x 45" which is not ideal but the best that could be done
with the given conditions. The north chamber stack is called the A stack
and the south chamber stack the B stack. Looking at the test side
of the stacks, the ports are labled 1 thru 6 reading from left to right on
both units. The sampling points for each port are numbered 1 through 9 with
point 1 located closest to the port and point 9 located nearest the far wall.
t
Thus, a specific point could be called A-2-3, which would be the #3 point
in the #2 port in the A stack. No sample point was closer than 4" to the
stack wall. Each stack had six traverses with nine test points for a total
of 54 sampling points. Figures IV-1, IV-2, and IV-3 fully describe the stacks,
port arrangements, and sample point locations.
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FIGURE IV-1
GENERAL LAYOUT
BRUNSWICK UNIT #5 PRECIPITATORS
Stack Test Ports
~"*-o o o
Gas i
jDistributing I
i Plates—*l
Electrostatic
jPrecipitator
Elevator
Stops
Here
To N. To S.
Chamber Chamber
From
Recovery
Boiler
17
ENGINEERING-SCIENCE, INC
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STACK DIMENSIONS
BRUNSWICK PULP & PAPER COMPANY
oo
Z
O
m
m
o
V
-
1
rh
270"
V///////.
Some vertical electrical conduits and
pneumatic lines, 2-3' from stack
A Stack-
r*.
i
I
B Stack "3/16" Steel
\o
co
9,
North Chamber
/ /////ft'///////////^7,
t- Roof Line LFlange
South Chamber
11"
Z
9
CO
o
m
Z
O
m
CD
C
73
Z
O
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FIGURE IV-3
CROSS SECTION OUTLET'STACK
(ONE OF TWO)
CM
CM
CM X-
tn
Port
#(1
E
D E
D E
D E
Traverse Points
234 56789
I I I I I I I I
I I I I I I I I I
o
r»
CM
72"
19
ENGINEERING-SCIENCE, INC.
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B. Sampling Procedures
The sample train box and eight-foot probe assembly, used for the testing,
was suspended from a monorail fixture which stands on four 7' long plastic
pipe legs. The trolley, which supports the weight of the test equipment, rolls
along the rail and allows for a simple means of traversing the stack. This
portable set-up was convenient for accommodating the six ports on each stack
because it was not necessary to disassemble the test equipment when moving the
support rig to the next port. Two monorail assemblies were utilized so that
the two stack could be tested simultaneously. Some difficulty was encountered
when moving the supports because some vertical electrical conduits were located
in the area. The varying port heights, due to the sloping roof, were handled
by changing the hanger length to the sample box.
A standard EPA sampling train with a cyclone separator was used during
all the testing. The cyclone was installed up stream of the filter holder
inside the heated box. A manometer with an expanded lower scale was used
instead of the standard unit in the RAC meter box. The 0-0.25 in WG manometer
was necessary because of the low gas velocities encountered in the stacks.
The sampling was conducted as specified by EPA Methods 1 through 5 with
the additional requirement that the impinger contents were collected and
analyzed for particulate content. These methods were published in the Federal
Register. Volume 36, No. 247, Part II, Thursday, December 23, 1971. The
procedure for recovery and analysis of the impinger contents are published in
the Federal Register, Volume 36, No. 159, Part II, Tuesday, August 17, 1971.
C. Analytical Procedures^
The clean-up area was located in an unused control room on the third
floor of the recovery boiler building. All sample train preparation and clean-up
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was performed in this clean, well-lighted area. The trains were capped and
sealed during all movement to and from the test site on the roof. The probes
were capped before and after testing and cleaned in a small well-lighted
enclosed area on the eleventh floor level. This eliminated the time and
handling necessary to move them in the small elevator to the third floor
area. All the integrated gas samples taken during the particulate sampling
were run through the Orsat analysis the same day they were collected, soon
after the test run was completed.
All samples obtained during testing at the Brunswick Pulp and Paper
Company were sealed in lead-free Wheaton glass bottles. The bottles, which
were not previously used, were acid washed in preparation for the testing.
All the sample containers were sent back to the laboratory for final analysis.
An outline of the analytical procedures followed by the laboratory is included
in Appendix E.
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