xe/EPA
United States
Environmental Protection
Agency
Office of Air Quality
Planning and Standards
Research Triangle Park NC 27711
rEMB"Report 80-DRY-10
October 1980
Air
Petroleum Dry Cleaners
Refrigerated System/
Condenser
Emission Test Report
Polly Prim Cleaners
Lakeland, Florida
-------
SOLVENT RECOVERY AND EMISSION CONTROL
PETROLEUM DRY CLEANING INDUSTRY
POLLY PRIM CLEANERS
Lakeland, Florida
Prepared for the
U.S. Environmental Protection Agency
Emission Measurement Branch
Research Triangle Park, N.C. 27711
Prepared by
Clayton Environmental Consultants, Inc.
25711 Southfield Road
Southfield, Michigan 48075
EMB REPORT NO. 80-DRY-10
Work Assignment 37
Contract No. 68-02-2817
-------
TABLE OF CONTENTS
List of Tables i
List of Figures ii
1.0 Introduction 1
2.0 Presentation of Results 3
3.0 Process Description 14
4.0 Location of Sampling Points 15
5.0 Sampling and Analytical Procedures 18
APPENDICES
A. FID Strip Chart Data and Field
Data Sheets
B. Strip Chart Data for Response
Factor Determinations
C. Velocity Traverse Data
-------
LIST OF TABLES
Table Page
2.1 Stoddard Concentrations 4
-------
LIST OF FIGURES
Figure Page
4.1 Process diagram and sampling 16
locations
5.1 Stack cross-section-dryer exhaust 19
duct
5.2 Moisture sampling train 20
5.3 FID system 22
5.4 Calibration system 24
11
-------
1.0 INTRODUCTION
The U.S. Environmental Protection Agency (EPA)
retained Clayton Environmental Consultants, Inc. to deter-
mine the stoddard solvent emission levels from, and recov-
ery performance of, a Hoyt Recovery Tumbler Dryer at the
Polly Prim Dry Cleaners, Inc. plant in Lakeland, Florida.
The results of this study will be used in research
and development efforts for supporting New Source Per-
formance Standards for the petroleum dry cleaning indus-
try. This study was commissioned as Project No.
80-DRY-10, Contract No. 68-02-2817, Work Assignment 37.
The testing program included determination of the
following:
(1) Total hydrocarbon concentrations (as stoddard)
at the condenser inlet and the dryer exhaust
duct during reclaim and deoddrize portions of
each cycle;
(2) Temperatures from the condenser inlet and outlet
for both cooling water and exhaust gas;
(3) Condenser water flowrate;
(4) Volumetric flowrates at the dryer exhaust duct;
and,
(5) Moisture content at the dryer exhaust duct.
- 1 -
-------
The following process conditions were varied and
controlled to quantify the throughput of solvent and the
material mass balance within the system: condenser water
flowrate and temperature, load size, and cycle duration.
These conditions were recorded and will be correlated by
TRW, Inc. to determine (1) the cost effectiveness of VOC
removal for recovery dryers utilizing a refrigeration
system to cool condenser water under high ambient tempera-
tures and humidity, and, (2) to develop and substantiate
operating limitations to ensure safe levels of stoddard
solvent (defined as a percent of LEL) within the system,
while maintaining minimal VOC stack emissions.
Field sampling began July 21, 1980 and was completed
August 7, 1980. The study was conducted by Messrs. N.
Steve Walsh, Bruce G. Bird and Timothy J. Palmer of Clay-
ton Environmental Consultants, Inc. Additional technical
assistance was provided by Messrs. John R. Jernigan, and
Steve Plaisance of TRW, who collected process data.
- 2 -
-------
2.0 PRESENTATION OF RESULTS
Table 2.1 presents all pertinent data needed to
determine the thermal conductivity of the condenser and
heat transfer capacity from the gas stream to the con-
denser water stream, including condenser water flowrate
and the temperature differential (AT) between the con-
denser water inlet and outlet. Gas flowrate and tempera-
ture differential between the condenser gas inlet and
outlet were also determined. Elapsed time of the reclaim
period and the type and quantity of metal used in the
condenser coils, with the applicable heat conductivity
constant, are not discussed.
Condenser gas flowrates were not measured during the
test program. Only condenser gas temperature differences
between the inlet and outlet gas can be discussed. Con-
denser gas (AT) data were not obtainable on 7/22/80 and
7/23/80 because the thermocouple had not been installed at
the condenser gas outlet location.
All temperature values reported in Table 2.1 are
averages of individual readings recorded during both the
reclaim and exhaust periods of each cycle. Stoddard
concentrations were determined by averaging 30-second
interval readings over the entire 6-minute exhaust
period. This average value was then used to calculate the
total mass of solvent (in pounds of stoddard per exhaust
period).
- 3 -
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TABLE 2.1. STODDARD CONCENTRATIONS
Date: 7-22-80
Start
Time
Batch
Number
Point in
Cycle
Condenser
Water Temp. (F)
Inlet
Outlet
Gas Temp. (F)
Inlet
Outlet
Solvent Concentration (in ppm stoddard)
Reclaim
Maximum a Finish b
Exhaust
Start0 Finishd
Condenser
Water
Flow
(gal/min)
Exhaust
Flowrate
(scfm)
Emission Rates
Total Ib
of stoddard
per period
Ib/hr of
stoddard
0911
0932
0944
1006
1019
1040
1054
1115
1127
1148
1231
1252
3
3
4
4
5
5
6
6
7
7
8
8
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
66
66
65
-
66
-
64
-
72
"•
78
78
78
-
78
-
75
-
84
~
113
108
109
-
107
-
108
-
110
~
154
155
155
152
_
153
155
4724
4882
4882
5039
4882
5039
f
f
f
f
f
f
3400
3496
4096
3936
3432
3624
2204
2348
3228
3104
2392
2080
7.59
8.92
8.34
9.44
9.42
10.5
306
306
306
306
306
306
1.94
2.01
2.60
2.60
2.01
1.89
19.4
20.1
26.0
26.0
20.1
18.9
a,
'Maximum solvent concentration
Solvent concentration at end of reclaim period
Q
Solvent concentration in exhaust stream at start of exhaust period
d
Solvent concentration in exhaust s.tream at end of exhaust period
Total mass of solvent emitted during exhaust period (in pounds stoddard and Ib/hr of stoddard)
FID response during end of reclaim was not recorded to allow sufficient purging of the dryer exhaust duct sample line.
-------
TABLE 2.1. STODDARD CONCENTRATIONS (CONTINUED)
Date: 7-23-80
Start
Time
Batch
Number
Point in
Cycle
Condenser
Water Temp. (F)
Inlet
Outlet
Gas Temp. (F)
Inlet
Outlet
Solvent Concentration (in ppm stoddard)
Reclaim
Maximum » Finish b
Exhaust
Start c Finish d
Condenser
Water
Flow
(gal/min)
Exhaust
Flowrate
(scfm)
Emission Rates
Total Ib
of stoddard
per period
Ib/hr of
stoddard
0804
0831
0843
0910
0921
0948
1003
1025
1039
1100
1115
1136
1147
1158
3
3
4
4
5
5
6
6
7
7
8
8
9
9
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
65
66
66
66
66
65
64
78
79
79
79
78
78
78
160
162
161
165
158
158
152
159
156
160
158
155
153
141
4410
4410
5512
5197
5984
5039
5039
f
4400
f
5160
f
f
f
3528
4032
3196
5197
3544
3464
3888
1952
2016
2520
2676
2268
2000
2600
8.07
8.63
7.87
7.82
8.71
7.77
9.12
312
312
312
312
312
312
312
1.91
2.34
2.37
1.34
1.99
1.97
2.28
19.1
23.4
23.7
13.4
19.9
19.7
22.8
Maximum solvent concentration
Solvent concentration at end of reclaim period
Solvent concentration in exhaust stream at start of exhaust period
a
Solvent concentration in exhaust stream at end of exhaust period
Total mass of solvent emitted during exhaust period (in pounds stoddard and Ib/hr of stoddard)
FID response during end of reclaim was not recorded to allow sufficient purging of the dryer exhaust duct sample line.
-------
TABLE 2.1. STODDARD CONCENTRATIONS (CONTINUED)
Date: 7-25-80
Start
Time
Batch
Number
Point in
Cycle
Condenser
Water Temp. (F)
Inlet
Outlet
Gas Temp. (F)
Inlet
Outlet
Solvent Concentration (in ppm stoddard)
Reclaim
Maximum a Finish b
Exhaust
Start0 Finish d
Condenser
Water
Flow
(gal/min)
Exhaust
Flowrate
(scfm)
Emission Rates
Total Ib
of stoddard
per period
Ib/hr of
stoddard
0803
0945
0959
Reclaim
Exhaust
Reclaim
62
60
73
77
154
142
84
122
85
FID NOT OPERATING
8.05
4.87
FID NOT OPERATING
Maximum solvent concentration
Solvent concentration at end of reclaim period
Solvent concentration in exhaust stream at start of exhaust period
jj
Solvent concentration in exhaust stream at end of exhaust period
Total mass of solvent emitted during exhaust period (in pounds stoddard ativi Ib/hr of stoddard)
-------
Date: 7-28-80
TABLE 2.1. STODDARD CONCENTRATIONS (CONTINUED)
Start
Time
0810
0836
0904
0931
0941
1007
1045
1056
1123
1134
1204
1214
1244
1253
1324
Batch
Number
2
2
3
3
4
4
5
6
6
7
7
8
8
9
9
Point in
Cycle
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Water Temp. (F)
Inlet
65
64
64
61
65
66
64
Outlet
81
80
81
81
81
81
81
Gas Temp. (F) Reclaim Exhaust A™ Flowrate ?Ot*\^b , Ib/hr of
Inlet
150
140
144
142
145
147
144
Outlet Maximum a Finish b Start0 Finish3 (gal/min) per period stoddard
90 5.24
-
89 5.87
131
90 4.47
129
130 FID NOT OPERATING FID NOT OPERATING
V "*** *-"• ~ii~ *l~ _
122
90 5.19
129
89 10.3
125
90
124
Maximum solvent concentration
Solvent concentration at end of reclaim period
CSolvent concentration in exhaust stream at start of exhaust period
Solvent concentration in exhaust stream at end of exhaust period
6Total mass of solvent emitted during exhaust period (in pounds stoddard and Ib/hr of stoddard)
-------
TABLE 2.1. STODDARD CONCENTRATIONS (CONTINUED)
Date: 8-4-80
Start
Time
Batch
Number
Point in
Cycle
Condenser
Water Temp. (F)
Inlet
Outlet
Gas Temp. (F)
Inlet
Outlet
Solvent Concentration (in ppm stoddard)
Reclaim
Maximum a Finish b
Exhaust
Start c Finish"3
Condenser
Water
Flow
(gal/min)
Exhaust
Flowrate
(scfm)
Emission Rates
Total Ib
of stoddard
per period
Ib/hr of
stoddard
1
GO
1
0829
0857
0905
0933
0941
1009
1034
1103
1113
1141
1154
1224
1240
1308
1321
1350
2
2
3
3
4
4
5
5
6
6
7
7
8
8
9
9
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
64
64
64
66
65
66
65
65
83
84
85
87
89
91
83
80
137
142
142
140
143
146
138
146
87
126
126
89
129
89
131
89
132
91
130
89
132
89
130
5810
5794
5878
5676
5911
6549
7372
6700
5571
5646
5496
4846
4653
4878
5614
4855
5048
5085
5309
4108
4076
4750
5350
3864
2954
3290
3402
3241
2856
2792
3270
2510
5.05
5.06
5.03
5.06
5.03
5.06
5.05
5.04
306
306
306
306
306
306
306
306
2.56
2.72
2.77
2.51
2.26
2.35
2.79
2.08
25.6
27.2
27.7
25.1
22.6
23.5
27.9
20.8
Maximum solvent concentration
Solvent concentration at end of reclaim period
Solvent concentration in exhaust stream at start of exhaust period
Solvent concentration in exhaust stream at end of exhaust period
Total mass of solvent emitted during exhaust period (in pounds stoddard and Ib/hr of-stoddard)
-------
TABLE 2.1. STODDARD CONCENTRATIONS (CONTINUED)
Date: 8-5-80
Start
Time
Batch
Number
Point in
Cycle
Condenser
Water Temp. (F)
Inlet
Outlet
Gas Temp. (F)
Inlet
Outlet
Solvent Concentration (in ppm stoddard)
Reclaim
Maximum a Finish b
Exhaust
Start c Finish d
Condenser
Water
'Flow
(gal/min)
Exhaust
Flowrate
(scfm)
Emission Rates
Total Ib
of stoddard
per period
Ib/hr of
stoddard
0719
0747
0812
0841
0856
0925
0941
1009
1020
1049
1058
1126
2
2
3
3
4
4
5
5
6
6
7
7
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
63
66
68
68
68
68
79
82
83
84
84
83
145
142
139
142
140
142
88
127
91
129
92
129
92
130
92
128
92
130
4413
5595
5678
5995
6328
5928
4378
4809
4941
5340
5738
5340
4278
4742
4875
5140
5538
5107
2620
2918
3217
3648
3880
3549
5.15
5.20
5.19
5.19
5.19
5.18
306
306
306
306
306
306
2.29
2.52
2.68
2.96
3.14
2.89
22.9
25.2
26.8
29.6
31.4
28.9
Maximum solvent concentration
Solvent concentration at end of reclaim period
°Solvent concentration in exhaust stream at start of exhaust period
Solvent concentration in exhaust stream at end of exhaust period
Total mass of solvent emitted during exhaust period (in pounds stoddard and Ib/hr of stoddard)
-------
TABLE 2.1. STODDARD CONCENTRATIONS (CONTINUED)
Date: 8-6-80
Start
Time
0727
0756
0815
0844
0857
0926
0939
1008
1028
1 1056
1109
o 1138
1152
1 1220
1233
1300
Batch
Number
1
1
2
2
3
3
4
4
5
5
6
6
7
7
8
8
Point in
Cycle
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Condenser
Water Temp. (F)
Inlet
64
68
70
71
70
70
72
72
Outlet
79
83
86
86
85
86
87
87
Gas Temp. (F)
Inlet
137
140
141
143
142
144
142
142
Outlet
87
128
91
129
94
127
94
128
93
131
94
129
95
129
94
130
Solvent Concentration (in ppm stoddard)
Reclaim
Maximum a Finish
7094 4330
8309 5262
8259 5096
8276 4962
8393 4896
9358 4862
9425 5162
9392 5096
Exhaust
Startc Finish d
3963 1732
5129 1798
4996 1898
4496 1765
4430 1665
4163 1565
4130 1565
4563 1465
Condenser
Water
Flow
(gal/min)
5.15
5.03
5.38
5.15
5.21
5.17
5.39
5.20
Exhaust
Flowrate
(scfm)
301
301
301
301
301
301
301
301
Emission
Total Ib
of stoddard
per period
1.59
1.97
1.93
1.72
1.61
1.47
1.38
1.43
e
Rates
lb/hr of
stoddard
15.9
19.7
19.3
17.2
16.1
14.7
13.8
14.3
Maximum solvent concentration
Solvent concentration at end of reclaim period
Solvent concentration in exhaust stream at start of exhaust period
Solvent concentration in exhaust stream at end of exhaust period
eTotal mass of solvent emitted during exhaust period (in pounds stoddard and lb/hr of stoddard)
-------
TABLE 2.1. STODDARD CONCENTRATIONS (CONTINUED)
Date: 8-7-80
Start
Time
Batch
Number
Point in
Cycle
Condenser
Water Temp. (F)
Inlet
Outlet
Gas Temp. (F)
Inlet
Outlet
Solvent Concentration (in ppm stoddard)
Reclaim
Maximum3 Finishb
Exhaust
Start0 Finishd
Condenser
Water
Flow
(gal/min)
Exhaust
Flowrate
(scfm)
Emission Rates
Total Ib
of stoddard
per period
Ib/hr of
stoddard
0706
0734
0754
0822
0834
0902
0924
0952
1009
1038
1048
1150
1
1
2
2
3
3
4
4
5
5
6
6
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
Reclaim
Exhaust
70
73
73
75
74
74
86
88
90
89
87
87
140
143
142
142
139
142
94
129
95
129
96
129
97
129
95
123
95
126
7510
7593
7976
9358
7693
8526
4862
4696
5046
5362
4463
4779
4862
4696
5046
5362
4463
4779
1499
1499
1682
1699
1365
1365
5.18
5.20
5.15
5.20
N/A
5.23
306
306
306
306
306
306
1.56
1.48
1.73
1.73
1.26
1.24
15.6
14.8
17.3
17.3
12.6
12.4
Maximum solvent concentration
Solvent concentration at end of reclaim period
CSolvent concentration in exhaust stream at start of exhaust period
Solvent concentration in exhaust stream at end of exhaust period
eTotal mass of solvent emitted during exhaust period (in pounds stoddard and Ib/hr of stoddard)
-------
Prior to each test, both the condenser water flow-
rate and temperature were set and regulated closely at
selected time intervals, using separate controls. Addi-
tionally, the volume of solvent reclaimed (ml) and wet
(solvent laden) load size for each batch, along with
clothing fabric type were recorded in conjunction with
these data by TRW, Inc. The ambient temperatures and
humidity of the air surrounding the dryer system varied
little from day to day, but increased noticably from the
early morning hours to mid-afternoon. Cost effective
operation of the solvent recovery tumbler dryer should be
determined from these settings as they affect the con-
sumption of all utilities. Consideration should be given
to achieving a safe level of stoddard solvent (percent
LEL) within this closed system during the reclaim period
of the cycle.
Condenser water inlet temperatures were regulated by
a thermostat on the refrigeration unit, calibrated for a
range of 55 to 80F. This control provided good response
at mid-range (60 to 75F), however, average temperatures at
the condenser water inlet outside this interval were not
recorded. An attempt to regulate condenser gas inlet
temperatures at 90F +5-degrees between 7/28/80 and 8/7/80
was less effective as condenser water temperatures were
increased. Condenser water flowrate was controlled at the
- 12 -
-------
condenser inlet by a manually actuated valve which pro-
duced a good response over the entire range of flowrates.
Dryer exhaust gas flowrate was held constant using a
constant speed fan which controlled the flow to 306 +6
scfm. Solvent concentrations at both the condenser inlet
and dryer exhaust duct locations appeared to vary pro-
portionally to all variables previously discussed. In
addition, the wet (solvent laden) weight and type (fabric
material) of the pre-dryer load had obvious consequences.
Experience with field measurements and obvious
trends in the response of the uncontrolled process condi-
tions to the controlled process conditions discussed
previously (Section 1.0) indicate some probable correla-
tions. Though several combinations of the data presented
in Table 2.0 could be evaluated statistically, full under-
standing of the integrity in the measurement methods
employed and the components of the dryer system and their
basic function dictate the particular conditions and
statistical technique chosen to evaluate the correlation.
To satisfy the basic objectives of the test program,
reclaim efficiency of the solvent recovery tumbler dryer
should be evaluated by taking into consideration variables
affecting cost, safety, and stack emissions.
- 13 -
-------
3.0 PROCESS DESCRIPTION
(To be provided by TRW).
- 14 -
-------
4.0 LOCATION OF SAMPLING POINTS
Figure 4.1 depicts the sampling locations with
respect to the process. Velocity traverse data sheets are
presented in Appendix C.
DRYER EXHAUST DUCT
The dryer exhaust duct was accessed through only one
1/2-inch sampling port for velocity traverses, since the
other port was inaccessible due to the lack of working
space behind the dryer. The port was located 5-feet
downstream and 2-feet upstream from the nearest disturb-
ance. This provided adequate upstream/downstream dis-
tances from disturbances and allowed the determination of
a representative velocity profile of the dryer exhaust.
Velocity pressures and temperatures were measured at
each of six sampling points. Stoddard solvent concentra-
tions, exhaust gas temperature, and moisture content were
also monitored from this same sampling port.
CONDENSER GAS INLET AND OUTLET
The condenser inlet was accessed through a single
1/2-inch port carefully positioned in the condenser bypass
damper housing. This sampling location was the best site
possible, however, it did not provide adequate upstream/
downstream distances as required by EPA Method 1 due to
internal dryer parts. Therefore, volumetric flowrates
were not measured. Only stoddard solvent concentrations
and temperatures were monitored at this location. Temper-
atures were recorded at both the condenser inlet and
outlet locations.
- 15 -
-------
Dryer
(a) Exhaust duct
(b) Condenser water inlet
(c) Condenser water outlet
(d) Condenser gas inlet
(e) Condenser gas outlet
(f) Totalizing meter
(g) Steam line to heater
(h) Reclaim to separator
Figure 4.1. Process diagram and sampling locations.
-------
CONDENSER WATER INLET AND OUTLET
The water temperature was monitored at both loca-
tions with an iron constantan (I/C) Type-J thermocouple
attached to a calibrated pyrometer and installed in the
condenser water lines. Condenser water flowrates were
measured by a positive displacement flow totalizing meter
positioned upstream of the condenser in conjunction with
the elapsed time of the reclaim portion of the cycle.
- 17 -
-------
5.0 SAMPLING AND ANALYTICAL PROCEDURES
DRYER EXHAUST DUCT
Velocity Traverse
Exhaust gas velocities were measured in accordance
with the procedures outlined in the U.S. Environmental
Protection Agency's Standards of Performance for New
Stationary Sources, 40CFR60, amended through August 17,
1977, Reference Methods 1, 2, and 4.
During a preliminary velocity traverse, the 6-inch
duct was divided into 6 equal annular areas at whose mid-
points exhaust gas velocities and temperatures were measured,
in accordance with EPA, Methods 1 and 2. Velocity pressures
were measured at each sampling point using an S-type Pitot
tube and inclined 0 to 10-inch water gauge manometer.
Temperatures were measured with an iron-constantan (I/C)
thermocouple attached to the Pitot tube and to a cali-
brated pyrometer. Exhaust gas flowrates were calculated
from the single port velocity traverse data. A diagram of
the stack cross-section is presented in Figure 5.1.
A modified moisture sampling train was run simul-
taneously with the velocity traverse. The train consisted
of preweighed portions of silica gel' in 18" x 5/8" O.D.
glass tubes connected to a calibrated limiting orifice and
dry gas meter followed by a vacuum pump (Figure 5.2).
- 18 -
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N
6-inches
I.D.
This
was
port
not
sampled
Point
1
2
3
4
5
6
Distance
(Inches)
5.7
5.1
4.2
1.8
0.9
0.3
Figure 5.1. Stack cross-section - dryer exhaust duct.
- 19 -
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o
I
Stack wall
Silica gel tube
Orifice
PVC tubing
Inclined
manometer
Thermometers
J L
PVC
PVC
o
Dry gas
meter
Vacuum
pump
Figure 5.2. Moisture sampling train.
-------
FID SYSTEM
Stoddard solvent concentrations were measured with a
Ratfisch/lPM Model RS5 and Beckman Model 400 hydrocarbon
analyzer equipped with a flame ionization detector and
recorded continuously on a strip chart recorder (Figure
(B\
5.3). Two 1/8" I.D. heated Teflon^ sample lines
(approximately 50-feet in length) were connected to sep-
arate 2-way valves and a diaphragm pump (used to purge the
lines) to minimize the FID response time when sampling
/e\
locations were switched. Heated Teflon^ sample lines
then connected these valves to another 2-way valve and
filter assembly. This assembly was then connected to a
"T" fitting with an on/off toggle valve. The purpose of
the toggle valve was to actuate the flow of calibration
gases entering the diaphragm pump following the "T" fit-
ting. In turn, the pump forced the sample gas and cal-
ibration gases into the FID at a regulated pressure and
flowrate. Temperatures were measured with a Type-J
thermocouple and recorded every 5-minutes for the duration
of a cycle. The strip chart and field data appear in
Appendix A.
CONDENSER GAS INLET AND OUTLET
Stoddard solvent concentrations at the condenser gas
inlet were measured using the FID system discussed above.
Temperatures were measured at both locations with a Type-J
thermocouple every 5-minutes for the duration of the cycle
- 21 -
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Chart
Recorder
FID
with sample
pump
From
condenser
inlet
Purge
pump
exhaust
Calibration gases
Purge pump
From dryer
exhaust duct
Figure 5.3. FID system.
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CONDENSER WATER INLET AND OUTLET
Condenser water flowrates in gallons per minute
(gpm) were determined by dividing the total volume of
water indicated on the totalizing meter by the elapsed
time of the reclaim portion of the cycle.
RESPONSE FACTOR DETERMINATIONS
The instrumental response factor determination
incorporated the following components: a compressed gas
supply of zero air «1 ppm total hydrocarbon) , monitored
and regulated by a dual stage regulator; a stainless steel
needle valve; a calibrated dry gas meter equipped with a
bimetallic thermometer at the outlet with ports before and
after the gas meter to obtain its internal gauge pressure
on a 0 to 1.0-inch inclined water manometer; a molecular
sieve; a "T" fitting containing a system for sample
injection; a Greenburg-Smith midget impinger (50-ml capac-
ity) placed in a heated oil bath; a heat traced "T" fit-
ting containing a 1/8" O.D. iron-constantan thermocouple;
a heat-traced two way-valve which allowed the gas sample
®
to pass into a Tedlar bag contained in a heated barrel;
a two way valve allowed the gas sample to pass to and from
the Tedlar^ bag inside the heated barrel; sample line
equipped with a temperature monitor; a Teflon pump
equipped with a bimetallic thermometer at the outlet; and
a Beckman Model 400 Hydrocarbon Analyzer having a flame
ionization detector (FID). Figure 5.4. displays the
instrumental response factor calibration system.
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Two-stage
regulator
Syringe
idget impinger
/T\Molesieve
j filter
Hydrocarbon
free air
cylinder
Dry gas
meter
0.40ft
/ Tedlar bag
Hot plate
to
Temperature Readout
Pressure Readout
Heated
Teflon
lines
Heated metal barrel
H.C. Analyzer
Recorder
Figure 5.4. Calibration system.
-------
Two hours were allowed for the entire system to heat
up and reach an equilibrium. It was then checked for
leaks at all branches of the 3-way valve. The system was
then purged with zero air (dilution gas) prior to each
sample injection until no measurable amount of hydrocarbon
could be detected from the system by the FID.
During this purging period, the flowrate of the zero
air through the system was set to approximately 0.1 cubic
feet per minute (cfm). This flowrate was kept constant
for all subsequent response factor calibrations by uti-
lizing the on/off valve positioned before the dry gas
meter to stop the gas flow.
Using the equations and the molecular weight of the
stoddard solvent (provided by TRW, Inc.), two approximate
volumes of stoddard sample were calculated for giving a
response of 50 and 125 ppm propane. Carrying out the
calculations, volumes of 1.2 and 2.9 microliters (yl) of
stoddard solvent would produce the instrumental response
relative to a propane concentration of 50 and 125 ppm,
respectively.
The hydrocarbon analyzer was calibrated directly by
using a 85 ppm propane NBS traceable standard and zero air
gases.
Initial data was collected from the calibration
system components and recorded:
- 25 -
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(1) Dry gas meter volume
(2) Dry gas meter outlet temperature
(3) Oil bath temperature
(4) Impinger outlet temperature
(5) Barrel temperature
The stoddard sample was injected into the impinger
and not more than 20-seconds later the dilution gas was
introduced. The dilution gas was allowed to flow by
opening the 3-way valve to the 0.4 cubic feet (ft )
(R)
TedlaxS' bag and the on/off valve. During dilution, the •
internal pressure of the dry gas meter was recorded.
After 0.35 ft of diluted gas, it was turned off by
closing the on/off valve and then the 3-way valve. The
dry gas meter volume was read and recorded. The 3-way
valve was opened to allow the TedlarM bag gas sample to
flow through to the FID. Auxiliary temperatures of the
sample line leading to the Teflon"-' pump and of the
sample line at the pump outlet were recorded. Strip chart
data was recorded for each stoddard volume calibrated and
appear in Appendix B.
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