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

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 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

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                 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

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                   LIST OF TABLES



Table                                      Page



 2.1    Stoddard Concentrations              4

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                  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

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                      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  -

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     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 -

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                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.

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                                                       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.

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                                                      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)

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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)

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                                                      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)

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                                                      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)

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                                                       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)

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                                                     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)

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      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 -

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3.0 PROCESS DESCRIPTION



(To  be provided by TRW).
    -  14  -

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              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  -

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           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.

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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.







                       -  23  -

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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.

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      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.
                        -  26  -

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