EPA-65Q/2-75-042
June 1975
Environmental Protection Technology Series
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                                  EPA-650/2-75-042
     DEMONSTRATION OF REDUCED
       HYDROCARBON EMISSIONS
FROM GASOLINE LOADING TERMINALS
                        by

                 B.C. Walker, H.W Husa,
                   and I. Ginsburgh

                   Amoco Oil Company
                    P.O. Box 400
                 Naperville, Illinois 60540
                 Contract No. 68-02-1314
                  ROAP No. 21AFD-021
                Program Element No. 1AB015
            EPA Project Officer: William J . Rhodes

                Control Systems Laboratory
            National Environmental Research Center
          Research Triangle Park, North Carolina 27711
                     Prepared for

          U.S. ENVIRONMENTAL PROTECTION AGENCY
           OFFICE OF RESEARCH AND DEVELOPMENT
                WASHINGTON, D. C. 20460

                      June 1975

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                       EPA REVIEW NOTICE

This report has been reviewed by the National Environmental Research
Center - Research Triangle Park , Office of Research and Development
EPA, and approved for publication.  Approval does not signify that the
contents necessarily reflect the views and policies of the Environmental
Protection Agency, nor does mention of trade names or commercial
products constitute endorsement or recommendation for use.
                   RESEARCH REPORTING SERIES

Research reports of the Office of Research and Development, U.S. Environ-
mental Protection Agency, have been grouped into series.  These broad
categories were established to facilitate further development and applica-
tion of environmental technology.  Elimination of traditional grouping was
consciously planned to foster technology transfer and maximum interface
in related fields.  These series are:

          1.  ENVIRONMENTAL HEALTH EFFECTS RESEARCH

          2.  ENVIRONMENTAL PROTECTION TECHNOLOGY

          3.  ECOLOGICAL RESEARCH

          4.  ENVIRONMENTAL MONITORING

          5.  SOCIOECONOMIC ENVIRONMENTAL STUDIES

          6.  SCIENTIFIC AND TECHNICAL ASSESSMENT REPORTS

          9.  MISCELLANEOUS

This report has been assigned to the ENVIRONMENTAL PROTECTION
TECHNOLOGY series. This series describes research performed to
develop and demonstrate instrumentation, equipment and methodology
to repair or prevent environmental degradation from point and non-
point sources of pollution.  This work provides the new or improved
technology required for the control and treatment of pollution sources
to meet environmental quality standards.
 This document is available to the public for sale through the National
 Technical Information Service, Springfield, Virginia 22161.

                Publication No. EPA-650/2-75-042
                                11

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                           CONTENTS
 Objectives

 Facility  Design

 Cost Factors

 Test Program

 Test Results

 Comparison to Other Systems

 Conclusions
Page No.

   1

   1

   4

   4

   8

   19

   19
              Figures

Figure 1 - Schematic of Oxidation System                       2
Figure 2 - P & T Diagram of System                             3
Figure 3 - Flow Schematic                                      6

               Tables

Table I - Special Instrumentation                              7
Table II - Reid Vapor Pressures                                8
Table III - Gasoline Vapor Concentration                       9
Table IVA - Oxidizer Feed Test Results                         11
Table IVB - Analysis of Air-Vapor Feed to Oxidizer           12 to 16
Table V - Oxidizer Effluent Test Results                       17
Table VI - Oxidizer Operation Test Results                     18

Appendix I - Daily Log of Truck Loading                        21
Appendix II - Analysis of Vapor Collecting Effectiveness       25
Appendix III - Design Manual                                   29
                          iii

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                                OBJECTIVES
      This contract involved test work to demonstrate  the  effectiveness  of
 hydrocarbon oxidation for  reducing  emissions  from a gasoline  truck loading
 terminal located at Philadelphia, Pennsylvania.   The  program's  major
 objectives were in the areas of control  efficiency, operational characteristics,
 and comparison with other  known systems.   The control efficiency was  measured
 by determining the emissions from tank truck  loadings,  by determining the
 emissions from the high temperature oxidizer, and by  estimating emissions  from
 all other sources.  Operational characteristics  were  determined with  safety
 and reliability being of primary importance.   Cost effectiveness of this
 system was compared to other known  technology for disposal of hydrocarbon
 emissions, both for this specific size system and extrapolations to smaller
 and larger systems, and'for the climatic  conditions found at  this location
 and other locations in this country.
                            FACILITY DESIGN

      The system installed  at  the  truck  loading  terminal  at  Philadelphia  is
 shown diagrammatically  in  Figure  1.  Air  displaced  from  the  truck
 compartments  during  liquid gasoline fillings  is collected at the  loading
 rack.   The  facility  employs either  top  or bottom loading, thereby
 permitting  the  terminal to service  all  existing types  of trucks.   The  air-
 gasoline vapor  mixture  is  conducted from  the rack to the vapor  tank which
 smooths out the peak flows encountered  during loading  and provides storage
 for  the gases prior  to  disposal.  The mixed gases in turn are drawn from
 the  vapor tank  by  a  blower, compressed  to thirteen  inches of water pressure
 and  fed to  the  oxidizer.   Here  they are burned  in the  presence  of sufficient
 air  to insure 98%  or better conversion  to carbon dioxide and water.  Burning
 temperature is  maintained  at  or below 1500°F  to limit  formation of nitrogen
 oxides.

      Oxidizer operation is controlled by  the volume of gas  in the vapor  tank,
 starting up at  about 30% capacity and shutting  down at 10%  capacity.   The
 oxidizer is ignited  by  a propane  pilot  and includes temperature sensing  and
 flame  reading controls  to  insure  that the burn  sequence  will fail safe.
 There  are also  provisions  to  insure against flashback  from  the  oxidizer  into
 either the  vapor tank or to trucks  connected at the loading  racks.

     The oxidizer  is a  simple, reliable,  commercial gas  furnace,  which turns
 on and operates as needed.  However,  if it is necessary  to  shut down the
 oxidizer during tank truck loading,  and if the  vapor tank fills beyond its
 capacity of 10,000 cubic feet  (about  8  truck  loads), excess  vapors are vented
 to the air.   So far,  truck  loading rate has not  exceeded this capacity.

      Details  of this process  flow,  start-up procedure, normal operating
 procedure,  cold-weather procedure,  and  shutdown procedure are given in the
 attached Design Manual  (Appendix III).   Details of the entire system are
given in the P & I  Diagram  (Figure 2).

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                                                   FIGURE 1
                                                 VAPOR GATHERING LINE
                                                                     Fl.AME ARRESTOR
                                                                                            FLOATING ROOF
    TRUCK VAPOR
     MANIFOLD
      .    LJn
             HOP LOADING VAPOR ^
TRANSPORT
  TRUCK
                  BOTTOM LOADING ARM
 VAPOR DIAPHRAGM
     SAMPLE POINT
                                               FLOW
                   VAPOR HOLDER
                                 BREATHING
                                /   VENT
                                     RELIEF VALVE
                LIQUID SUPPLY LINE




CONTROL SHANTY AIR

               HYDROCARBON OXIDIZER

                   COMBUSTION AIR BLOWER
                                                            FLAME ARRESTOR

                                                     PROPANE TANK
                                                FLAME ARRESTOR
                                              u VAPOR BLOWER


                      SCHEMATIC VAPOR GATHERING  AND OXIDATION  SYSTEM
                                         PT.  BREEZE.  PA. TERMINAL

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                                                          Figure  2


                                                    P &  I  Diagram
l-'J—L-L	K§	.
                                                                                                                                                         I
                                                                                                                                                         (_>
COHT30L  3JH.PrMC
                                                                                                                                  —Ptl
                                                                                                                                 VAPOR OXIDATION SYSTEM
                                                                                                                                 PHILADELPHIA TEPMINAL

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                                     -4-
                               COST  FACTORS
     The capital costs for the vapor control and oxidation system at the
Philadelphia Terminal were as follows:

                Item
     Truck Rack Piping, Product
     Vapor Piping
     Vapor Holder
     Air Control System
     Hydrocarbon Furnace
     Foundation and Yardwork
     Furnace Piping
     Propane System
     Control House
     Condensate Tank
     Painting
     Electrical
     Engineering
     Beckman Oxygen Analyzer
                                                     $160,494 total

     The following are the annual oxidizer operating costs experienced by
the Philadelphia Terminal:

     Propane Consumption                     3,600 gals.
     Electric Consumption                    36,000 KWH
     Manpower Routine Checks                 300 manhours
     Maintenance                             $3,000
                             TEST PROGRAM

     The general objective of the test program was to evaluate performance
under widely varying conditions of temperature and loading.  Seasonal
temperatures in the Philadelphia area vary widely, causing wide variations (3-50%')
in the hydrocarbon content of the incoming air.  The varying number
of trucks being loaded at a given time results in substantial variations in
the amount of hydrocarbons to be handled.  Special attention was given to
operation of the propane safety system.  Propane is added to maintain all
parts of the system above the upper explosive limit, thus eliminating the
possibility of an explosion.

     A detailed evaluation of performance was done at four different periods
during the year to cover spring, summer, fall, and winter operation.  The
emphasis on seasonal variation was necessary because of changes in temperature
and variations in the vapor pressure of the gasoline supplied at different
times of the year.  As a consequence, the displaced gases from the truck

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                                       -5-
  loading operation can vary both in hydrocarbon content  and  hydrocarbon
  distribution.   Still another  factor affecting the  hydrocarbon content  of
                                                           "•""-lo.ding and
       The  streams  involved  are  shown  in  Figure  3,  a  simplified  schematic
  diagram of  the  oxidation system.   Instrument  locations  are  identified  by
  number  (also  see  Table  I)  and  flow streams  by  letter.   In addition  to  the
  measurements  by the  instruments  listed  in Table I,  the  normal  measurements
  at  the  facility were also  necessary, e.g.,  amount of gasoline  shipped  each
  day,  number of  trucks,  oxidizer-control  instrument  readings, etc.   Wherever
  possible, measurements  were continuously recorded on a  data logger   By
  careful planning, a maximum of required  information was obtained.

       There are  two main streams  (Figure  3)  feeding  the  oxidizer  (B  and C)
  and   one exhaust  stream (D).  Stream B comes from the vapor holder  and is
  mixed with air  (stream  C)  in the oxidizer.  There,  the hydrocarbons are '
  oxidized and the  products emitted  through the exhaust stack  stream D.
  As a  safety precaution, stream A was used when necessary to add propane to
  raise the hydrocarbon concentration in the vapor holder above  the upper
  flammable limit.

      For instrumentation,  a Beckman oxygen meter and a Ranarex density
 balance were used  in location 1 to monitor the total  hydrocarbon content
 from the trucks to the  vapor holder.   A dry gas meter was  used at location 5
 to measure the amount of propane  added to the vapor  holder.   The propane
 passing  location 6 to the  pilot light also was measured  (with  a dry gas
 meter) because it  contributes  to  the  total  input to  the  oxidizer.
   H ^ i°^ati0nu2'  the t0tal maSS flow was dete™ined with a dry gas meter
 and the hydrocarbon  content with a flame ionization detector (FIEO    The
 amount of air in stream B was calculated from the  difference between total
 mass and hydrocarbon mass.   At location 3,  a pitot tube was used  to measure
 the amount of air to the oxidizer.   Temperature  and humidity also were
 determined when appropriate.

      Characteristics of the effluent from the  oxidizer,  stream D,  were
 measured at location 4.   The  total  mass  flow was measured  to verify the  use
 of  measured mass  input  for  calculated mass  output.   Thereafter, the mass of
 the effluent was  calculated from the various  input  streams.   The  total
 hydrocarbon content  of  the  effluent  was  obtained with  FID  while NDIR gave
 the CO concentration.   NOX  concentrations were expected  to be  low   and
 periodic wet chemical measurements were  sufficient.  Periodic  determination
 of  the water content  of  the  stream provided  additional   information
 and  the  temperature  of  the  stream was continuously  recorded.

     In  order to provide adequate correlations for  supporting  the test
 objectives,  data in addition to the above were recorded and  summarized
These were:   (1) the number of times propane was added to  the vapor holder
 and the  reason, (2) number and type or trucks loaded,  (3)  total gallonage

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                            Figure  3
                    FACILITY SCHEMATIC
TANK
TRUCK
                                         STREAM D
                                            STACK
                             i
VAPOR
                   HOLDER   i
                   T—rt
                            STREAM B
         AIR
               STREAM C 3
                           BURNER
                  STREAM E
                 STREAM A
                               PROPANE
                                TANK
                         -fc-
                                                   PILOT
                                                   LINE
                                       NOS. 1-6 DENOTE LOCATIONS OF INSTRUMENTATION
                                                    LISTED IN TABLE I

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                                    TABLE  I

                             SPECIAL INSTRUMENTATION
Location
1


5
7
6
2




3

4






Stream

	

Fuel A
Fuel E
Fuel A
Fuel B




Air C
Out
Effluent D






Parameter

hydrocarbons
constituents
propane
propane
propane
stream flow
hydrocarbons
air

constituents
air

steam flow
steam flow
hydrocarbons
CO
NOx
water
temperature
Measurement
Ranarex density balance
Beckman (02 meter)
Gas chrom.
Dry gas meter
Dry gas meter
Dry gas meter
Dry gas meter
FID with dilution
	

Gas chrom.
pitot tube

	
pitot tube
FID
NDIR
dry chem. (c)
psychroneter
temp, probe
Recorder No. ^a)
1
1
...
2 (b)
2 (b)
1 (b)
1 (b)

	

.._


	
	
1
2
	
	
2
Information

hydrocarbon content
species present (periodic)
propane mass added from tank
propane added directly to burner
propane mass added from tank
total stream mass flow
total hydrocarbons
mass of air from difference between
total mass and hydrocarbons
species present (periodic)
mass air

total mass from input
total mass flow (initially only)
total hydrocarbons
CO concentration (attempt continuous]
NOx concentration (periodic)
water concentration (periodic)
exit flue gas temperature
(a)  If a magnetic  tape  system is  also  used,  these  measurements  along with
    any other appropriate  variables  will  be  recorded  on  tape  also.

(b)  Optional.
 (c) As N02; UNICO Model 400 gas detector using Kitagawa  tubes.

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                                      -8-


 of gasoline loaded,  (4) total vapor collected,  (5)  total amount of propane
 used, (6) total air  combusted, (7)  total emissions,  (8)  cost  of electricity,
 (9) cost of propane, (10)  cost of operating labor (man-hours),  (11) cost  of
 repairs, (12)  nonoperating time due to pollution control problems, and  (13)
 any other data that  proved informative.   In addition to  collecting data
 during the normal operating routine of the  facility, it  also  was necessary
 to periodically alter  operations in order to meet the test  objectives.

      Each seasonal test period lasted  about a week.   During nontest periods,
 instrument readings  were recorded continuously.   In  order to  eliminate  and
 isolate  as many unknown effects as   possible, each test  period  included
 baseline tests.   These baseline tests  consisted  of several  preset propane-
 air concentrations used as input to the  oxidizer.  The vapor  holder was
 bypassed and propane was added directly  to  the burner (stream E),  together
 with air (stream C).  During the test  periods, operations were  planned  to
 give maximum variations in controllable  parameters.   For example,  the vapor
 holder was filled with vapors obtained from top  loading  trucks  only, and
 then bottom loading  trucks only.

      All of these tests and data were  appropriately  correlated  and
 interpreted  to   meet   the   objectives   of     the    program.
 These objectives  fall  into three main  categories:  control  efficiency,
 operability and cost effectiveness.  Under  control efficiency are  the
 effects  of hydrocarbon feed content, ambient  temperature, and gasoline  vapor
 pressure (seasonal gasoline variations,  flow  rates,  etc.).  on   emissions.
 Operability encompasses the safety  and reliability of the propane  addition
 system under varying flow  rates,  hydrocarbon  compositions,  temperatures,  etc.
 The  cost effectiveness  was  determined  by the  initial  cost,  the maintenance
 cost,  and operating  cost in relation to  the cost  of  alternative  control
 systems.   Finally, a determination was made as  to the applicability of
 this  system to systems  of  other  size and  in other climatic  and geographical
 locations.

                             TEST RESULTS
      The  following gasoline  stocks were  loaded at the terminal during the
four  seasonal test periods:
    Stock
Leaded Regular
Unleaded Regular
Premium
     The gasoline vapor content of the mixed feed gas to the oxidizer
during the test periods is shown below:

Fall
11.5-12.2
12.5-12.8
12.4
TABLE II
Reid Vapor Pressures
Reid Vapor Pressure, psi
Winter Spring
13.4 12.2
13.3 11.4
13.4 13.1

Summer
10.4
9.1
10.4

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                                     -9-

                                TABLE III
                      Gasoline Vapor Concentration

Test Period                % Saturation           Ambient Temperature. °C

Normal  Terminal  Operation  (Top-Loaded and Bottom-Loaded Trucks)
Fall                            78                          478
Winter                          67                          4.6
Spring                          60                         17.2
Summer                          93                         15.0

    -Loaded Trucks
_	
FalT                           100                         7.2
Winter                          100                        -7.8
Spring                           89                         13.4
Summer                           94                         21.7

Bottom-Loaded Trucks
Fall75                          4.5
Winter
Spring                          73                         10.0
Summer                          79                         23.9
     The gases processed by the oxidizer were at a significantly higher
vapor content during the spring and summer tests because of the higher
ambient temperature.  The vapor concent was also higher for top-loaded
trucks because splash filling increases evaporation rate of the gasoline.

     Appendix I gives the daily log for truck loading at the terminal for
the period November 12, 1973 to May 2, 1974.  Roughly three-fourths of the
gasoline shipped at the terminal was bottom-loaded, with the rest top-
loaded about equally between tank wagons and tank trucks.  Average shipment
was about 291,000 gallons per day.

     Five methods of terminal operation were run for each seasonal test
period:

     1)  Pilot operation only:  measurements were taken on the
         oxidizer effluent with only the pilot light of the
         burner operating.
     2)  Baseline-propane gas:  measurements on oxidizer effluent
         when propane was burned at about the same rate as
         gasoline vapor during normal terminal operation.
     3)  Normal terminal operation:  measurements taken during
         filling of both top- and bottom-loaded trucks.
     4)  Top-loaded trucks:  measurements taken during filling
         of top-loaded trucks only.  This type of loading
         (splash-filling) usually generates excess vapor.
     5)  Bottom-loaded trucks:  measurements taken during filling
         of bottom-loaded trucks only.  Bottom-loading reduces
         gasoline agitation and therefore generates less vapor
         than top-loading.

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                                    -10-
      In addition,  two special  tests  were  run during  the winter  and  spring
 periods to simulate  operation  of  the terminal in  extremely  cold weather.
 This  was done  because the  ambient  temperature during the winter test was
 only  about -8°C,   and data for colder weather were needed.   Because
 hydrocarbon concentration  in gasoline vapor  (hydrocarbon-air mixture at
 equilibrium) decreases with temperature,  cold-weather operation was
 simulated by diluting the  vapor in the vapor holder  with air.   This test
 also  determined the  lower  limit of satisfactory operation of the burner.

      Analytical data for the oxidizer feed,  vapor composition,  oxidizer
 effluent,  and  oxidizer operation are shown in Tables IVA, IVB,  V,  and
 VI respectively.   As shown in  Table  IVA,  the mixed gas feed rate to the
 oxidizer during truck loading  ranged from 2.18 to 3.02 cubic meters per
 minute  and was fairly consistent throughout   the  four test  periods.  The
 hydrocarbon content  of the gas  was 22.6 to 48.5%, with the highest
 concentration  existing during  summer.  Average molecular weight of the
 hydrocarbons ranged  from 56 to  65  with over  one-hundred different molecular
 structures identified.  For the baseline  tests and pilot operation only,
 in which only  propane was  burned,  the gas hydrocarbon content was slightly
 lower,  with 4-5 components of  average molecular weight from 43.0 to 44.1
 Detailed composition of the vapor  is shown in Table  IVB.

      Effluent  from the oxidizer (Table V)    during its operation contained
 19 to 35  ppm carbon  monoxide,  1 to 45 ppm hydrocarbon (as methane) 1 to 10
 ppm nitrogen oxides,  and 0.9 to 3.2% (9,000  to 32,000 ppm) carbon dioxide.
 During  the  summer  test period,  hydrocarbon emission  was lower and carbon
 dioxide  was higher because of the  higher  flame temperature  in the oxidizer
 (Table  VI).   The  higher  flame temperature  also produced  slightly
more nitrogen  oxides.

     For pilot operation only,  hydrocarbon emission  was higher  than
normal because of  inefficiency  of  combustion  of the  pilot flame, as shown
by the lower perc<  ".age  of destruction or hydrocarbons (Table  VI).  For
the baseline test, in which only propane was  burned,   the lower  flame
temperature produced higher hydrocarbon and  lower carbon dioxide emissions
than normal.  For other than pilot operation,  however, destruction of the
hydrocarbons reaching  the  oxidizer was better  than
     For the two special tests conducted during the winter and spring
periods to simulate terminal operation in extremely cold weather, dilution
of the vapor holder gas with air decreased the oxidizer temperature.  This
resulted in less-efficient combustion as shown by the higher hydrocarbon
content and lower carbon dioxide in the effluent.  As the hydrocarbon
content of the feed gas was reduced by dilution to 3.5 vol. %, the  flame
pattern changed from full coverage of the manifold ports to stable
individual blue flames, one for each hold in the distributor manifold.
Further reduction below the 3.5 vol. % hydrocarbon level (spring test)
produced flame instability and excessive unburned hydrocarbons.  The excess
air had a tendency to blow out the individual flames.  The 3.5% value
corresponds to terminal operation at ambient temperatures estimated from
 -40  to -46°C.  This concentration was easily handled by the oxidizer,
flame  stability was good,  and operation  was entirely safe.

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  Test
 Period
    Test
Description
   Mixed Gas
   Feed Rate
M3/min. ® N.T.P.(a)
           TABLE

         OxiJ.tr.er Feed



 Measured Fraction(b)

Air         Hydrocarbons
 Fall     pilot  operation only
 Winter   pilot  operation only
 Spring   pilot  operation only
 Summer   pilot  operation only

 Fall     baseline,  propane  gas
 Winter   baseline,  propane  gas
 Spring   baseline,  propane  gas
 Summer   baseline,  propane  gas
                    2.16+0.03
                    2.17+0.01
                    3.02+0.01
                    2.86+0.02
Fall    normal terminal operation  2.78±0.04
Winter  normal term inal operation  2.18+0.03
Spring  normal terminal operation  2.47+0.01
Summer  normal terminal operation  2.41+0.05
Fall    top-loaded trucks
Winter  top-loaded trucks
Spring  top-loaded trucks
Summer  top-loaded trucks

Fall    bottom-loaded trucks
Winter  bottom-loaded trucks
Spring  bottom-loaded trucks
Summer  bottom-loaded trucks

Winter  special-vapor holder
        gas diluted with air

Spring  specail-vapor holder
        gas diluted with air
                    2.75±0.04
                    2.64+0.02
                    2.50+0.01
                    2.37±0.02
                0.8077-0.0026
                0.8048+0.0038
                0.7899+0.0053
                0.7966±0.0239

                0.7622-0.0026
                0.7746+0.0028
                0.7105+0.0251
                0.5856+0.012

                0.6627+0.0026
                0.7742+0.0028
                0.6275+0.0028
                0.5153+0.019
            0.1923+0.0026
            0.1952+0.0038
            0.2101±0.0053
            0.2034+0.0239

            0.2378+0.0026
            0.2254+0.0028
            0.2895+0.0251
            0.4144+0.012

            0.3373±0.0026
            0.2258+0.0028
            0.3725<-0.0028
            0.4847-0.019
                    2.71+0.04    0.7703+0.0026     0.2297±0.0026
                   2.542+0.003  0.7228+0.0025
                   2.39±0.016   0.5914+0
                                 0.2772±0.0025
                                 0.4086+0
                   2.234+0.008  0.8890+0.0044     0.1110+0.0044     58rl


                   2.97+0.02    0.9646+0.0024     0.0354+0.0024     62-2
                               a)  cubic meters per minute at normal
                                   temperature and pressure  (60°F
                                   and 1 atmos.)
                               b)  by oxygen analyzer
                                                                                                Hydrocarbons
Measured
Molecu lar
Weightfc)
--
"* ™
45 + 1
44+1
43+1
44.»-2
60-1
59::1
62+1
56-^2
60+1
56+1
61 + 1
63 + 2
62+1
62 + 1
65+0
_ Grab
Calculated
Molecular
Weight
44.0
43.6
43.0
44.0
43.6
43.0
44.1
63.4
. 62.6
64.3
66.3
63.2
61.2
63.3
66.8
63.5
64.4
66.8
Sample
Number of
Components
Identified (d)
4
5
4
4
5
4
5
96
75
78
70
100
96
72
70
80
80
69
                                                                   62.3
                                                                   64.2
                                                                    c)   by density balance
                                                                    d)   by mass  spectrometer
                                                                 89
                                                                                                       48

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             TABLE  IVB
  Analysis of Air-Vapor Feed to Oxidizer
Fall Tesl-s

Item
No.
1
9
3
4
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30
31
32
33
34
35
base- Loading
Hydrocarbon Component
Methane
Ethane
Ethane; 'Ethylene
Methane; Ethane; Ethylene
Propylene
Propane
Item 5 + Item 5
Isobutane
Isobutylene + 1; Butene
N- Butane
T-2-Butene
Item 10 + Item 11
C-2-Butene
3-Me-l-Butene
Esopentane
1-Pentene
2-Me-l-Butene
2-Me-l, 3-Butadiene
N-Pentane
T-2-Pentene '
Item 19 4 Item 20
C-2-Pentene
2-Me-2-Butene •
2,2-Dimethylbutane
Cyclopentene
3-Me-l-Pcntene; 4-Me-l-Pcntene
4-Me-C-2-Pentene
2,3-Dimethyl-l-Butene
Item 27 4 Item 28
4-Me-C-2-Pentene; 2-Me-l, 4 Pentadiene
Cyclopentanc
4-Me-T-2-Pentene
2.3 Dimethylbutane
Item 32 4 Item 33
2-Me-Pentane
line normal
#13 #11
2.78
0.59
0.46
1

99.10
3.69
0.27 14.52
1.14
0.04 36.19
1.77

1.17
0.23
17.79
0.50
0.84

5.78
0.95

0.59
1.34
0.24
0.14
0.08
0.02
0.04


0.35
0.06
0.58

1.83
top
#12
2.86

0.46



3.77
14.72
1.06
35.83
1.67

1.04
0.21
17 . 65
0.46
0.77
0.01
5.60
0.85

0.52
1.21
0.23
0.13
0.07
0.02
0.04


0.33
0.05
0.55

1.75
hot.
#10
2.32

0.29



3.64
15.12
1.32
34.90
2.07

1.40
0.26
18.98
0.55
0.92



6.47
0.66
1.44
0.23
0.13
0.08
0.02
0.04


0.33
0.06
0.61

1.86

base- Loading
line normal
#17 #16



0.20 3.71


99.37 4.07
21.38 19.82
1.65
0.13 28.64
2.35

1.77
0.36
19.11
0.61
1. 00

4.18
0.94

0.66
1.44
0. 14
0. 13
0.08

0.07


0.30
1) . 05
11.50

0 . 08
top
#14



3.27


7.68
21.44
1.70


33.42
1.65
0.29
16.02
0.53
0.88



5.24
0.57
1.31
0.16
0.11
0.08


0.06

0.27
0.05
0.43

0.07
hot.



4.17


4.17
0.31
1.58
29.14
2.14

1.57
0.31
19.14
0.56
0.94

4.24
0.83

0.62
1.38
0.15
0. 12
0.03


0.06

0.29
0.04
0 . -i 9

0.07

Spring Tests
base- Loadine
line normal
#21 -'20
1.92
'
0.57
0.98


98.56 3.67
17.55 23.95
1.24
0.15 29.63
1.89

1.28
0.27
21.13
0.54
0.88



6.85
0.66
1.47
0.23
0.15
0.09
0.02
0.04


0.37
0.05
0.61

0 09
top
#24
1.59

0.56



3.68
22.17
1.79
25.37
2.68

1.94
0.36
19.77
0.65
1.11

5.02
0.95

0.72
1.72
0.19
0.17
0.12

0.05

0.02
0.30
0.06
0.50

0.08
hot.
#22
1.13

0.30



2.89
24.19
1.58
27.32
2.47

1.77
0.33
20.90
0.62
1.05
0.02
4.63
1.03

0.70
1.55
0.16
0.16
0.09

0.05

0.02
0.30
0.05
0.55

0.119
spec
:"23
0.40

0.31



2.82
24.19
1.61
27.20
2.43

2.28
0.35
21.04
0.61
1.09

4.44
0.95

0.78
1.52
0.14
0. 14
0.06

0.07


0.2B

n.r>5

n.ng



Summer Tests
base- Lo.ndine
line normal
#26 #28
0.23
0.11
o.ns

2.63 0.06
96.93 4.15

0.25 19.08
1.30
0.08 23.25
2.00

1.37
0.20
21.27
0.88
1.25



11.46
0.50
1.13
0.31
0.1 1
0.08

0.05


0.61
0.05
0.63

0.08
top.
#29
0.47

0.16

U.03
2.68

12.23
0.52
27.25
0.84

0.49
0. 10
24.67
0.34
0.44



16.80
0.37
0.71
0.51
0.08
0.04
0.01
0.02


0.89
0.02
0.70

0.05
hot.
"27
0.24

0.05

0.07
3.67

18.67
1.50
21.39
2.23

1.57
0.26
21.92
0.69
0.99



9.91
0.64
1.55
0.26
O.lfi
0.10

0.08


0.54
n.07
0.71

0.12
continued next page

-------
                                                                         TABLE  IVB
                                                             Analysis of Air-Vapor Feed to Oxidizcr (cont'd.'.

base-
Item line
No. Hydrocarbon Conponont -113
36 2-Me-l-Pentene
37 3-Me-Pentane; l-Hexene; 2-Ethyl-l-Butene
38 C-3-Hexene
39 T-3-Hexene
40 teem 38 + Item 39
41 3-Me-Cyclopentene
42 2-Me-2-Pentcne
43 item 41 + Item 42
44 3-Me-T-2-Pentene
-5 Item 41 + Item 42 + Item 44
4fi N-Hexane
•i7 N-llcvane; 4,4-Uimethyl-l-Pentene
4? T-i-Hexene
*'* C-2-Hexene
50 item 48 + Item 49
51 Item 47 + 3-Me-T-2-Pentene
52 Item 51 + Item 48
53 item i7 + Item 48 + Item 49
54 3-Me-C-2 Pentene
55 i,A-Dimethyl-T-2-Pentene
56 7.tem 54 + Item 55
57 Me-Cyclopentane; 3,3-Dimethyl-l-Pentene
58 2,2-Dimethylpentane
[59] [2,2-Dimeth.ylpentane; 2,3-Dimethyl-2-Butene;1
2,3,3-Trimethyl-l-Butene
60 Item 57 + Item 59
61 2,4 Dimethylpentane
[62] r2,4-Dimethyl-2-Pentene; 3-Ethyl-l-Pentene;,
3-Me-l-Hexene '
63 Benzene
64 2,2,3-Tritnethylbutane
65 2,4-Dimethyl-l-Pentene
Loadine
normal
*lt
0.09
1.12
0.04
0.05



0.07
0.17


0.83
0.07
0.07




0.10


0.49

0.05


0.12


0.15

0.03
top
#12
0.08
1.06
0.04
0.05



0.08
0.14


0.80
0.07
0.06




0.10


0.51

0.09


0.13


0.21

0.05

base- Loading
bot. line
#10 #17
0.09
1.14


0.09




0.23
0.82



0.03



0.10


0.49 0.44
0.05



0.13


0.05


nornal
* IS
0.08
0.93


0.08


0.20




0.05


0.72


0.09


0.40

0.04


0.10


0.07


top
#14
0.07
0.83


0.07


0.19




0.06


0.65


0.08
0.01

0.43

0.05


0.10


0.16


base-
hot, line
#18 #21
0.07
0.93
0.03
0.04



0.07
0.11


0.72
0.06





0.09
0.01

0.55

0.04


0.10


0.10






Sprint; Tests Siimner Tests
Loadine base- In.nrlino
norma 1
•'•'20
0.09
1.16
0.04
0.05

0.10
0.14





0.08



0.93

0.11
0.02

0.45

0.05


0.11


0.17
0.02
0.03
top
«24
0.08
0.96
0.03
0.05

0.08
0.13





0.06



0.70

0.09


0.51

0.04


0.08




0.05
bot. spec line
#22 ?23 >>2r-
0.09 0.08
1.03 1.01
0.04
0.05
0.08
0.10
0.13
0.15




0.06



0.76 0.86

0.10
0.01
0.11
0.59

0.05


0.10 0.09

0.11


0.05
normal
"28
0.08
1.56


0.07




0.18







1.43
0.08






0.55
0.10


0.38

0.09
top.
#29
0.05
1.67


0.05


0.05
0.08








1.39
0.06






0.42
0.09


0.44

0.06
bot.
#27
0.12
1.79


0.12




0.29




1
H- »
U)
1
1.74
0.13






0.78
0.14


0.4'2

0.14
66 Item 64 -I- Item 65
67 Item 63 + Item 64
68 Item 64 + 4,4-Dimethyl-C-2-Pentene
                                  0.04   0.01
                                                                   0.17
0.02   0.02   0.04
                                                                                                               0. 11
                                                                                       0.02   0.02  0.03
                                                              continued  next page

-------
           TABLE  IVB
Analysis of Air-Vapor Feed to Oxidizer (cont'd.)

Item
No.
.69
70
71
72
{73}
74
{75}
76
77
78
79
80
81
QO
84
85
86
87
88
f89}

90
91
92
93
94
95
96
97
98
99
100
base-
line
Hydrocarbon Component #13
l-Me-Cyclopentene
Item 69 + 2-Me-C-3-Mexene
Item 69 + 2,4-Dimethyl-2-Pentene
Item 70 + 2,4-Dimethyl-2-Pentene
[2,4-Dimethyl-2-Pentene; 3-Ethyl-l-Pentenc;1
3-Me-l-Hexene
2,3-Dimethyl-l-Pentene; 2-Me-T-3-Hexene
[Item 74 + 5-Me-l-llexene; T-3,5-Dimethyl-1
Cyclopentene; C-3,5-Dimethycyclopentene
3,3-Dimethylpentane
Cyclohexane
Cyclohexane; 4-Me-C-2-Hexene
2-Me-Hexane; 5-Me-C-2-Hexene
1, 1-Dimechylcyclopentane
Item 79 + T :..-.., SO
Cyclohextmc
2-Me-Hexane; I ,1-Dimethylcyclopentane
2, 3-Dimethylpentane
Item 86 +• 3,4-Dimethyl-C-2-Pentene
3-M3-Hexane
( l-C-3-Dimethy Icyc lopentane ; 2-Me- 1-llexene ;}
3,4-Dimethyl-T-2-Pentene
l-T-3-Dime thy Icyc lopentane
Item 90 + 1-Hcptene; 2-Ethyl-l-Pentene
3-Ethyle Pentane ; 3-Me-T-2-llexene
l-T-2-Dime thy Icyc lopentane
Item 92 + Item 93
2,2,4-Trimethylpentano
Item 95 + T-3-lleptene
Item 93 +• 3-Ethylpentane
C-3-lleptene; 1,4-Dimethylcyclopentene
3-Me-C-3-IIexene ; 2-Me-2-Hexene
Item 99 + 3-Me-T-3-Hexene
Loading
normal top
#11 #12
0.09
0.02
0.02
0.01
0.12
0.01


0.13
0.21
0.07

0.06



0.06
0.23


0.02

0.03
0.10
0.05
0.03
0.01
0.11
0.22
j.Ol
0.01

0.13

0.23
0.07

0.06



0.06
0.23


0.02

0.03
base- Loading
hot. line normal top
#10 #17 »lf, m
0.10
0.02
0.01
0.10
0.01
0.21
0.12

0.20
0.07

0.05



0.06
0.25


0.01

0.02
0.07
0.02
0.02
0.10
0.17


0.11

0.16
0.06

0.05



0.05
0.19


0.02


0.07
0.03
0.02
0.09
0.01
0.01
0.15
0.10

0.14
0.06

0.04




0.18

0.05



Sprins Tests
base-
boc . line normal
>ns fi ="o
0.07
0.02
0.02
0.10
0.01
0.01
0.16
0.11

0.15
0.06

0.05



0.05

0.18

0.01

0.02
0.09
0.02
0.02
0.01
0.09
0.22
0.01

0.12

0.21
0.07

0.05




0.26

0.06
0.02
0.03

Loading
top bot.
#24 #??
0.08
0.03
0.02
T
0.08
0.15
0.01

0.08

0.15
0.05


0.04



0.16

0.04
0.01
0.02

0.10
0.03
0.02
0.01
0.09
0.18
0.01

0.10

0.17
0.07

0.05



0.05
0.22


0.01

0.02

base- Loading
spec line normal top.
«T) yop JJ7O yno
0.10
0.20



0.09
0. 18
0.05


0.04


0.05
0.20





0.01
0.01
0.03
0.08
0.27


0.13

0. 28
0.05


0.07
0.04
0.14


0.02




0.01
0.01
0.03
0.05
0.23


0.11

0 24
0.03


0.05
0.03
0.13


0.01




bot.
0.04 !
0.04
0.14
t
J
0.40


0.18

0 41
0 09


0.11
0.07
0.20


0.03




       continued next  page

-------
            TABLE IVB
Analysis of Air-Vapor Feed to Oxidizer (cont'd.1
Item
No.
101
102
103
104
105
106
107
108
109
110
111
112
113
114
115
116
117
118
119
120
121
122
123
124
125
126
127
128
129
130
131
132
Fall Tests
base- Loadina
3-Ethyl-2-Pentene
T-2-lIcptene
N-Heptane; 3-Me-C-2-Hexene
Item 103 + 2,3-Dimethyl-2-Pentene
Item 103 + 2,3-Dimethylcyclopentene
Item 104 + Item 105
2,3-Dimethyl-2-Pentenc
Item 107 + C-2-Hcptene; 3--Ethy Icyclopentene
C-2-Heptenc
Item 109 + 3-Ethy Icyclopentene
l-C-2-Dimethylcyclopentane
2,2-Dimethyl llexane
Item 111 + Item 112
Me-Cyclohexane; 1, 1,3-Trimethylcyclopentane
2,5-Dimethylhexane
Ethylcyclopentane
2,4-Dimethylhexane
Item 116 + Item 118
2,2,3-Trimethylpentane
Item 117 + Item 119
l-T-C-4-Trimethycyclopentane
3,3-Dimethylhexane
Toluene
l-T-2-C-3-Trimethylcyc lopcntane
Item 122 + Item 123-Item 124
Ethylhenzene
P-Xylene
H-Xylene
0-Xylene
C-8 Saturates and Olefins
Isopropylbenzene
N-Propylbenzene
normal
41 1
0.017
0.01
0.15
0.01
0.02

0.08
0.04
0.02


0 03
0.01
0 01

0.87

0.05
0.04
0.12
0.08
0.35
0.01
0.04
top
112
0.01
0.01
0.17
0.02
0.02

0.09
0.04
0.02


0 04
0.01
0 01

0.86
0.01

0.05
0.05
0.12
0.06
0.45
T
0.01
	 Winter Tests
	 base- Loadine
bot. line normal
#10 #17 ,t\t,
0.01
0.14
0.12
0 01

0.03

0.08
0.04
0.01



0.01
0 01

0.83

0.04
0.02
0.11
0.08
0.33
T

0.02

0.07
0.03
0.01
0.02


0.01

0.68

0.02
0.02
0.07
0.04
0.19
0.03
top
Q
T 	
0.01
0.11
0.11
0.17 0.14
0.01
0.02 0.02

0.06 0.07
0.03 0.04
0.01
0.02
0.02
0.01
o.ni 0.02



0.87 0.52
0.04
0.03
0.10
0.06
0.28 0.28
T
0.01
0.01
0.03
0.01
0.06
0.02

0.04
T
0.01

0.76

0.03
0.02
0.06
0.04
0.22
0.01
0.01
0.01
0.02
T
0.04
0.02

0.03
T
0.01

0.64

0.02
0.02
0.05
0.03
0.17
0.01
0.01
bot.
#27
0.01
0.27
0.02
0.04
0.01
0.10
0.04

0.07

0.02

1.07

O.Ofi
0.04
0.10
0.06
0.33
0.02
0.01
   continued next page

-------
              TABLE  IVB
Analysis of Air-Vapor Feed to Oxidizer (cont'd.)
Fall Tests

Item
No.
133
134
135
136
137
138
139
140
[1411

1*2
lo
base- Loading
Hydrocarbon Component
l-Me-3-Ethylbenzene
l-Me-4-Ethylbenzene
l-Me-2-Ethylbenzene
1,3,5-Trimethylbenzene
1 , 2 ,4-Trimethylbenzene
1,2,3-Trimethylbenzene
C-9+ Saturates and Olefins
l-Me-2-Isopropylbenzene
[ 1,3- Dime thy 1-2-Ethylbenzene;]
l,3-Dimethyl-4-Ethylbenzene
C-IO Saturates and Olefins
C-10 + Aromatics
line normal
#13 #11
0.01
0.02
0.05

0.01
T
0.06




0.05
top
#12
0.02
0.01
0.01
0.01
0.03
T
0.06




0.01
Winter Tests
base-
hot, line
#10 #17
0.02
0.01
0.01
0.01
0.03







Loading
normal
#16
0.01
0.02
0.01
0.01
0.04
0.04
0.02





top
#16
0.03
0.02
0.01
0.01
0.04

0.02
0.01
0.02



basc-
bot. line
#18 #21
0.01
0.01
0.01
0.01
0.02

0.02





Sprinn Tests Summer Tests
Loading base-
normal
*20
0.02
0.01
0.01
0.01
0.03

0.04



0.02

top
#24
0.01


0.01
0.03

0.03





hot. spec line
#22 #23 -*26
0.03
0.02
0.01
0.02
0.06
0.01
0.03



0.03
0.04
Loadine
norma 1
«28
0.02

0.01
0.03
0.02

0.01





top.
#'9
0.01
0.01
T
0.01
0.02

0.01





bot
#27
0.02

0.01
0.01
0.03

0.02






-------
                                                                             TABLE V
                                                                          Oxldlzcr  Eff luent

Test
Period
Fall
Winter
Spring
Summer
Kail
Winter
Spring
Sun.iner
Fall
Winter
Spring
Summer
Fa 1 1
Winter
Spring
Suinncr
Knll
Winter
Spring
Summer

Test
. Description
pilot operation only
pilot operation only
pilot operation only
pilot operation only
baseline, propane gas
baseline, propane gas
baseline, propane gas
baseline, propane gas
normal terminal operation
normal terminal operation
normal terminal operation
normal terminal operation
top- loaded trucks
top- loaded trucks
top-luaded trucks
top-loaded trucks
hot torn- 1 oiided trucks
bottom-loaded trucks
bottom-loaded trucks
bottom-loaded trucks
Carbon Monnxlc'e
Measured
3.4-.0.5
1.9+0.4
2.1*.0.4
2.7*3.0
21.0*0.7
20.8*0.6
21 .'4
19.0*0.1
26.0-0.2
25.3*0.5
23*3
35*1
25.4*0.6
33*6
24t 3
28-2
25.6*0.2
.
23 + 1
28 + 1
Cr.ib
•BK
1-2
10
0-4
16
13-27
20-40
12-18
19
17-20
20-30
37-41
1ft
19-20
10-20
25
16
..
10-40
25
ppm(volume basis'*
Hydrocarbon
as Methane Nttroprn Oylrfes
Measured
90*6
69*7
79 + 7
8 2.' 2
58'8
44*5
43*2
42.t5
25<4
33*4
21*5
5-0.5
14 + 5
45*14
14*3
1*1
24*4
.
20.13
5.-.1
Crab
Sarnie tonsured

63-78
108-159
53-102
43
42-43
51-57
26-42
22
38-39
17-33
17-29
13
33-39
9-30
3-7
26
_•
9-36
12-16
0
0
0
--
1-5
1-5
1-5
1-2
1-5
1-5
1-5
8-10
1-5
1-5
1-5
--
1-5
m .
1-5
2
fir.ib

0.3
0.3
0
— —
0.8
0.4
2.5
— —
0.6
1.5
1.8
..
1.0
1-1.6
2.0
«••
_ —
1.6
4.3
f'oisuro'J (.1)

_ —
	
--
15,700
11,200
17,000
52,000
2 1 , 700
20.6CO
52,000
45,800
50,000
24 , COO
99,500

26,300

45,900
--
Water Vnpor
C.ilc-
7 100
e|ooo
13,800
13,800
16,900
16,000
20,000
28,500
23,000
20,400
30,?0l)
65!800
32,000
19,000
32,400
53,700
26,000

28,100
46,100
Carbon Dioxide
AnMcnt fal
6Qnn
, OU-'
5, 700
13,500
13,500
6,800
5,°00
5,5cn
15,000
3 , 200
5,700
8,700
34,000
3,300
2,000
4,500
18,700
6.800

6 , 000
14,800
Or s.it



--
8,000
8,000
7,000
9,000
17,000
9,000
14,500
23,000
22,000

20.0CO
32,000
12.000

15,500
26,000
Calc-
ulate' fc}

600

--
8,000
s.oon
11 ,000
10,500
16.500
1 2 , 000
17,500

22,800

23JOOO
28,500
15.900

18,000
27.000
Sajro 1 c

cnn
j\j'j
o
0

2,800
1,500
2,000

2,300
3^900
9.0CO

2,800
3J900
H.OOO


2,300
7.000
Winter    special-vapor  holder        19il         20
          gas diluted with air

Spring    special-vapor  holder        39+2        10-20
          gas diluted with nlr
58_'13
         58-69
226*18   270-420
1-5
                     1-5
                              0.3
                              0.4-2
                                        12,000
                               !5,100
                                                    10,000
7,500
                                            5,300
7,000    6,400
            2,000    2,900
                                                                                                   1,400
                    400-700
                                                                 al  by wet and dry bulb ther^iomstry
                                                                 b)  by oxygen balance; Includes ambient air water vapor
                                                                 c)  by cnrbon balance; Includes ambient air cnrhon dioxide

-------
                                                  -18-
                                               TABLE  VI

                                          Oxldizer Operation


Test
Period
Fall
Winter
Spring
Summer
Fall
Winter
Spring
Summer
Fall
Winter
Spring
Summer
Fall
Winter
Spring
Summer
Fall
Winter
Spring
Summer


Test
Description
pilot operation only
pilot operation only
pilot operation only
pilot operation only
baseline-propane gas
base line -propane gas
baseline-propane gas
base line -propane gas
normal terminal operation
normal terminal operation
normal terminal operation
normal terminal operation
top-loaded trucks
top-loaded trucks
top- loaded trucks
top-loaded trucks
bottom-loaded trucks
bottom-loaded trucks
bottom-loaded trucks
bottom-loaded trucks
Pilot Fuel
(propane)
ID"* M3/min.
@ N.T.P.
1.367±0.007
1.40+0.02
1.41±0.01
1.38+0.02
1.367+0.007
1.37±0.01
1.40+0.02
1.33+0.01
1.410+0.006
1.41±0.01
1.3H0.02
1.28+0.01
1.363+0.009
1.39+0.03
1.34+0.02
1.26+0.01
1.38±0.01
._-
1.37+0.01
1.26±0.01

Combustion
Air
VP/min.ff» N.T.P.
170+8
170+8
170+8
170t8
170+8
170+8
170+8
170t8
170+8
170+8
170+8
170±8
170+8
170+8
170+8
170+8
170+8
___
170+8
170±8
                                                                                         Destruction
                                                                      Temperature           of
                                                                   Oxidizer   Ambient   Hydrocarbons
                                                                     "C         °C           %
                                                                    16+8
                                                                     10
                                                                    25.6
                                                                    28.3

                                                                    174+2
                                                                    168+2
                                                                    234+5
                                                                    243+3

                                                                    321±35
                                                                    229+1
                                                                    364+46
                                                                    565+11

                                                                    434±6
                                                                    238±16
                                                                    463+10
                                                                    643±3
                                           8.4+0.5
                                             3.3
                                           25.6
                                           27.8

                                           8.4+0.5
                                           4.0+0.8
                                           8.6+0.5
                                           26.5+0.5

                                           4.8+0.5
                                           4.6+0.5
                                           17.2.±0.5
                                           15.0±0.5

                                           7.2±1.4
                                          -7.8+1.7
                                           13.4+0.6
                                           21.7+0.7
                                                                    300±28    4.5+0.2
                                                                    360+9
                                                                    560±4
                                           10.0+0.5
                                           23.9+0.8
                                    62.6+2.5
                                    72.1+4.9
                                    68.5+4.6
                                     66.8

                                    99.2+0.1
                                    99.4+0.1
                                    99.6+0.1
                                    99.6±0.1

                                    99.8+0.1
                                    99.7+0.1
                                    99.9+0.1
                                    99.9+0.1

                                    99.9±0.1
                                    99.7+0.1
                                    99.9+0.1
                                    99.9±0.1

                                    99.8+0.1

                                    99.9+0.1
                                    99.9+0.1
Winter    special-vapor holder
          gas diluted with air
1.39±0.02
170+8
  114±2
1.9+0.5
99.7+0.1
Spring    special-vapor holder
          gas diluted with air
1.40+0.02
170+8
63.1+1.4    8.7+0.5
            91.3+1.8

-------
                                     -19-
     Although the oxidizer disposed of 99% of the gasoline vapor it received,
only about 70% of the air-vapor mixture displaced during truck loading
reached the oxidizer during the fall and winter test periods (Appendix II).
Unusually high pressures  (21" H^O) produced in the truck during loading
were responsible for the vapor loss through maladjusted hatch covers and
faulty vacuum-relief valves on the truck.  The low vapor transfer and
pressure build-up were due to blockage by a column of gasoline in the hose
that connects the truck vapor manifold to the vapor collecting system.  The
hatch cover and valve problems were corrected and modifications made to
insure that the connecting vapor hoses would not collect liquid gasoline,
as shown by the greatly improved vapor recovery from the truck during the
spring and summer test periods (Appendix II).  Reliability of the system
has been excellent, with only one failure during the year of testing. This
failure was caused by ignitor spark plug failure on the oxidizer.

                      COMPARISON TO OTHER SYSTEMS

     In 1972, a study was made comparing systems employing four methods of
vapor recovery at terminals; hydrocarbon oxidation, absorption, condensation,
and adsorption.  At that time, the majority of the systems were still in the
development stage and commercial units had been built by only a few companies.
Recovery of the vapors could not be justified economically with any of the
commercial systems.  Selection among the available systems on any rational
economic basis could not be made because the net values after capital
charges at 10 PI were very similar.  Selection was, therefore, made on the
basis of recovery efficiency, demonstrated performance, and ability to meet
air quality standards through a wide range of ambient conditions.  For these
reasons, hydrocarbon oxidation was preferred for terminals pumping less than
3 million barrels of gasoline per year (Philadelphia terminal pumps about
2 million).  For larger terminals, a recovery system using an activated
carbon adsorption unit (to concentrate the vapors and replace the vapor
holder) together with a reduced capacity conventional absorption unit
downstream  might be preferred.

                                CONCLUSIONS

     Tests run at the Philadelphia terminal during each of the four seasons
showed that the oxidizer safely and efficiently disposes of 99+% of the
vapor collected, even in extremely cold weather when the air-gasoline vapor
mixture is in the flammable range.  Emissions from the oxidizer are well
within acceptable limits because of high efficiency and low flame temperature
to limit formation of nitrogen oxides.
     Capital costs for the installation were about $160,000, with an annual
maintenance of $3,000.   Annual operating costs were:  propane consumption,
3,600 gals.; electric consumption, 36,000 KWH, and manpower for routine
checks, 300 man-hours.

-------
                                -20-
     The only serious trouble encountered was at the beginning of the tests
when a considerable portion of the vapor from, the trucks was not reaching
the oxidizer.  This blockage was caused primarily by liquid gasoline
carryover to the vapor collection system.  This and minor instrument
problems were corrected, however, and overall disposal efficiency of the
entire system now exceeds 90%.

-------
                    -21-
               APPENDIX  I




TRUCK LOADING AT PHILADELPHIA TERMINAL




               DAILY LOG






Top Loading
Bottom Loading
Tank Wagons


Date
11-12-7.1
1.3
14
15
16
1.7
1.8
19
20
21
22
23
24
25
26
27
23
29
30
12--1.-73
2
.')
A
5
6
f.
fj
10
11
1.2
13
U
l!i
16
17
18
J.«

Total
No. Gal.
11 44000
7 25700
7 2 .',.': 00
6 2:500

17 65100
Sunday
8 29300
7 26000
8 30(JOO
Holiday

17 69900

11 39700
10 36700
8 27800
S 23000
9 33100

Sunday
1.1 5.1900
If! ",7'»00
10 3"?200
•;i 34000
IB 7>300
Sunday
a 31000
3 33000
7 23800
«* 33000
10 37400
0 ?.3500

6 7.2100
7 7 3 ft 'JO
U) 7.2000

Avg.
Gal.
4000
3671.
3114
3583

3829

3662
3714
3862


4112

3609
3670
3475
3500
3678


3727
3730
3720
377M
4100

3875
3667
3400
3667
3740
3722

3683
3371
.3200

7. of
Total
14.2 -
9.1
9.4
7.9

14.0

1.0.1
9.5
10.4


15.5

14.6
12.5
10.4
1.0.1
14.0


10.4
1?..9
12.9
11. 9
12.1

10.9
12.2
8.3
11.3
15.2
1.3 . 1

9.2
12.3
11.0


No.
4
8
6
5

5

4
5
6


5

2
6
3
5
2


10
7
7
7
8

3
5
2
5
4
f.

2
2
10
Tank Trucks

Total
Gal.
29600
59000
40500
36400

39700

26000
39900
46300


38100

16200
46500
21400
39900
14500


77200
57600
57600
57600
65600

23700
32700
15400
33700
26400
34600

9100
11700
75400

Avg.
Gal.
7400
7375
6750
72SO

7940

6500
7980
7717


7620

8100
7750
7133
7980
7250


7720
8228
8228
8228
8200

7900
6540
7700
6740
6600
5767

2550
5850
7540

7o of
Total
9.5
20.9
15.4
13.3

8.6

8.9
14.5
15.7


8.4

5.9
15.8
8.0
14.4
6.2


14.4
20.0
20.0
20.2
10.8

8.3
12.1
5.4
11.5
10.7
13.6

3.8
6.1
26.0


No.
32
26
26
31

49

32
28
30


47

30
29
30
29
25


54
26
26
26
62

28
26
30
28
26
26

26
22
25
Tank Trucks

Total
Gal.
237200
197200
196900
21.5500

359700

236300
209100
218700


344000

216700
211100
21.7900
209500
188400


404300
193400
193400
194200
470100

230300
204000
245900
226400
182500
187300

208500
156400
182800

Avg.
Gal.
7412
7585
7573
6952

7341

7384
7468
7290


7319

7223
7279
7263
7224
7536


7487
7438
7438
7469
7582

8225
7846
8197
8086
7019
7204

8019
7109
7312

% of
Total
76.3
70.0
75.2
78.8

77.4

81.0
76.0
73.9


76.1

79.5
71.7
81.0
75.5
79.8


75.2
67.1
67.1
67.9
77.1

80.8
75.7
86.3
77.2
74.1
73.3

87.0
81.6
63.0
Total
Gallons
Shipped
31.0800
281900
262000
273400

464500

291.600
275000
295900


452000

272600
294300
267100
277400
236000


537400
2S3300
288200
285800
609500

285000
269700
285100
293100
246300
255400

239700
191700
290200

-------
                     -22-
Top Loading
Bottom Loading
Tank Wagons


Date
12-20-73
21
22
23
24
25
26
27
28
29
30
31
1--1-74
2
3
ft
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20 .
21
22
23
24
25
26
27
28
29
30
31

Total
No. Gal.
6 22100

14 50700

8 31300

9 30200
9 32200

16 57800

8 25200


17 72900

20 76200

8 29400
7 26400
8 28000
7 26000

22 84300
Sunday
10 37700
8 28200
8 27800
12 45200

16 61300
Sunday
8 30500
8 28200
9 32100
7 26200

17 65900
Sunday
8 28500
10 39100
8 28800


Avg.
Gal.
3683

3621

3912

3356
3578

3612

3150


4288

3810

3675
3771
3500
3714

3832

3770
3525
3475
3767

3831

3812
3525
3567
3743

3876

3562
3910
3600


7. of
Total
10.9

10.5

12.5

12.8
12.1

12.9

10.5


11.9

14.7

12.5
10.2
12.2
12.3

21.2

16.2
11.6
11.4
17.5

13.5

12.5
15.2
13.2
16.5

14.8

12.0
18.7
11.8



No.
4

8

4

5
4

7

4


16

3

4
4
3
4

3

5
3
4
3

7

3
2
7
1

6

5
3
4

Tank Trucks

Total
Gal.
28000

58100

28400

36100
28400

53800

27000


1*0300

25300

30600
31600
24800
31200

20658

36000
22700
31700
22300

54200

17000
16500
54900
8300

51800

36700
25400
32800


Avg.
Gal.
7000

7262

7100

7220
7100

7686

6750


9519

8433

7650
7900
8267
7800

6886

7200
7567
7925
7433

7743

5666
8250
7843
8300

8633

7340
8467
8200


% of
Total
13.8

12.1

11.4

15.4


12.0

11.3


19.6

4.9

13.0
12.1
10.8
14.7

5.2

15.4
9.3
13.0
8.6

12.0

6.9
8.9
22.7
5.2

11.7

15.4
12.2
13.5



No.
22

54

24

23
26

50

25


55

55

23
25
23
20

39

21
25
24
25

45

26
19
20
17

43

23
19
24

Tank Trucks

Total
Gal.
152800

372300

189700

168700
206300

337400

187700


421300

416800

175900
202200
176000
154500

292200

159200
192700
184100
190700

338000

197700
140803
155300
124200

326000

173100
144000
182200


Avg.
Gal.
6945

6894

7904

7335
7935

6748

7508


7660

7578

7648
8088
7652
7725

7492

7581
7708
7671
7628

7511

7604
7411
7765
7306

7581

7526
7579
7592


% of
Total
75.3

77.4

76.1

71.8


75.1

78.2


68.5

80.4

74.5
79.7
77.0
73.0

73.6

68.4
79.1
75.6
73.9

74.5

80.6
75.9
64.1
78.3

73.5

72.6
69.1
74.7

Total
Gallons
Shipped
202900

481100

249400

235000
266900

449000

239900


614500

518300

235900
260200
228800
211700

397158

232900
243600
243600
258200

453500

245200
185503
242300
158700

443700

238300
208500
243800


-------
                   -23-
Top Loading
Bottom Loading
Tank l\ra
4
5
h
7
ii
'}
\ '•
I ;
;;;
13
14
15
10
17
; i<
10
".0
21.
7.2
2.T
24
:"i
?•!>

Total
No. Gal.
20 74500
Sunday
6 22400
10 35400
9 31800
24500

13 49800
Sunday
11 43700
9 32200
8 24800
9 26300
4 14800
7 22500
Sund.iv
Holiday
1.5 56800
9 27600
13 45900

19 70200
Sunday
9 26000
/, 74 9 nn
'I i-^t.CVA'
7 34600
11 34100

36 74900
Sunday
10 '32100
6 25300
7 22600
7 25100

I? 46400
Sunday
}', 32600
6 24800
10 39100
4 16000

17 54900
Sunday
S 28400
10 33300
10 34200
10 35000

15 55700
Sunday
7 24300
30 34? 00

Avg.
Gal.
3725

3733
3540
3533
3500

3831

3973"
3578
3100
2922
3700
3214


3787
3067
3531

3695

2056
l.n~>'\
*•• 1 I. ' .1
4943
3100

4681

3210
4217
3229
3586

3569

3260
4133
3910
4000

3229

3550
3330
3420
3500

3713

3471
3 A 20

7. of
Total
14.1

10.2
13.8
11.7
11.9

11.3

14.6
12.8
9.6
10.8
7.0
8.9


17.9
11.8
17.1

18.9

19.4
ion
1 j . O
22.0
16.0

12.5

10.6
9.4
8.8
13.8

11.7

15.3
11.0
15.4
6.2

14.5

12.7
13.3
13.1
14.9

13.6

10.0
13.5


No.
3

4
3
5
4

3

7
9
7
6
5
2


11
4
5

12

3
•)
£m
3
4

11

5
2
6
4

7

9
4
7
3

4

3
2
4
6

7

8
4
Tank Trucks

Total
Gal.
23100

27400
25800
41700
28000

24300

58000
66900
51700
44800
41100
11000


82.300
31400
38500

86900

281.00
1 ROOO
JL O • ! IV
23100
34700

89300

40600
17500
45200
31300

52400

67100
35800
52300
20400

29900

21900
14200
32800
43200

47100

52600
31200

Avg.
Gal.
7700

6850
8600
8340
7000

8100

7286
7433
7386
7467
8220
5500


7482
7850
7700

7242

9367
onfiO
i \j\j\f
7700
8675

8118

8120
8750
7533
7825

7486

7456
8950
7471
6ROO

7475

7300
71.00
8200
7200

6728

6575
7800

7« of
Total
4.4

12.6
10.0
1.5.3
13.5

5.5

16.9
26.7
20.1
18.4
19.6
4.4


26.0
13.4
14 . 3

23.4

20.6
14 7
J r • /
14.7
16.3

14.9

13.4
6.5
17.6
17.2
'
13.1

31.5
15.9
20.6
8.0

7.9

9.8
5.7
12.6
18.3

11.5

21.6
12.3


No.
57

23
26
27
20

49

28
21
25
24
22
29


23
23
24

29

1.1
H
13
19

57

30
30
25
16

39

15
23
23
29

39

27
30
29
25

40

26
?.8
Tank Trucks

Total
Gal.
429700

1691.00
195600
199000
154200

368300

206300
151800
180700
172900
154500
218400


177500
1.75100
183900

213700

S2000
80000
99400
144400

43.3800

229900
226100
188800
126100

299900

113200
164400
162700
219600

293700

172800
202400
193400
157300

306600

166300
188500

AVR.
Gal.
7538

7352
7523
7370
771.0

7516

73 6S
722rt
7228
7204
7023
7531


7717
7613
7662

7369

If; 54
7273
7646
7600

761.0

7663
75.37
7557.
7881

7690

7547
7148
7074
7572

7531

6400
6747
6669
6292

7665

6396
6732

7. of
Total
81.5

77.2
76.2
73.'0
74.6

8312

68.5
60.5
70.3
70.8
73.4
86.7


5(1.1
74.8
6R.6

57.7

60.0
6fi.5
63.3
f-7.7

72.6

76.0
84.1
73.6
69.0

75.2

5.3.2
73.1
64.0
85.8

77.6

77.5
81.0
74.3
66.8

74.9

68.4
74.2
Total
Gallons
S h 1 p pc d
527300

218900
256SOO
272500
206700

447400

7,01000
250900
257200
244000
2iMM
7.5190')


3? -600
2.34100
26K1GO

370800

136700
] i ""5 o n
1 5 7 1 Of)
7.1. WO

598000

307.600
?.6vQ,900
256600
182500

398700

212900
225000
254100
256000

376500

223100
249900
260400
235500

409400

243200
253900

-------
                    -24-
Top Loading
Tank Wacons


Date
3-27-74
28
29
30
31
it- -I.- 74
2
3
4
5
6
7
8
9
10
11
12
13
14
IS
1ft
17
1»<
19
20
21
22
23
24
23
26
27
28
29
30
b--l-74
2

Total
No. Gal.
9 32600
8 27500
9 32400
6 22800
Sunday

17 55900
10 33800
9 29000

14 48400
Sunday
8 26200
10 34100
8 26800
9 29200
Holiday
10 33200
Sunday
9 31700
7 22400
10 34100
9 30100

17 62000
Sunday
7 25600
6 22900
8 28500
12 44300

17 62300
Sunday
5 " 18600
7 24200
8 26600
8 26600

Avg.
Gal.
3622
3437
3600
3800


3288
3380
3222

3457

3275
3410
3350
3244

3320

3522
3200
3410
3344

3647

3657
3817
3562
3692

3665

3720
3457
3325
3325

7. of
Total
11.9
13.8
13.5
9.2


12.9
11.9
11.4

10.2

9.6
15.9
10.0
10.0

10.8

11.5
9.9
14.9
12.5

12.5

9.5
8.2
11.5
17.8

11.0

6.2
9.6
9.4
8.4

Tank

Trucks

Total AVR.
No.
6
4
5
4


12
10
6

12

5
5
7
6

5

4
5
7
3

11

3
11
1
3

9

10
9
5
9
Gal.
39800
26100
36500
32500


95500
76200
43100

85400

39200
32300
46800
40400

38400

26700
33900
35000
23400

78700

23900
76000
6100
19500

64100

76400
68500
32400
62800
Gal.
6633
6525
6500
8125


7958
7620
7183

7116

7840
6460
6685
6733

7680

6675
67SO
5000
7800

7154

7967
6909
6100
6500

7122

7640
7611
6480
6978
Tank Trucks

7. of
Total
14.6
13.0
15.6
13.1


21.9
26.9
16.9

18.0

14.3
15.0
17.5
13.9

12.6

9.7
15.0
15.3
9.8

15.9

8.9
27.0
2.4

•
11.4

25.3 '
27.1
11.4
20.0


No.
30
22
26
29


38
23
24

45

27
20
26
29

31

28
23
21
25

47

29
24
29
25

58

27
21
30
30

Total
Gal.
200600
146300
169900
192800


284000
173400
183000

341200

207800
148700
193900
221000

234400

216500
170300
159400
186000

354800

220200
182100
213600
184400

438600

206900
160000
225300
225300

AVR.
Gal.
6686
6650
6534
6648


7473
7539
7625

7582

7696
7435
7457
7620

7561

7732
7404
7590
7440

7549

7593
7588
7366
7376

7562

7663
7619
7510
7510

% of
Total
73.5
73.2
70.9
77.7


65.2
61.2
71.7

71.8

76.1
69.1
72.5
76.1

76.6

78.8
75.1
69.8
77.7

71.6

81.6
64.8
86.1


77.6

68.5
63.3
79.2
71.6
Tctal
Gallons
Shirocd
273000
199900
239800
248100


435400
283^00
255100

475000

273200
215100
267500
290600

306000

274900
226600
228500
239500

495500

269700
281000
248200
248200

565000

301900
252700
284300
314700
                                                 Average    291,157

-------
                                        -25-
                                    APPENDTX II

                   ANALYSIS OF VAPOR COUJ-CT ING EFFECTIVFNESS
 Sunday



 Holiday


 Sunday
 Sunday
Sunday
Sunday



Date
11-12-73
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30
12-1-73
2
3
4
5
6
7
8
9
10
11
12-12-73
13
14
15
16
17
18 '
19
20
21
22
23
24
Displaced Gases
to Oxidizcr
Ambient T & P
Ft3
35100
34000
16100
19100
20300
17500

36600
13900
32700

15000
23700

28200
27500
18300
25900



70500
24600
38600
19500
15300


56400
24000
28600
28700
25300


40600
11600
19000
17800
6600


33100

Gasoline
Shipped
Gallons
310ROO
281900
262000
273400

464500

291600
275000
295900


452000

272600
294300
2671.00
277400
236000 }


537400 )
288300
288200
285800

609500 ]
\
i
285000 )
269700
285100
293100
246300
255400

239700 - •'
191700
290200
202900




  Collecting
 Effectiveness
Volume Burned 7
Volume Displaced

    0.84
    0.90
    0.46
    0.52

    0.61

    0.94
    0.38
    0.83
    0.64

    0.77
    0.70
    0.51
    0.70
                                                                   0.68
                                                                   0.64
                                                                   1.00
                                                                   0.51
                                                                   0.60
                                                                   0.67
                                                                   0.75-20
                                                                   0.73
                                                                   0.77
                                                                   0.61
                                                                   0.45
                                                                   0.49:
                                                                   0.66
                                                                   0.41

-------
                                     -26-
Holiday
Sunday




Holiday











Sunday
Sunday
Sunday
Sunday
Sunday
Sunday
Date
12-25-73
26
27
28
29
30
31
1 — 1-74
2
3
4
5
6
7
8
9
10
11
12
13
l/i
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30
31
2—1-74
2
3
4
5
6
7
8
9
10
11
12
13
14
Displaced Gases
to Oxidizer
Ambient T & P
Ft3

11700
15200
14000


364 00

27300
11300
27100


36400
21100
10900
7300
6700


21.900

45100
15500

Winter Test Interval
System Overhaul


29030
19490
17380


60990
27360 .
31340
28500
31530


51365
30765
32415
22480
31215


52595
28890
33095
26590
Collecting
Gasoline Effectiveness
Shipped Volume Burned f
Gallons Volume Displaced

235000
266900
)
449000 (
(
239900 )

*
614500 f
)
518300 f
(
235900 )
260200
228800
211700
)
39 71 53 (
(
232900 ;
243600 |
243600 /
258200





242300
158700
)
443700 \
(
238300 ;
208500
243800
267700
)
527300 (
(
218900 ;
256800
272500
206700

442400 (
(
301000 ;
250900
257200
244000

0.37
0.43



0.55


0.47



0.63
0.61
0.36
0.26



0.34

0.69
0.45





0.90
0.92



0.86
0.98
0.96
0.80



0.83
0.90
0.89
0.81



0.84
0.86
0.96
0.82

-------
                                      -27-
               Date
Saturday
Sunday
Holiday
Saturday
Sunday
Saturday
Sunday
Saturday
Sunday
Saturday
Sunday
Saturday
Sunday
2-15-74
  16
  17
  18
  19
 . 20
  21
  22
  23
  24
  25
  26
  27
  28
3--1-74
   2
   3
   4
   5
   6
   7
   8
   9
  10
  11
  12
  13
  14
  15
  16
  17
  18
  19
  20
  21
  22
  23
  24
  25
  26
  27
  28
                             Displaced Gases
                               to Oxidizcr
                              Ambient T &-P
                                  20880
43740
12880
25355
29700
18825
                                  25410
                                   9540
                                  16000
                                  19825
                                  30475
                                  60320
                                  35300
                                  30660
                                  19190
                                  23130
                                  41355
                                  28525
                                  23760
                                  26280
                                  14455
                                  56355
                                  29225
                                  32475
                                  29260
                                  23305
                                  80445
                                  32670
                                  24750
                Gasoline
                Shipped
                Gallons

                 210400
                 251900
316600
234100
268300

370800

136700
122200
157100
213200

598000

302600
268900
256600
182500

398700

212900
225000
254100
256000

378500

223100
249900
260400
235500

409400

243200
253900
273000
199900
               Collecting
              Effectiveness
             Volume Burned 7
             Volume Displnccd

                 0.74
                                                                    0.74
                                                                    0.81
                                                                    0.83
                                  0.65
                                  0.58
                                  0.76
                                  0.70
                                  0.75
                                  0.98
                                  0.89
                                  0.79
                                  0.79
                                  0.95
                                  0.70
                                  0.77
                                  0.88
                                  0.87
                                  0.93
                                  0.93
                                  0.86
                                  0.90
                                  0.93

-------
                                              -28-
                              Displaced Cases
 Snturday
 Sunday
 Saturday
 Sunday
Holiday

Sunday
Saturday
Sunday
Sunday
to Oxidizer Gasoline

Date
3-29-74
30
31
4—1-74
2
3
4
5
6
7
8
9
10
11
Ambient T
Ft3
26200


50290
28300
36320
29990
25260


41260,
21700
30615
32335
New vacuum-break valves
12
13
14
15
16
17
18
19
20
21
22



26
27
28
29
30
5—1-74
2



66430
28120
2330
32280
27710


66990

& P Shipped
Gal Ions
239800
J 248100 \
( (
\ (
1 435400 J
283400
255100
) )
I 475000 I
(
1 273200 ;
215100
267500
290600
installed on 5 trucks

306000 >

274900 ,
226600
228500
239500
) )
( 495500 I
( (
) 269700 )

Spring Test Interval

34210
31110
14260
23440
30790
36980
35S70
.


)
301900 j
252700
284300
314700
  Collecting
 Effectiveness
Volume Burned -
Volume Displaced

     0.82
                                                                     0.86
                                                                     0.96
                                                                     0.88
                                                                     0.66 * Vacuum valves
                                                                     0.75    omitted on
                                                                     0.86    cleaned trucks
                                                                     0.83
                                                                     0.86
                                                                     0.93
                                                                     0.08 * Power failure,
                                                                     1.01    Oxidizer out
                                                                             of service
                                                                     0.93
     0.86

     0.93
     0.91
     0.97
     0.85

-------
                                 -29-

                         APPENDIX III


                         DESIGN MANUAL
                    Philadelphia Terminal
              Vapor Recovery and Oxidation  System
                           Index
     General Information

     A.  Vapor Control Facilities
     B.  General Description of Process
     C.  Plot Plan
II   Process Flow

     A.  Vapor Collection
     B.  Vnpor Storage
     C.  Vapor Enrichment
     D.  Vapor Oxidation
     E.  Compressed Air System
III  Start-Up Procedure

     A.  General
     B.  Initial Start-Up
     C.  Normal Start-Up
IV   Normal Operating Procedure

     A.   Genera 1
     fl.   Checking and Maintaining Critical Bouipment
'•'    Cold Weather Procedure


VI   Shutdown Procedure

-------
                                        -39-
                            Philadelphia Terminal
                    Vapor Recovery and Oxidation System

I   General Information

    A.  Vapor Control  Facilities

        A recent ordinance of iho City of Philadelphia requires that all
        hydrocarbon vapors wilh a vapor pressure greater lhan 1.5 psi
        absolute  (such as gasoline) resulting  from  truck or other loading operation
        be collected and disposed of in such a manner that no more than 10%
        would be discharged into the atmosphere.  To comply with this or-
        dinance Amoco examined several methods of vapor recovery. Since
        the cost of vapor recovery was high compared to the small quantity
        of liquid recovered, it was decided to oxidize the vapors.  The
        products of combustion      (primarily water vapor  and carbon
        dioxide)are not air pollutants and are  acceptable for discharge into
        the air.  Amoco accordingly designed and built  a   vapor oxi-
        dation  plant which  converts  98% of the truck loading vapors into
        harmless components for  discharge  into the air.

    B.  General Description of the^ Process

        This vapor control and oxidation plant consists of the following
        parts:

        1.  A  vapor collection system
        2.  A  vapor holder  for storage
        3.  A  vapor enrichment system
        4.  A  vapor disposal or oxidation  system

        The vapor'collection system consists of two sub-systems, namely,
        the bottom loading  system and the top loading system.   In the
        bottom loading  collection  system the truck vapor spaces are piped
        via a common  header to a dry break  connection near the truck
        manifold.  This dry break  is mated to one attached  to the vapor
        line at the loading dock thus allowing the vapors expelled by the
        loading operation to be conveyed to the vapor holder.  In top loading
        an air operated combination loading and vapor arm is inserted in the
        truck dome. The pressure created by loading forces the vapor through
        a spring loaded check valve into the vapor section of the arm, where
        it is conveyed  to the vapor gathering system and thus to the vapor
      .  holder.
        Since the volume of vapor produced varies considerably from
        hour to hour and the oxidizer consumes at a cons'tant rate, it is
        necessary to use a vapor holder for storage. The vapor holder con-
        sists of a tank with an internal flexible diaphragm giving a vari-
        able volume of about 5000 c.f. between lower and upper limits.
        The diaphragm is attached to an external reading level gauge con-
        taining upper  and  lower limit switches which are used to start
        and stop the oxidation process.

-------
                                 -31-
     Gasolir.c vapors collected from truck loading are normally ovcrrich,  that
     is, they arc above the flammability range which is normally about
     li% to 9% of hydrocarbon by volume with air.  This normally does
     not present a problem in warm weather when the gasoline vapor
     air saturation point is in the neighborhood of 50%;  however, in cold
     weather when the saturation point drops to 2S% or less and a new
     truck is placed in service, an inordinate amount of air is introduced
     to the system which can drop the vapor to near the flammable range.
     To avoid this, propane is introduced into the vapor stream to keep
     the air-vapor ratio at or above the 11% level. Instrumentation is
     provided to measure both the oxygen level and the density of the
     vapor and at  a critical level to introduce propane into the stream en-
     tering the vapor holder.  In the event of an instrument failure and to
     ensure  safety, a temperature-flow instrument is installed to in-
     troduce propane at any time Ihc temperature fails below 15° F.

     The vapor is  disposed of by burning it in an oxidizer  at a  rate of
     about 100 c.f.m.  A vapor blower boosts the pressure of the vapor
     stream from the i inch of water in the vapor holder to  14 inches of
     water.  An adjustable pressure control valve then reduces the pres-
     sure to a proper burning level which is about 4 inches of water. An
     air blower supplies the oxidizer with a constant 6500 c.f.m. air supply.
     Since the temperature of the gas leaving the oxidizer cannot exceed
     1500°F  in order to limit the  possibility  of excess  NOX,  and the
     composition of the gasoline vapor can vary over a wide range, the
     vapor  flow to the burner is regulated by  a  temperature control
     valve which controls the amount  of vapor  entering the oxidizer so
     as  to maintain a temperature  of  1400°F.

C.  Plot Plan

    A plot  plan showing the  location of the vapor oxidation  facilities
    at the  terminal and the relation of the facilities to the other
    operating areas is given  in the attached drawing  31-57-023  of
    this appendix.

-------

-------
                                     -33-
II   Process Flow

    Refer to  the P & I diagram of the text,  drawing  31-520, Figure 2.

    A.  Vapor Collection

        Truck loading is performed at two bottom and one top loading racks.
        The gasoline loading rates at each rack are:

            Amoco Premium        350  gpm
            Regular               350  gpm
            Amoco                 600  gpm

        This loading  is accomplished through ticket -printing set stop
        meters.

        In bottom loading, the truck is loaded through a dry break
        connection on  the truck manifold which mates  with a dry break
        connector on  the bottom loading arm.   The vapors  created by
        loading  are collected from each compartment in a vapor mani-
        fold which terminates in a dry break  connection near the truck
        manifold.  A  three  inch dry  break coupling is mated to  the
        truck vapor connection  and the vapors are conducted through a
        three inch hose  to four inch pipe header and  thence via a 6~
        inch header to the vapor  holder.  As each compartment  is loaded,
        it is necessary to open  the liquid manifold valve to the compart-
        ment.  It is also necessary to  lift the vapor vent valve to the com-
        partment otherwise  the  loading rate may be  restricted  since it re-
       'quires a pressure of one  p.s.i. to open this vent.

        Flow of product is also controlled by the truck grounding clamp which
        is intergally wired to the pump and solenoid valve circuit.  The bottom
        loading trucks have high level switches in each compartment to prevent
        overfilling .  If a compartment  is overfilled it must be  drained
        down below the  high level switch before loading can proceed
        on the other compartments.  There  is also a shut down  sv/itch
        in the dispatcher's  building which can stop all rack loading.

        Top loading is accomplished  through an air operated combination,
        liquid and vapor loading  arm which is raised and lowered by an air
        cylinder^using 60 psi air.  The head of the loading arm is forced down
        by the air pressure against the truck dome forming a tight  seal.  As  the
        head is  forced into the  dome a collar  is raised which actuates  a
        valve that lets air into  the liquid  shut off valve making  it opera-
        ble.   When the liquid line valve and the set stop  valve are opened.
        the liquid flowing  into the tank forces open  the vapor  check valve
        in the loading head when the pressure reaches one-half p.s.i.  The
        loading head contains a float which when the liquid level is too high

-------
                                -34-
    will bleed the air from the leading valve thus closing it.  If for any rea-
    son the arm comes out of the dome during loading the collar on the head
    will retract actuating the air valve which will bleed air from the loading
    valve thus closing it.  If the vapor line is blocked, the pressure in the
    compartment will force the loading head out thus stopping the product
    flow.  Flow is also controlled by the grounding clamp and the switch
    in the dispatcher's building.

    The vapor piping system  isolates each truck  loading rack by
    means of a flame  arrestor  installed in each line to the bottom
    loading racks.  Also  the vapor collection piping is isolated from
    the  vapor holder  by a flame arrestor in the 6 inch vapor header.
    These flame arrestors are to prevent the propagation of a flame
    between truck racks and  between the truck racks and the vapor holder.

    The pressure in the vapor collection system will  vary depending
    on the truck loading  rate and  the number of  trucks  loading simul-
    taneously.  It  will normally be no  more than one p.s.i.  at the
    truck to as little as one-quarter  (1/4) inch of water at the vapor
    holder. Should the hand operated valve at the entrance to the vapor
    holder be closed there is a relief valve in the six inch vapor line
    set  to open at 6 inches of water  pressure.

B.  Vapor Storage

    If three trucks  were simultaneously loading two gasolines each, they
    would be creating vapor at the rate of 300 c.f.m.   By the same
    token if ,one truck was loading one product the vapor production
    would be about 50 c.f.m.   Since the oxidizer  burns vapor at about
    100 c.f.m., and the vapor production is variable, it is necessary to pro-
    vide storage for the vapor.  This vapor storage consists of a tank, or
    holder, containing a flexible internal diaphragm which rises and falls
    with the amount of vapor introduced or withdrawn from the tank.

    The vapor holder contains about 5000 c.f. of operating vapor space
    from a gauge reading of 0'-3"  to 24'-0".  However,  since the vapor
    entering  the tank could be greater than the burner can handle  the
    operating  limits of the diaphragm are set at 4'-6"  and 17'-0"  which
    gives an  operating capacity of 3000 c.f.

    The-operating  pressure of the  diaphragm is 1/4 inch of water.   To
    protect the diaphragm there is a relief valve set at  1.25 inches of
    water pressure and 0.865  inches of water vacuum.   In  the event of
    any condensation in  the vapor holder a 1500  gallon spherical drain
   -tank is provided which is connected to  the sump  in  the center of
    the  holder by  a 2"  line.   Since the holder is  under vapor pressure
    the  underground tank has a 2  inch  pressure equalizing line to the holder.

-------
                                 -35-
C.  Vapor Enrichment

    The flammabilily range of gasoline vapor is generally between H%and 9%
    gasoline to air by volume. Normally the vapor in trucks, in gasoline service
    is well above this range especially if they are top loaded. .Also, after a truck
    dumps its load there is enough product clingapc left in the compartment
    to enrich the vapor space during the return trip.  However, in the case
    of a switch load or a gas free compartment,  there is a chance that the flam-
    mable range could be reached especially in  the case of bottom loading.

    Temperature  is also a factor in the saturation of  gasoline vapor.
    As the temperature drops the heavier molecules (pcntanes and hexanes)
    begin to cemlcn.se leaving the lighter molecules.  Saturations at various
    temperatures are approximately as follows:

            0°F               14%
          30°F               25%
          50°F               33%
          70°F               40%
          90°F               55%


    When the temperature gets near C°F the saturation approaches  the
    upper flammable limit.

    To protect against the vapor being  in the  flammable  range propane
    is injected into the  vapor pipe at the inlet to the vapor sphere.
  _  To control-the injection of propane  three  instruments  have been
    installed in the 6" vapor line,  as followr,:

    1.  ACH-100  (Analysis Control High)  is a Beckman Oxygen Ana-
       lyzer which  continuously measures the oxygen content in  the
       vapor  stream.   When the oxygen  reaches a level of 18.6%
       corresponding to a hydrocarbon saturation of 11% it opens  the
       solenoid  valve SDV  100  (Figure 2) allowing propane to enter
       the stream.  The  propane is metered through an orifice FO-101
       at a  rate of  about  17 c.f.m.

    2.  DCL-100 (Density Control Low) is a Ranarcx density control
       meter that continually measures the density of the vapor
       stream.  When the density reaches a low level of 1.13
       corresponding to a saturation of 11% it opens the solenoid
       valve SDV ]CO allowing propane to enrich the stream.

    3.  TCL-100  (Temperature Control Low) measures the temperature
       and when it drops  to 15° F, or lower, and  the FS-100  (flow
       switch) indicates vapor flowing in  the 6" vapor  line it will
       open the solenoid  valve SDV  IOC  to begin propane injection.

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                                 -36-
    In addition to the three automatic means of injecting propane, a hand
    valve by-pass of SDV 100 is provided in the event operator sampling in-
    dicates the need for additional propane enrichment.  An analysis port
    AP-100 is provided en the vapor holder for sampling the contents.

    Since the vapor pressure of propane falls to 23 psi at 0° F there is danger
    of having insufficient pressure to  enrich the vapor.  To forestall this dif-
    ficulty an external heating coil is installed on the propane tank controlled
    by a thermostat (TCL-101) set to maintain a temperature of 15° F.

    In the event the level in the propane tank should fall to 12 inches, or below,
    a red light will show on the board. An alarm (LAL-100) is connected to
    this switch to sound at low propane level.

D.   Vapor Oxidation

    1.  Flow To Oxidizer

        Provided  the air blower and the pilot light in the oxidizer
        are operating, when the diaphragm in the vapor holder
        reaches its upper operating limit of 16 feet the ground level
        reading gauge actuates  a built in switch (LSH-200) which
        starts the vapor blower and the alarm horn (LA-200) . The
        vapor blower  takes suction through a three inch line at
        tank pressure and boosts the pressure to 14 inches
        of water at 100 c.f.m.   Downstream from  the  vapor
        blower is  an  adjustable pressure regulator  (PCV-200)
        which is  set to control the vapor pressure to the burner
        at 4 inches of water.

       At the same time the vapor blower starts  an electric
       impulse opens two shutdown  valves (SDV-200 and
       SDV-201).  When SDV-200  starts  to open, it will shut
       off the alarm  horn (LA-200) .  This alarm horn will
       come on again only if SDV-200 closes before it re-
       ceives a closing  signal from low level switch  (LSL-200).
       SDV-200 will  open only if the low pressure switch
        (PSL-200)  and the high pressure switch  (PSH-201)
       indicate the correct pressure in the vapor line.  PSL-200
       is set  to shut down SDV-200  if the pressure falls below
       2 oz/s.i.  (3-1/2  in. water).  PSH-201  is  set to shut down
       SDV-200 s*hould the pressure in the line exceed 6 oz/s.i.
       (10-1/2 in. water).

       At the same time SDV-200 and SDV-201 are actuated vent
       valve (SDV-202) is closed. This valve vents the 3" vapor
       header between the block valves to prevent pressure build

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                             -37-
up during shut down periods that would pass the limit of PSH-
201 and not allow SDV-200 to open.

Since the oxidizer operates en the principle of
constant  air supply with variable  fuel supply to obtain
proper combustion, the vapor supply  reaching  the
burner is regulated  by the Maxon  burner control valve.
The operation of the valve is ccnh-olled by a Barber-
Colman  537G temperature indicating controller (TIC-200)
which indicates  the burning  temperature and is normally
set to maintain a burning temperature of 1400°F.   A ther-
mocouple  in the furnace sends an electric signal  to
TIC-200 which in  turn furnishes a signal to the liarber-
Colman PO2R  current to pneumatic transducer (TY-200).
TY-200 is operated on 20 psi instrument air.  This ins-
trument converts the electric  signal it receives lo a pneu-
matic signal which operates the burner  control valve.
The pneumatic control  line between TY-2CO and the burner
control valve  contains  a shutdown  valve  (SDV-203) that
opens to allow air pressure lo reach the burner control valve
by the signal that opens the safety valve SDV-200.  When SDV-200
closes, SDV-203 closes the line to TY-200 and vents the line to
the burner control valve to prevent overpressure of the elements.

A pressure indicator (PI-200) is located  in the three  inch
vapor header  downstream of the burner control valve.  PI-
200 indicates  the set pressure (4"  of water) to the  burner.
Flame arrcs"tors are  located in the 3 inch vapor line,  one
near the burnr-r and one near the  vapor holder.  These
flame arresters are to  prevent any backflash from the
burner reaching  the vapor holder.

Two Barber-Colman  model 72F, high temperature shut downs
(TSH 201 and TSH 202)  are  set to limit, the  oxidizer tempe-
rature at  no more than 1500°F.   If a. temperature of 1500°F
is  exceeded ons or both of these  switches will close the
main vapor line shut down valve  (SDV-200) . The closing of
SDV-200 will sound the alarm horn (LA-200) and close the
blocking valve (SDV-201).

When th"e  vapor holder diaphragm  reaches the bottom,
a reading of 4 feet-6 inches on the level indicator,
the level switch low  (LSL-200) will  be actuated which
will shut  down the vapor blower,  close valves SDV-
200. SDV-20]  and SDV-203,  and open the vent valve
SDV-202.   The unit  will remain in this  shut down status
until the level switch  high  (LSH-200)  on the vapor
holder again starts the cycle.

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                                -38-
2.   Oxidizer
    The vapor is burner! in a. hydrocarbon oxidizer which is
    designed to burn a mixture of butanes and pentanes with a
    vapor-air saturation  of between 7-1/2% and 50%.   The oxi-
    dizer  is fed a constant supply  of air  at a rate of 6500 cfm
    with the  vapor supply being regulated to maintain an oxi-
    dation chamber temperature at  or below  1400°F.

    The oxidizer consists of  a burner chamber  and an oxidizing
    chamber.  The burner chamber houses the Maxon Combusti-
    fume gas burner  system  along  with the pilot light,  spark
    igniter and flame rod.  The burner  has  a maximum capacity
    of 10,200,000 BTU/HR.  The normal oxidizing rate  is about
    100 c.f.m.   The oxidizing chamber is approximately. 10'-6"
    high with overall outside dimensions  of 5'-6" by  5'-6".   The
    top of the chamber is  20'-7"  above grade.  The  chamber is
    equipped with a stainless steel gravity type rain cap which
    is opened by the air  blower pressure. There is a peep sight
    for flame viewing.

    The constant air supply  to the  burner is  supplied by an air
    blower that delivers  6500 cfm against  a static head  of 2
    inches of water.  The blower is started by a push button
    on the control board provided  the control building air purge
    has been completed.   This fan  must operate before  the pilot
    can be lit.  A pressure switch  (PS-202) is located in the
    discharge duct of the fan and if the fan  stops  for any reason
    it will shut down the pilot and as a result the whole oxidation
    cycle.

3.   Pilot Light

    The burner  section of the oxidizer has a  continuously burning
    propane pilot.  Propane  is supplied  from the 1000 gallon propane
    tank used for  the vapor  enrichment system through an outlet in-
    dependent of the vapor enrichment system.  At the tank outlet there
    is a pressure reducing valve (PCV-201) which maintains downstream
    pressure of 11 inches of water.  A £ inch propane pilot line leads to
    the control rack where an adjustable pressure reducing
    valve PCV-202 further reduces the pressure to 7" of
    water.  A pressure indicator is mounted  on  the  control
    rack that indicates the propane pressure  to  the pilot.

    Propane enters the burner through a solenoid shut down
    valve (SDV-204) which is opened by turning on the burner
    switch (IIS-201) provided the air blower is operating and

-------
                                   -39-
        there is sufficient propane.  When the burner switch
        (HS-201) is turned on,  there is a 60 second delay (KC-200)
        before SDV-204 will open,  then it will only open for 15
        seconds (KC-201)  while the igniter  is operating.   If the
        pilot lights and the flame rod.  (TSL-200) so indicates,
        then SDV-204 will remain open to supply propane  to the
        pilot.   If TSL-200 indicates a  flame before the 15 seconds
        expire the igniter will be stopped.  If TSL-200 is not. satis-
        fied the process must be repeated by pressing the reset
        button.

    4.   Control Building

        The electrical controls are located in the control building
        which is  pressurized by a continuous 300 c.f.m.  purge
        air  blower.  The building  purge air blower must be acti-
        vated for five minutes before  the  oxidation system can be
        started.  The purge air blower is started by a push button
        (HS-202).  When the discharge pressure, activates the  pres-
        sure switch (PS-203) in the duct a  timer (KC-202) is started
        and after five minutes the oxidizer air blower can be started.
        The discharge duct contains an electric heater to maintain 45° F
        in the building.  If the electric heater should fail a propane
        space heater is provided for back-up.

E.  Compressed Air System

    Compressed air is provided for the loading arms and the burner control
    by a Champion VRI-6 air compressor with a 60 gallon storage tank.
    The compressor is operated by a pressure control switch set  to operate
    between a cut in pressure of 150 psi and a cut out pressure of 180 psi.
    A Wilkerson model 1137-3FX air filter is used along with a Wilkerson
    S4103-21-H continuously regenerating  air dryer. Pressure reducing
    valves are used on each branch line to maintain a pressure of 90 psi
    to the loading arms and a pressure of 20 psi to the burner control
    (TY-200).

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                                    -40-
III  Start-Up Procedure

    A.  General
        This start-up procedure is written as a guide for the safe start
        up of the vapor recovery and oxidation system.  Since certain
        hazards are inherent when handling  hydrocarbons and their
        vapors il is necessary that a very rigid and precise procedure
        be followed when  starting the equipment.  The procedure no
        matter how  carefully drawn  cannot cover all conditions that  may
        exist, and the operator should be on alert for  those  situations
        and should  institute such additional  steps as may be necessary
        to cope with them.

        Since the truck loading is in operation  and follows a generally
        known and understood system it will not be covered in the start-
        up procedure.
        The start-up of the recovery and oxidation system follows the
        following general  pattern:

             1.   Start control building purge air
             2.   Place vapor stream analyzers in operation
             3.   Put propane enrichment system on stream
             4.   Check contents  of vapor holder for flammable limits
             5.   Put vapor holder on  stream
             6.   Start air  blower
             7.   Start air compressor
             8.   Put propane pilot light system on stream
             9.   Light pilot

     B. Initial Start-Up

        This procedure is used on either original startup or startup after the
        vapor holder has been taken out of service and gas freed.  It precedes
        the normal start up procedure outlined in the following Section C. The
        following steps shall be taken:

             1.  ,Close both fill and discharge line valves at vapor holder.
                                                            %
             2.   Check that all vapor holder openings are closed.

             3.   Remove pallet from tank vent valve to provide an air
                 vent.

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                                -41-
    4.  Open drain valve in drain tank and close vapor equalizing
        valve.  Check tank to be sure it is empty.

    5.  Purge vapor holder through gauge port of drain tank^with 4000
        s.c.f. of nitrogen.

    6.  Close vent by replacing pallet and fill vapor holder with nitrogen
        (about 6000 s.c.f.).

    7.  If vapor line to truck rack is vapor free, remove a bottom loading
        vapor connection at each rack and discharge the vapor holder.  Stop
        flow before the diaphragm reaches its bottom position (4'-6"on the
        gauge). Otherwise open tank vent.

    8.  Take readings at the vapor holder sample connection with oxygen ana-
        lyzer (obtain from Regional Office). Oxygen should be 2% or less.
        If not, repeat steps 6,7,and 8 until a proper reading is obtained.

    9.  Proceed with normal start-up procedure outlined in Section C omit-
        ting steps 6 and  7.

C.  Normal Start-Up Procedure

    1.  Place all 110V and 440V electrical breakers in control building
        in "on" position.

    2.  Turn on console  power by closing selector switch.

    3.  Start building purge air fan. Air pressure from fan will close
        air pressure switch PS-203 in duct which will energize the purge
        timer control KC-202.  After five (5) minutes the purge timer will
        energize the circuit to the air blower which will be indicated on
        the board by a green "purge complete" light.

    4.  Place vapor stream analyzers in operation.  Normally these units
        remain in operation during periods of shutdown.  However,  in the
        event they are down they should be started or if operating they
        should be checked in the following manner:

           ,a.  Open hand valve at vapor line.

           b.  Turn on unit power.

           c.  Follow start-up and unit check instructions in Appendix D
               for Beckman Oxygen analyzer and Appendix E for Ranarex
               density meter.

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                             -42-
 5.  Place the propane enrichment system on stream being sure to
    complete the following steps:

        a.  Check level of propane in tank and if below 24 inches
            order replenishment.

        b.  Open  all four hand valves on propane line.  Two at
            tank and two at vapor  line.

        c.  Check that bypass valve around solenoid is closed.
6.  Check the contents of the vapor holder through the sample port
    (AP-100) with a combustible gas analyzer.  If vapor4s in flammable
    zone (11% or less hydrocarbon-air mixture) open bypass valve
    around solenoid valve SDV100 on propane feed line.  Check vapor
    holder every ten minutes until  vapor is above flammable limit.
    Close bypass valve.  Omit this  step if initial start-up procedure
    was used.

7.  Open inlet valve to vapor holder.

8.  Open hand operated drain and return vapor valves on undergi-ound
    tank and check to be sure the pump out connection is in place and
    tiBht.

9.  Open all three hand valves in 3 inch Vapor line between vapor
    holder a'nd oxidizer.

10. Start air supply blower to oxidizer.  This fan  cannot be started un-
    less green "purge complete" light is on board. Pressure in the dis-
    charge duct will close the pressure switch PS-202 which will energize
    the burner selector switch and  bring on the board a green "supply
    fan on" light.

11. Start air compressor.  Check instrument air supply controller  to  be
    sure it is set at 20 p.s.i.  Loading arm supply controller should be
    between 60 and 90 p. s . i.

12. Put propane pilot system on stream by opening hand valve at tank and
    hand valve in 2" propane line before control valve PCV 202.  Check
    pressure gauge PI 201 which should  read 11 inqes water (4 inches
    water when pilot is lit).

13. Light the pilot by turning the burner selector switch  (HS-201)  to "on".
    The built-in timer (KC-200) will after a 60 second delay energize the
    igniter and open the pilot gas valve (SDV-204).  Once the pilot is esta-
    blished and detected by the flame rod (TSL-200) the igniter will be
    de-cnergi7.ed and the pilot gas valve (SDV-204) will remain open.  If
    the pilot is not proved in  15 seconds  (KC-201) the igniter stops and

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                                       -43-
            the pilot gas valve closes. To again start the pilot, it is necessary to
            press the red reset button behind the control board. When the pilot
            is proved a "pilot on" amber light shows on the board.
            i
The unit is now on stream and programmed to operate automatically.

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                                    -44-
IV. Normal Operating Procedure

    A.  General

        The unit is programmed  to operate automatically when  the. high
        vapor level switch turns on the unit and will automatically stop
        when  the low vapor  level switch is  closed.  The  air blower
        and pilot light will operate continuously.  Positive action by the
        operator is not required  except to monitor and  maintain the
        equipment and handle emergencies.

        In the  normal operating sequence when the level  of the vapor in
        the holder reaches  17'-0" on the gauge (LI-200) the  level switch
        high (LSH-200) will close and  start the  vapor blower along with
        the alarm  horn.   The pressure  from the vapor  blower  will close
        the low pressure switch  (PSL-200) and provided  the high pressure
        switch (PSH-201) is satisfied will bring  a green light on the
        board indicating "gas pressure  on" . The energizing  of the
        vapor blower and  the satisfying of the pressure switches  (PSL-200
        and PSH-201) will open the safety valve  (SDV-200) provided the
        two high temperature switches  (TSH-201  and TSH-202) in the
        oxidizer are r.ctisfied.   The opening of the safety valve (SDV-200)
        will do three things, narn«ly:

            1.   Stop the alarm horn which will normally  have
                been sounding for about 3 to 5 seconds.

            2.   Open the blocking solenoid  valve  (SDV-201)  and
                close the vent valve (SDV-202)  thus allowing the
                vapor stream to  reach  the burner.

            3.   Bring an. amber  light on the board indicating
                "main gas on" .
        Each time the vapor saver switch (LSH-200) closes it will  sound
        the alarm horn (LA-200) until  the safety valve (SDV-200) begins
        to open.  Opening of this valve will silence the horn.  If the
        safety valve  (SDV-200), does not open the horn will continue to
        sound.   If the valve  (SDV-200) should close during  the  burning
        cycle for' some reason other  than being  closed by  the low level
        switch (LSL-200), the horn will begin to  sound, indicating-trouble
        in the unit.  Should  the horn  continue to sound, press the horn
        off button on the control panel  thus bringing .on;the  trouble light, and
        proceed  to find the trouble.

        Once the valves  (SDV-200 am  SDV-201) are opened, the  amount
        of vapor reaching the oxidizer is controlled by the Maxon  burner
        control  valve.  The operation of this valve is  controlled  by a

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                                 -45-
    Darbcr Colcman 537G, board mounted, temperature indicating
    controller  (TIO200) which measures the temperature in the
    oxidizer  and  transmits it to the Barber Coleman PO2R
    electric pneumatic transducer (TY-200).   TY-200 then  '
    opens or closes the  Maxon burner control valve pneu-
    matically to maintain the  set temperature of  1400°F,  pro-
    vided there is  sufficient vapor concentration to reach the
    temperature,  otherwise it will operate wide  open.

    When the vapor holder level reaches 4'-6" on  the  gauge
    (LI-200)  the  level switch (LSL-200) will  open  thus shutting
    down the vapor blower, safety valve  (SDV-200),  and blocking
    solenoid  valve  (SDV-201) and opening the vent valve (SDV-202)
    Also the  valve  on the air line from the current to pneumatic
    transducer (TY-200) to the Maxon burner control  valve will
    close.  The oxidation  cycle thus stopped will  remain so  until
    the level switch high  (LSH-200)  again starts the cycle.

B.  Checking and Maintaining Critical  Equipment

    To comply  with the  law, it is necessary that we keep the  oxida-
    tion  unit in operation  at lop efficiency at  all times.  To  keep a
    plant in  continuous  operation  requires constant checking  and
    preventative  maintenance by the  operators.  It is impossible
    to  set forth a complete list of items 1o be monitored  by the ope-
    rator.  Also  it  is  impossible to provide a  complete maintenance
    list.  The check and  maintenance lists contained herein are  only
    a guide.  The operator should study the unit and the various
    equipment to  determine other areas to be monitored and items
    on which preventalive maintenance can be  applied.

        1.  Daily Check and  Maintenance

            These items  should be checked at the  start of each
            shift:

            a.  Check control board to be sure  unit is
               ready for operation, that is,  purge fan
               on, air  blower  on and pilot on.  If not
               ready for operation return to "Start Up
               Procedure" and bring  unit on line.

            b.  Check Beckman Oxygen Analyzer


            c.  Check Ranarex Density Meter

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                           -46-
    d.  Record date and lime on Brown recorder
        charts for furnace and system  temperature.

    e.  Check any unusual odor in building.

    f.   Check air compressor for oil level, power
        and pressure.

    g.  Check, propane tank for level,  pressure
        and on-'stream condition.

    h.  Check vapor in vapor holder to assure that
        air vapor mixture is at,  or above, 11%.

2.   Weekly Check  and  Maintenance

    The following equipment should be checked once
    a week in accordance with Appendix K:

    a.  Beckman Oxygen Analyzer
    b.  Ranarex Density Meter
    c.  Air Compressor
    d.  Wilkerson Air Drier
    e.  Main Gas Pressure PI-200
    f.   Pilot Gas Pressure PI-201
    g.  Oxidizer Air Blower
    h.  Check drain tank level
    i.   Check space above diaphragm
        for combustible gas.

3.   Quarterly  Check and  Maintenance List

    The following equipment should be inspected and
    maintained once a quarter unless experience indicates
    otherwise:

    a.  Pull flame arrestor banks  and  clean
        as necessary.

    b.  Check pallet in vapor holder relief
        valve  to be sure it is clean and
        operable.

    c.  Check pallet in vapor line relief valve
        to be sure it is clean and operable.

    d.  Check and clean free  vent screens on
        vapor holder.

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                       -47-
c.  Chuck operation of all hand valves.

f.   Check operation of all relief valves.

g.  Change air compressor crank cane oil.
The above list should be added to by the operator
as he finds areas that require checking and main-
taining .

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                                -48-
V .  Cold Weather Procedure

    When the temperature falls to 0°F the  gasoline vapor - air mixture
    could be in the flammable range especially for mixtures of less than
    100% saturation.   To assure we are on the safe side we have selected
    a temperature of  15°F, or below,  as being critical and requiring special
    procedures.

    The  procedure when the temperature goes below 15° F is to be sure that
    our propane injection system is operating properly.  This can be done
    by the following steps:

    1.  When it is expected  that the temperature will go below. 15 °F and
        the propane tank  is  half full, or  below, have the tank filled.

    2.  Check  the vapor in the vapor holder with the explosimeter on
        each shift to  assure  that it is above 11% gasoline vapor air
        mixture. If below 11% turn off burner selector switch on board,
        close hand operated  vapor holder  inlet valve, and  open propane
        enrichment system bypass valve of SDV-100.  Check vapor
        holder  until correct  reading is obtained.  When mixture is at  or
        above the 11% mark  close propane bypass  valve.  Check the
        propane enrichment  system to determine why the mixture was
        not being enriched.   When satisfied the system is working proceed
        to open vapor holder inlet valve  and turn on burner  selector  switch.
        Be sure  "pilot on" light comes on board.

    3.  Check  the propane  tank  pressure  each shift to determine if it is
        35 psi,  or above.   The tank has a heater set to maintain  15°F in
        the tank.  A  pressure of 35 psi corresponds to a product temperature
        of 15°F.

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                                    -49-

VI  Shutdown Procedure

    A.  Normal Shutdown

        This procedure applies  to short periods not longer  than over
        a weekend  or  holiday.

        1.  Close the  inlet and  outlet vapor line valves on  the
            vapor holder.

        2.  Turn burner selector switch  to "off" position.

        3. '  Turn off air supply blower to oxidizer.

        4.  Close propane  supply valve to  pilot at propane  tank-.

        5.  Shutdown  air compressor by  turning off electric
            power switch and closing globe valve at tank outlet.

    B.  Long Term  Shutdown

        This procedure applies  where the unit  is to be shut down
        cither longer than  two days or for  major equipment repairs.

        1.  Complete all steps for normal shutdown.

        2.  Close propane  enrichment hand valves at tank and at
            six inch vnpor line.
                    i
        3.  Place locks on both inlet and outlet vapor  line valves
            of vapor holder.

        4.  Shutdown  both Beckman Oxygen Analyzer and Ranarex
            Density meter by turning off  the power to the instruments
            and closing the gas bottle valves feeding the instruments.

        5.  Turn off building purge  air fan by pressing stop button.

        6.  Turn console power switch to "off".

        7.  Open all 110V and 440V circuit switches in control building.
                 *
    C.  Secure Vapor Holder

        This procedure applies  when it is desired  to place  the vapor
        holder in a safe condition for either long term shutdown or
        work on the holder.   After completing long term shutdown pro-
        cedure, the vapor holder is then inertcd  by filling with nitrogen
        through the drain tank connection, after the drain tank has been
        completely evacuated,  and venting through the sample connection
        as outlined in initial startup procedure.   Test with a combustible
        gas tester using a dilution attachment set at 80% air until a reading

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                             -50-
of 50%L.E.L. is obtained.  The dilution attachment can
be obtained from the Regional Office.  The tank is then
gas freed with air until safe for entrance.

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                          	-51-	
                                 TECHNICAL REPORT DATA
                          (Please read Instructions on the reverse before completing)
 1. REPORT NO.
  EPA-650/2-75-042
                            2.
                                                       3. RECIPIENT'S ACCESSION-NO.
 «. TITLE AND SUBTITLE
 Demonstration of Reduced Hydrocarbon Emissions
    from Gasoline Loading Terminals
             5. REPORT DATE
             June 1975
             6. PERFORMING ORGANIZATION CODE
 7. AUTHOR(S)
                                                       8. PERFORMING ORGANIZATION REPORT NO
  D.C. Walker, H.W.  Husa, and I.  Ginsburgh
 9. PERFORMING ORGANIZATION NAME AND ADDRESS
 Amoco Oil Company
 Research and Development Department
 P.O. Box 400
 Naperville. Illinois 60540	
             10. PROGRAM ELEMENT NO.
             1AB015: ROAP 21AFD-021
             11. CONTRACT/GRANT NO.
             68-02-1314
 12. SPONSORING AGENCY NAME AND ADDRESS
  EPA,  Office of Research and Development
  NERC-RTP, Control Systems Laboratory
  Research Triangle Park, NC 27711
             13. TYPE OF REPORT AND PERIOD COVERED
             Final; 6/73 - 9/74	
             14. SPONSORING AGENCY CODE
 15. SUPPLEMENTARY NOTES
 is. ABSTRACT!"^ report gives results of test work to demonstrate the effectiveness of
  hydrocarbon oxidation for reducing emissions from a gasoline truck loading terminal
  in Philadelphia that pumps about 2 million barrels of gasoline per year. Major
  objectives of the program were to determine control efficiency, to observe opera-
  tional characteristics, and to compare this installation with other known systems.
  Tests run during each of the four seasons showed that the oxidizer safely and
  efficiently disposes of 99+% of the vapor it receives, even in extremely cold weather
  when the  air-gasoline vapor mixture is in the flammable range. Initially, a large
  portion of the vapor from the trucks was not  reaching the oxidizer, primarily
  because of blockage caused by liquid carryover to the vapor collection system. After
  this was corrected, collection and disposal of the vapor exceeded 90%. High efficiency
  and low flame temperatures of the oxidizer limit formation of emissions.
 7.
                             KEY WORDS AND DOCUMENT ANALYSIS
                 DESCRIPTORS
                                           b.IDENTIFIERS/OPEN ENDED TERMS
                         c. COS AT I Field/Group
 Air Pollution
 Hydrocarbons
 Gasoline
 Tank Trucks
 Materials Handling Equipment
 Oxidation
Air Pollution Control
Stationary Sources
Loading Terminals
13B
07C
2 ID
13F
 8. DISTRIBUTION STATEMENT
                                           19. SECURITY CLASS (This Report)
                                           Unclassified
                         21. NO. OF PAGES

                              51
 Unlimited
20. SECURITY CLASS (Thispage)
Unclassified
                         22. PRICE
EPA Form 2220-1 (9-73)

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