f/EPA
           United States
           Environmental Protection
           Agency
           Effluent Guidelines Division
           WH-552
           Washington DC 20460
EPA 440/1 -79/014-b
December 1979
           Water and Waste Management
Development
Document for
Effluent Limitations
Guidelines and
Standards for the

Petroleum Refining
Proposed
           Point Source Category

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         DEVELOPMENT DOCUMENT

             for Proposed

   EFFLUENT LIMITATIONS GUIDELINES,

  NEW SOURCE PERFORMANCE STANDARDS,

                 and

        PRETREATMENT STANDARDS

               for the

          PETROLEUM REFINING

        POINT SOURCE CATEGORY
          Douglas M. Costle
            Admin istrator
          Robert B. Schaffer
Director, Effluent Guidelines Division
          John M. Cunningham
           Project officer

               John Lum
           Project officer

            December 1979
     Effluent Guidelines Division
 Office of Water and Waste Management
 U.S. Environmental Protection Agency
       Washington, D.C.  20460

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                          TABLE OF CONTENTS


Section                     Title                             Page

   I     EXECUTIVE SUMMARY                                     *

  II     INTRODUCTION                                          7
           Purpose and Authority                               7
           Prior EPA Regulations                               7
           Overview of the Industry                            1
           Preliminary Industry Profile                        8
           Industry Survey                                     8
           Wastewater Sampling Program                         9
           Control and Treatment Technology,                   9
              Cost Analysis

 III     WASTE CHARACTERIZATION                               13
           General                                            13
           1977 EPA Petroleum Refining Industry               13
              Survey
           Survey Data Related to Wastewater                  14
              Characterization
           Wastewater Sampling Program Results                15
              RSKERL and B & R Sampling Program               16
              Pretreatment Sampling Program                   18

  IV     SUBCATEGORIZATION                                    87
           Introduction                                       87
           Flow Modeling Effort                               89
              Data Screening and Evaluation                   89
              Regression Analysis                             89
              BPT Model                                       90
              Current Flow Model Development                  91
           Effluent Flow Model                                94
           Use of the Flow Model                              95

   V     SELECTION OF POLLUTANT PARAMETERS                    97
           Introduction                                       97
           Pollutants From Petroleum Refining                 97
              Industry
           Selection of Regulated Pollutants                  97
              for Direct Dischargers
           Selection of Regulated Pollutants                  98
              for Indirect Dischargers
                                 iii

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                                                         Page

  VI     CONTROL AND TREATMENT TECHNOLOGY                 109
           Introduction                                   109
           In-Plant Source control                        109
              In-Plant Treatment Options                  109
                 Sour Waters                              11°
                 Cooling Tower Slowdown                   111
              Chemical Substitutions                      i±2
              Wastewater Reduction and Reuse              112
           End-of-Pipe Treatment
              Biological Treatment
              Filtration
              Granular Activated Carbon
              Powdered Activated Carbon
              Metals Removal                              121
              RSKERL Carbon Studies                       121
              Ultimate Disposal Methods                   lzz
           Existing Technology                            124
              Effluent Concentrations                     126

 VII     COSTS, ENERGY AND NON-WATER QUALITY ASPECTS      189
           Introduction                                   189
           Cost and Energy Requirements of Technologies   190
              Considered
              Biological Treatment                        189
              Filtration                                  191
              Granular Activated Carbon                   191
              Powdered Activated Carbon                   192
              Low Flow Rate System                        192
              In-Plant Control                            193
           Non-Water Quality Aspects                      194
              Solid Wastes                                194
              Air Pollution                               195
           Cost and Effectiveness of Technology           195
              Options
           Effectiveness of Guidelines                    199

VIII     BAT                                              247

  IX     BCT                                              253

   X     NSPS                                             255

  XI     PRETREATMENT STANDARDS                           257

 XII     ACKNOWLEDGEMENTS                                 259

XIII     BIBLIOGRAPHY                                     261

 XIV     GLOSSARY AND ABBREVIATIONS                       275
                                  IV

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                                           Page

Appendix
1.   1977 Petroleum Refinery Industry       281
     Survey Form and
     Supplemental Flow Question
2.   EPA Regional Surveillance and          315
     Analysis Sampling Surveys,
     Analytical Results for Priority
     Pollutants
3.   American Petroleum Institute           341
     Sampling Results
                    v

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                                TABLES

Number                      Title                             Page

1-1      Effluent Limitations Based on Best Avail-             3
         able Technology Economically Achievable
         (BATEA)

1-2      Effluent Limitations Based on Best Con-               4
         ventional Pollutant Control Technology (BCT)

1-3      Pretreatment Standards for Existing and               5
         New Sources (PSES and PSNS)

1-4      Pretreatment Standards for Existing and               6
         New Sources Discharging to POTW's with
         304(h) Waivers

II-1     List of Toxic Pollutants                             H

III-1    Recommended List of Priority Pollutants              19

III-2    Summary of Responses to Portfolio B of 1977          21
         Survey (Number of Refineries)

III-3    Petroleum Refining Wastewater Flow Data              26

III-4    Priority Pollutant Discharge Monitoring Report       38
         Data Reported in the 1977 Survey

III-5    Analytical Results for Traditional Parameters        41
         for the RSKERL and B&R Sampling Program

III-6    Analytical Results for Priority Pollutants           48
         for the RSKERL and B&R Sampling Program -
         Volatile Organics

III-7    Analytical Results for Priority Pollutants           51
         for the RSKERL and B&R Sampling Program -
         Semivolatile Organic

III-8    Analytical Results for Priority Pollutants           56
         for the RSKERL and B&R Sampling Program -
         Pesticides

III-9    Analytical Results for Priority Pollutants           59
         for the RSKERL and B&R Sampling Program -
         Cyanides, Phenolics and Mercury

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                                                             Page

III-10   Analytical Results for Priority Pollutants           69
         for the RSKERL and B&R Sampling Program -
         Metals

III-11   Analytical Results for Traditional                   75
         Parameters in the Pretreatment Sampling
         Program - Week 1

III-12   Analytical Results for Priority Pollutants           76
         for the Pretreatment Sampling Program -
         Week 1, Volatile Organics

III-13   Analytical Results for Priority Pollutants           77
         or the Pretreatment Sampling Program -
         Week 1, Semivolatile Organics

111-14   Analytical Results for Priority Pollutants           79
         for the Pretreatment Sampling Program -
         Week 1, Pesticides

III-15   Analytical Results for Priority Pollutants           80
         for the Pretreatment Sampling Program -
         Week 1, Metals

III-16   Analytical Results for Traditional Parameters        81
         for the Pretreatment Sampling Program - Week 2

III-17   Analytical Results of Priority Pollutants            82
         for the Pretreatment Sampling Program -
         Week 2, Volatile Organics

III-18   Analytical Results of Priority Pollutants            83
         for the Pretreatment Sampling Program -
         Week 2, Semivolatile Organics

III-19   Analytical Results of Priority Pollutants            85
         for the Pretreatment Sampling Program -
         week 2, Pesticides

III-20   Analytical Results for Priority Pollutants           86
         for the Pretreatment Sampling Program -
         Week 2, Metals

V-1      Toxic Pollutants Not Detected In Treated            100
         Effluents  (Direct Dischargers)

V-2      Toxic Pollutants Found In Only One Refinery         102
         Effluent  (at Concentrations Higher Than Those
         Found in the Intake Water) and Which Are
                                 vii

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                                                              Page
         Uniquely Related to the Refinery at Which  It
         Was Detected  (Direct Discharge)

V-3      Toxic Pollutants Detected in Treated Effluents        103
         of More Than One Refinery or Detected in the
         Treated Effluents of One Refinery But Not
         Uniquely Related to the Refinery at Which  It
         Was Detected  (Direct Discharge)'

V-4      Toxic Pollutants Detected in Discharges               104
         To POTW's  (Indirect Discharge)

V-5      Toxic Pollutants Not Detected  in Discharges           105
         to POTW's  (Indirect Discharge)

V-6      Toxic Pollutants Found to Pass  Through                107
         POTW1s With Only Primary Treatment
          (Indirect  Discharge)

VI-1     Sour Water Treatment In Petroleum Refineries          130

VI-2     Effect of  California Crudes on  Reuse                  134
         of Sour Waters

VI-3     Reuse of Sour Waters - Industry Status                135

VI-4     Cooling Tower Make-up Flow Rates in the               137
         Petroleum  Refining Industry

VI-5     Profile of Plants At or Below  U8 Percent              142
         of Model Flow  (Level 2 Plants)

VI-6     Geographical Breakdown of Level 2 Plants              144

VI-7     Summary of Crude Capacities for Level 2               145
         Plants

VI-8     BPT Subcategory Breakdown of Level 2                  146
         Plants

VI-9     Refineries That Utilize, or Plan To                   147
         Utilize Filtration Systems

VI-10    Analytical Results For RSKERL Granular                148
         Activated  Carbon Study, Traditional Pollutants

VI-11    Analytical Results For RSKERL Granular                151
         Activated  Carbon Study, Priority Pollutants
                                 Vlll

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                                                             Page

VI-12    Analytical Results For RSKERL Powdered               155
         Activated Carbon Study, Traditional Pollutants

VI-13    Analytical Results For RSKERL Powdered               156
         Activated Carbon Study, Priority Pollutants

VI-14    Zero Discharge Refineries                            158

VI-15    Treatment Operations and Water Usage For             162
         1973 and 1976

VI-16    Summary of Treatment Technologies For                174
         1973 and 1976

VI-17    Planned Wastewater Flow Reductions                   175

VI-18    Future Wastewater Treatment Modification             181

VI-19    Refinery Flow vs. Final Effluent Concen-             187
         tration For 17 Screening Plants

VI-20    Refineries Included In The Development of Waste-     188
         water Flow Reduction Factor

VII-1    Cost Basis                                           189

VII-2    Raw Wastewater Equalization Systems                  202
         Capital and Operating Costs

VII-3    Rotating Biological Contactors  (RBC's) as            203
         Roughing Systems Equipment Cost Basis and
         Energy Requirements

VII-U    Rotating Biological Contactors  (RBC's) as            204
         Roughing Filters Capital and Operating
         Costs

VII-5    Powdered Activated Carbon Equipment Cost             205
         Basis and Energy Requirements 80 mg/1
         Dosage Rate

VII-6    Powdered Activated Carbon Capital Costs              206
         80 mg/1 Dosage Rate

VII-7    Powdered Activated Carbon Annual Operating           207
         Costs 80 mg/1 Dosage Rate
                                  IX

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                                                             Page

VII-8    PACT Comparison of Operating Costs Carbon             208
         Regeneration vs. Throwaway 80 mg/1
         Dosage Rate

VII-9    Powdered Activated Carbon Equipment Cost              209
         Basis and Energy Requirements Including Costs
         for Sludge Disposal 80 mg/1 Dosage Rate

VII-10   Powdered Activated Carbon Capital Costs,              210
         Including Costs for Sludge Disposal,
         80 mg/1 Dosage Rate

VII-11   Powdered Activated Carbon Annual Operating            211
         Costs Including Credit for Sludge Disposal
         80 mg/1 Dosage Rate

VII-12   Tertiary Filtration Equipment Cost Basis              212
         and Energy Requirements

VII-13   Tertiary Filtration Capital and Operating             213
         Costs

VII-1U   Granular Activated Carbon Equipment Cost              214
         Basis and Energy Requirements

VII-15   Granular Activated Carbon Capital Costs               215

VII-16   Granular Activated Carbon Annual                      216
         Operating Costs

VII-17   Powdered Activated Carbon Equipment Cost              217
         Bases and Energy Requirements 150 mg/1
         Dosage Rate

VII-18   Powdered Activated Carbon Capital Costs               218
         150 mg/1 Dosage Rate

VII-19   Powdered Activated Carbon Annual Operating            219
         Costs 150 mg/1 Dosage Rate

VII-20   PACT, Comparison of Operating Costs,                  220
         Carbon Regeneration vs. Throwaway, 150 mg/1
         Dosage Rate

VII-21   Powdered Activated Carbon, Equipment Cost             221
         Bases and Energy Requirements, Including Costs
         for Sludge Disposal, 150 mg/1 Dosage Rate

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                                                             Page

VII-22   Powdered Activated Carbon, Capital Costs,            222
         Including Costs for Sludge Disposal, 150 mg/1
         Dosage Rate

VII-23   Powdered Activated Carbon, Annual Operating          223
         Costs, Including Credit for Sludge Disposal,
         150 mg/1 Dosage Rate

VII-24   Supplemental Economic Cost Information               224
         Capital and Operating Cost for 10,000
         Gallons Per Day Treatment Systems

VII-25   Cooling Tower Slowdown Rates Petroleum               225
         Refining Industry  (Million Gallons Per Day)

VII-26   Chromium Removal Systems Equipment Cost              227
         Basis and Energy Requirement

VII-27   Chromium Removal Systems Capital and                 228
         Operating Costs

VII-28   Wastewater Recycle - Capital and Operating           229
         Costs

VII-29   Water Softening of Recycled Wastewater               230

VII-30   Capital and Operating Costs by Refinery              231
         Number

VII-31   Capital and Operating Costs, Indirect                236
         Discharge - Option 1

VII-32   Capital and Operating Costs, Indirect                240
         Discharge - Option 2

VII-33   Effectiveness of BAT Options for Direct              242
         Dischargers, Pounds Removed from BPT to
         Level 1

VII-34   Effectiveness of BAT Options for Direct              244
         Dischargers, Pounds Removed from BPT to
         Level 2
                                  xi

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                               FIGURES

Number                      Title                             Page

IV-1     Process Wastewater Flow vs. Refinery Size              96

VI-1     Flow Diagram of a Granular Activated                  127
         Carbon System

VI-2     Carbon Regeneration System                            128

VI-3     Flow Diagram of One PACT Treatment Scheme             129

VII-1    Pumping Capital Cost vs. Pumping Distance             200

VII-2    Refinery Size vs.  Pumping Distance                    201
                                 xii

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                              SECTION I

                          EXECUTIVE SUMMARY


This development document presents the technical data  base  developed
by  EPA  to  support effluent limitations guidelines for the petroleum
refining  point  source  category.   Technologies  to  achieve   these
limitations  are  defined  as  best  available technology economically
achievable   (BAT),  best  conventional  pollutant  control  technology
 (BCT),  and  best  available  demonstrated  technology   (BADT).   This
document outlines the technology options considered and the  rationale
for  selecting each technology level.  These technology levels are the
basis for the proposed effluent limitations.

The rationale by which the Agency selected the technology  option  for
each  of  the proposed effluent limitations guidelines is presented in
Sections VTII, IX, X, and XI.  Effluent limitations  guidelines  based
on  the  application  of  BAT  and  BCT  are  to be achieved by direct
dischargers  by July 1, 1984.  New source performance standards  (NSPS)
based  on  BADT  are  to  be achieved by new facilities.  Pretreatment
standards for both existing sources   (PSES)  and  new  sources  (PSNS)
 (based   on   application   of  BAT  to  those  pollutants  which  are
incompatible with a POTW) are to be achieved by indirect  dischargers.
These  effluent  limitations  guidelines and standards are required by
sections 301, 304, and 307 of  the  Clean  Water  Act  of  1977  (P.L.
95-217) .

The  petroleum  refining industry discharges significant quantities of
toxic, conventional, and non-conventional pollutants.  The  Agency  is
proposing  to  control  the  toxic pollutants chromium  (both total and
hexavalent)  and phenol (total 4AAP) ; and the  conventional  pollutants
oil  and  grease, total suspended solids  (TSS), and biochemical oxygen
demand (BOD).  Non-conventional pollutants such as  ammonia,  sulfite,
and  chemical  oxygen  demand  (COD) are also regulated under existing
BPT.

EPA is proposing  BAT  effluent  limitations  based  on  reduced  flow
through  greater recycle and reuse of wastewaters; or based on the use
of powdered  activated carbon and/or rotating biological contractors as
pretreatment before BPT.  Table 1-1 lists these limitations.

EPA is proposing BCT effluent limitations  based  on  BAT  technology.
These limitations are listed in Table 1-2.

For  NSPS, EPA is proposing to prohibit the discharge of pollutants to
navigable  waters.   This  standard  is  based  on  existing  industry
practice at exemplary facilities and demonstrated technologies.

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EPA is proposing PSNS and PSES based on removal of metals and existing
PSES  control  technology  for  oil and grease and ammonia.  Table 1-3
lists these limitations.

EPA also is proposing separate PSES  and  PSNS  for  those  refineries
discharging  into  a  POTW  which  has received a waiver under Section
301(h) of the Clean Water Act of  1977.   Such  waivers  would  exempt
POTW's   from   achieving  effluent  limitations  based  on  secondary
treatment.  These pretreatment standards are listed in Table  1-4  and
are  based  on  the  same  technology  as  that  for  the proposed BAT
guidelines.  These standards, however, set explicit  numerical  values
on  the  concentration  of  regulated  pollutants.  Informational mass
limitations are also provided for POTWs wishing to  limit  total  mass
discharge.

EPA  estimates the annual costs for the petroleum refining industry to
comply with the proposed regulation to be $53.9 million.

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                                                            TABLE 1-1
                                      Effluent Limitations Based on Best Available Technology
                                                  Economically Achievable (BATEA)

                                               (Effluent Limitation- Basic Allowance
                                                                     + Cracking Adjustment
                                                                     + Asphalt and Lube Adjustment)

                                        Metric Units  (kilograms per day)
                              Pollutant or                       Average of daily
                              Pollutant        Maximum for       values for 30
                              Property	any one day	consecutive days
                                                                           English Units (pounds per day)
                                                                                          Average of daily
                                                                           Maximum for    values for 30
                                                                           any one day    consecutive days
Basic Allowance
Cracking Adjustment
Asphalt and Lube
Adjustment
Phenol (4AAP)    0.0031C
Total Chromium   0.0332C
Hexavalent Chrom.0.0028C

Phenol (4AAP)    0.0351K
Total Chromium   0.3812K
Hexavalent Chrom 0.0326K
Phenol (4AAP)    0.0365AL
Total Chromium   0.397SAL
Hexavalent Chrom 0.0340AL
0.0015C
0.0194C
0.0013C

0.0170K
0.2234K
0.0147K
                                                                   0.0177AL
                                                                   0.2332AL
                                                                   0.0154AL
0.0011C
0.0116C
0.0010C
0.0123K
0.1336K
0.0114K
0.0005C
0.0068C
0.0005C
0.0060K
0.0783K
0.0052K
                                        0.0128AL
                                        0.1393AL
                                        0.0119AL
0.0062AL
0.0817AL
0.0054AL
Notes:  The folowing terms are defined in metric units as thousand cubic meters per day and in English units as thousand barrels per day:
        AL= sum of ashphalt and lube processes (throughput)
            Asphalt Production
            Asphalt Oxidizer
            Asphalt Emulsifying
            Hydrofining, Hydrofinishing, Lube Hydrofining
            White Oil Manufacture
            Propane Dewaxing, Propane Oeasphalting, Propane Fractioning,
               Propane Deresining
            Duo Sol, Solvent Treating, Solvent Extraction, Duotreating.
               Solvent Dewaxing, Solvent Deasphalt
            Lube Vac Twr, Oil Fractionation, Batch Still  (Naphtha Strip),
               Bright Stock Treating
            Centrifuge and Chilling
            MEK Dewaxing, Ketone Dewaxing, MEK-Toluene Dewaxing
            Deoiling (wax)
            Naphthenic Lubes Production
            SO2 Extraction
            Wax Pressing
            Wax Plant (with Neutral Separation)
            Furfural Extracting
            Clay Contacting - Percolation
            Wax Sweating
            Acid Treat
            Phenol Extraction
            Lube and Fuel Additives
            Sulfonate Plant
                                                       MIBK
                                                       Wax Slabbing
                                                       Rust Preventives
                                                       Petrolatum Oxidation
                                                       Grease Mfg. V. Allied Products
                                                       Misc. Blending and Packaging

                                                       K= sum of cracking processes (throughput)
                                                          Hydrocracking
                                                          Visbreaking
                                                          Thermal Cracking
                                                          Fluid Catalytic Cracking
                                                          Moving Bed Catalytic Cracking

                                                       C= sum of crude processes (throughput)
                                                          Atmospheric Crude Distillation
                                                          Crude Desalting
                                                          Vacuum Crude Distillation

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                                                                  TABLE  1-2

                             Effluent Limitations Based on  Best  Conventional  Pollutant  Control  Technology  (BCT)

                                                     (Effluent  Limitation^ Basic Allowance
                                                                          + Cracking Adjustment
                                                                          + Asphalt and Lube Adjustment)
Basic Allowance
Cracking Adjustment
Asphalt and Lube Adjustment
                                        Metric  Units  (kilograms  per day)
                                                                                                          English Units (pounds per day)
Pollutant
or Pollutant
Property
BODS
TSS
Oil and Grease
BODS
TSS
Oil and Grease
BODS
TSS
Oil and Grease
Maximum for
any one day
2.195C
1 . 509C
0.686C
25.24K
17.35K
7.89K
26.33AL
18.10AL
8.23AL
Average of daily
values for 30
consecutive days
1.166C
0.9601C
0.366C
13.41K
11.04K
4.21K
13.99AL
11.52AL
4 . 39AL
Maximum for
any
0.
0.
0.
8.
6.
2,
9,
6,
2
one day
7691C
5288C
240C
.84SK
.081K
, 76K
.229AL
.34 SAL
. 88AL
Average of daily
values for 30
consecutive days
0.
0.
0.
4,
3
1
4
4
1
4086C
3365C
.128C
.699K
.870K
.47K
.903AL
.038AL
.54AL
Notes:  Refer  to notes on Table 1-1   for definition of terms.

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                                                  TABLE  1-3

                     PRETREATHENT STANDARDS  FOR NEW AND EXISTING SOURCES, PSES AND PSNS
                            (Unless  the POTH  has a waiver  from  achieving effluent
                                  limitations based on  secondary treatment)


a.   The  following  standards  apply  to the  total effluent  flow:

     milligrams per liter  (mg/1)

     Pollutant
     or Pollutant        Maximum for
     Property	any  one day

     Oil  and Grease          100
     Ammonia  (as N)          100

b.   The  following  standard is applied to  the cooling tower blowdown portion of the effluent flow or may
     be applied to  the total  effluent flow by multiplying  the  standard by the ratio (R) of the cooling
     tower blowdown flow to the total effluent flow:

     milligrams per liter  (mg/1)

     Total Chromium          1.0

c.   Informational  mass limitations for the  total effluent flow are as follows:

                                                           Maximum  for any one day
Pollutant
or Pollutant
Property
Oil and Grease
Ammonia (as N)
Total Chromium
Metric Units
(kilograms per day)
9.50C + 109. 5K + 114. 3AL
9.50C + 109. 5K + 114. 3AL
Rx(0.095C + 1.095K + 1.143AL)
English Units
(pounds per day)
3.33C + 38.39K + 40.06AL
3.33C + 38.39K + 40.06AL
Rx(0.033C + 0.3839K + 0.4006AL)
Notes:  R is defined in section  (b) above.  Refer to notes on Table  1-1 for definition of terms.

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                                                TABLE  1-4

                     PRETREATMENT STANDARDS FOR NEW AND EXISTING SOURCES, PSES AND PSNS
                              WHICH DISCHARGE TO POTW's WITH 304 (h)WAIVERS
     Pollutant or
     Pollutant
     Property	
Maximum for
any one day
Average of dally
values for 30
consecutive days
                          milligrams per liter (rag/1)
     Phenol (4AAP)         0.07
     Total Chromium        0.73
     Hexavalent Chromium   0.06
                     0.03
                     0.43
                     0.03
Informational mass limitations are as follows:
Basic Allowance
                                   (Effluent Limitations = Basic Allowance
                                                         + Cracking Adjustment
                                                         + Asphalt and Lube Adjustment)
                                   Metric Units  (kilograms per day)
                         Pollutant or                      Average of daily
                         Pollutant        Maximum for      values for 30
                         Property	any one day	consecutive days
                         Phenol(4AAP)       0.0031C
                         Total Chromium     0.0332C
                         Hexavalent Chrom.  0.0028C
                                       0.0015C
                                       0.0194C
                                       0.0013C
                                                           English Units (pounds per day)
                                                                         Average of daily
                                                           Maximum for   values for 30
                                                           any one day   consecutive days
                                             0.0011C
                                             0.0116C
                                             0.0010C
                0.0005C
                0.0068C
                0.0005C
Cracking Adjustment
 Phenol  (4AAP)      0.0351K
 Total Chromium     0.3812K
 Hexavalent Chrom.  0.0326K
                       0.0170K
                       0.2234K
                       0.0147K
0.0123K
0.1336K
0.0114K
0.0060K
0.0783K
0.0052K
 Asphalt and Lube
 Adjustment	
 Phenol  (4AAP)      0.0365AL
 Total Chromium     0.3975AL
 Hexavanent Chrom.  0.0340AL
                       0.0177AL
                       0.2332AL
                       0.0154AL
0.0128AL
0.1393AL
0.0119AL
0.0062AL
0.0817AL
0.0054AL
 Notes:   Refer to Table  1-1  notes for definition of terms.

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                              SECTION II

                             INTRODUCTION


PURPOSE AND AUTHORITY

This development document details the technical basis for the Agency's
proposed effluent limitations reflecting BAT, BCT, NSPS, PSES and PSNS
for the petroleum refining industry.  These limitations  are  proposed
under  authority  of  Sections 301, 304, 306, 307, 308, and 501 of the
Clean Water Act  (the Federal water Pollution Control Act Amendments of
1972, 33 USC 1251 et seq., as amended by the Clean Water Act of  1977,
P.L.  95-217)  (the  "Act").   These  regulations are also proposed in
response to the Settlement  Agreement  in  Natural  Resources  Defense
Council,  Inc.  v.  Train, 8 ERC 2120  (D.D.C. 1976), modified March 9,
1979 and in response to the decision of the  United  States  Court  of
Appeals  in  American  Petroleum Institute v. EPA, 540 F.2d 1023 (10th
Cir. 1976).

PRIOR EPA REGULATIONS

EPA promulgated BPT, BAT, NSPS, and PSNS for  the  petroleum  refining
point  source  category on May 9, 1974  (39 FR 16560, Subparts A-E).  A
Development Document was published in April 1974  (EPA-440/1-74-014-a)
This document provided the bases  for  the  1974  regulations  and  is
henceforth  referred  to  as  the 1974 Development Document.  The BPT,
BAT, and NSPS  regulations  were  challenged  in  the  courts  by  the
American  Petroleum  Institute  and  others.   Both  BPT and NSPS were
upheld by the court, but BAT was remanded for  further  consideration.
Interim final PSES were promulgated on March 23,  1977  (42 FR 15684) in
response to the Settlement Agreement.

OVERVIEW OF THE INDUSTRY

The  petroleum  refining  industry  is defined by Bureau of the Census
Standard Industrial Classification  (SIC) 2911.  The  raw  material  in
this  industry is petroleum material  (generally, but not always, crude
oil) .  Petroleum refineries process this  raw  material  into  a  wide
variety of petroleum products, including gasoline, fuel oil, jet fuel,
heating  oils  and gases and petrochemicals.  Refining includes a wide
variety of physical separation and chemical reaction  processes.   The
1974 Development Document lists over one hundred processes used in the
petroleum  refining industry.  Because of the diversity and complexity
of the processes used and the products produced, petroleum  refineries
are generally characterized by the quantity of raw material processed,
rather than by the quantity and types of products produced.

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 EPA  has   identified  285 petroleum  refineries  in the United  states  and
 its possessions.   The smallest refinery can refine  fifty  barrels   of
 oil  per   day  (one   barrel  equals 42 gallons), while the largest  can
 refine  665,000  barrels per day.

 The U.S.  refining  industry processes  a  total  of  about  15   million
 barrels  per  day.  However industry growth has slowed in recent  years
 due to  a  number of factors including  efforts  to  conserve  petroleum
 supplies   and competition from foreign suppliers.  Growth has  averaged
 about five percent per year and has resulted largely from additions to
 existing  refineries rather than by  construction  of  new  ones.    The
 ratio  of growth  in U.S. refining capacity by additions to  existing
 refineries to the growth by construction of new  refineries  has  been
 approximately 3.5 to  1.

 Additional information can be found in the 1974 Development  Document.

 PRELIMINARY INDUSTRY  PROFILE

 One  of the initial efforts on this project was to review and  evaluate
 existing   industry-wide   data   on   such   factors   as     refinery
 characteristics,    production    capacities,    wastewater    handling
 techniques, and wastewater  characteristics.   A  contractor's report
 which  summarizes  the results of  this effort was previously  prepared
 and submitted to EPA  (76).  This report covered:

     (1)   Industry distribution (geographic);
     (2)   Intake water characteristics;
     (3)   Wastewater treatment techniques;
     (4)   Refining capacities;
     (5)   Water  usage  characteristics;
     (6)   Discharge permit identification;
     (7)   In-plant control techniques; and
     (8)   Cooling service characteristics.

 The   preliminary  industry  profile  was  based   on   the   published
 literature,   government  reports,   contacts  with  the  industry,   and
 contacts  with various  State and EPA regional  offices.   In  order   to
 develop new regulations,  however, the Agency needed to supplement this
 existing   data  base  with  more  recent  information  in the  areas of
 wastewater characteristics and toxic pollutants.

 INDUSTRY  SURVEY

 To acquire up-to-date information for use in the establishment of   BAT
 guidelines  for  the  petroleum  refining  category,  a  comprehensive
 questionnaire   (see  Appendix  1)    was  developed  and  sent   to    all
refineries   throughout   the   United   States  and  its  territorial
possessions.    This  questionnaire  sought  information  necessary   to

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generate   a   profile   of  the  petroleum  refining  industry.   The
questionnaire is henceforth referred to  as  the  1977  EPA  Petroleum
Refining Industry Survey or the "1977 survey."

In addition to updating the industry profile. The information gathered
from  this  survey  was  used  to aid in the selection of plants for a
nationwide wastewater sampling program, and develop a flow  model  for
the analysis of refinery wastewater production.

WASTE WATER SAMPLING PROGRAM

The  Settlement  Agreement cited above required the Agency to consider
the potential limitations of the discharge of  65  "toxic"  substances
(Table II-1).  The Agency undertook a sampling and analysis program to
obtain  information  on  the  65  "toxic" substances from the refinery
industry.  The program was designed to do the following:  (a)   analyze
for the presence of the "toxic" substances in the plants' intake water
source;   (b)  analyze  the plants' raw wastewater to determine the net
production of  "toxic"  substances  resulting  from  refinery  process
operations;  and   (c)  analyze  the  plants'  final  effluent  for the
presence of "toxic" substances and determine the removal  efficiencies
of  BPT-type  wastewater  treatment  systems for these substances  (See
Section III for details) .

CONTROL AND TREATMENT TECHNOLOGY. COST ANALYSIS

Three major efforts were undertaken to identify and evaluate available
control and treatment technologies:

     (1) A literature search compiled the available information on  the
advances  being  made  by the industry relative to wastewater handling
and disposal.

     (2) A review of the responses to the 1977 EPA  Petroleum  Refining
Industry  Survey  determined the status of the industry with regard to
in-plant source control and end-of-pipe treatment.

     (3) Petroleum refineries were visited  to  review  in  detail  the
sources of wastewater production, as well as to review wastewater  flow
reduction  practices,  reuse,  and  in-plant and end-of-pipe treatment
operations.

These  studies  established  a  range   of   control   and   treatment
technologies available to this industry.  Section VI discusses them in
detail.

The  study  next  determined  the  cost  of  the  various  control and
treatment technologies; these are outlined in Section VII.

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The results of the above  described  programs  are  presented  in  the
subsequent  sections  of  the  document.   A thorough discussion of the
industry processes, the source of wastewater and the  BPT  end-of-pipe
treatment technologies appears in the 1974 Development Document.
                                10

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                             TABLE II-l
                      LIST OF TOXIC POLLUTANTS
Acenaphthene
Acrolein
Acrylonitrile
Aldrin/DieIdrin
Antimony and compounds*
Arsenic and compounds
Asbestos
Benzene
Benzidine
Beryllium and compounds
Cadmium and compounds
Carbon tetrachloride
Chlordane (technical mixture and metabolites)
Chlorinated benzenes  (other than dichlorobenzenes)
Chlorinated ethanes  (including 1,2-dichloroethane, 1,1,1-tri-
                     chloroethane, and hexachloroethane)
Chloroalkyl ethers  (Chloromethyl, chloroethyl, and mixed ethers)
Chlorinated naphthalene
Chlorinated Phenols  (other than those listed elsewhere; includes
                     trichlorophenols and chlorinated cresols)
Chloroform
2-chlorophenol
Chromium and compounds
Copper and compounds
Cyanides
DDT and metabolites
Dichlorobenzenes  (1,2-,1,3-, and 1,4-dichlorobenzenes)
Dichlorobe nzidene
Dichloroethylenes  (1,1-and 1,2-dichloroethylene)
2,4-dichlorophenol
Dichloropropane and dichloropropene
2,4-dimethylphenol
Dinitrotoluene
DiphenyIhdraz ine
Endosulfan and metabolites
Endrin and metabolites
Ethylbenzene
Fluoranthene
Haloethers (other than those listed elsewhere; includes chlorophenylphenyl
            ethers, bromophenylphenyl ether, bis(dischloroisopropyl)
            ether, bis-(chloroethoxy) methane and polychlorinated
            diphenyly ethers)
Halomethanes (other than those listed eleswhere; includes methylene chloride
              methylchloride, methylbromide, bromoform, dichloro-
              bromomethane,trichlororfluoromethane,  dichlorodifluoro-
              methane)
Heptachlor and metabolites
Hexachlorobutadiene

                                 11

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                           TABLE II-l (Continued)
Hexachlorocyclohexane  (all isomers)
Hexachlorocyclopentadiene
Isophorone
Lead and compounds
Mercury and compounds
Naphthalene
Nickel and compounds
Nitrobenzene
Nitrophenols  (Including 2,4-dinitrophenol, dinitrocresol)
Nitrosamines
Pentachlorophenol
Phenol
Phthalate esters
Polychlorinated biphenyls (PCBs)
Polynuclear aromatic hydrocarbons  (Including benzanthracenes,
                     benzopyrenes, benzofluoranthene, chrysenes,
                     dibenzanthracenes, and indenopyrenes)
Selenium and compounds
Silver and compounds
2,3,7,8,- Tetrachlorodibenzo-p-dioxin (TCDD)
Tetrachlorcethylene
Thallium and compounds
Toluene
Toxaphene
Trichloroethylene
Vinyl chloride
Zinc and compounds
* As used throughout this table the term "compounds"  shall  include
 organic and inorganic compounds.
                               12

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                             SECTION III

                        WASTE CHARACTERIZATION


GENERAL

The   Agency   had  considerable  data  available  characterizing  the
discharges of "traditional" pollutant parameters  (BOD, COD, TSS,  NH3,
sulfide,  oil  and grease, etc.)-  These parameters have been measured
in wastewaters for years  (1,3,8).  With few exceptions, however,  data
on  the 65 pollutants or classes of pollutants  (Table II-1) are almost
non-existent.

The Agency conducted a sampling program to determine the presence  and
concentrations  of  the 65 toxic substances in refinery wastewater and
the  effectiveness  of  candidate  treatment  technologies  to  reduce
discharges  of  toxic pollutants.  The list of 65 toxic pollutants and
classes of  pollutants  potentially  includes  thousands  of  specific
pollutants.   The  Agency  has  selected 129 specific toxic pollutants
(Table III-1) for analysis in this rulemaking.

The Agency also requested data from the industry  ("1977  survey")  on:
(1)   toxic   pollutants  purchased,  manufactured,  and  analyzed  in
wastewater;   (2)  treatability  data  on  toxic  pollutants;  and  (3)
wastewater  flow  from  each  of  the  refinery  processes.  Measuring
concentrations  of  these  pollutants  is  difficult,  requires   very
expensive equipment, and requires highly qualified operators.

1977 EPA PETROLEUM REFINING INDUSTRY SURVEY

To  acquire  the  up-to-date  information needed to establish effluent
guidelines for  the  petroleum  refining  category,  EPA  developed  a
comprehensive  questionnaire  for all refineries throughout the United
States and its territorial possessions.  This survey  was  made  under
section  308 of the Clean Water Act.  The questionnaire is referred to
as the 1977 EPA  Petroleum  Refining  Industry  Survey  or  the  "1977
Survey."  More detailed information also was requested of the industry
in a  subsequent  mailing,  referred  to  as  the  "Supplemental  Flow
Question"  (See  Appendix  1).  Finally, because of extensive industry
comments on the accuracy of the data  collected,  the  Agency  made  a
third mailing to verify the reported data—this mailing is referred to
as the "Verification Report."

The   information   from   this  survey  was  combined  with  existing
information to  develop  an  industry  profile,  including  number  of
plants,  their  size, geographic location, and manufacturing processes
and the wastewater generation, treatment,  and  discharge  methods  at
refining  facilities.   Questionnaire  data  also  aided  in the final
                                 13

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 selection of plants for  wastewater  sampling.   Flow  data   from  the
 questionnaire  were  used  to develop a flow model  for the analysis of
 refinery wastewater production.  Another objective  of the  survey  was
 to  obtain  information identifying the use or generation of  123  toxic
 pollutants and determining the  availability  of  plant  data  on  the
 effectiveness  of  their  removal.   Since  the  initial questionnaire
 survey,, the list of toxic pollutants has been revised from  123 to the
 present list of  129 specific substances.

 Survey Data Related to Wastewater Characterization

 Toxic  pollutant  data  contained  in  the  1977  survey   have   been
 summarized.   The  following toxic pollutants were  not included in the
 survey because they were added to the toxic pollutant list  after  the
 questionnaire mailing in February of 1977:

         di-n-octyl phthalate
         PCB 1221  (Arochlor 1221)
         PCS 1232  (Arochlor 1232)
         PCB 12 U 8  (Arochlor 1248)
         PCB 1260  (Arochlor 1260)
         PCB 1016  (Arochlor 1016)

 Table  III-2  lists  the  number of refineries with positive  responses
 regarding priority pollutants as:

    a.   Chemicals purchased as raw or intermediate materials;  and

    b.   Chemicals manufactured as a final or intermediate material;

 Seventy-one toxic pollutants were listed as being purchased as  a  raw
 or   intermediate   materials;  19  of  these  toxic  pollutants   were
 individual purchases by single refineries, while at least ten  percent
 of the refineries purchased the following toxic pollutants:

    benzene
    carbon tetrachloride
    1,1,1-trichloroethane
    phenol
    toluene
    zinc and compounds
    chromium and compounds
    copper and compounds
    lead and compounds

Zinc  and  chromium  were  purchased  by 28 percent of the refineries,
while lead was purchased by nearly 48 percent of the plants.
                                 14

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Forty-five toxic pollutants were manufactured as final or intermediate
materials; 15 of these toxic pollutants were  manufactured  at  single
refineries,  while  benzene,  ethylbenzene,  phenol,  and toluene were
manufactured by at least ten percent of the refineries.  Eight percent
of the refineries manufacture cyanides; greater than 20 percent of the
refineries manufacture benzene/toluene.

Table III-3 presents industry data on wastewater generated in 1976 and
the discharge flows reported in the NPDES permit in 1976 on a plant by
plant basis.  Also included for comparison is the calculated flow  for
each  plant,  which  was  determined  on the basis of the process data
supplied for each plant and the original  197U  EPA  flow  model  (see
Section IV for details).

The  1977  survey  has  also requested data on daily average discharge
concentration of priority pollutants for the month of December in 1975
and 1976.  These data are summarized in Table III-4.   Pollutants  for
which  data  were  reported  include  cadmium,  copper, cyanide, lead,
mercury, zinc, arsenic, nickel, silver, selenium,  and  free  cyanide.
Phenol  and  chromium  are  limited  by  existing BPT regulations, and
therefore do not appear in  the  table.   About  ten  percent  of  the
industry currently has effluent limits for zinc and cyanide.

WASTEWATER SAMPLING PROGRAM RESULTS

EPA  determined  the  presence and magnitude of the 129 specific toxic
pollutants  in  petroleum  refining  wastewaters  in  a  sampling  and
analysis  program  involving 23 refineries and two POTWs.  The sampled
plants  were  selected  to  be  representative  of  the  manufacturing
processes,  the  prevalent  mix  of  production  among plants, and the
current treatment technology in the industry.  Seventeen  plants  were
direct dischargers and six were indirect dischargers.

Sampling  visits  were made to correspond to three consecutive days of
plant operation.  Raw  wastewater  was  sampled  prior  to  biological
treatment;  treated  effluent  was  sampled  subsequent  to biological
treatment.  In some instances,  samples  were  taken  after  polishing
(i.e.,  polishing  pond,  sand  filter).   The  intake  water also was
sampled to  determine  the  presence  of  toxic  pollutants  prior  to
contamination by refining processes.

Samples  for  conventional,  nonconventional and toxic pollutants came
24-hour composite samples.   The  laboratory  combined  aliquots  from
these  samples  in equal portions to obtain the 72-hour composites for
toxic pollutant analysis  (acid and base-neutral extractible  organics,
pesticides,  and  metals).   Grab  samples  were  taken  in  specially
prepared vials for volatile  (purgeable) organics,  total  phenols  and
cyanide.   Prior to the plant visits, sample containers were carefully
washed and prepared by specific methods, depending upon  the  type  of
                                  15

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 sample  to  be  taken.   Samples  were  kept  on  ice prior to express
 shipment in insulated containers.

 The  analyses for toxic pollutants were performed according  to  groups
 of   chemicals  and  associated  analytical  schemes.   Organic  toxic
 pollutants  included  volatile   (purgeable),  base-neutral  and   acid
 (extractable)  pollutants,  total  phenols, and pesticides.   Inorganic
 toxic pollutants included heavy metals, cyanide, and asbestos.

 The  primary  method  used  to  screen  and  verify   the   volatiles,
 base-neutral,   and   acid   organics   was  gas  chromatography  with
 confirmation and quantification of all  priority  pollutants   by  mass
 spectrometry   (GC/MS).   Total  phenols  were  analyzed  by   the 4-AAP
 method.  GC was employed for analysis of pesticides  with  limited  MS
 confirmation.   Toxic  heavy metals were analyzed by atomic adsorption
 spectrometry   (AAS),  with  flame  or  graphite  furnace   atomization
 following appropriate digestion of the sample.  Duplicate samples were
 analyzed   using   plasma   emission  spectrometry  after  appropriate
 digestion.  Samples were  analyzed  for  cyanides  by  a  colorimetric
 method, with sulfide previously removed by distillation.  Analysis for
 asbestos was accomplished by microscopy and fiber presence reported as
 chrysotile  fiber  count.  Analyses for conventional pollutants (BODJ5,
 TSS, pH, and Oil and Grease)  and nonconventional pollutants   (TOC  and
 COD)  were  accomplished using "Methods for Chemical Analysis of Water
 and  Wastes," (EPA 625/6-74-003) and amendments.

 Three sampling programs were conducted in this project:  (1) the Robert
 S. Kerr Environmental Research Laboratory  (RSKERL)  Sampling  Program
 (12  refineries) ;  (2)   the  Burns and Roe (BSR) Supplemental Sampling
 Program (5 refineries)  and (3)  the Burns and  Roe  Indirect   Discharge
 Sampling  Program  (6  refineries and two POTW's).  In addition,  eight
 refineries were sampled by the  U.S.  EPA  regional  surveillance  and
 analysis field teams in conjunction with their routine SSA work.   This
 sampling  was  performed  after  the RSKERL and Burns and Roe sampling
 program  and  generally  followed  the   same   screening   procedure.
 Analytical data from refineries 1, 83, 131, 132, 133, 134, 157  and 181
 for  S&A sampling of raw water supply, raw wastewater, final  effluent,
 and  some in-plant sampling, are included in Appendix 2 of this  report.

 RSKERL and B &_ R Sampling Program

 The PSKERL and  B  &  R  sampling  program  was  designed  to  do  the
 following:  (a)  analyze for the presence of the 129 toxic pollutants in
 the   plants'   intake  water  source;  (b)  analyze  the  plants9   raw
 wastewater to determine the  net  production  of  priority  pollutants
 resulting  from  refinery  process  operations;  and  (c)  analyze the
 plants'  final effluent  for  the  presence  of  toxic  pollutants  and
measure  the  effectiveness  of  in-place  treatment in removing  toxic
pollutants.

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The program was undertaken in two parts: The RSKERL sampling  included
12 refineries selected according to the following criteria:

    a.   They should be meeting the July 1, 1977, effluent limitations
specified in the NPDES permit;

    b.   They should have single discharge points  for  their  treated
process wastewater.

    c.   Their process types,  geographic  locations,  and  wastewater
treatments  were  representative  of  the  industry  and  provided the
broadest coverage on a national basis.

The selection procedures is detailed in  two  Burns  and  Roe  reports
(S1 - Analysis  of  Self  Reporting  Data From Refineries to Determine
Compliance with July 1,  1977,  Effluent  Limitations  (78)  and  S2 -
 Selection of Refineries for RSKERL Sampling Program (79)).

The RSKERL program involved two segments: segment A sampled six of the
selected  plants;  segment  B covered the remaining six refineries and
also  tested  the  toxic  removal  efficiency  of  carbon   adsorption
treatment  on  a pilot scale.  Granular activated carbon was tested at
six plants and powdered activated carbon was tested  in  four  of  the
same  six  plants.  These pilot test results are included in section V
of this report.

The B & R program was initiated to supplement the RSKERL sampling  and
studied  five  refineries.   This  program  did  not include any pilot
carbon testing.

Tables III-5 through III-10 present the analytical  results  from  the
RSKERL  and  B  &  R  sampling  programs.   The traditional parameters
analyzed include  BODS,  COD,  TOC,  TSS,  oil  and  grease,  ammonia,
sulfides, hexavalent chromium, and pH.  Each of the three, consecutive
24-hour,  composites  collected  at  each sampling location in a given
refinery was tested for the traditional parameters other than oil  and
grease.   Grab  samples  collected  at the end of each sample day were
used for the oil and grease  analyses.    Table  IV-5  summarizes  the
traditional   pollutant   analytical   results  reported  for  all  17
refineries.

Sources of asbestos in the petroleum refining  industry  are,  in  all
probability,  the  same  as  in  other  point  source  categories:  (a)
insulation materials that have deteriorated; and (b) residues from the
brake linings of equipment and vehicles used in the processing  areas.
Because  EPA  believes  that  these  may not be significant sources of
asbestos, and because of the expense  of  asbestos  analyses  and  the
liklihood  of  similar  data  within  other  point  source categories,
samples from only four petroleum refineries were analyzed.
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Since asbestos contributions to wastewater streams could  be  affected
by  rainfall  (i.e.,  runoff could wash fragmented insulation into the
sewer), EPA sampled two refineries for  asbestos  during  dry  weather
condition and two during or shortly after a significant rainfall.  The
Agency  sampled  refinereies in which treatment detention time did not
affect significantly the rainfall criteria.  Composites of three daily
grab samples from Refineries I, L, M and P were analyzed for asbestos.
Rainfall data also were collected and analyzed.  The analytical method
for  asbestos  includes  the  use  of  an  electron   microscope   for
verification  of  each  fiber  and  confirmed  by  nondispersive x-ray
fluorescence.  All of the samples had low concentrations of  suspended
solids, and an absence of vegetal and biological debris.

Abestos was not detected in the intake or final effluent from the four
refineries.   Asbestiform  mineral  fibers  of  3.4 million fibers per
liter  were  observed  and  verified  in  only  one  sample,  the  API
separator  effluent  from  Refinery L.  It had been raining during the
time that samples were collected at Refinery L.

During this  RSKERL/Burns  and  Roe  sampling  program,  the  American
Petroleum  Institute  and  some  individual  plants were provided with
replicate samples for  their  own  analysis.   The  results  of  these
analyses are presented in Appendix 3 of this report.

Pretreatment Sampling Program

Burns  and  Roe conducted a sampling program at two Los Angeles county
Sanitation District municipal treatment plants  and  refineries  which
contribute  wastewater  to these plants.   A three day sampling period,
similar to the RSKERL and Burns and Roe sampling program, was utilized
at the final effluent points of six refineries, and at various  points
in  the  municipal  treatment  plants.   Analytical  results  of  this
sampling program are presented in Tables  III-11 thru 111-20.
                                18

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                                          TABLE III-l
                            RECOMMENDED LIST OF PRIORITY POLLUTANTS
* No.     Compound
  IB     acenaphthene
  2V     acrolein
  3V     acrylonitrile
  4V     benzene
  SB     benzidine
  6V     carbon tetrachloride
  TV     chlorobenzene
  3B     1,2,4,-trichlorobenzene
  98     hexachlorobenzene
  10V    1,2-dichloroethane
  11V    1,1,1-trichloroethane
  12B    hexachloroethane
  13V    1,1-dichloroethane
  14V    1,1,2-trichloroethane
  1SV    1,1,2,2-tetrachloroethane
  16V    chloroethane
  17B    bis(chloromethyl) ether
  18B    bis(2-chloroethyl) ether
  19V    2-chloroethylvinyl ether
  20B    2-chloronaphthalene
  21A    2,4,6-trichlorophenol
  22A    parachlorotneta cresol
  23V    chloroform
  24A    2-chlorophenol
  2SB    1,2-dichlorobenzene
  26B    1,3-dichlorobenzene
  27B    1,4-dichlorobenzene
  28B    3,3'-dichlorobenzidine
  29V    1,1-dlchloroethylene
  30V    1,2-trana-dichloroethylene
  31A    2,4-dichlorophenol
  32V    1,2-dichloropropane
No.    Compound
3 3v    1,2-diohloropropylene
34A    2,4-dloethylphenol
3SB    2,4-dinitrotoluene
36B    2,6-dinitrotoluene
37B    1,2-diphenylhydrazine
38V    ethylbenzene
39B    fluoranthene
408    4-chlorophenyl phenyl ether
41B    4-bromophenyl phenyl ether
42B    bis(2-chloroisopropyl) ether
43B    bis(2-chloroethoxy) methane
44V    methylene chloride
45V    methyl chloride
46V    methyl bromide
47V    bromoform
48V    dichlorobromomethane
49V    trichlorofluoroniethane
50V    dichlorodifluoromethane
51V    chlorodibromomethane
52B    hexachlorobutadiene
538    hexachlorocyclopentadiene
54B    isophorone
5 SB    naphthalene
S6B    nitrobenzene
57A    2-nitrophenol
58A    4-nitrophenol
59A    2,4-dinitrophenol
60A    4,6-dinitro-o-cresol
61B    N-nitrosodimethylamine
62B    N-nitrosodiphenylamine
63B    N-nitrosodi-n-propylamine
64A    pentachlorophenol
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No.   Compound
65A    phenol
66B    bis(2-ethylhexyl) phthalate
67B    butyl benzyl phthalate
68B    di-n-butyl phthalate
69B    di-n-octyl phthalate
70B    diethyl phthalate
71B    dimethyl phthalate
72B    benzo(a)anthracene
738    benzo(a)pyrene
74B    3f4-benzofluoranthene
75B    benzo(k)fluoranthane
76B    ohrysene
77B    acenaphthylene
78B    anthracene
798    benzo(ghi)perylene
80S    fluorene
BIB    phenanthrene
82B    dibenzo(a,h)anthracene
83B    ideno(1,2,3-cd)pyrene
84B    pyrene
85V    tetrachloroethylene
86V    toluene
87V    trichloroethylene
88V    vinyl chloride
89P    aldrin
90P    dieldrin
91P    chlordane
92P    4,4'-DDT
93P    4,4'-DDE
94P    4,4' -ODD
95P    a-endosulfan-Alpha
96P    b-endosulfan-Beta
97P    endosulfan sulfate
98P    endrin
99P    endrin aldehyde
100P   heptachlor
101P   heptachlor epoxide
        Compound
        a-BHC-ftlpha
 103P   b-BHC-Beta
 104P   r-BHC-Gamma
 105P   g-BHC-Delta
 106P   PCB-1242
 107P   PCB-12S4
 108P   PCB-1221
 109P   PCB-1232
 110P   PCB-1248
 111P   PCB-1260
 112P   PCB-1016
 113P   toxaphene
 114M   antimony (total)
 115M   arsenic(total)
 116    asbestos(fibrous)
 117M   beryllium(total)
 118H   cadmium(total)
 119M   chromium (total)
 120M   copper(total)
 121M   cyanide!total)
 122M   lead(total)
 123M   mercury(total)
 124M   nickel(total)
 125M   selenium(total)
 126M   silver(total)
 127M   thallium(total)
 128M   zinc(total)
 129B    2,3,7,8-tetrachloro-
        dibenzo-p-dioxin(TCDD)
* V   volatile organics
  A - acid extractables
  B   base/neutral extractables
  P   pesticides
  M   metals
                                    20

-------
                          TABLE  III-2
         Summary of Responses to  Portfolio B of 1977 Survey
                       (Number of Refineries)
Priority Pollutants
acenaphthene
acrolein
acrylonitrile
benzene
carbon tetrachloride
chlorobenzene
1,2-dichloroethane
1,1,1-trichloroethane
hexachloroethane
1,1-dichloroethane
1,1,2-trichloroethane
1,1,2,2-tetrachloroethane
chloroe thane
2,4,6-trichlorophenol
chloroform
2-chlorophenol
1,2-dichlorobenzene
1,3-dichlorobenzene
dieldrin
benzidine
p-chloro-m-cresol
3 respondents summarized)
(1)
Chemicals
purchased
as a raw or
intermediate
material
9
1
2
42
30
0
6
26
1
2
4
me 1
1
1
9
2
2
0
1
0
0
(2)
Chemicals
manufactured
as a final or
intermediate
material
8
0
0
62
2
0
0
2
0
0
0
0
0
0
0
0
0
0
2
4
0
(3)
Chemicals
for which
analyses have
been performed
in wastewater
1
0
1
6
3
1
1
2
1
1
1
1
1
0
1
1
2
1
0
0
1
                                  21

-------
                       TABLE III-2  (Continued)

         Summary  of  Responses to  Portfolio  B  of  1977  Survey
                       (Number  of Refineries)
 Priority Pollutants

 1,4-dichlorobenzene

 1,1-dichloroethylene

 1,2-trans-dichloroethylene

 2,4-dichlorophenol

 1,2-dichloropropane

 1,3-dichloropropylene

 2,4-dimethylphenol

 asbestos

 ethylbenzene

 fluoranthene

 methylene chloride

 methyl bromide

 trichlorofluoromethane

 dichlorodifluoromethane

 naphthalene

 nitrobenzene

 pentachlorophenol

 4-nitrophenol
methyl chloride

 isophorone
3 respondents summarized)
(1)
Chemicals
purchased
as a raw or
intermediate
material
0
6
lene 2
0
6
3
9
18
24
13
2
1
12
s 9
18
1
10
1
1
0
(2)
Chemicals
manufactured
as a final or
intermediate
material
0
0
0
0
0
0
11
0
31
11
0
0
0
0
18
0
1
0
0
1
(3)
Chemicals
for which
analyses have
been performed
in wastewater
1
1
0
2
1
1
14
1
3
1
0
0
0
0
2
0
1
0
0
1
                                22

-------
                            TABLE III-2  (continued)
        Summary of Responses to Portfolio B of 1977 Survey
                      (Number of Refineries)
Priority Pollutants
phenol
bis(2-ethylhexyl) phthalate
butyl benzyl phthalate
di-n-butyl phthalate
diethyl phthalate
dimethyl phthalate
PCB-1242
PCB-12S4
1,2-benzanthracene
benzo  (a)pyrene
3,4-benzofluoranthene
11,12-benzofluoranthene
chrysene
acenaphthylene
anthracene
1,12-benzoperylene
fluorene
phenanthrene
3 respondents summarized)
(1)
Chemicals
purchased
as a raw or
intermediate
material
32
alate 1
1
1
1
1
1
1
14
14
10
IB 10
16
11
16
14
10
16
(2)
Chemicals
manufactured
as a final or
intermediate
material
32
1
1
1
1
1
0
0
12
12
12
12
14
12
14
12
12
14
(3)
Chemicals
for which
analyses have
been performed
in wastewater
154
0
0
0
0
0
0
0
1
1
1
1
1
1
2
1
3
2
                                  23

-------
                             TABLE  III-2  (continued)

         Summary  of  Responses to  Portfolio B  of  1977 Survey
                       (Number of Refineries)
Priority"Pollutants

1,2:5,6-dibenzanthracene

indeno  (1,2,3-C,D)pyrene

pyrene

2,3,7,8-tetrachlorodib

tetrachloroethylene

toluene

trichloroethylene

vinyl chloride

antimony and compounds

arsenic and compounds

zinc and compounds

beryllium

cadmium and compounds

chromium and compounds

copper and compounds

cyanides

lead and compounds

mercury and compounds
3 respondents summarized)
(1)
Chemicals
purchased
as a raw or
intermediate
material
ne 11
ne 11
16
enzo-p-dioxin 0
2
53
12
0
8
6
71
0
4
80
26
1
121
5
(2)
Chemicals
manufactured
as a final or
intermediate
material
12
12
14
1
1
53
0
0
1
1
6
0
0
5
1
20
9
0
(3)
Chemicals
for which
analyses have
been performed
in wastewater
1
1
2
0
2
7
2
1
15
65
98
16
75
156
87
94
94
63
                               24

-------
                            TABLE  III-2  (continued)

        Summary of Responses to Portfolio B of 1977 Survey
                       (Number of Refineries)

                   (253 respondents summarized)

                                (1)            (2)            (3)
                               Chemicals     Chemicals     Chemicals
                               purchased     manufactured  for which
                               as a raw or   as a final or analyses have
                               intermediate  intermediate  been performed
Priority Pollutants            material      material      in wastewater

nickel and compounds               21             6              71

selenium and compounds              2             1              27

silver and compounds                6             1              36

thallium and compounds              11               5
                              2-5

-------
             TABLE III-3





PETROLEUM REFINING WASTEWATER  FLOW  DATA
Refinery
No.
1
2
3
4
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
Wastewater
Generated in 1976
(qal/bbl)
8
3
13
.04
4
4
4
11
14
35
192
31
7
5
9
7
14
3
22
4
13
4
Calculated
BPT Flow
(gal/bbl)
35
13
89
13
30
13
39
23
78
58
89
40
14
20
32
47
47
78
47
13
43
13
NPDES Discharge
in 1976 (gal/bbl)
8
3
13
0
4
4
0
11
14
35
21
0
0
0
0
0
0
.06
22
0
0
0
     26

-------
             TABLE  III-3




PETROLEUM REFINING  WASTEWATER FLOW DATA
Refinery
No.
24
25
26
29
30
31
32
33
35
36
37
38
39
40
41
42
43
44
45
46
Wastewater
Generated in 1976
(gal/bbl)
7
10
9
37
12
.6
70
10
15
3
31
37
11
34
36
5
62
25
43
22
Calculated
BPT Flow
(gal/bbl)
15
43
16
56
13
22
51
20
13
40
79
39
13
27
55
13
53
30
47
81
NPDES Discharge
in 1976 (gal/bbl)
7
0
0
0
12
0
40
0
0
0
31
0
0
34
36
0
46
0
0
22
          27

-------
            TABLE III-3





PETROLEUM REFINING WASTEWATER FLOW DATA
Refinery
No.
48
49
50
51
52
53
54
55
56
57
58
59
60
61
62
63
64
65
66
67
68
Wastewater
Generated in 1976
(gal/bbl)
112
5
10
67
107
19
6
2
29
129
26
24
11
17
19
36
68
29
UNKNOWN
65
41
Calculated
BPT Flow
(gal/bbl)
24
28
24
49
78
47
33
14
24
32
25
33
31
38
89
33
43
35
13
58
27
NPDES Discharge
in 1976 (qal/bbl)
0
5
S
67
107
19
6
0
29
129
0
24
1.3
17
19
36
68
29
0
64
41
           28

-------
            TABLE III-3




PETROLEUM REFINING WASTEWATER FLOW DATA
Refinery
No.
70
71
72
73
74
76
77
78
79
30
81
82
83
84
85
86
87
88
89
90
91
Wastewater
Generated in 1976
(gal/bbl)
17
13
23
25
10
56
12
26
UNKNOWN
5
22
281
35
21
25
15
18
6
22
25
3
Calculated
BPT Flow
(gal/bbl)
13
22
51
23
41
75
20
23
14
34
28
13
51
21
38
33
13
13
34
89
13
NPDES Discharge
in 1976 (gal/bbl)
17
13
23
0
10
56
12
0
0
5
22
0
35
21
25
0
18
6
22
18
3
            29

-------
             TABLE III-3





PETROLEUM REFINING WASTEWATER FLOW DATA
Refinery
No.
92
93
94
95
96
97
98
99
100
102
103
104
105
106
107
108
109
110
111
112
Wastewater
Generated in 1976
(gal/bbl)
44
15
23
29
25
3
13
3
9
32
2
30
30
18
4
19
21
7
24
36
Calculated
BPT Flow
(gal/bbl)
89
13
25
13
54
19
31
20
13
17
13
41
12
38
40
89
12
13
43
13
NPDES Discharge
in 1976 (gal/bbl)
42
8
23
0
22
3
12
3
9
32
2
24
28
14
4
19
21
7
0
36

-------
             TABLE III-3




PETROLEUM REFINING WASTEWATER FLOW DATA
Refinery
No.
113
114
115
116
117
118
119
120
121
122
124
125
126
127
128
129
130
131
132
133
134
135
Wastewater
Generated in 1976
(gal/bbl)
13
12
27
21
36
9
16
38
17
72
14
9
163
30
4
23
31
24
35
86
45
0
Calculated
BPT Flow
(gal/bbl)
25
20
56
49
30
88
78
89
27
47
36
28
36
43
13
16
20
38
41
60
32
13
NPDES Discharge
in 1976 (gal/bbl)
12
12
27
21
36
7
13
35
17
72
14
9
54
30
0
23
0
24
35
86
45
0
             31

-------
           TABLE III-3




PETROLEUM REFINING  WASTEWATER  FLOW DATA
Refinery
No.
136
137
138
139
140
141
142
143
144
145
146
147
148
149
150
151
152
153
154
155
156
157
158
Wastewater
Generated in 1976
(gal/bbl)
11
2
26
2
9
.09
26
38
14
5
24
9
10
27
24
25
83
35
209
13
20
16
13
Calculated
BPT Flow
(gal/bbl)
13
13
17
13
29
13
42
43
20
13
14
49
43
23
22
41
40
29
89
35
29
35
26
NPDES Discharge
in 1976 (gal/bbl)
0
0
0
0
0
0
26
38
4
0
24
9
0
27
24
25
83
19
23
7
17
16
13
            32

-------
            TABLE III-3




PETROLEUM REFINING WASTEWATER FLOW DATA
Refinery
No.
159
160
161
162
163
164
165
166
167
168
169
172
173
174
175
176
177
179
180
181
182
Wastewater
Generated in 1976
(gal/bbl)
15
8
14
30
20
6
5
16
33
19
56
98
224
109
81
14
134
12
46
47
27
Calculated
BPT Flow
(gal/bbl)
20
17
16
85
26
13
47
89
31
31
31
66
89
89
67
31
89
45
53
37
37
NPDES Discharge
in 1976 (gal/bbl)
14
8
8
27
20
0
5
0
31
18
55
98
224
109
78
11
134
12
46
4
0
              33

-------
             TABLE  III-3




PETROLEUM REFINING  WASTEWATER FLOW DATA
Refinery
No.
183
184
185
186
187
188
189
190
191
192
193
194
195
196
197
199
200
201
202
203
204
205
206
Wastewater
Generated in 1976
(gal/bbl)
13
22
11
13
16
27
3
5
9
201
.2
43
1
61
16
24
24
14
1
44
34
24
3
Calculated
BPT Flow
(gal/bbl)
16
47
24
24
43
30
13
13
43
13
13
60
13
50
13
13
36
20
13
47
29
23
13
NPDES Discharge
in 1976 (gal/bbl)
13
22
0
13
0
0
3
5
0
0
0
47
0
61
16
24
0
14
0
0
34
24
0
               34

-------
           TABLE III-3




PETROLEUM REFINING  WASTEWATER FLOW DATA
Refinery
No.
207
208
209
210
211
212
213
214
215
216
218
219
220
221
222
224
225
226
227
228
229
230
Wastewater Calculated
Generated in 1976 BPT Flow
(gal/bbl) {gal/bbl)
2
18
8
3
7
13
4
DATA NOT SUBMITTED
DATA NOT SUBMITTED
54
.1
17
2
29
42
12
35
8
37
16
3
30
13
41
20
13
21
20
13
-
-
45
13
28
85
17
10
14
36
13
25
14
27
40
NPDES Discharge
in 1976 (gal/bbl)
0
18
0
.2
7
13
4
0
0
35
0
17
0
29
42
0
0
8
16
0
0
30
               35

-------
           TABLE III-3





PETROLEUM REFINING  WASTEWATER FLOW DATA
Refinery
No.
231
232
233
234
235
236
237
238
239
240
241
242
243
244
245
246
247
248
249
250
251
252
253
Wastewater
Generated in 1976
(gal/bbl)
169
22
10
18
21
28
10
27
10
130
76
147
6
54
26
53
12
.01
21
0
0
21
DATA NOT SUBMITTED
Calculated
BPT Flow
(gal/bbl)
13
29
33
53
36
33
89
20
19
89
89
89
18
28
29
41
14
13
16
13
13
20
_
NPDES Discharge
in 1976 (gal/bbl)
169
22
10
18
21
28
10
27
10
130
50
147
6
0
0
0
0
0
0
0
0
21
0
                36

-------
           TABLE III-3





PETROLEUM REPINING WASTEWATER FLOW DATA
Refinery
No.
254
255
256
257
258
259
260
261
264
265
266
278
291
292
295
296
298
302
303
305
307
308
309
310
Wastewater
Generated in 1976
(gal/bbl)
.7
4
11
16
15
4
13
14
5
12
25
0
12
UNKNOWN
129
0
1
.04
0
4
0
0
18
.9
Calculated
BPT Flow
(gal/bbl)
89
13
17
31
110
19
89
14
13
25
13
13
13
13
13
13
13
13
13
13
13
13
18
13
NPDES Discharge
in 1976 (gal/bbl)
0
4
11
16
15
4
13
14
0
12
25
0
0
UNKNOWN
129
0
0
0
0
0
0
0
11
0
                  37

-------
                                  TABLE III-4

              Priority Pollutant  Discharge Monitoring Report
                        Data Reported in the 1977 Survey
               Refinery
               Number
   December 1975
DMR Daily Average
(mg/1)     (Ib/day)
                   December 1976
                DMR Daily Average
                (mg/1)    Ib/day)
Cadmium
               018
               025
               071
               182
               029
               038
               043
               045
 0.035
   ND
                  0.015
                    ND
                                         ND
Copper
               013
               018
               096
               153
               182
 0.072
   ND
  ND

  6
 0.63
  ND
                              0.042
           2.0
           0.85 .
          31.3™
Lead
               018
               057
               059
               060
               065
               068
               071
               073
               151
               153
               029
               038
               043
               045
               061
               062
               063
               064
               208
              013
              057
              096
              153
              182
              029
              038
              043
              045
              061
              062
              208
 0.005
 0.008
 0.037

 0.086
 0.0
 0.30
 0.03
 0.081
 0.03
                                     ND
 0.067
  ND
0.052
0.017
 0.01
10.4
 0.49
                                                2.75
  ND

  4
 0.59
  ND
0.036
0.129
0.006

0.036
0.0
0.64
0.007
                  0.047
                  0.03
                              0.02
                                ND
0.018
  ND
                              0.008
23
 0.13
                                               3.35
                                                                           22.2
 ND

 4.0
 0.36
 ND
                             0.03

                             7.9
                                     3  8

-------
                               TABLE III-4 (Cont.)
Mercury
Zinc
Arsenic
                Refinery
                Number
                058
                096
                182
                029
                038
                043
                045
                061
                013
                020
                024
                032
                041
                050
                057
                060
                065
                093
                096
                108
                114
                153
                182
                242
                029
                037
                038
                043
                045
                061
                062
                208
                295
                013
                182
                242
                029
                038
                043
                045
                208
   December 1975
DMR Daily Average
(mg/1)    (Ib/day)
            0.056
                   December 1976
                DMR Daily Average
                (mg/1)    Ib/day)
  0.59
  0.15
  0.23
  0.43
  0.131
   ND
   ND
             1.5
             0.30
             1.0
            18
 0.0024
12
 0.32

 1.1
31.2
 0.32
                                                             ND
                              1.1
                  0.14
                  0.04
0.31
0.193
           (0.98 kg/day)
            7.35
            1.6
 ND
 ND
0.53
                                          2.16
                            ND
                            0.11
                            0.10
                            5.1
                           22
 0.0011
 8
 0.22

 3.96 ,
27.9™
 0.22
                              0.1
 ND
 ND
                                      (0.45 kg/day)
                          10.5
                           0.57
 ND
 ND
0.20
                                                                      0.78
                                    39

-------
                                TABLE III-4 (Cont.)
 Nickel
Silver
Selenium
Cyanide (Free)
Refinery
Number

182
029
038
043
045
182
029
December 1975
DMR Daily Average
(mg/1)
ND

_

ND
(Ib/day)
ND



ND
December 1976
DMR Daily AveraoB
(mg/1)
ND

~
-
ND
Ib/day)
ND



ND
                182
                045
                153
                                          0.81
                                                            ND       ND
                                                           0.002    0.03
 NOTES:    ND -  Not  Detectable
          (a)    Data  are maximum values.
                          40

-------
                                                                         TABLE  II1-5
Sample - Day

Refinery A
  Intake - 1
  Intake - 2
  Intake - 3
  Separator effluent - 1
  Separator effluent - 2
  Separator effluent - 3
  Final effluent - 1
  Final effluent - 2
  Final effluent - 3

Refinery  B
  Intake - 1
  Intake - 2
  Intake - 3
  DAF effluent - 1
  DAF effluent - 2
  DAF effluent - 3
  Final effluent - 1
  Final effluent - 2
  Final effluent - 3

Refinery c
  Intake - 1
  Intake - 2
  Intake - 3
  Separator effluent - 1
  Separator effluent - 2
  Separator effluent - 3
  Treated effluent - 1
  Treated effluent - 2
  Treated effluent - 3
  Final effluent - 1
  Final effluent - 2
  Final effluent - 3
Concentration (nig/l)
BOD-1
L2
LI
2
20
20
25
L2
L2
3
L3
L3
2
130
170
270
15
9
30
2
L3
2
150
160
78
28
34
40
37
40
45
BOD-2 BOO- 3 COD
L2 4
LI 4
4 8
24 130
18 91
30 99
L2 36
L2 40
2 28
L3 9
L3 9
L3 9
140 420
110 440
220 500
14 150
7 120
7 120
1
1
2
110 380
120 370
85 220
130
120
120
130
130
100
TOC
1
2
2
36
25
26
11
11
11
13
25
18
100
110
110
47
39
43
12
8
5
88
75
49
44
39
41
42
37
36
TSS
5
4
LI
490
390
260
44
30
42
9
13
11
38
50
38
22
24
20
LI
LI
LI
22
36
26
20
18
28
20
22
16
NH3
Ll.O
11
1.0
13
11
11
16
11
9.0
Ll.O
Ll.O
Ll.O
8.4
7.3
6.7
18
16
18
Ll.O
Ll.O
Ll.O
52
50
13
8.4
5.6
4.5
7.8
17
3.9
+6
Cr
L.02
L.02
L.02
.09
.03
.05
.04
L.02
L.02
L.02
.02
L.02
L.02
.10
L.02
L.02
L.02
L.02
L.02
L.02
L.02
.05
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
if2
L.I
L.I
.2
9.0
6.9
8.5
.2
.2
.4
.2
.2
.4
.6
1.0
1.2
.5
.5
.6
L.5
L.S
.3
L.S
3.8
.3
L.S
L.S
.2
.5
.5
.4
OSG









19
7
6
33
18
11
53
24
15
8
10
4
150
100
28
8
15
11
7
11
11
        Flow (HGD)
7.6
9.0
8.B
8.6
8.5
9.0
6.9
7.4
7.0
6.2
8.1
*.3
S.2
8.6
9.5
7.2
7.6
7.4
7.6
7.8
7.4
8.6
9.1
8.7
7.8
7.7
7.6
8.0
8.1
7.6
 .433
 .427
 .432
3.91
3.86
4.12
1.78
1.81
1.81
1.69
2.07
1.48
  .0715
  .0848
  .1526
  .1787
  .1411
  .2357
Note: L - Less than
      G - Greater than

      BOD-1 indicates analytical method used seed from a domestic sewage treatment plant.

      BOD-2 indicates analytical method used seed from refinery final effluent.

      BOD-3 indicates analytical method where no seed was used.

-------
                                                                        TABLE III-5   (Continued)
                                               Analytical Results for Traditional Parameters for the RSKERL and BSR Sampling Program
                                                                            Concentration (mg/l)
Sample - Dav
Refinery L
Intake - 1
Intake - 2
Intake - 3
DAF effluent - 1
DAF effluent - 2
DAF effluent - 3
Final effluent - 1
Final effluent - 2
Final effluent - 3
Refinery E
Intake - 1
Intake - 2
Intake - 3
DAF effluent - 1
.Js, DAF effluent - 2
tO DAF effluent - 3
Final effluent - 1
Final effluent - 2
Final effluent - 3
Refinery F
Intake - 1
Intake - 2
Intake - 3
Cooling tower blowdown-1
Cooling tower blowdown-2
Cooling tower blowdown-3
Final effluent - 1
Final effluent - 2
Final effluent - 3
BOD-1

L5
1
3
160
140
120
50
210
150

3
2
2
54
52
45
18
2
LI

40
40
42
25
130
47
18
36
20
BOD-2

20
4
6
L220

L360




4
3
3
56
41
44




50
52

42
G160
36



BOD-3 COD

20
4
4
10OO
500
390
40 820
62 670
90 490

43
59
39
160
160
150
18 47
LI 75
LI 55

340
350
35 340
210
300
350
18 260
36 270
18 260
TOC

10
5
8
300
150
100
29O
220
150

15
15
15
48
42
39
10
7
13

96
110
97
62
78
95
iio
75
82
T33

24
32
16
60
36
32
64
60
60

14
19
28
17
13
16
9
20
13

68
68
40
64
76
80
110
96
100
Nil

Ll.O
2.2
2.0
36
29
40
36
42
39

1.0
7.8
7.8
13
12
15
35
11
13

1.7
68
63
3.9
10
19
3.9
2.8
3.9
rr-16 s 2 OK.G uH Flow (MGD)

L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
.03

L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02

L.02
.02
L.02
.05
.09
.41
L.02
L.02
.03

L.I
L.I
L.I
15
18
15
1.7
1.1
.8

L.I
L.I
L.I
1.8
1.5
1.5
.3
.5
.6

1.6
.9
.7

1.0
L.I

2.0
L.I

7.3
7.4
7.3
8.9 .932*
8.5
8.6
7.7 .932*
7.7
7.6

7.7 18.00
7.6 16.56
7.5 18.00
7.3
7.1
7.2
7.6 5.02
7.5 4.59
7.5 4.61

8.2 1.5*
8.1
8.0
7.3 0.17*
8.1
6.8
8.6 0.017*
8.5
8.6
* Average flow during  72-hour sampling period.

-------
                                                                                   TABLE III-5   (Continued)
U)
Sample-Day


 Refinery G
   Intake - 1
   Intake - 2
   Intake - 3
   Separator effluent - 1
   Separator effluent - 2
   Separator effluent - 3
   DAF effluent - 1
   DAF effluent - 2
   DAF effluent - 3
   Final effluent - 1
   Final effluent - 2
   Final effluent - 3

 Refinery  H
   Intake  - 1
   Intake  - 2
   Intake  - 3
   Separator effluent -  1
   Separator effluent -  2
   Separator effluent -  3
   Final effluent - 1
   Final effluent - 2
   Final effluent - 3

 Refinery  I
   Intake  - 1
   Intake  - 2
   Intake  - 3
   Separator effluent -  1
   Separator effluent -  2
   Separator effluent -  3
   Final effluent-1
   Final effluent-2
   Final effluent-3
Analytical Results for Traditional Parameters for

BOD-1
L3
L3
U
240
250
260
240
2BO
220
15
10
6
L2
L2
2
60
20
30
L6
L6
3
L3
L3
L3
88
76
55
L12
LI 2
LI 2

BOD- 2
L3
L3
L3
280
240
290
270
280
260



L2
L2
2
80
L15
31







32
66



the RSKERL and BSR Sampling Program
Concentration (mg/1)
BOD- 3 COD
L3 20
28
24
260 820

860
250 860
900
1200
12 200
L10 220
LI 4 210
12

23

200
180
L6 40
" 36
3 48
4
5

™ 260
260
250
88
"2 76
L12 72
TQC
12
16
8
240

220
200
360
290
60
64
56
9

14

57
50
20
18
21
5
4

89
80
75
34
29
29
TSb
LI
18
16
54
252
112
64
152
176
36
76
64
14
113
167
120
66
121
8
10
8
LI
LI
2
38
46
32
6
8
10
NH3
Ll.O
Ll.O
Ll.O
20

8.0
14
12
10
IS
15
12
Ll.O

Ll.O

7.3
6.2
6.2
5.0
5.0
Ll.O
Ll.O

3.4
4.5
5.0
Ll.O
Ll.O
1.7
Cl*6
L.02
L.02
L.02
.02
.02
L.02
.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
.04
L.02
.02
.04
L.02
L.02
L.02









-2
S
L.I
.6
.3
22
32
28
18
28
30
2.0
1.8
2.1
.3
L.I
.1
3.7
4.4
1.2
.2
.2
.1
.5

.4
.5

.6
.7

.4
MG
23
7
8
130
56
110
190
250
220
24
9
10
31
13
8
80
51
24
37
13
3
2
4
5
30
25
42
5
3
9
                                                                                                                                                                         E»
                                                                                                                                                                        7.6
                                                                                                                                                                        7.6
                                                                                                                                                                        7.7
                                                                                                                                                                       10.2
                                                                                                                                                                       10.3
                                                                                                                                                                       10.6
                                                                                                                                                                        9.9
                                                                                                                                                                       10.2
                                                                                                                                                                       10.4
                                                                                                                                                                        8.3
                                                                                                                                                                        8.O
                                                                                                                                                                        8.0
8.2
8.5
7.9
7.3

8.6
7.4
8.4
7.8
                                                                                                                                                                        7.8
                                                                                                                                                                        8.6
                                                                                                                                                                        7.6
                                                                                                                                                                        5.7
                                                                                                                                                                        9.1
                                                                                                                                                                        8.9
                                                                                                                                                                        7.1
                                                                                                                                                                        7.2
                                                                                                                                                                        7.5
               3.22
               3.13
               3.20
               2.50
               2.27
               2.04
                                                                                                                                                                                      35. •
               3.53
               3.53
               3.53
               2.99
               3.26
               3.29
               2.75
               2.27
               2.44
 *Average flow during the campling period.

-------
                                                                               TABLE III-5  (Continued)
eiinery  l

 Intake-1
 Intake-2
 Intake-3
 Separator 1 effluent-1
 Separator 1 effluent-2
 Separator 1 effluent-3
 Separator 2 effluent-1
 Separator 2 effluent-2
 Separator 2 effluent-3
 Separator 3 effluent-1
 Separator 3 effluent-2
 Separator 3 effluent-3
 Separator 4 effluent-1
 Separator 4 effluent-2
 Separator 4 effluent-3
 Separator 5 effluent-1
 Separator 5 effluent-2
 Separator 5 effluent-3
 Bio-pond influent-1
 Bio-pond influent-2
 Bio-pond influent-3
 Final effluent-1
 Final effluent-2
 Final effluent-3
Concentration (mg/1)

BOD-1
L5
2

51
76

85
G84

15
20

GSO
70

10
12

96
G84

6
6


BOD-2 BOD-3


3
39
78
50
G84
GB4
G84
58
22
32
100
55
60
10
10
18


G84


6

COD
16
40
20
210
160
160
310
690
660
160
180
220
310
270
430
83
75
92
610
570
480
87
87
92

TOO
14
19
10
60
39
55
57
200
230
52
45
63
66
58
97
23
22
31
50
100
120
34
26
32

TSS
10
3
1
54
82
22
64
196
108
62
38
34
36
26
94
26
16
48
24
16
18
20
7
8

NH,
2.0
Ll.O
Ll.O
2.0
1.0
1.7
8.4
14
8.4
3.0
6.2
4.5
3
7.3
8.4
2.0
1.0
Ll.O
22
24
20
6.8
5.0
5.6
+6
Cr
L.02
.02
L.02
.02
L.02
.03
L.02
.04
.02
.02
.02
.04
L.02
L.02
.05
.14
.13
.09
.08
.10
.08
L.02
L.02
L.02
-2
S
L.I
L.I
.3
.7
1.8
1.8
5.5
11
15
1.8
5.3
1.5
6.8
9.1
5.1
L.I
1.0
12
14
49
3.5
.2
1.0
.9

040
16
11
11
74
120
36
84
140
250
25
23
54
65
34
150
7
9
25
11
9
20
20
6
16
7.5
7.8
7.3
8.9
8.2
7.9
8.2
8.2
8.2
7.4
7.3
7.3
7.7
7.3
7.6
8.1
8.1
7.1
7.4
7.7
7.5
7.0
7.3
7.9
.464
.122
.572
2.70
2.55
2.73

-------
                                                                                    TABLE  III-5   (Continued)
in
Refinery  K
  Intake-1
  Intake-2
  Intake-3
  OAF effluent-1
  DAP effluent-2
  OAF effluent-3
  Final effluent-1
  Final effluent-2
  Final effluent-3

Refinery L
  Intake-1
  Intake-2
  Intake-3
  Separator 1 effluent-1
  Separator J effluent-2
  Separator 1 effluent-3
  Separator 2 effluent-1
  Separator ? effluent-2
  ieparator 2 effluent-3
  Final effluent-1
  Final effluent-2
  Final effluent-3

Refinery M
  Intake-1
  Intake-2
  Intake-3
  DAF effluent-1
  DAF effluent-2
  DAF effluent-3
  Final effluent-1
  Final effluent-2
  Final effluent-3
Concentration (mg/1)
BOD-1
4
4
L6
L120
220
L120
8
L6
11
2

L2
100

180
32

40
3

11
L6
L6
L6
51
50
36
LI 2
L6
L6
BOP- 2



LI 20
210
L120



3
L5
L3
130
100
1.70
38
31
42






25
52
40



BOD-3
4
4
L6
80
200
LI 20
7
6
10
2
L3
L5
120
98
150
34
42
40
3
L4
8
L6

L6
34
40
34
L12
L6
L6
COP
27
23
24
530
1000
540
96
130
140
56
20
24
390
350
530
200
210
170
75
44
71
10
9
8
260
220
220
92
86
73
TOC

11
10
180
350
180

39
42
13
10
6
110
110
140
49
56
46
19
15
14
6
10
4
72
62
66
18
16
14
TSS
12
14
10
260
3 BO
210
21
16
32
290
220
120
140
110
120

36
48
34

21
LI
LI
LI
18
9
7
8
15
11
NH3
Ll.O
Ll.O
1.0
6.7
6.7
6.2
2.2
3.4
3.9
Ll.O
Ll.O
Ll.O
6.2
10
20
7.8
15
9.0
Ll.O
3.4
3.0
Ll.O
Ll.O
Ll.O
13
9.5
12
Ll.O
Ll.O
1.0
tlj
Cr
L.02
L.02
L.02
L.02
.04
.02
L.02
L.02
L.02
.25
L.02
.05
L-02
L.02
.07
.05
L.02
L.02
L.02
.11
.01
L.02
L.02
L.02
.75
L.02
L.02
L.02
L.02
L.02
s~2
.4
.4
.3
.8
1.6
.6
.5
.3
.3
.1
1.0
1.0
.9
1.5
1.2
.8
1.7
.9
.4
.3
.9
.2
.2
.3
.6
.5
.4
.4
.4
.3
OSG
9
6
14
590
190
98
31
15
12












4
8
11
16
18
18
13
12
14
                                                                                                                                                           DH
                                                                                                                                                            7.4
                                                                                                                                                            7.8
                                                                                                                                                            7.3
                                                                                                                                                            7.7
7.2
7.5
7.1
7.9
8.3
8.6
8.0
6.3
8.4
7.2
6.9
7.2
                                                                                                                                                            8.0
                                                                                                                                                            8.0
                                                                                                                                                            8.1
                                                                                                                                                            6.9
                                                                                                                                                            8.4
                                                                                                                                                            8.2
                                                                                                                                                            7.7
                                                                                                                                                            7.9
                                                                                                                                                            7.8
                                                                                                                                                                          14.1*
 3.88
 3.86
 4.28
 7.15
 5.37
 4.98
11.03
 9.23
 9.26
             1.64
             1.52
             1.47
         Average flew  during 72-hour sampling period.

-------
                                                                                 TABLE II1-5  (Continued)

                                                      Analytical Results for Traditional  Parameters jor  the RSKERL  and _B&R Sampling^rogram
                                                                                    Concentration (mg/lj
          Re f ine ry  N
            Intake-1
            In take-2
            Intake-3
            Separator  effluent-1
            Separator  effluent-2
            Separator  effluent-3
            Chem.  plant effluent-1
            Chem.  plant effluent-2
            Chem.  plant effluent-3
js.          Final  effluent-1
Q\          Final  effluent-2
            Final  effluent-3

          Refinery 0
            Intake-1
            Intake-2
            Intake-3
            OAF effluent-1
            DAF effluent-2
            DAF effluent-3
            Final  effluent-1
            Final  effluent-2
            Final  effluent-3
BOD-l












L2
L5
L3
120
100
85
6
L10
94
BOD-2 BOD- 3
LI
L5
L2
83
100
120
74
140
34
10
8
10

L5
L2

75
88

L10
L8
COD
40
16
28
360
430
440
340
810
240
140
120
140
11
26
12
380
410
480
150
140
120
TOO
12
a
12
88
120
100
93
240
69
33
33
36
10
21
25
120
110
180
48
40
52
TSS
18
22
26
68
112
76
28
36
40
50
40
44
10
10
14
21
32
42
24
26
24
NH
— j
Ll.O
Ll.O
Ll.O
12
15
13
1.1
Ll.O
2.0
6.2
6.7
3.0
Ll.O
Ll.O
Ll.O
5.3
6.4
18
2.5
3.1
2.5
	 ^ 	
Or
L.02
.07
.09
L.02
L.02
L.02
L.02
L.02
L,02
L.02
L.02
L.02
L.02
.02
.02
L.02
L.02
L.02
L.02
.02
L.02
s o&s
.3
.3
1.1
2.9
8.1
9.2
.7
.9
.9
.6
.9
.9
.5
L.I
.1
3.9
4.1
2.9
.6
.5
.4
                                                                                                                                                   O&S          J>H
8.4
7.7
7-3
8.1
8.1
7.9
6.8
6.6
6.7
8.6
7.4
7.4
7.1
6.8
7.0
8.4
8.6
8.8
7.9
24.69
26.84
25.91
15.25
15.25
18.25
0.8
0.95
0.9
14.75
15.9
17.6



2.88*


2.88*
          *Average  flow during 72-hour period.

-------
                                                                                  TABLE  III-5  (Continued)
                                                       Analytical Results for Traditional Parameters tor  the  RSKERI, and BtR Sampling Program
Sample-Day

Befinery P
  Intake-!
  Intake-2
  Intake-3
  Separator effluent-1
  Separator effluent-2
  Separator effluent-3
  Final effluent-1
  Final effluent-2
  Final effluent-3

Refinery Q
  Intake-1
  Intake-2
  Intake-3
  Separator eff luent-1
  Separator effluent-2
  Separator effluent-3
  Final effluent-1
  Final effluent-2
  Final effluent-3
Concentration (mg/1)
BOD-1
L2
L5
L2
320
210
150
LS
L5
L3
L2
L2
L3
80
40
66
28
20
30
BOD-2 BOP-3 COD
4
LS 6
L2 L4
600
220 540
160 470
64
L5 49
L3 41
4
4
24
50 370
70 330
64 260
260
2SO
230
TOC
3
7
7
170
140
140
16
24
31
8
11
9
91
84
65
59
78
60
ms
Ll
Ll
Ll
68
78
42
11
2
7
3
2
Ll
28
10
12
38
22
26
NHi
Ll.O
Ll.O
Ll.O
11
16
18
1.4
2.0
2.0
Ll.O
Ll.O
Ll.O
45
48
39
53
49
42
Cr+6
L.02
L.02
L.02
L.02
.15
.05
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
r2
L.I
L.I
L.I
25
25
23
.3
.6
L.I
.4
.3
.3
9.3
5.6
2.4
.7
.6
.5
OtG









5
9
13
62

38
45
45
37
 7.0
 6.8
10.1
 9.9
 7.7
 7.5
 7.1
 7.4
 7.5
 9.2
 9.3
 9.8
 8.8
 8.3
 8.7
                                                                                                                                                                                   Flow (MSP)
.2783
.3086
.3186

-------
                                   TABLE III-6

                    ANALYTICAL RESULTS FOR PRIORITY POLLUTANTS

                      FOR THE RSKEKL AND B&R SAMPLING PROGRAM

                       VOLATILE ORGANICS (CONCENTRATIONS, ug/1)
                                                      Refinery A
 Compound

 4   Benzene
 23  Chloroform
 29  1,2-trans-Dichloro
 38  Ethylbenzene
 44  Methylene chloride
 85  Tetrachloroethylene
 86  Toluene
 4   Benzene
 23  Chloroform
 44  Methylene chloride
 4   Benzene
 10   1,2-Dichloroethane
 23   Chloroform
 38   Ethylbenzene
 44   Methylene  chloride
 4    Benzene
 38   Ethylbenzene
 86   Toluene
 4    Benzene
 38   Ethylbenzene
 44   Methylene  chloride
 85   Tetrachloroethylene
 86   Toluene
 87   Trichloroethylene
6   Carbon tetrachloride
11  1,1,1-Trichloroethane
44  Methylene chloride
4   Benzene
44  Methylene chloride
86  Toluene
4   Benzene
23  Chloroform
44  Methylene chloride
86  Toluene



ithylene











Intake
ND
ND
D(L
ND,
85b















e
ne


Intake Water
NDb
70
i ND
ND
G (100)°
ND
ND

Intake Water
X
NDb
D(L 10)
22d

Separator Effluent
G(100).
D(L 5)°
20
G(100),
G(100)D
G(50)
G(100)
Refinery B°
DAF Effluent
h
ND°
11
30b
Refinery Ce
Final Effluent
ND b
D (L 5)
ND
ND b
G(100)
D(L 10)
ND

Final Effluent
h
D(L 10)°
D(L 10)°
NDb

Water Separator Effluent Treated Effluent Final Effluent
417b
, 16
Db ND
P

Intake Water
ND
ND
ND

Intake Water
ND
ND,
50d
50
ND
20

Intake Water
G(50)
G(50) d
D(L 10)

ND
ND
ND
"9
Refinery D
Separator Effluent
G(100)
G(100)
G{100)
Refinery E
DAF Effluent
G(100)
G(100)
10d
ND
G(100)
ND
Refinery F
ND
ND
ND
NO,
20d

Final Effluent
ND
ND
ND

Final Effluent
ND
ND,
10d
ND
ND
ND

Cooling Tower Slowdown Final Effluent
ND
ND.
70b
Refinery Ge
ND
ND
D(L 10)d

Intake Water Separator Effluent DAF Effluent Final Effluent








»<&"
D(L 1)

Intake Water
NDb
D(L 10)
ND
ND
409b 2,
293°
96 76,
Refinery Hc
Separator Effluent
NDb
55b
ND
ND
005 D(L 1)
563b 12d
405 D(L 1)

Final Effluent
$

70°
D(L 10)
                                       48

-------
                               TABLE III-6   (Continued)
4   Benzene
23  Chloroform
38  Ethylbenzene
44  Methylene chloride
86  Toluene
                                                        Refinery  I

                                      Intake Water   Separator Effluent  Final  Effluent
D(L
8/d(L
ND/ND
12/73
ND/ND
2434
ND
812
19d  „
11767C
                                                      ND
                                                      ND
                                                      74b   b
                                                      D(L 1)
                                                        Refinery K

                                     Intake Water   Separator Effluent  Final Effluent
4   Benzene
10  1,2-Cichloroethane
IS  1,1,2,2-Tetrachloroethane
23  Chloroform
30  1,2-trans-Dichloroethylene
38  Ethylbenzene
44  Methylene chloride
85  Tetrachloroethylene
86  Toluene
                 ND
                 ND
                 ND
                 D(L 10)
                 ND
                 ND.
                 NDb
                 ND
                 ND
                     NDb
                     ND b
                     100
                     ND°
                     NDb
                     11DO
                     ND°    -
                     D(L 10)
                    ND
                    D(L 10)
                    D(L 10) ,
                    D(L 10)°
                    D(L 10)
                    D(L 10)
                    ND
                    D(L 10)
                    ND
4   Benzene
23  Chloroform
38  Ethylbenzene
44  Methylene chloride
86  Toluene
                                Refinery L
                                                           Final
Intake Water  Separator 1 Effluent  Separator 2 Effluent  Effluent

                                                             ND
                                                             ND
                                                             ND
                                                             60b
                                                             ND
ND
ND
40b
ND
G(100)
10
GdOOK
G(100)
G(100)
G(100)
10
G(100)
50b
G(100)
                                                        Refinery M
    Benzene
6   Carbon tetrachloride
23  Chloroform
44  Methylene chloride
86  Toluene
                                      Intake Water

                                         14b
                 91
                 D(L 10)
                 DAF Effluent

                     12d
                     D(L 10)
                     55%
                     180d
                     D(L 10)
                                                                        Final Effluent
                    D(L 10)
                    D(L 10)?
                    D(L 10)
                    D(L 10)
                                                        Refinery N
                        Intake Water  Chem.Plant Effluent  Separator Effluent Final Effluent
4   Benzene
23  Chloroform
38  Ethylbenzene
44  Methylene chloride
86  Toluene
     ND
     ND
     ND
     G(IOO)
     ND
        90
        10
        20
        G(100)
        G(100)
G(100)
15
G(100)h
G(100)°
G(100)D
6d
ND
ND h
G{100)
35
                                                        Refinery 0
4   Benzene
6   Carbon tetrachloride
23  Chloroform
44  Methylene chloride
86  Toluene
             Intake Water

                 ND
                 D(L 10)
                 55
                 130
                 D(L 10)
                 DAF Effluent

                     D(L 10)b
                     ND
                     13
                     ND
                     16
              Final Effluent

                    D(L 10)u
                    D(L 10)
                    32?
                    44
                    ND'
                      d
                                                        Refinery P

                                     Intake Water  Separator Effluent  Final Effluent
4   Benzene
6   Carbon tetrachloride
15  1,1,2,2-Tetrachloroethane
23  Chloroform
30  1,2-trans-Dichloroethylene
38  Ethylbenzene
44  Methylene chloride
85  Tetrachloroethylene
86  Toluene
87  Trichloroethylene
                 D(L 10)°
                 ND
                 D(L 10),,
                 D(L 10)
                 11
                 ND
                 ND
                 D(L 10)
                 D(L 10)
                 D(L 10)
                     1,100
                     ND
                     ND b
                     100
                     ND
                     28   t
                     1,600
                     ND
                     655
                     ND
                   D(L 10)°
                   D(L 10)°
                   D(L 10)h
                   D(L 10)
                   ND
                   ND
                   41
                   ND
                   ND
                   D(L 10)
                                           49

-------
                             TABLE  III-6  (Continued)
4   Benzene
23  Chloroform
44  Methylene chloride
48  Dichlorobromomethane
86  Toluene
                                                        Refinery Q

                                    Intake Water  Separator Effluent  Final Effluent
D(L 1)
ND
63
ND
ND
894
6°
4d
24
167
ND
ND
ND
ND
Notes:
     Volatile organic compounds not listed for a refinery were not detected in samples
     taken at that refinery.

     ND - Compound was not detected.

     D(Lx)  - Compound was detected at some concentration less than x, but the concentration
     could not be quantified.

     G(x) - Compound was detected at  u level greater than x.

     a)  Midwest Research Institute conducted the analyses for volatile organic compounds
     in samples from Refineries A, D, E,  F,  L, N.  See Reference No. 149.

     b)  Compound was detected in sample  blank.

     c)  NUS Corporation conducted the analyses for volatile organic compounds in samples
     from Refineries B,  H, K,  M, 0, P.

     d)  Compound was detected at a greater level in sample blank than in sample.

     e)  Gulf South Research  Institute conducted the analyses for volatile organic
     compounds in samples from Refineries C, G, I,  Q.   These data represent results
     from one-time grab  samples collected during revisits to these refineries.
     Additional sampling was  necessary because the  initial volatile organic results
     had been considered invalid due  to improper analytical techniques.  Since the
     revisit to Refinery J was conducted  by an EPA  regional surveillance and analysis
     sampling team,  the  results are not presented in this table.

     f)  Concentrations  presented are for unpreserved/preserved samples.
                                         50

-------
                                          TABLE III-7

                          ANALYTICAL RESULTS FOR PRIORITY POLLUTANTS

                            FOR THE RSKERL AND B&R SAMPLING PROGRAM

                           SEMiyOLATILE QRGANICS  (CONCENTRATIONS, uo/11
Compound
Base - Neutral Extraetables

  1  Acenaphthene
 55  Naphthalene
 77  Acenaphthylene
 81  Phenanthrene/78 Anthracene
 68  Di-n-butyl phthalate
 70  Diethyl phthalate

Acid Extraetables
~65Phenol
     Intake water
          ND
          ND
          ND
           D(LO.l)
          0.2
          ND
                                             ND
   Refinery Aa

Separator Effluent
       37
       68
        4
        5
       1.3
       12
                                                                 13
                                               Final Effluent
 ND
 ND
 ND
 ND
 0.7
 ND
                                                                                     ND
Base-Neutral Extractables

Acid Extraetables

 22  Parachlorometa cresol
 34  2,4 - Dimethylphenol
 58  4- Nitrophenol
 65  Phenol
Base-Neutral Extractables

 55  Naphthalene
 81  Phenanthrene/78 Anthracene
 66  Bis(2-ethylhexyl) phthalate

Acid Extractables

 65  Phenol

Intake Hater
ND
ND
ND
ND
ND

Intake Separator
Water Effluent
ND 950
ND 190
150 290
Refinery Bu
DAF Effluent
ND
ND
10,000
ND
ND
Refinery C-l
Treated
Effluent
ND
ND
900

Final Effluent
ND
D (L 10)
D (L 10)
D (L 10)
D (L 10)

Final
Effluent
ND
ND
310
                                     ND
                  2200
                                  ND
                                                ND
Base-Neutral Extractables

Acid Extractables
Final Effluent

     ND

     ND
                                                              Refinery C-2
Base-Neutral Extractables

 39  Fluoranthene
 55  Naphthalene
 73  Benzo  (a) pyrene
 76  Chrysene
 81  Phenanthrene/78 Anthracene
 84  Pyrene

Acid Extractables
                                   Intake Water
     ND
      2
     ND
     ND
      D(LO.l)
     ND

     ND
                           Refinery D

                       Separator Effluent9
        3
      190
       ND
      0.1
      140
       11

       ND
                                                                                 Final Effluent
 ND
 ND
  3
1.4
 ND
  7

 ND

-------
                                         TABLE  III-7(continued)
                                                             Refinery E

                                    Intake Water    DAF  Effluent13   Final Effluent   Final Effluent
Base-Neutral Extractables
1
25
27
39
55
76
80
81
84
68
Acid
34
65
Acenaphthene
1 , 2-Dichlorobenzene
1 , 4-Dichlorobenzene
Fluoranthene
Naphthalene
Chrysene
Fluorene
Phenanthrene/78 Anthracene
Pyrene
Di-n-butyl phthalate
Extractables
2 , 4-Dimethylphenol
Phenol
                                        1.8
                                     D(L0.5)
                                     D(L0.5)
                                     D(L0.2)
                                        ND
                                        ND
                                        ND
                                        ND
                                     D(LO.l)
                                       0.4
                                       ND
                                       ND
                    150
                    ND
                    ND
                    ND
                    106
                    0.3
                    110
                     50
                      5
                     ND
                    G(100)
                    G(100)
ND
ND
ND
ND
ND
D(LO.l)
ND
ND
D(L0.5)
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
D(LO.
D(LO.
ND
ND
ND







1)
5)



Base-Neutral Extractables
                                                             Refinery  F

                                   Intake Water-*-  Cooling Tower  Slowdown   Final Effluent
  39  Fluoranthene                      29
  73  Benzo  (a) pyrene                  33
  76  Chrysene                          49
  81  Phenanthrene/78 Anthracene       160
  84  Pyrene                           140

Acid Extractables                      ND
                    ND
                    10
                     7
                     2
                    10

                    ND
                         ND
                         1.3
                         0.8
                         ND
                         ND

                         ND
Base-Neutral Extractables

 39  Fluoranthene/84 Pyrene
 55  Naphthalene
 76  Chrysene/72 Benzo  (a)
       Anthracene
 81  Phenanthrene/78 Anthracene
 66  Bis  (2-ethylhexyl)phthalate

Acid Extractables
                                                            Refinery  G-l

                                   Intake Water   Separator Effluent   DAF  Effluent   Final Effluent
 65  Phenol
    ND
    ND
    ND

    ND
  1100
                                       10
   40
 1100
   40

 1100
  700
                                                        4900
 ND
 700
 ND

 600
1100
                                                                           2400
 ND
 ND
 ND

 ND
850
                                                                                           ND
                                   Final Effluent
                                                            Refinery G-2
Base-Neutral Extractables
 70  Diethyl phthalate

Acid Extractables
     1

     ND
Base-Neutral Extractables
 66 Bis(2-ethylhexyl)phthalate
Acid Extractables

 31  2,4-Dichlorophenol
 34  2,4-Dimethylphenol
 65  Phenol
Intake Water

     ND
     ND
     ND
     ND
     Refinery H

Separator Effluent

        ND
     ND
     175
     440
                                                                                 Final Effluent
                                                 D  (L  10)
           10
           ND
           ND
                                             52

-------
                                           TABLE III-7(continued)

                                                                 Refinery I-le

                                   Intake Water        Separator Effluent       Final Effluent
Base-Neutral Extractablea

 55  Naphthalene
 66  Bis(2-ethylhexyl)phthalate
 68  Di-n-butyl phthalate

Acid Extractables

 65  Phenol
    ND
   950
    30
                                        ND
     290
     300
      ND
                                                            390
                  ND
                  600
                  10
                                                                                     ND
                                                                  Refinery 1-2
 Base-Neutral Extractable

 Acid Extractable
Final Effluent

     ND

     ND
 Base-Neutral Extractables

   1  Acenaphthene
  39  Fluoranthene/84 Pyrene
  55  Naphthalene
  76  Chrysene/72 Benzo (a)
        anthracene
  81  Phenanthrene/78 Anthracene
  80  Fluorene
  66  Bis(2-ethylhexyl)phthalate
  70  Diethyl phthalate
  71  Dimethyl phthalate

 Acid Extractables

  34  2,4-DimethyIphenol
  64  Pentachlorophenol
  65  Phenol
                                    Intake Water
     ND
     ND
     ND
     ND

     ND
     ND
     110
     ND
     ND
     ND
     ND
     ND
                                                    Separator 1
                                                     Effluent
 ND
 30
 ND
 30

 30
 ND
180
 ND
 ND
 ND
 ND
420
                              Refinery J

                              Separator 2
                                Effluent
    ND
    ND
    350
     30

     90
    ND
    300
    ND
    ND
    ND
    ND
    160
                          Separator 3
                            Effluent
ND
ND
ND
50

ND
ND
50
ND
ND
ND
ND
ND
                                                                  Refinery J  (continued)
 Base-Neutral Extractables
                                     Separator 4
                                       Effluent
   1  Acenaphthene                       50
  39  Fluoranthene/84 Pyrene             20
  55  Naphthalene                        ND
  76  Chrysene/72 Benzo(a)anthracene     40
  81  Phenanthrene/78 Anthracene        230
  80  Fluorene                           80
  66  Bis(2-ethylhexyl)phthalate        600
  70  Diethyl phthalate                  ND
  71  Dimethyl phthalate                 ND
 Acid Extractables

  34  2,4-DimethyIphenol
  64  Pentachlorophenol
  65  Phenol
    650
    850
 16,000
               Separator 5
                Effluent
                    ND
                    ND
                    ND
                    ND
                    ND
                    ND
                    ND
                    ND
                    ND
 ND
 ND
 ND
            Bio-Pond
            Influent
                ND
                ND
                ND
                ND
                ND
                ND
                210
                ND
                ND
    750
    ND
G(12,000)
                Final
               Effluent
                   ND
                   ND
                   ND
                   ND
                   ND
                   ND
                   190
                    30
                     3
ND
ND
ND
 Base-Neutral Extractables

 Acid Extractables

  24   2-Chlorophenol
  34   2,4-DimethyIphenol
  58   4-Hitrophenol
  59   2,4-Dinitrophenol
  65   Phenol
                                    Intake Water

                                         ND
     ND
     ND
     ND
     ND
     ND
                              Refinery K

                    Separator Effluent

                         ND
      315
    1,150
    5,800
   11,000
      105
                                                                           .d
                          Final Effluent

                               ND
                   ND
                   ND
                   ND
                   ND
                   ND
                                                53

-------
                                             TABLE III-7(continued)
                                   Intake
                                   Water
            Separator
             Effluent
                 Refinery L

                 Separator 2
                  Effluent
                 Final
                Effluent
Base-Neutral Extractables

  1  Acenaphthene                   29
 39  Fluoranthene                  0.2
 55  Naphthalene                     1
 76  Chrysene                      ND
 77  Acenaphthylene                0.2
 80  Fluorene                        1
 81  Phenanthrene/78 Anthracene      1
 84  Pyrene                        0.3
              ND
              ND
              500
               20
              ND
              270
              230
              ND
                       3,000
                           9
                         280
                           2
                         ND
                         300
                         ND
                           7
                 D(LO.l)
                     0.1
                     0.3
                   ND
                   ND
                     1
                 D(LO.l)
Acid Extractables

 34  2,4-Dimethylphenol
 65  Phenol
ND
ND
G(100)
G(100)
      G(100)
      G(100)
   ND
   ND
Base-Neutral Extractables
                                                                 Refinery M

                                   Intake Water        DAF Effluent        Final  Effluent

                                        ND                  ND                  ND
Acid Extraetables
 22  Parachlorometa cresol
 34  2,4-Dimethylphenol
 58  4-Nitrophenol
 59  2,4-Dinitrophenol
 65  Phenol
    ND
    ND
    ND
    ND
  D(L 10)
            ND
           18,300
            1,400
            2,660
           33,500
                10
                ND
                ND
                ND
              D(L 10)
                                   Intake
                                   Water
         Chera. Plant
           Effluent
                 Refinery N

             Separator^      Final
              Effluent     Effluent
Base-Neutral Extractables
  1  Acenaphthene
 39  Fluoranthene
 55  Naphthalene
 76  Chrysene
 77  Acenaphthylene
 81  Phenanthrene/78 Anthracene
 84  Pyrene

Acid Extractables
 22  Parachlorometa cresol
 34  2,4-Dimethylphenol
 65  Phenol
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
  ND
  ND
  27
D(LO.l)
  ND
   1
   1
  10
G(100)
  40
 522
   8
 302
   6
  87
 140
  16
  ND
  71
G(100)
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
                                   Intake Water
Base-Neutral Extractables
                             Refinery O

                   DAF Effluent        Final Effluent
  1  Acenaphthene
 39  Fluoranthene
 54  Isophorone
 55  Naphthalene
 68  Di-n-butyl phthalate
 71  Dimethyl phthalate
 76  Chrysene
 77  Acenaphthylene
 78  Anthracene
 80  Fluorene
 81  Phenanthrene
 84  Pyrene

Acid Extractables
 34  2,4-Dimethylphenol
 65  Phenol
    ND
    ND
    ND
    ND
    ND
    ND
    ND
    ND
    ND
    ND
    ND
    ND
    ND
    ND
            390
             ND
          2,500
          3,750
             ND
             ND
             ND
            530
          1,750
            495
          1,750
             ND
          2,000
          1,900
                ND
                ND
                ND
                ND
                ND
                ND
                ND
                ND
                ND
                ND
                ND
                ND
                ND
                ND
                                           54

-------
                                             TABLE  III-7(continued)
Base-Neutral Extractables

  1  Acenaphthene
 54  Isophorone
 55  Naphthalene
 77  Acenaphthylene
 78  Anthracene
 81  Phenanthrene

Acid Extractables
 57  2-Nitrophenol
 58  4-Nitrophenol
 59  2,4-Dinitrophenol
 60  4,6-Dinitro-o-cresol
Base-Neutral Extractables

 66 Bis(2-ethylhexyl)phthalate
 68 Di-n-butyl phthalate
 71 Dimethyl phthalate

Acid Extractables

 65 Phenol
Base-Neutral Extractables

 70  Diethyl phthalate

Acid Extractables
                                        Intake Hater
   ND
   ND
   ND
   ND
   ND
   ND
D (L 10)
D (L 10)
   ND
   ND
                                        Intake Water
 1,100
    20
    20
                                              10
                                        Final Effluent
     1

    ND
                    Refinery P

                Separator Effluent
       315
     3,550
     3,200
       665
       660
       660
     1,350
        20
       110
        60

     Refinery Q-le

Separtor Effluent
       320
       ND
       ND
                                                                  60

                                                                Refinery Q-2f
                                                                                Final Effluent
ND
ND
ND
ND
ND
ND
ND
ND
ND
ND
                                                                                Final Effluent
2,000
ND
ND
                                                                                     ND
NOTES:
     Semivolatile organic compounds not listed for a refinery were not detected in samples taken
     at that refinery.

     ND - Compound was not detected.

     D(LX) - Compound was detected at some concentration less than X, but the concentration could
     not be quantified.

     G(X) - Compound was detected at a level greater than X.

     (a)  Midwest Research Institute conducted the analyses for semivolatile organic compounds in
          samples from Refineries A,D,E,F,L,N.  See Reference No. 149.

     (b)  Base-neutral extract was diluted 1:10 before analysis.
     (c)  Concentrations represent sums for these two compounds which elute simultaneously and
          have the same major ions for GC/MS.

     (d)  NUS Corporation conducted the analyses for semivolatile organic compounds in samples
          from Refineries B, H, K, M, 0, P.

     (e)  Ryckman, Edgerley, Tomlinson & Associates and Gulf South Research Institute conducted
          the analyses for semivolatile organic compounds in samples from Refineries C,G,I,J,Q.

     (f)  Gulf South Research Institute conducted the analyses for semivolatile organic compounds
          in additional samples from Refineries C,G,I,Q.  These data represent results from one-
          time grab samples collected during revisits to these refineries.  Since the revisit to
          Refinery J was conducted by an EPA regional surveillance and analysis sampling team, the
          results are not presented in this table.

     (g)  Both acidic and base-neutral extracts  were diluted 1:10 before analysis.

     (h)  This sample was stored for 6 weeks prior to extraction for base-neutral and acidic
          organic compounds.

     (i)  Base-neutral extract was diluted 1:5 before analysis.
                                                55

-------
                                       TABLE III-8

                         ANALYTICAL RESULTS FOR PRIORITY  POLLUTANTS

                           FOR THE RSKERL AND B&R SAMPLING  PROGRAM

                               PESTICIDES (CONCENTRATIONS,  ug/1)
                                                        Refinery  A
Comp
109
94
97
100
103
104
106
107
108
109
110
111
112
ound
PCB-1239
4,4' -ODD
Endosulfan sulfate
Heptachlor
b-BHC-Beta
r-BHC-Gamma
PCB-1242
PCB-1254
PCB-1221
PCB-1232
PCB-1248
PCB-1260
PCB-1016
 Pesticides
                                 Intake
                                 Water
                                  ND
 106
 108
 89
 93
105
106
107
108
109
110
111
112
 PCB-1242
 PCB-1221
 106   PCB-1242
 91  Chlordane
103  b-BHC-Beta
108  PCB-1221
 95  a-Endosulfan-Alpha
106  PCB-1242
109  PCB-1232
112  PCB-1016
                            Intake
                            Water

                            ND
                            ND
                            ND
                            ND
Aldrin
4,4 -DDE
g-BHC-Delta
PCB-1242
PCB-1254
PCB-1221
PCB-1232
PCB-1248
PCB-1260
PCB-1016
Intake Water Separator Effluent
ND 0.9
Refinery B
Intake Water DAF Effluent
ND D(L 5)
ND D(L 5)
ND D(L 5)
ND D(L 5)
ND D(L 5)
ND D(L 10)
ND D(L 10)
ND D(L 10)
ND D(L 10)
ND D(L 10)
ND D(L 10)
ND D(L 10)
Refinery Ca
Separator Treated
Effluent Effluent
ND ND
Refinery Da
Intake Water Separator Effluent
ND 1.1
ND ND
Refinery Ea
Intake Water DAF Effluent
ND 0.2
Refinery Fa
Intake Water Coolinq Tower Slowdown
2.8 ND
ND 0.7
ND 0.1
Refinery Ga
Separator DAF
Effluent Effluent
ND 0.1
0.5 0.5
ND 3.5
1.8 7.9
Refinery Hb
Intake Water Separator Effluent
ND D(L 5)
ND 7
ND D(L 5)
ND D(L 10)
ND D(L 10)
ND D(L 10)
ND D(L 10)
ND D(L 10)
ND D(L 10)
ND D(L 10)
Final Effluent
ND

Final Effluent
ND
ND
D(L 5)
D(L 5)
ND
D(L 10)
D(L 10)
D(L 10)
D(L 10)
D(L 10)
D(L 10)
D(L 10)

Final
Effluent
ND

Final Effluent
ND
D(L 5)

Final Effluent
ND

Final Effluent
ND
ND
ND

Final
Effluent
ND
ND
ND
ND

Final Effluent
ND
ND
ND
D(L 10)
D(L 10)
D(L 10)
D(L 10)
D(L 10)
D(L 10)
D(L 10)
                                      56

-------
                                       TABLE  III-8(Continued)
Pesticides
106  PCB-1242
109  PCB-1232
112  PCB-1016
106  PCB-1242
109  PCB-1232
112  PCB-1016
101  Heptachlor epoxide
106  PCB-1242
107  PCB-12S4
108  PCB-1221
109  PCB-1232
110  PCB-1248
111  PCB-1260
112  PCB-1016
106  PCB-1242
106  PCB-1242
107  PCB-1254
108  PCB-1221
109  PCB-1232
110  PCB-1248
111  PCB-1260
112  PCB-1016
101  Heptachlor epoxide
108  PCB-1221
109  PCB-1232
112  PCB-1016
102  a-BHC-Alpha
 89  Aldrin
 96  b-Endosulfan-Beta
100  Heptachlor
103  b-BHC-Beta
105  g-BHC-Delta
          Intake Water

               ND
        Refinery I

        Separator Effluent

                 ND

        Refinery Ja
Separator 1
Effluent
ND
ND
ND
Separator 2
Effluent
0.5
0.5
0.2
            Final Effluent

                  ND
                                                Separator 3
                                                  Effluent

                                                     ND
                                                     ND
                                                     ND
                                                       Refinery J  (continued)
Separator 4
  Effluent

     ND
     ND
     ND
Separator 5
  Effluent

     ND
     ND
     ND
Bio-Pond
Influent

   0.1
    ND
    ND
                                                       Refinery
                                                                Kb
                                        Intake Water   Separator Effluent
               ND
               ND
               ND
               ND
               ND
               ND
               ND
               ND
               D(L  5)
               D(L 10)
               D(L 10)
               D(L 10)
               D(L 10)
               D(L 10)
               D(L 10)
               D(L 10)
                                                       Refinery IT
                                Intake
                                Water
                                 0.2
                 Separator 1
                   Effluent
                 Separator 2
                   Effluent
                                                    5.2             ND

                                                       Refinery Mb

                                        Intake Water       DAF Effluent
Intake
Water

  ND
  ND
  ND
  ND
ND
ND
ND
ND
ND
ND
ND

Chemical
D(L 10)
D(L 10)
D(L 10)
D(L 10)
D(L 10)
D(L 10)
D(L 10)
Refinery Na
Plant Separator
Effluent Effluent
4.6
ND
0.1
1.3
ND
0.1
0.5
1.9
                                                       Refinery 0

                                        Intake Water       DAF Effluent

                                             ND
          Intake Water

               ND
               ND
               ND
               ND
               ND
               D(L 10)

        Refinery P

        Separator Effluent

                 12
                 13
               D(L  5)
               D(L  5)
                 12
 Final
Effluent

   ND
   ND
   ND
            Final Effluent

                  ND
                D(L 10)
                D(L 10)
                D(L 10)
                D(L 10)
                D(L 10)
                D(L 10)
                D(L 10)
                Final
               Effluent
                                                                                   ND
                                               Final Effluent

                                                   D(L 10)
                                                   D(L 10)
                                                   D(L 10)
                                                   D(L 10)
                                                   D(L 10)
                                                   D(L 10)
                                                   D(L 10)
                                  Final
                                 Effluent

                                    ND
                                    ND
                                    ND
                                    ND
            Final Effluent

                  ND



            Final Effluent

                  ND
                  ND
                  ND
                  ND
                  ND
                                      57

-------
                                       TABLE III-8(Continued)


                                                       Refinery Qa

                                        Intake Water   Separator Effluent    Final Effluent

Pesticides                                   ND                 ND                 ND


Notes:  Pesticide compounds not listed for a refinery were not detected in samples
        taken at that refinery.

        ND-Compound was not detected.

        D(Lx)-Compound was detected at some concentration less than *., but the
        concentration could not be quantified.

        a)   Ryckman, Edgerley,  Tomlinson and Associates conducted the analyses for
        pesticide compounds in samples from Refineries A,C,D,E,F,G,I,J,L,N,Q.  Since
        these results have not been verified by GC/MS, the reported identifications
        must be considered tentative.

        b )NUS Corporation conducted the analyses for pesticide compounds in samples
        from Refineries B,H,K,M,0,P.
                                           58

-------
                                 TABLE III-9
                  ANALYTICAL RESULTS FOR PRIORITY  POLLUTANTS
Sample-Day3

Refinery A
  Intake-1
  Intake-1
  Intake-2
  Intake-2
  Intake-3
  In take-3
  Intake-composite
  Intake-composite
  Separator efflue
  Separator efflue
  Separator efflue
  Separator efflue
  Separator efflue
  Separator efflue
  Separator efflue
  Separator efflue
  Final effluent-1
  Final effluent-1
  Final effluent-2
  Final effluent-:
  Final effluent-3
  Final effluent-3
Refinery B
  Intake-1
  Intake-2
  Intake-3
  Intake-composite
  DAF effluent-1
  DAF effluent-2
  DAF effluent-3
  DAF effluent-o
  Final effluent-1
  Final effluent-2
  Final effluent-3
FOR THE RSKERL
CYANIDE, PHENOLICS,







lite
site
fluent- 1
fluent-1
fluent-2
fluent-2
:luent-3
fluent-3
fluent-composite
fluent-composite
it-1
it-1
lt-2
it-:
it- 3
Lt-3
it-composite
it-composite



;ite
•1
•2
•3
•composite
it-1
it-2
it- 3
it-composite
AND B&R
MERCURY
Lab
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
2
2
2
2
2
2
2
2
2
2
2
SAMPLING PROGRAM
CONCENTRATIONS
Cyanide
L.01b

L.01

L.01



.05

.06

.04



L.03

L.03

L.03



L.02
L.02
L.02

.04
.05
.04

L.02
L.02
L.02

, oig/1)
Phenolic!
L.010

L.010

L.011



L.52

.14

.15



L.021

.010

L.011



L.010
L.005
L.005

32.
34.
22.

.064
.048
.045

 .0001

 .0001

 .0001
L.0005
 .0001

 .0002

 .0002


L.0005
 .0008

 .0002

 .0002

 .0002
L.0005
 .0003
L.0005
L.0005
                                                                       L.0005
                                  59

-------
                              TABLE III-9(Cont.)
Sample-Day

Refinery C
  Intake-1
  Intake-1
  Intake-2
  Intake-2
  Intake-3
  Intake-3
  Intake-composite
  Separator effluent-1
  Separator effluent-1
  Separator effluent-2
  Separator effluent-2
  Separator effluent-3
  Separator effluent-3
  Separator effluent-3
  Separator effluent-3
  Separator effluent-composite
  Treated effluent-1
  Treated effluent-1
  Treated effluent-1
  Treated effluent-2
  Treated effluent-2
  Treated effluent-2
  Treated effluent-3
  Treated effluent-3
  Treated effluent-3
  Treated effluent-composite
  Final effluent-1
  Final effluent-1
  Final effluent-2
  Final effluent-2
  Final effluent-2
  Final effluent-3
  Final effluent-3
  Final effluent-composite
  Intake-4
  Separator effluent-4
  Treated effluent-4
  Final effluent-4

Refinery D
  Intake-1
  Intake-1
  Intake-2
  Intake-2
                                      Lab
                                                          Phenolics
1
3
1
3
1
3
1
1
3
1
3
1
3
3
3
1
1
3
3
1
3
3
1
3
3
1
1
3
1
3
3
1
3
1
3
3
3
3
2
1
2
1

L.01

L.01

L.01


1.1

.12

.07
.07



.12


.17


.08



.03

.05
.04

.06

L.02
L.02
.05
.07
L.02

L.02

.0014
.004 .0010
.0016
.006 .0060
.0013
.004 .0010
.0013
.0011
12. L.0010
.0012
3.2 .0060
.0015
1.6 .0020
1.4 .0050
.0780
.0012
.0008
L.001 .0020
.0006
.0010
.011 .0050
.016
.0010
L.001 .0090
.0060
.0012
.0011
.002 .0010
.0014
.006 .0010

.0013
.002 .0060
.0013
L.0001
L.0004
L.0002
.0005

.0001

.0002
                               60

-------
                              TABLE III-9(Cont.)
Sample-Day

Refinery D (Cont.)
  Intake-3
  Intake-3
  Intake-composite
  Intake-composite
  Off effluent-1
  DAF effluent-1
  DAF effluent-2
  DAF effluent-2
  DAF effluent-3
  DAF effluent-3
  OAF effluent-composite
  DAF effluent-composite
  Final effluent-1
  Final effluent-1
  Final effluent-2
  Final effluent-2
  Final effluent-3
  Final effluent-3
  Final effluent-composite
  Final effluent-composite

Refinery E
  Intake-1
  Intake-1
  Intake-2
  Intake-2
  Intake-3
  Intake-3
  Intake-composite
  Intake-composite
  DAF effluent-1
  DAF effluent-1
  DAF effluent-2
  DAF effluent-2
  DAF effluent-3
  DAF effluent-3
  DAF effluent-composite
  DAF effluent-composite
  Final efflnent-1
  Final effluent-1
  Final effluent-2
  Final effluent-2
  Final effluent-3
  Final effluent-3
  Final effluent-composite
  Final effluent-composite
                                      Lab
ranide
L.02



.05

.06

.04



Phenolics
0.23



3.7

5.1

8.0



Mercury

.0001
L.0005
.0002

.0002

.0001

.0002
L.0005
L.0001
 .03

 .03

L.02
 .0002

 .0002

 .0002
L.0005
 .0002
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
.03

L.03

L.03



L.03

L.03

L.03



L.03

L.03

L.03



L.011

.015

L.010



6.8

9.9

11.0



.013

.011

L.010




L.0001

L.0001

L.0001
L.0005
L.0001

L.0001

L.0001

L.0001
L.0005
L.0001

.0001

L.0001

.0001
L.0005
.0001
                                    61

-------
                              TABLE III-9(Cont.)
Sample-Day

Refinery F
  Intake-1
  Intake-1
  Intake-2
  Intake-2
  Intake-3
  Intake-3
  Intake-composite
  Intake-composite
  Cooling tower blowdown-1
  Cooling tower blowdown-1
  Cooling tower blowdown-2
  Cooling tower blowdown-2
  Cooling tower blowdown-3
  Cooling tower blowdown-3
  Cooling tower blowdown-composite
  Cooling tower blowdown-composite
  Final effluent-1
  Final effluent-1
  Final effluent-2
  Final effluent-2
  Final effluent-3
  Final effluent-3
  Final effluent-composite
  Final effluent-composite

Refinery G
  Intake-1
  Intake-1
  Intake-2
  Intake-2
  Intake-3
  Intake-3
  Intake-composite
  Separator effluent-1
  Separator effluent-1
  Separator effluent-1
  Separator effluent-2
  Separator effluent-2
  Separator effluent-3
  Separator effluent-3
  Separator effluent-composite
  DAF effluent-1
  DAF effluent-1
  DAF effluent-2
  DAF effluent-2
                                      Lab
                                                          Phenolics
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
1
3
1
3
1
3
1
1
3
3
1
3
1
3
1
1
3
1
3
L.03

L.03

L.03



.52

.83

.83



.06

.07

.08




L.01

L.01

L.01


1.2
1.2

1.2

1.5


1.9

2.0
.21

.21

.21



.037

.041

.057



.022

-D24

.026




.010

L.001

.008


23.
24.

25.

23.


22.

26.

.0002

.0007

.0009
L.0005
.0006

.0004

.0005

.0007
L.0005
.0005

.0003

.0003

.0003
L.0005
.0004
.0013
.0005
.0021
.0004
.0023
L.0005
.0008
.0017
L.0002

.0009
L.0002
.0018
.0002
.0003
.0011
L.0002
.0011
.0005
                                     62

-------
                              TABLE III-9(Cont.)
Sample-Day

Refinery G (Cont.)
  DAF effluent-3
  DAF effluent-3
  DAF effluent-composite
  Final effluent-1
  Final effluent-1
  Final effluent-1
  Final effluent-2
  Final effluent-2
  Final effluent-2
  Final effluent-3
  Final effluent-3
  Final effluent-composite
  Intake-4
  Separator effluent-4
  DAF effluent-4
  Final effluent-4

Refinery H
  Intake-1
  Intake-2
  Intake-3
  Intake-composite
  Separator effluent-1
  Separator effluent-2
  Separator effluent-3
  Separator effluent-composite
  Final effluent-1
  Final effluent-2
  Final effluent-3
  Final effluent-composite

Refinery I
  Intake-1
  Intake-1
  Intake-2
  Intake-2
  Intake-3
  Intake-3
  Separator effluent-1
  Separator effluent-1
  Separator effluent-1
  Separator effluent-2
  Separator effluent-2
  Separator effluent-3
  Separator affluent-3
                                      Lab
 3.0
 .09
 .07
 .09

 .30

L.02
 .60
 .13
 .17
                                                         Phenolics
               22.
              .047
              .020
L.02
L.02
L.02
.16
.07
.08
.02
.01
.02
.011
L.005
L.005
2.3
2.2
1.9
L.010
.010
.012
 .0010
 .0010
 .0003
 .0008
 .0010
 .0007
 .0018
L.0002

 .0008
 .0005
 .0004
                         L.0005
                         L.0005
                         L.0005
1
3
1
3
1
3
1
3
3
1
3
1
3

L.005

L.005

L.005

.010


.015

L.005

L.001

L.001

.004

6.0
5.6

4.4

5.0
.0013
.0007
.0011
.0005
.0014
.0007
.0012
L.0002
L.0002
.0028
.0008
.0011
.0008
                                     63

-------
                             TABLE III-9(Cont.)
Sample-Day
                                                       Phenolics
Refinery I (Cont. )
Separator effluent-3
Final effluent-1
Final effluent-1
Final effluent-1
Final effluent-2
Final effluent-2
Final effluent-2
Final effluent-3
Refinery J
Intake-1
Intake- 1
Intake-1
Intake-2
Intake-2
Intake- 3
In take- 3
In take- 3
Intake-3
Intake-composite
Separator-1 effluent-1
Separator-1 effluent-1
Separator-1 effluent-2
Separator-1 effluent-2
Separator-1 effluent-2
Separator-1 effluent-3
Separator-1 effluent-3
Separator-1 effluent-composite
Separator-2 effluent-1
Separator-2 effluent-1
Separator-2 effluent-1
Separator-2 effluent-2
Separator-2 effluent-2
Separator-2 effluent-3
Separator-2 effluent-3
Separator-2 effluent-composite
Separator-3 effluent-1
Separator-3 effluent-1
Separator-3 effluent-1
Separator-3 effluent-2
Separator-3 effluent-2
Separator-3 effluent-3
Separator-3 effluent-3
Separator-3 effluent-composite

3
1
3
3
1
3
3
3

1
3
3
1
3
1
3
3
3
1
1
3
1
3
3
1
3
1
1
3
3
1
3
1
3
1
1
3
3
1
3
1
3
1



L.005
L.005

L.005
L.005
L.005


.01


.01

L.01




.01

.01
.01

.01


.01


.01

.01


.01


.01

.01


5.2

.018


.014

.012


.017


.024

.002




1.0

1.0


.2


1.0
1.0

2.0

2.5


.690
.5

1.3

.270



.0042
L.0002

.0012
L.0002

.0010

.0007
.0001
.0004
.0009
.0002
.0019
.0020
.0070
.0070
.0005
.0001
.0030
.0012
L.0001

.0012
.0010
.0005
.0028
.0001

.0016
.0050
.0003
L.0010
.0006
.0002
L.0001

.0006
.0010
.0009
.0006
.0010
                          64

-------
                              TABLE III-9 (Cont.)
Sa
   pie-Day
                                      Lab
                                                          Phenolics
                                                                        Mercury
Refinery J (Cont.)
  Separator-4 effluent-1
  Separator-4 effluent-1
  Separator-4 effluent-2
  Separator-4 effluent-2
  Separator-4 effluent-2
  Separator-4 effluent-3
  Separator-4 effluent-3
  Separator-4 effluent-3
  Separator-4 effluent-composite
  Separator-S effluent-1
  Separator-S effluent-1
  Separator-5 effluent-2
  Separator-5 effluent-2
  Separator-5 effluent-3
  Separator-5 effluent-3
  Separator-5 effluent-composite
  Bio-pond influent-1
  Bio-pond influend-2
  Bio-pond influent-3
  Final effluent-1
  Final effluent-1
  Final effluent-2
  Final effluent-2
  Final effluent-3
  Final effluent-3
  Final effluent-3
  Final effluent-composite

Refinery K
  Intake-1
  In take- 2
  Intake-3
  Intake-composite
  DAF effluent-1
  DAF effluent-2
  DAF effluent-3
  DAF effluent-composite
  Final effluent-1
  Final effluent-2
  Final effluent-3
  Final effluent-composite
1
3
1
3
3
1
3
3
1
1
3
1
3
1
3
1
3
3
3
1
3
1
3
i
3
3
1

.06

.05


.06



.02

.02

.02

.22
.34
.26

.07

.08

.OB
.08


9.5

2.0
2.0

1.5
1.5


.294

.214

.246

120.
110.
83.

.008

.024

.002


.0002
.0002
.0013
.0050
.0070
.0016
.0020

.0004
.0003
L.0001
.0011
.0002
.0016
.0020
.0005
.0020
.0060
.0030
.0008
L.0001
.0013
.0060
.0009
.0040

.0005
L.02
L.02
L.02
            L.010
               .7
             .029
                         L.0005
                         L.0005
                         L.0005
                                  65

-------
                              TABLE HI-9(Cont.)
Sample-Day

Refinery L
  Intake-1
  Intake-1
  Intake-2
  Intake-2
  Intake-3
  Intake-3
  Intake-composite
  Intake-composite
  Separator-1 effluent-1
  Separator-1 effluent-1
  Separator-1 effluent-2
  Separator-1 effluent-2
  Separator-1 effluent-3
  Separator-1 effluent-3
  Separator-1 effluent-composite
  Separator-1 effluent-composite
  Separator-2 effluent-1
  Separator-2 effluent-1
  Separator-2 effluent-2
  Separator-2 effluent-2
  Separator-2 effluent-3
  Separator-2 effluent-3
  Separator-2 effluent-composite
  Separator-2 effluent-composite
  Final effluent-1
  Final effluent-1
  Final effluent-2
  Final effluent-2
  Final effluent-3
  Final effluent-3
  Final effluent-composite
  Final effluent-composite

Refinery M
  Intake-1
  Intake-2
  Intake-3
  Intake-composite
  DAF effluent-1
  DAF effluent-2
  DAF effluent-3
  DAF effluent-composite
  Final effluent-1
  Final effluent-2
  Final effluent-3
  Final effluent-composite
                                                          Phenolics
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
1
2
2
2
2
2
2
2
2
2
2
2
2
L.06

L.06

L.06



.19

.36

.58



.16

.21

.08



.08

.08

.08



L.02
L.02
L.02

.01
.02
.03

L.02
L.02
L.02

L.010

L.010

L.010



51.

52.

61.





22.

L2.6



L.010

.010

L.010



L.010
L.010
L.010

4.7
4.2
4.3

L.010
L.010
L.010


L.0001

.0002

.0002

.0002

.0014

.0014

.0008

.0015

.0006

.0004

.0004

.0005

.0003

.0003

.0003

.0003












                              66

-------
                              TABLE III-9(Cont.)
Sample-Day                            Lab

Refinery N
  Intake-1                             2
  Intake-1                             i
  Intake-2                             2
  Intake-2                             1
  Intake-3                             2
  Intake-3                             1
  Intake-composite                     2
  Intake-composite                     1
  Separator effluent-1                 2
  Separator effluent-1                 1
  Separator effluent-2                 2
  Separator effluent-2                 1
  Separator effluent-3                 2
  Separator effluent-3                 1
  Separator effluent-composite         2
  Separator effluent-composite         1
  Chem plant effluent-1                2
  Chem plant effluent-1                1
  Chem plant effluent-2                2
  Chem plant effluent-2                1
  Chem plant effluent-3                2
  Chem plant effluent-3                1
  Chem plant effluent-composite        2
  Chem plant effluent-composite        1
  Final effluent-1                     2
  Final effluent-1                     1
  Final effluent-2                     2
  Final effluent-2                     1
  Final effluent-3                     2
  Final effluent-3                     1
  Final effluent-composite             2
  Final effluent-composite             1

Refinery O
  Intake-1                             2
  Intake-2                             2
  Intake-3                             2
  Intake-composite                     2
  DAF effluent-1                       2
  DAF effluent-2                       2
  DAF effluent-3                       2
  DAF effluent-composite               2
  Final effluent-1                     2
  Final effluent-2                     2
  Final effluent-3                     2
  Final effluent-composite             2
                                                         Phenolics
L.oe

L.03

L.oe



L.oe

.04

L.oe



L.oe

L.03

L.oe



L.oe

L.03

L.06



L.010

L.011

L.010



6.2

6.5

4.7



L.260

.073

.074



L.015

L.011






.0002

.0001

.0002
L.OOOS
.0002

.0004

.0006

.0004
L.OOOS
.0005

L.0001

.0004

.0002
L.OOOS
.0002

.0004

.0002

.0001
L.OOOS
.0001
L.02
L.02
L.02

 .21
 .16
 .13

L.03
L.03
L.03
L.010
L.005
L.005

  11.
  10.
  11.

 .052
 .049
 .036
L.OOOS
L.OOOS
                         L.OOOS
                                 67

-------
                              TABLE IH-9 (Cont. )
                                                  03
                                                  03
Sample-Day                            t-ab     Cyanide

Refinery P
  Intake-1                             2        L..03
  Intake-2                             2        L.02
  Intake-3                             2        L.02
  Intake-composite                     2
  Separator effluent-1                 2         .09
  Separator effluent-2                 2         .06
  Separator effluent-3                 2         .04
  Separator effluent-composite         2
  Final effluent-1                     2        L
  Final effluent-2                     2        L
  Final effluent-3                     2        L.03
  Final effluent-composite             2

Refinery Q
  Intake-1                             1
  Intake-1                             3        L. 01
  Intake-2                             1
  Intake-2                             3         .02
  Intake-3                             1
  Intake-3                             3        L.01
  Separator effluent-1                 1
  Separator effluent-1                 3        L.01
  Separator effluent-1                 3
  Separator effluent-2                 1
  Separator effluent-2                 3        L.01
  Separator effluent-3                 1
  Separator effluent-3                 3         .03
  Final effluent-1                     1
  Final effluent-1                     3        L.01
  Final effluent-1                     3        L.01
  Final effluent-1                     3
  Final effluent-2                     1
  Final effluent-2                     3         .32
  Final effluent-2                     3         .32
  Final effluent-3                     1
  Final effluent-3                     3         .01
  Intake-4                             3        L.02
  Separator effluent-4                 3        L.02
  Final effluent-4                     3        L.02
                                                          Phenolics
                                                L.010
                                                L.005
                                                L.005

                                                 106.

                                                  29.

                                                 .012
                                                 .011
                                                 .010
                                                            L.001

                                                             .004

                                                             .010

                                                             .102
                                                             .113

                                                             .116

                                                             .118

                                                             .016
                                                             .018
                                                             .018
                                                             .014
                                                                          L.0005
                                                                          L.0005
                                                                          L.OOOS
                                                               .0021

                                                               .0012
                                                               .0010
                                                               .0034
                                                               .0060
                                                               .0002
                                                               .0060

                                                               .0003
                                                              L.0002
                                                               .0003
                                                              L.0002
                                                               .0003
                                                               .0060
                                                               .0120
                                                               .0002
                                                               .0003
                                                               .0020
                                                              L.0002
                                                               .0008
                                                              L.0002
                                                              L.0001
                                                              L.0002
                                                              L.0001
Notes:  (a)  If a value is not listed for a particular sample location and time,
            then the indicated laboratory did not test that sample for the
            specified pollutant.
Labs:
        (b)
        (c)
L - less than.
Grab samples collected during revisits to Refineries C, G, Q are
indicated as Day 4.

  EPA Region V Laboratory.
  Robert S.  Kerr Environmental Research Laboratory, EPA.
  Ryckman,  Edgerley,  Tomlinson and Associates
                                 68

-------
TABLE 111-10
ANALYTICAL
RESULTS
FOR PRIORITY POLLUTANTS
FOR THE RSKERL AND BSR SAMPLING PROGRAM
Sample-Day3
Refinery A
-1
-2
-3
-Composite
-Composite
SE-1
SE-2
SE-3
SE-C
SE-C
PE-1
FE-2
FE-3
FE-C
FE-C
Refinery B
1-1
1-2
1-3
I-C
I-C
DAF E-l
DAF E-2
DAF E-3
DAF E-C
DAF E-C
FE-1
FE-2
FE-3
FE-C
FE-C
Refinery C-l
1-1
1-1
1-2
1-2
1-3
1-3
I-C
I-C
SE-1
SE-1
SE-2
SE-2
SE-3
SE-3
SE-C
SE-C
TE-1
TE-1
TE-2
TE-2
TE-3
TE-3
TE-C
TE-C
FE-1
FE-1
FE-2
FE-2
FE-3
FE-3
FE-C
FE-C
Refinery C-f
I
SE
TE
FE
METALS (CONCENTRATIONS, ug/1)
Concentration (uq/1)
Lab

1
1
1
1
2
1
1
1
1
2
1
1
1
1
2

1
1
1
1
2
1
1
1
1
2
1
1
1
1
2

1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3

3
3
3
3
*a

L2S
L2S
L2S
L25
L5
L2S
L25
L25
L2S
LS
L2S
L25
L25
L25
L5

LI
LI
2
2
L5
LI
LI
LI
LI
LS
LI
LI
LI
LI
LS

L25

L25

L25

L25
LI
L25

L25

L25

L25
LI
L25

L25

L25

L25
LI
L2S

L2S

L2S

L25
LI





Be

L2
L2
L2
L2
L3
L2
L2
L2
L2
L3
L2
L2
L2
L2
L3

LI
LI
LI
LI
L3
LI
LI
LI
LI
L3
LI
LI
LI
LI
L3

L2

L2

L2

L2
LI
L2

L2

L2

L2
LI
L2

L2

L2

L2
LI
L2

L2

L2

L2
LI





Cd

L20
L20
L20
L20
LI
L20
L20
L20
L20
LI
L20
L20
L20
L20
LI

L2
L2
7
L2
LI
L2
L2
3
L2
LI
8
L2
L2
L2
LI

L20

L20

L20

L20
LI
L20

L20

L20

L20
LI
1,20
13
L20
9
L20
15
L20
16
L20

L20

L20

L20
LI





Cr

L24
L24
L24
L24
L5
L24
L24
1220
30
32
L24
L24
L24
L24
5

30
30
50
60
LS
50
50
60
60
L5
70
70
40
50
LS

L24

L24

L24

L24
2
575
770
518
820
669
940
574
880
133
940
128
470
770
1100
342
490
112

118

142

120
3





Cu

L4
L4
L4
L4
L5
26
23
39
23
17
L4
L4
6
5
L5

30
20
40
30
LS
L6
9
10
10
7
L6
L6
L6
L6
LS

12

9

11

21
2
231

151

140

182
190
27
100
26
190
SI
260
59
230
19

50

24

27
10





Ni

L50
L50
LSO
L50
L15
LSO
LSO
LSO
LSO
23
LSO
LSO
LSO
LSO
L15

6
6
20
20
L1S
LS
LS
LS
LS
L15
LS
LS
LS
LS
L15

LSO
L2
LSO
L2
LSO
L2
LSO
1
LSO

LSO

LSO

LSO
LI
LSO
9
LSO
6
LSO
44
LSO
18
LSO
7
LSO
7
LSO
7
LSO
IS





Pb

L60
L60
L60
L60
L15
147
109
224
114
64
L60
L60
L60
L60
L15

60
60
50
70
L15
L20
L20
L20
L20
L15
L20
L20
L20
L20
L15

L60
LI
L60
LI
L60
LI
119
1
71

L60

64

227
12
L60

66

LSO

331
17
L60
26
113
58
L60
26
112
50





Zn As

31
45
68
43
L10 L10
253
239
329
272
220 12
64
65
77
51
30 L10

L60
L60
100
100
IS L20
L60
L60
L60
L60
30 L20
L60
L60
LSO
L60
25 L20

79

44

109

1450
20 4
607
630
517
670
614
550
3420
690 8
527
930
489
440
881
930
4780
780 6
478
590
565
620
526
590
1080
700 5

LI
679
519
543
Sb Se





L25 L10




L25 L10




L2S L10





L25 L20




L25 L20




L25 L20


4

13

4

1 5

11

8

9

LI 15

10

L6

8

1 15

13

10

19

3 19





Tl





L25




L15




L15





L1S




L15




L15


LI

3

LI

L2

LI

LI

LI



LI

LI

LI



3

7

LI

L2

LI
LI
LI
LI
  69

-------
TABLE  111-10 (Cont.)
Concentration fug/1)
Sample- Day
Refinery D
1-1
1-2
1-3
I-C
I-C
DAF E-l
DAF E-2
DAF E-3
DAF E-C
DAF E-C
FE-1
FE-2
FE-3
FE-C
FE-C
Refinery E
1-1
1-2
1-3
I-C
I-C
DAF E-l
DAF E-2
DAF E-3
DAF E-C
DAF E-C
FE-1
FE-2
FE-3
FE-C
FE-C
Refinery F
1-1
1-2
1-3
I-C
I-C
CT B-l
CT B-2
CT B-3
CT B-C
CT B-C
FE-1
FE-2
FE-3
FE-C
FE-C
Refinery G-l
1-1
1-1
1-2
1-2
1-3
1-3
I-C
I-C
SE-1
SE-1
SE-2
SE-2
SE-3
SE-3
SE-C
SE-C
DAF E-l
DAF E-l
DAF E-2
DAF E-2
DAF E-3
DAF E-3
DAF E-C
DAF E-C
FE-1
FE-1
FE-2
FE-2
FE-3
FE-3
FE-C
FE-C
A
Lab

1
1
1
1
2
1
1
1
1
2
1
1
1
1
2

1
1
1
1
2
1
1
1
1
2
1
1
1
1
2

1
1
1
1
2
1
1
1
1
2
1
1
1
1
2

1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
I
3
1
3
1
3
1
3
1
3
1
3
1
3

Ag.

L250
L250
L250
L250
L5
L250
L2S
L25
L25
L5
L25
L25
L25
L25
15

L25
L25
L25
L25
L5
L25
L25
L25
L25
L5
L25
L25
L25
L25
LS

L250
L250
L250
L250
L5
L250
L250
L25
L2S
L5
L25
L2S
L25
L25
LS

L25

L25

L25

L25
LI
L25

L25

L25

L25
LI
L25

L25

L25

L25
LI
L25

L25

L2S

L25
LI

Be

L20
L20
L20
L20
L3
L20
L2
L2
L2
L3
L2
L2
L2
L2
L3

L2
L2
L2
L2
L3
L2
L2
L2
L2
L3
L2
L2
L2
L2
L3

L20
L20
L2
L2
L3
L2
L2
L2
L2
L3
L2
L2
L2
L2
L3

L2

L2

L2

L2
LI
L2

L2

L2

L2
LI
L2

L2

L2

L2
LI
L2

L2

L2

L2
L2

Cd

L200
L200
L200
L200
LI
L200
L20
L20
L20
LI
L20
L20
L20
L20
LI

L20
L20
L20
L20
2
L20
L20
L20
L20
LI
L20
L20
L20
L20
LI

L200
L200
L20
L20
LI
L20
L20
L20
L20
LI
L20
L20
L20
L20
LI

L20

L20

L20

L20
LI
L20

L20

L20

L20
LI
L20

L20

L20

24
LI
L20

L20

L20

L20
LI

Cr

L240
L240
L240
L240
L14
1020
681
479
719
730
1230
1160
875
1080
1000

25
58
35
42
35
104
86
89
89
76
42
52
44
42
36

L240
L240
72
58
60
50
60
79
57
44
73
31
29
45
7

L24

L24

L24

L24
1
615
820
676
790
73
1200
606
1000
526
710
414
680
73
930
425
800
89

86

73

L24
1

Cu

L40
L40
L40
L40
L5
L40
15
6
7
L5
L4
L4
L4
L4
L5

5
8
15
10
a
L4
L4
L4
L4
LS
L4
L4
L4
L4
LS

50
190
184
151
210
278
350
510
405
50C
195
86
84
125
125

L4

L4

L4

L4
7
6

53

L4

8
7
L4

L4

L4

8
3
L4

L4

L4

L4
7

Ni

L500
L500
L500
L500
LI 5
LSOO
LSO
L50
L50
LI 5
L50
L50
LSO
L50
L15

LSO
LSO
LSO
LSO
51
LSO
LSO
LSO
LSO
28
LSO
LSO
LSO
LSO
19

LSOO
LSOO
57
62
58
64
101
134
88
77
68
74
71
64
58

LSO

52

LSO

LSO
LI
LSO

85

LSO

93
LI
LSO

LSO

LSO

104
1
57

63

LSO

LSO
LI

Pb

L600
L600
L600
L600
LI 5
L600
L60
L60
L60
L1S
L60
L60
L60
L60
L15

L60
L60
L60
L60
23
L60
L60
L60
L60
L1S
L60
L60
L60
L60
L15

LSOO
L600
L60
L60
L15
L60
L60
L60
L60
L15
L60
L60
L60
L60
L15

78

102

L60

L60
2
181
420
308
160
L60
430
181
278
159
270
115
320
L60
360
144
260
107

90

L60

L60
2

Zn As

L250
L250
L250
L2SO
33 L10
410
242
181
262
280 L10
515
480
338
430
400 L10

141
102
130
127
110 L10
61
47
54
74
50 L10
49
77
59
44
30 L10

L250
L250
127
133
120 27
229
342
452
342
330 41
125
151
112
132
100 31

52
LI
72
LI
2f
LI
30
36 5
125
60
117
24
170
110
179
66 5
93
44
94
87
64
92
139
53 L4
51

46

64

30
36 5

Sb Se Tl





L25 L10 L15




L25 L10 L15




L25 L10 L15





L25 LlO L15




L25 LlO U.5




L25 12 L15





L25 12 L15




L2S LlO L15




L25 LlO L15


LI

LI

U.

LI 3 L2

9 LI

10 LI

6 LI

LI 6 L2

5 LI

13 LI

7 LI

1 9 L2

32 6

9 12

7 5

U 3 L2

 70

-------
TABLE 111-10  (Cent.)
             Concentration (ug/1)
Sample-Day
Refinery G-f
I
SE
DAF E
FE
Refinery H
1-1
1-2
1-3
I-C
I-C
SE-1
SE-2
SE-3
SE-C
SE-C
FE-1
FE-2
FE-3
FE-C
FE-C
Refinery I
1-1
-1
-2
-2
-3
-3
I-C
I-C
SS-1
SE-1
SE-2
SE-2
SE-3
SE-3
SE-C
SB-C
FE-1
FE-1
FE-2
FE-2
FE-3
FE-3
FE-C
FE-C
Refinery J
-1
-1
-2
-2
-3
-3
I-C
I-C
SI E-l
SI E-l
SI E-2
SI E-2
SI E-3
SI E-3
SI E-C
SI E-C
S2 E-l
S2 E-l
32 E-2
32 E-2
S2 E-3
32 E-3
S2 E-C
S2 E-C
S3 E-l
S3 E-l
S3 E-2
S3 E-2
S3 E-3
S3 E-3
Lab

3
3
3
3

1
1
1
1
2
1
1
1
1
2
1
1
1
1
2

1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3

1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
&






LI
LI
LI
LI
L5
LI
LI
LI
LI
L5
LI
LI
U
LI
LS

L2S

L25

L25

L2S
LI
L25

L2S

L25

L2S
LI
L25

L25



L25
LI

L2S

L25

L25

L25
LI
L2S

L25

L25

L2S
LI
L25

L25

L25

L25
LI
L25

L25

L25

Be






LI
U.
LI
LI
L3
LI
LI
LI
LI
L3
LI
LI
LI
LI
L3

L2

L2

L2

L2
LI
L2

L2

L2

L2
LI
L2

L2



L2
LI

L2

L2

L2

L2
LI
L2

L2

L2

L2
LI
L2

L2

L2

L2
LI
L2

L2

L2

Cd






L2
L2
a
L2
U
L2
L2
L2
L2
LI
L2
L2
20
L2
LI

L20

L20

L20

L20
LI
L20

L20

L20

L20
LI
L20

L20



L20
LI

L20

L20

L20

L20
LI
L20

L20

L20

L20
LI
L20

L20

L20

L20
LI
L20

L20

L20

Cr






20
10
20
10
L5
10
7
20
10
LS
20
10
10
10
LS

L24

L24

L24

L24
1
98

91

102

98
3
L24

L24



L24
1

L24

L24

L24

L24
1
36

620
100
SO
16
52
76
440
4SO
1050
1100
411
390
SS4
780
547
830
1010
1200
350
660
Cu






L6
9
10
7
LS
30
20
30
30
7
10
10
9
7
L5

L4

6

20

16
10
157

167

146

157
6
85

22



71
3

5

10

L4

4
1
L4

1370

33

25
2
L4

231

L4

55
7
14

16

16

Ni






LS
LS
LS
LS
L1S
LS
LS
LS
LS
L1S
LS
LS
LS
LS
L15

LSO

L50

LSO

LSO
LI
LSO
7
LSO
L2
LSO
L2
LSO
5
LSO

LSO



LSO
LI

LSO

LSO

LSO

LSO
1
LSO

771

LSO

LSO
LI
LSO

69

LSO

61
LI
118

LSO

LSO

Pb






L20
L20
L20
L20
L15
L20
L20
L20
L20
L1S
80
30
L20
30
L15

L60

L60

79

78
2
L60

L60

90

168
2
L60

L60



211
2

L60

L60

L60

L60
2
L60

958

L60

L60
4
190
190
2080
2000
876
380
810
870
123

L60

L60

Zn Aa Sb






L60
L60
L60
L60
IS L20 L2S
L60
L60
70
L60
30 L20 L25
L60
60
L60
L60
25 L20 L2S

69

52

836

536
25 L4 LI
172
110
237
100
1070
100
1120
100 5 LI
69

69



2000
60 L4 LI

72

54

62

62
54 3 LI
150
120
499
250
432
420
257
320 3 LI
316
290
1400
2100
790
680
658
740 5 LI
194
150
245
210
280
280
Se Tl

LI
LI
LI
LI





L20 L1S




L20 'L15




20 L15


LI

LI

LI

2 LI

L4 LI

L4 LI

7 LI

4 L2

25 LI

23 LI



16 L2


LI

LI

LI

3 L2

7 LI

16 LI

L4 LI

5 L2

16 3

12 LI

14 LI

8 3

17 LI

13 LI

31 LI
       71

-------
TABLE 111-10 (Cont.)
Sample-Day
Refinery J
S3 E-C
S3 E-C
34 E-l
S4 E-l
34 E-2
S4 E-2
S4 E-3
34 E-3
S4 E-C
S4 E-C
S5 E-l
S5 E-l
35 E-2
S5 E-2
S5 E-3
S5 E-3
S5 E-C
S5 E-C
B-P 1-1
B-P 1-1
B-P 1-2
B-P 1-2
B-P 1-3
B-P 1-3
B-P I-C
B-P I-C
FE-1
FE-1
FE-2
FE-2
FE-3
FE-3
FE-C
FE-C
Refinery K
1-1
1-2
1-3
I-C
I-C
DAP E-l
DAF E-2
OAF E-3
DAF E-C
DAF E-C
FE-1
FE-2
FE-3
FE-C
FE-C
Refinery L
1-1
1-2
1-3
I-C
I-C
SI E-l
SI E-2
SI E-3
31 E-C
31 E-C
S2 E-l
32 E-2
S2 E-3
32 E-C
32 E-C
FE-1
FE-2
FE-3
FE-C
FE-C
a Lab
(Cont. )
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3
1
3

1
1
1
1
2
1
1
1
1
2
1
1
1
1
2

1
1
1
1
2
1
1
1
1
2
1
1
1
1
2
1
1
1
1
2
*a

L25
1
L25

L25

L25

L25
2
31

L2S

L25

L25
Ll
L25

L25

L25

L25
LI
L25

L25

L25

L25
LI

LI
LI
LI
LI
L5
LI
LI
LI
LI
L5
LI
LI
LI
LI
L5

L250
L250
L2S
L250
L5
L2SO
L250
L250
L250
L5
L25
L25
L25
L25
L5
L25
L2S
L25
L25
L5
Be

L2
LI
L2

L2

L2

L2
LI
2

L2

L2

L2
LI
L2

L2

L2

L2
LI
L2

L2

L2

L2
LI

LI
LI
LI
LI
L3
LI
LI
LI
LI
L3
LI
LI
LI
LI
L3

L20
L20
L2
L20
L3
L20
L20
L20
L20
L3
L2
L2
L2
L2
L3
L2
L2
L2
L2
L3
Cd

L20
LI
L20

L20

L20

L20
LI
L20
4
L20
5
L20
9
L20
7
L20

L20

L20

L20
LI
L20

L20

L20

L20
LI

L2
L2
3
L2
LI
L2
L2
L2
L2
3
L2
L2
L2
L2
1

L200
L200
L20
L200
LI
L200
L200
L200
L200
LI
L20
L20
L2D
L20
LI
L20
L20
L20
L20
LI
Cr

626
570
835
1500
1210
1300
1860
1700
1300
1900
1580
2200
2790
4900
1500
1800
2010
3600
L24
9
L25
5
L24
6
29
22
96
150
94
27
102
27
82
54

20
10
10
20
5
1000
2000
1000
1000
1600
100
60
100
100
73

L240
L240
L24
L240
30
1000
L240
L240
L240
290
773
831
928
802
870
205
119
165
144
190
Cu

25
2
38

21

77

42
10
51

47

51

45
182
41

7

L4

17
2
9

L4

6

L4
32

10
10
10
10
6
200
400
200
300
280
60
10
20
30
18

L40
L40
22
L40
20
170
L40
100
100
180
43
54
31
42
50
24
19
31
24
39
Hi

63
LI
L50

L50

L50

L50
LI
189

L50

L50

79
1
L50

L50

L50

L50
LI
53

L50
7
65
6
L50
3

L5
L5
L5
L5
US
9
20
L5
20
28
LS
L5
L5
L5
L15

L500
L500
L50
L500
21
L500
L500
L500
L500
70
L50
L50
L50
L50
16
L50
L50
L50
L50
IS
Pb

71
2
80

L60

L60

69
12
164

L60

L60

101
2
72

L60

L60

L60
3
82

L60

L60

L60
9

70
40
80
40
L15
50
200
60
100
70
L20
L20
L20
L20
L15

L600
700
64
L600
40
L600
L600
L600
L600
45
L60
L60
L60
L60
17
L60
L60
L60
L60
L15
Zn As

215
260 3
411
340
261
290
579
620
304
560 3
464
600
609
740
417
520
491
760 9
148

54

65

55
L2
130

51

46

62
62 L4

200
70
60
70
45 L20
1000
3000
1000
2000
1400 L20
100
70
100
1000
120 L20

810
L250
125
L250
120 L20
490
290
290
360
370 L20
382
304
314
325
290 L20
174
157
161
174
140 L20
Sb


LI







1







LI







LI







Lll





L25




L2S




L25





L25




L25




L2S




L25
Se


6

25

24

4

11

7

29

19

23

20

10

18

22

20

27

16

12





L20




L20




L20





L20




L20




L20




L20
Si.


L2

LI

LI

LI

L2

LI

4

6

L2

Ll

LI

Ll

L2

Ll

Ll

Ll

L2





L15




L15




L15





L15




L15




L15




L15
        72

-------
TABLE  111-10 (Cont.)
Sample-Day a
Refinery H
1-1
1-2
1-3
I-C
I-C
DAF E-l
DAF E-2
DAP E-3
OAF E-C
OAF E-C
FE-1
FE-2
FE-3
FE-C
FE-C
Refinery N
1-1
1-2
1-3
I-C
I-C
SE-1
SE-2
SE-3
SE-C
SE-C
CPE-1
CPE- 2
CPE-3
CPE-C
CPE-C
FE-1
FE-2
FE-3
FE-C
FE-C
Refinery 0
1-1
1-2
1-3
I-C
I-C
DAF E-l
DAF E-2
DAF E-3
DAF E-C
DAF E-C
FE-1
FE-2
FE-3
FE-C
FE-C
Refinery P
1-1
1-2
1-3
I-C
I-C
SE-1
SE-2
SE-3
SE-C
SE-C
FE-1
FE-2
FE-3
FE-C
FE-C
Concentration (ug/1)
Lab

1
1
1
1
2
1
1
1
1
2
1
1
1
1
2

1
1
1
1
2
1
1
1
1
2
1
1
1
1
2
1
1
1
1
2

1
1
1
1
2
1
1
1
1
2
1
1
1
1
2

1
1
1
1
2
1
1
1
1
2
1
1
1
1
2
A3.

LI
LI
LI
LI
LS
LI
LI
LI
LI
LS
LI
LI
4
4
L5

L2S
L25
L250
L2S
LS
L250
L250
L25
L2S
•LS
L2S
L2S
L2S
L2S
LS
L2S
L25
L25
L25
LS

LI
LI
LI
LI
LS
LI
LI
LI
LI
LS
LI
LI
LI
LI
LS

LI
LI
LI
LI
LS
LI
LI
LI
LI
LS
LI
LI
LI
LI
LS
Be

LI
LI
LI
LI
L3
2
2
2
2
L3
2
2
LI
LI
L3

L2
L2
L20
L2
L3
L20
L20
L2
L2
L3
L2
L2
L2
L2
L3
L2
L2
L2
L2
L3

LI
LI
LI
LI
L3
LI
LI
LI
LI
L3
LI
LI
LI
LI
L3

LI
LI
LI
LI
L3
LI
LI
LI
LI
L3
LI
LI
LI
LI
L3
Cd

L2
L2
L2
L2
LI
L2
L2
L2
L2
LI
3
L2
L2
L2
LI

L20
L20
L200
L20
LI
L200
L200
L20
L20
LI
L20
L20
L20
L20
LI
L20
L20
L20
L20
LI

L2
L2
L2
L2
LI
L2
L2
L2
L2
LI
L2
L2
L2
L2
LI

L2
L2
L2
L2
LI
L2
L2
L2
L2
LI
L2
L2
L2
L2
LI
Cr

30
10
20
20
LS
200
100
90
100
73
90
100
90
100
24

L24
L24
3000
L24
7
1000
2000
980
1280
1400
SOS
679
499
701
650
L24
159
131
137
120

LS
LS
L5
LS
8
200
300
300
200
240
SO
SO
SO
SO
110

LS
LS
L5
LS
40
900
50
700
600
72
LS
LS
LS
L5
40
CU

300
100
100
200
180
10
10
9
10
6
10
10
20
20
a

L4
L4
L40
L4
LS
L40
L40
7
14
61
L4
8
7
L4
13
L4
L4
L4
L4
11

L6
L6
L6
L6
L5
30
10
8
20
30
L6
L6
L6
L6
LS

L6
L6
L6
L6
LS
L6
L6
L6
L6
LS
L6
L6
L6
L6
LS
Ni

10
LS
LS
LS
L1S
LS
LS
LS
LS
L15
L5
LS
10
20
L1S

L50
L50
790
L50
L15
L500
L500
LSO
L50
16
LSO
LSO
LSO
LSO
L15
LSO
LSO
LSO
LSO
L15

LS
LS
LS
LS
L15
LS
LS
LS
L5
L15
L5
LS
LS
L5
L1S

LS
LS
LS
LS
L15
L5
LS
LS
L5
L15
LS
LS
LS
LS
L1S
Pb

200
L20
40
60
25
L20
L20
L20
L20
L15
L20
SO
L20
30
L15

L60
L60
L600
LSO
L15
L600
L600
L60
L60
18
L60
L60
L60
L60
L1S
L60
L60
L60
L60
L15

L20
L20
L20
L20
L15
L20
L20
L20
L20
27
L20
L20
L20
L20
L15

L20
L20
L20
L20
L15
L20
L20
L20
L20
L15
L20
L20
L20
L20
L15
Zn As Sb Se

200
90
100
100
75 L20 L2S L20
200
100
90
100
140 L20 L25 L20
90
100
100
200
90 L20 L2S L20

56
29
L250
36
19 L20 L25 L20
480
760
573
603
570 L20 L2S L20
6520
4110
4260
5210
4800 L20 L25 L20
L25
118
61
104
35 L20 L25 L20

L60
L60
L60
L60
L10 L20 L2S L20
L60
L60
100
60
74 L20 L25 L20
L60
L60
L60
L60
L10 L20 L25 L20

L60
L60
L60
L60
61 L20 L25 L20
L60
L60
L60
L60
55 L20 360 L20
L60
L60
L60
L60
43 L20 370 L20
Tl





L15




L15




L1S





L15




L15




L1S




L15





L15




US




L15





L1S




L15




L15
     73

-------
                                                TABLE 111-10 (Cont.)
Sample-Day     Lab
Refinery Q-l
  1-1           1
  1-1           3
  1-2           1
  1-2           3
  1-3           1
  1-3           3
  I-C           1
  I-C           3
  SE-1          1
  SE-1          3
  SE-2          1
  SE-2          3
  SE-3          1
  SE-3          3
  SE-C          1
  SE-C          3
  FE-1          1
  FE-1          3
  FE-2          1
  FE-2          3
  FE-3          1
  FE-3          3
  FE-C          1
  FE-C          3

Refinery Q-2
  IE            3
  SE            3
  FE            3
Concentration (ug/1)
Ag_
L25

L25

L25

L25
LI
L25

L25

L25

L25
LI
L25

L25

L25

L25
LI



Be
L2

L2

L2

L2
LI
L2

L2

L2

L2
LI
L2

L2

L2

L2
LI



Cd
L20

L20

L20

L20
LI
L20

L20

L20

L20
LI
L20

L20
LI
L20
LI
L20
5



Cr
L24

L24

L24

L24
1
L24

L24

L24

L24
1
L24

L24

L24

L24
2



Cu
37

37

20

53
120
7
60
L4
140
6
60
15
210
11

20

6

23
180
240
380
300
Ni
L50

L50

L50

L50
LI
L50

L50

L50

L50
LI
L50

L50

L50

L50
LI



Pb
L60

L60

L60

167
2
L60

L60

L60

101
10
L60

L60

L60

102
15



Zn
70

62

329

2820
35
274
330
444
470
511
640
1460
470
245
380
329
360
300
350
1270
340
LI
262
167
As







7

480

460

460

440

790

900

680

800
35
350
500
Sb Se

L6

6

10

LI 6

9

7

6

LI 10

11

10

22

1 20



Tl

LI

LI

LI

L2

LI

LI

LI

L2

LI

LI

LI

L2



Notes:  a)  If a value is not listed for a particular sample location and time, then the indicated laboratory
            did not test that sample for the specified pollutant.

        b)  These data represent results from one-time grab samples collected during revisits to Refineries
            C, G, Q.

        L       Less than
        I       Intake
        SE      Separator effluent
        DAF E   OAF effluent
        TE      Treated effluent
        FE      Final effluent
        CT B    Cooling Tower blowdown
        B-P I   Bio-pond influent
        CPE     Chemical plant effluent
Labs:   1   EPA Region V Laboratory
        2 - Robert S.  Kerr Environmental Research Laboratory, EPA
        3   Ryckman,  Edgerley, Tomlinson and Associates
                                                74

-------
                                                                                            TABLE III-ll
(JI
Analytical Results

Sampling
Location
1. Refinery No. 25
Effluent
2. POTO No. 1
a. Raw Influent
b. Final Effluent
c. Primary Sludge
d. Secondary Sludge

Day
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3

PH
8.9
8.7
8.68
7.50
7.50
7.30
7.40
7.55
7.80
5.9
8.5
6.78
7.3
7.45
7.60

SS
mg/1
19
45
25
316
290
524
1
2
2
21 ,200
39,160
12.450
1,948
3,536
3,000
for Traditional Parameters in the Pretreatment Sampling Progr

Sulfide
mg/1 S
<0.1
<0.1
<0.1
0.25
0.20
0.40
<0.1
<-0.1
<0.1
35.0
110.0
33.0
0.25
0.80
0.50

B005
mg/1
310
320
355
212
240
235
3
4
5
•>4,930
8,920
1,230
745
1,460
5,680

COD
mg/1
690
710
700
505
580
580
34
30
35
28,600
39,700
30,100
2,070
42,300
15,800

CN
mg/1
3.0
2.6
3.0
0.1
*
0.02
0.06
0.07
0.05
0.24
*
0.05
0.15
*
0.17

Phenol
mg/1
123
88
99
1.7
It
0.113
0.003
0.011
0.012
2.30
*
0.622
0.074
*
0.169

O&G
mg/1
41.4
42.3
61.8
54.1
59.0
22.4
1.3
1.0
0.9
2,660
5,260
1,044
29.5
59.5
42.0
am - Week

Cr+6
mg/1
0.26
0.48
0.22
< 0.02
<0.02
<0.02
< 0.02
^0.02
cO.02
<0.02
<0.02
<0.02
•fQ.02
<0.02
<0.02
l

NH3-N
mg/1 N
39.1
36.1
36.4
22.6
26.3
23.2
8.8
12.0
9.7
74.2
51.7
3].8
10.4
10.7
6.1
                     NOTE:  Day  1 - 8/16/78;   Day 2  -  8/17/78;   Day 3 -  8/18/78
                            *  in trace, but  below detection  limit
                            All  samples were  analyzed  by the Water Quality Labs associated with POTW No.  1.

-------
                                        TABLE III-12

         ANALYTICAL RESULTS FOR PRIORITY POLLUTANTS  FOR THE  PRETREATMENT  SAMPLING
                  PROGRAH-HEEK 1.  VOLATILE  ORGANIC   CONCENTRATIONS, ugTT
Pollutant
Benzene


Chlorobenzene


Pol
No.
4


7


1,1,1-trichloro-ll
ethane

1 ,1-dichloro-
ethane

Chloroform


1,2-trans-


13


23


30
dichloroethylene

Ethyl benzene


Methylene
chloride

Tetrachloro-
ethyl ene

Toluene


Trichloro -
ethyl ene


38


44


85


86


87


Day
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
Ref.No. x
25
Eff. to
POTW
4,200
5,800
1,600

31



-


-

21
17
.
-
-
9,000
5,600
4,000
.
-
-
it
-
18
15,000
9,900
5,700
-
-
-
poW
Inf.
23
81
*
-
.
-
5
22
*
_
*
-
_
10
*
.
-
*
25
20
*
*
*
*
88
117
19
84
103
24
38
57
27
X X
Primary Secondary
Eff. Eff.
17
64
14
-


.
16
10
.
-
-
.
*
* *
_
-
*
38 *
25
*
* *
* *
* *
43 *
160 16
24 *
67
no
31
21 *
78 *
36 *
Finalx
Eff.
.



-


-
15

-

_
*
*


-

*
-
*
.
23
*
10
23
.
.
-
*
*
*
XX
Primary
Sludge
9
13

-
-
-
-


16
-
-


-
60
-
50
50
20
-
30
(11) *
(11) *

.
-
30
30
10
150
.
20
XX
Secondary
Sludge
-


-
-
-
.
-

.
-
-
.
.


-
-


-
10
120
18(15)

.

.
.
-
_
7
-
NOTE:   -  Not detected.
       *  In traces,but  below  detection  limit.
     (  )  Sample blank.   No volatile  organics detected  in  other  sample blanks.
       x  Analysis  performed by  West  Coast  Technical Service.
      xx  Analysis  performed by  Pomeroy,  Johnston and Ba'iley.
          Of the 30 volatile organics, only 11 were detected.
                                   76

-------
   TABLE  111-13
ANALYTICAL RESULTS FOR PRIORITY
POLLUTANTS FOR
THE PRETREATMENT SAMPLING
PROGRAM-MEEK 1, SEHIVOLATILE ORGANICS (CONCENTRATIONS, ug/1)


Pol 1 utants
2,4-Oimethyl-
phenol

Pentachloro-
phenol

Phenol


1,2 dichloro-
benzene

1,3 dichloro-
benzene

1 ,4 dlchloro-
benzene

Isophorene


Naphthalene


N1 trobenzene


Bis(2-ethyl-
hexy1)phthalate

Butyl benzyl
ph thai ate


Poll **
NO.
34 AE


64 AE


65 AE


25 BNE


26 BNE


27 BNE


54 BNE


55 BNE


56 BNE


66 BNE

67 BNE


Ref.No.
25
Eff.to
Day POTW
1 1,700
2
3 233
1
2
3 830
1 2,900
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1 620
2
3 370
1
2
3
1
2
3
1 16
2
3
X
POTW*
Inf.
69
.
25
_
.
-
575
700
980
*
4
15
*
19
10
28
29
24
.

-
113
121
20
_
-
-
124
112
130
55
63
39

Primary*
Eff.
72
-
34

-
-
520
700
1.100
_
17
11
_
17
11
23
30
30
.
23
-
93
156
35
_
-
-
94
56
150
59
43
68

Secondary"
Eff.
*
*
-
_.
*

*
*
*
*
*
*
_
*
*
*
*
10
.
-
-
*
*
-

-
-
*
*
-
-
-
*

Final"
Eff.
*
.
-
*
*

*
it
*
*
.
*
*
-
*
*

*


*
*
-
*
_
.
-
*
-
-
-
*

XX
Primary
Sludge

-
-
_
.


355
180
13
7
10
30
15

30
15
9
.
-
-
440
30

5
.
-
130
240
170
25
14

XX
Secondary
Sludge
.
.
-
_
.
-
_
405
1,200
20
9
-

5
-

5
-
.
-
-
-
-
-
_
-
-
75
180
140

-
-
77

-------
                                  TABLE  111-13  (Continued)

        ANALYTICAL RESULTS FOR PRIORITY  POLLUTANTS  FOR  THE  PRETREATHENT SAMPLING
              PROGRAM-WEEK. 1.  SEHJVOLATILE  0°GA*!IC£ (CONCENTRATIONS,  ug/1)
                                  Ref.No.x
                                   25         xx         x       x      xx          xx
Pollutants
Di-n-butyl
Phthalate

Oi-n-oc'tyl
Phthalate

Die thy 1
Phthalate

Dimethyl
Phthalate

Acenaphthylene


Anthracene


Fluorene


Phenanthrene'1"


Pyrene


Poll
No.
68

69


70


71


77


78


30


81


84


**
BNE

BNE


BNE


BNE


BNE


BNE


BNE


BNE


BNE


Day
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
Eff.to
POTW
40
*





14


-




60
51
30

63
32
60
51
30

21
-
POTW
Inf.
24
28
34
12


.
13
*






*
*
*

*
*
+
*
•*



Primary Secondary Final
Eff. Eff. Eff.
19 * *
21 *
17 * *
*
*

27 *
17 *
* 15 *
* if
*
* *

.
*
*
*
* *
it
*

*
*
* *



Primary Secondary
Sludge Sludge





190 5

11
9

















    Of  59 semi-volatile  organics,  only 20  were  detected.
 *  in traces,  but below  Detection  Limit.
 ** AE - Acid extractable;  BNE   Base/neutral  extractables
 +  Anthracene  and Phenanthrene  are unresolved
    Not detected.
 x  Samples were analyzed by West Coast Technical  Services
xx  Samples were analyzed by Pomeroy,  Johnston and Bailey.
                                         78

-------
Pollutant
                                       TABLE  111-14

               ANALYTICAL  RESULTS  FOR  PRIORITY POLLUTANTS FOR THE PRETREATHENT
                  SAMPLING PROGRAM-WEEK 1.  PESTICIDES(CONCENTRATIONS. ug/1)
              Poll.
                No.
                     Day
Refinery*
tto'25      POTW*  Primary* Secondary* Final" Primary" Secondary"
           Inf.     Eff.      Eff.      Eff.   Sludge    Sludge
Eff.to
                           POTW
4,4'-DDE        93    1
                      Z
                      3

Heptachlor     100    1
                      2
                      3

b-BHC-8eta     103    1
                      2
                      3

r-8HC-Gamma    104    1
                      2
                      3
           0.68     0.39



           0.12     0.13

   0.18

   0.10    0.55     0.49
                    6.3
           0.14     0.13
                                       1.1
                                       1.2
NOTE:    Of 25 pesticides only 4 were found; none of the four were confirmed by GCMS.

       - Not detected.

       x Samples were analyzed by West Coast Technical Service.

      xx Samples were analyzed by Pomeroy, Johnston and Bailey.
                                        79

-------
                                                                         Table 111-15
                                 Analytical Results for Priority Pollutants for the Pretreatment Sampling Program - Week 1,
                                                               Metals (Concentrations, ug/1)
Pollutant
Antimony


Arsenic


Beryllium


Cadmium


Chromium


Copper


Lead


Mercury


Nickel


Selenium


Silver


Thallium


Zinc


Poll. No.
114


115


117


118


119


120


122


123


124


125


126


127


128


Day
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3

Influent
X
_
-

27
-
26
-

-
61
29
42
335
3S7
241
263
248
202
251
218
324

1.50
0.41
204
123
92
31
38
32
-
11
11
-
-
-
836
911
857
POTW No.
Primary
Effluent
X



_
28
-

_

37
20
20
197
188
140
161
132
106
148
105
141


0.44
190
89
73
30
41
-

-




492
462
449
1
Secondary
Effluent
X
_
-
-

-

«


„

-
39
33
31
56
16
16
37

39
1.48
0.41
0.38
90
89
68


30
_

-
„

-
122
93
143

Final
Effluent
X

-



-
.


_


18
16
15
34

32
29

38
0.52
1.06
0.51
81
86
69
—
-
35


-
„

-
58
64
69

Primary
Sludge
XX
1250
830
60
86
174
66
12
_
4
1590
610
180
17900
17900
2870
7800
11200
3300
15700
9000
2800
14
253
46
3220
3400
700

6
-
80
80
60
20
80
70
40000
15800
6340

Secondary
Sludge
XX
830
210
23
73
76
60
6

10
240
320
310
4080
5560
5140
2500
3300
3000
1200
1500
1600
17
23
20
710
850
750

6
9
50
60
60
20

10
6100
3400
8040
Effluent to
POTW from
Refinery No.
25
X
.

-
30




-
.
_
-
1994
1473
1649
29
26
15
28
26
30


-
.

-
193
322
267

_



-
155
119
171
Notes:     -    Hot Dectected
          x    Analyzed  by  EVA Region IV Laboratory
         xx    Analyzed  by  Pomeroy, Johnston and Bailey
                                                               80

-------
                                                                                            TABLE 111-16
00
Sampling
Location
1. Effluent to POTW from
a. Ho. 13


b. No. 21


o. Ho. 1*5


Day
Refinery No.
1
2
3
1
2
3
1
2
3
d. No. 1*3 Direct Dia 1


No. 43


e. No. 16


2. POTW No. 2
a. Influent


b. Primary Effluent


c. Final Effluent


d. UNOX Influent


e. UNOX Effluent


f . Primary Sludge


g. Digested Sludge


h. Centrate


2
3
1
2
3
1
2
3

1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
PH

10.8O
10.00
11.1*2
8.75
8.56
8.65
7.32
6.90
7.13
8.21*
7.60
7.29
7.68
7.81*
7.52
7.51
7.10
8.13

7.50
7.57
7.51
7.50
7.58
7.51
7.68
7.77
7.55
7.51
7.71
7.20
6.91
6.98
7. 00
6.38
6.00
+
7.20
7.01
t
7.59
7.58
+
ss

81*
86
56
20
26
21*
22
21*
6
11*
36
36
58
30
8
29
23
li*

390
321*
552
82
112
92
188
181*
232
78
82
791
7
16
9
43,510
39,220
+
28,210
27,25*
+
13,970
13,9to
f
SulfldH
as S

<0.1
0.1
<0.1++
<0.1
<0.1
<0.1++
<0.1
«.£
<0.1++
<0.1
<0.1++
<0.1++
<0.1
<0.1
<0.1++
<0.1
<0.1++
<0.1"

1.0
1.1*
0.8
0.2
0.2
0.1
0.6
0.1*
0.1*
0.1
0.2
0.8
<0.1
<0.1
<0.1
0.3
0.5
+
0.3
0.1
+
0.1*
0.2"
-f
BOJ>5

1*50
1*02
361
83
202
90
169
159
132
1*6
57
12
508
528
556
89
102
168

311
330
32!*
190
198
180
181
203
187
188
195
278
3
6
6
ll*,200
l!*,950
+
3,100
3,270
+
2,060
2,350
+
con*

972
789
761*
289
1*1*1
322
506
395
386
11*9
130
111
1,770
2,1*30
3,330
398
517
537

791*
752
831*
1*37
1*20
1*50
539
502
603
1*1*7
1*06
1,280
61
86
86
60,500
1*1,500
4-
28,1*00
26,700
+
17,500
16,600
+
CN

0.13
O.ll*
0.31*
0.01
0.02
0.03
i*.o
i*.o
8.0
0.03
0.01
0.05
3.0
8.0
9.0
0.08
0.09
0.03

0.06
0.09
0.26
0.05
0.11
0.1*1*
0.06
0.11
0.1*1*
0.07
0.16
0.09
0.06
0.05
O.OU
2.2
1.9
+
2.6
2.6
+
1.5
1.8
+
Phenol

51
60.6
106
1.2
2.1
1.1
20
11*. 3
ll*.8
0.21
o.oi*
0.06
133
151
ll*8
3.6
3.2
1*.3

2.61*
3.01
3.81
3.16
3.11
l*.35
2.79
3.07
l*.ll*
2.99
1*.OO
l*.29
<0.01
0.03
<0.01
2.67
3.91*
+
1.27
1.00
+
0.88
0.77
+
0 & G

7?1*
83,6
13.9
36
31*. 5
32.7
21.2
11.7
10.9
l*.0
3.8
3.1
11*1*
ll*2
117
2l*.9
35.3
52.2

113
82
82
29.3
32.3
3i*.7
38.7
1*7.3
52.0
28.0
3<*.0
29.0
1.1
3.1
1.0
3,100
6,580
+
2,1*20
2,61*0
+
1,660
1,680
+
Cr*>

<0.02
<0.02
<0.02
<0.02
<0.02
*0.02
<0.02
<0.02
<0.02
0.06
<0.02
<0.02

-------


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• . Int Lit . tnl LI t tfr t i ill i ., LI: iiliMiju blu,|(j,: CLiKt-
t»2 71 /a - 4U 1 / b Uuu ^2o - " Jbi)
57 67/7'o2 • 240 ' 4/ 14O
24 27 4'j - 31 J'j 1 .10 ly - J4y i'JB 319
-__ .5.. -___-
Hi _-. _._-_•-
luO - --ib4 - 0 - -- --
_
JO JO / 1 J J *
19 - - 14 - b4 - la - -
bOO /14 * 021 ii - - - ' Jl - J4
iroO 9fl JUi, - .__ - ..__
5J5 9b li« .'Jl 'J/ 14 - - - Ib -
-jo -
• 1 1 li) J-3 it ~ ~ ' ~
5j ,___-_
i j i j 10 - ii - - ia - * -
11 14 U Ib 12 'J Jl *
21 ill 14 14 ly - - - ' la
JU __-,-_
jU -
. _ - - - -
: : - .:::::
JJ 41 Jl - /O t>b ^5 ItiUHi) lUU - - J« J
3y 51 4/ • bj • 1JO - - 170
b, .1C n - 48 ,', ^ i',u /i Ib 4,o ^u 7b
^21 15 II 44 _--,-_
3V 14 40 - 'j4u C li -
; . _
7 /u db y ----.
c, i.s 1,7 i -py ______
o c t y« i n /o
1G 197 2O.' I4O bl)tL' Ib 4UHOI* 4^u - * HVO
U JbL, 174 ' * * 4-:u - • 170
t, l'£ u6 UU ob Jon '/'j H 4olii» /buu 4i7
12 Ib 211 J".U - -
14 21 L'o 22 - -_-._-
12 li: 24 * Ib • JbU 10 - - -

-------



Pollutant
ParacMnruat>t.icrr:tol
2-Ollorophur.el

2,4-diMthylfhenol


FentacMorofhcnol


thfr.ol


Acenaphthone


1.2.4-trichlcro
benzene

1.2 dichlorobenzene


1.3-dichlorobenzen0


l,4-dichlorobenz«ne


2, 4-dini trotclacne


1,2-dipher.ylh.i-irazinc


nuorathenc





• *
AC
AE

A£


AE


AE


BNE


BNE


K-E


BNE


BNE


BNE


Bi.-E


BNE


bis (2-chloroisopropyl) BNE
ether

bis (2-chloroe:hoxy)
•ethane

Kaphoreae


MphthtleiU!

tvnltroio dlphenyl
•sine

bls(2-ethylhe*yl)
pkthaUte
Butyl benzyl
phthAlate*
dl-n-bctyl phthalate

di.n-octyl phthalate




Bra


ate


BHE

BHE


BNE

BHE

HIE

BHE





Foil
No.
24

34


64


65


1


8


25


26


27


35


37


39


42


43


54


55

62


66

67

68

69





Pay
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
AIM VI



Inf."
-

300
220
720
-
.
-
700
150
840
•
-
•
•

20
48
27
13
•
20
12
17
20
12
.
.
-
-
-
-
.
-
-
.
-
-

-
-
.
.
-
28
•
27
-
-
-
13
30
43
-
21
*>
*
11
-
"
-
l»*.M "



~TYI™
ElT.
-

_
230
750
.
.
-
840
210
600
•

•
29


57
32
14
•
•
•
17
16
•
_
.
-

.
-
_
.
-
-
-
-
.
.
-
.
.
-
23
35
25
-
-
-
33
29
23
28
13
14
27
11
-
•
-
TrtMl t il'.-lil
::UIT.; !"• i-M.'i.rrv rvri.tTAM-.; ]•.«< 'iiir PU»TITVVI NT -.^MM.r:-
JiMIlV MATir '• I'r .\Xli-;; K-.-N. . \rHTH'N«'lf, /I)

rn<\ K^M -


r»™ N.,..' Effluo-.U ...
\MoxTm,.k>! Pfl.j1 »v~l'"-.-«« IH.I.X. KTlt.-V
Inf. Etf. E((. » IVhtv.iul-liM'!.' SIU.I.U- V'll",YxJ '•>*
<;:-..: ki: 1 	
--96 ....
.
317 ....
210 - 180 1100
470 740 .... 300O
....
... -
... ....
620 1300 470 1900
1
550
_
_
-
218
63
119
_
.
-
_
.
-
.
.
-
_
.
-
.
-
-
.
.
-
-
-
-
_
_
-
-
.
-
-
-
•
-
.
-
285
140
62
-
—
-
-
t
*
-
•
10
•
-
-
-
-
wn K ?



i.5X Ktiuct 43x '.sx
I . -
...
459 - 599 385
7JO • 9300 250
2400 16
- - -
... •
- . -
4203 - - 944
1000 - 14, D:O 1S5
2200
17 • -
41 • -
• •
.
...
-
-
... —
-
...
... .
_
...
... —
-
20
... .
-
- - 23
... -
-
...
• . — *
-
_
- - -
• _
.
... .
-
-
... -
-
425 fa
91 IS
170
...
... .
41
. . •
• • —
. •
-
• - • -
«• 14 * —
„ •
...
•. - _ _
•
83

-------
                                                                                 TABLE 111-18 (Continued)

                                                ANALYTICAL RESULTS OF PRIORITY POLLUTANTS FOR THE PRETREATMENT SAMPLING PROGRAM - WEEK 2
00



Poll
Pollutant ** No.
diethyl phthalate BNE 70


dimethylphthalate BNE 71


benzo (a) anthracene BNE 72


Chrysene BNE 76


Acenaphythylene BNE 77

Anthracene BNE 78


Fluorene BNE 80


Phenanthrene BNE 81


Pyrene BNE 84


SEMIVOLATILE ORGANICS (CONCENTRATIONS, ug/ 1)

POTW No. 2






Effluent to POTW from Refinery No.
x Pri.x Unoxx Unoxx Final" xx pri.xx oig.xx Filtexx
Day Inf. Eff. Inf. Eff. Eff. Centrate sludge Sludge Cake(mg/kg)13!t 21x
1 - 10 * 6 14 6
2 * * * - -
3***-* 10 15 6 -
!-*_ - __-
2 - - *
3 - - - _ _ - - _-
I . _--
2
3 _ - _ _ _ - - --
1--- - _--
2
3----- - - - -
1--- _ -_-
2
1*** - -_-
2 * * *
3***_* _ _ - —
1 * _ _ - ---
2 - « *
3*---- - - ._
1*** - __-
2 * * * — -
3 * * * _ * _ _ _ _
!-*- - __-
2 - - -
3 _ _ _ _ _ - - --
_
sa 12
-
-
-
-
_
* _
12
-
* _
12
-
-
4
36 *
29 *
_
14
*
*
36 *
29 *
-
* _
*
43x
45X Direct
_ *
-
-
-
-
-
_
* *
*
-
* *
*
-
-
81 *
39
54 *
_
-
-
81 *
39
54 *
_ *
16 *
* _
43x 16X
11
-

*
-

_
* _

-
* _

-
-
* *
-

_
_ *

* *
-

-
_ *

                  NOTE:         Of 59 semivolatiles, only 31 were detected
                            *   in traces, but below detection limit
                           **   AE - Acid Extractablej BNE - Base/Neutral Extractable
                            +   Anthracene and Phenanthrene are unresolved
                           ++   Chrysene and Benzo (a) anthracene are unresolved
                                Not detected
                            x   Samples analyzed by West Coast Technical Services
                           xx   Samples analyzed by Pomeroy, Johnston & Bailey

-------
                                           TABLE  111-19




Pollutant

Aldrin


Dieldrin


4,4'-DDT


4, 4 '-ODE


00 4,4'-DDD
(Jl

A-endosulfan-Alpha


Heptachlor


Heptachlor
epoxide

A-BHC-Alpha


B-BHC-beta


R-BHC -Gamma


G-BHC-Delta





Poll
No.

89


90


92


93


94


95


100


101


102


103


104


105





XX
Day

1
2
3
1
2
3
I
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
1
2
3
Analytical Results of


j{
Primary Unox11
Inf* Ef £ . Inf

- - _
-
3.60 - 0.10
-
_
_
-
0.17
0.11
0.09 0.35
0.19 - 0.11
0.66
0.38
-
-
-
-
0.12 - 0.52
0.47 0.10 0.45
-
0.70
_
-
2.10
1 . 30
0.24
0.88 - 1.20
0.16 0.76
_
_
0.27
-
_
1.25 0.45 1.50
_
0.27
Priority Pollutants for the Pretreatment Sampling Program - Week 2
Pesticides (Concentrations, MR/ 1)
FOTW No. 2
vv vv „„ Effluent to POTH from Refinery No.
Unoxx Finalx xx Primary Digested Filter ^x
Eff Eff Centrate sludge Sludge Cake 13X 2 IX 4SX Direct 43x
(rag/kg)
- _ — — — — — _
_ _
- - - - - 1.0 0.29 0.82
_ _ _ _ _ - - -
- 0.08 -
-_ - - _ _-- __
- 0.30 -
0.08 - 0.09
- - - - - - 0.39 - - 0.83
-___ __-_
-- 0.17 - - - -
0.17 - - - -----

- _
-- - _ - ___ __
---- ____
- - -
0.22 --- -----
-_-- ____
1.75 - - -
_- - - - -__ __
---- ____
- -
-- - - - -- - -0.32
- - - - - 0.52
1.5 1.62 - 0.17 0.27 0.36 2.21
1.40 0.76 - - - - 0.43 0.08
---- ____
- - - - - 0.32
-- - - - -__ __
---_ ____
- - - - - -
-- - - - ___ __
---- ____
- - -
-- - - - -__ __





16X

_
-

-
-

4.90
-

-
-

_
_

-
-

-
-

-
-

-
0.41

_
-

_
-

-
-

    Of the 25 Pesticides, only 12 were found; however,  none of then were confirmed by GCMS
    not detected
x   samples analyzed by West Coast Technical Services
xx  samples analyzed by Pomeroy,  Johnston and Bailey

-------
                                                                                                                                               TABLE  111-20
00
Analytical Results for Priority Pollutants for the Pre




Poll.
Pollutant No.




Arsenic 115


Beryllium 117


Cadntiuo 118




Lead 122

Mercury 123



Selenium 125


Silver 126


Thallium 127


Zinc 128






Day


2
3
1
2
3
1
2
3
1
2
:i
2
3
3
1
3
1
2
3
j
2
3
1
2
3
1
2
1
1
1
3
1
2
3




Influent
X

33
-
40
37
66
_
-
-
28
27
28
427
573
349
529
235
254
0.25
0.37
399
265
304
_
33
37
15
11
13
_
-
-
945
952
1593




primary
Effluent
X

33
-
_
-
-
_
-
-
12
20
13
154
164
153
176
62
70
1.69
0.25
0.49
206
190
228
-
-
-
_
-
-
-
-
-
274
375
385




Unox
Influent
X

_
-
26
-
49
_
-
-
1
1
7
17
124
162
1019
58
277
1.82
0.43
220
246
143
35
36
66
_
-
40
-
-
-
232
452
2086


po™ No. 2

Unox Final
Effluent Effluent
X X

35
-
29
_
-
_
~
-
20
25
26
45 334
50 456
23 311
25 341
135
168
2.46 0.49
-
"
236 272
310 343
29
37
-
_
11
10
-
-
-
144 820
178 010
178 1027




Generate
XX

1000

162
196

10
2

580
1040

27600
12300
4200

94
90

6500
5
5

70
60

20
50

25600
43400

treatment Sampling




Sludge
XX

1000

324
427

4
10

2020
1200

39600
31000
18600

124
171

6930
3
5

80
100

80
50

69000
52600





Sludge
XX

625

285
297

4
10

1050
1580

42500
19200
10800

232
147

9610
6
7

50
90

10
50

47000
70000

program - Week 2,




Cake
xx(roq/kg)

13

3
2

0.04
0.07

16
9

461
249
243
173
214
247
1.6
1.5

67
0.06
0.06

0.93
1

0.3
0.3

771
457




Effluent to POTV from
43x
13 21 45 Direct
XXX X

-
-
27
-
-
-
-
-
_
_
-
845 824 646 192
1133 1254 603 186
17 19
- 15 19
43 42 33 35
36 — —
38
0.79 - 0.67
0.37 - 0.46
l.OB - - -
- -
101 - 132
109 33 158
110 - 140
- -
- -
- -
-
- _
- -
190 153 183 115
116 173 182 137
55 189 174 158






Refinery Ho.
43
X

_
-
60
67
69
_
-
-
_
-
"
70
64
47
38
-
-
_
-
~
27
248
514
682
_
-
-
_
*
-
57
49
36
16
X

_
-
_
35
34
_
-
-
_
-
"
2196
1800
17
12
14
39
36
„
-
~
-
90
199
149
_
-
-
_
-
-
196
405
398
                                                                                  -  Not Detected.
                                                                                  x  Analyzed  by EPA Region IV Laboratory.
                                                                                 xx  Analyzitd  by poaioroy, Johnston and  Bailey.
                                                                                     c
-------
                              SECTION IV

                          SUBCATEGORIZATION


INTRODUCTION

Section 304(b)(2)(B) of the Act requires EPA  to  take  the  following
factors  into  account in assessing best available technology:  (1) age
of equipment and facilities involved;  (2) the  process  employed;  (3)
the engineering aspects of the application of various types of control
technology;   (<*)  process  changes;   (5)  the  cost  of achieving such
effluent  reduction;   (6)  non-water  quality   environmental   impact
(including  energy  requirements),  and  (7) such other factors as the
Administrator deems appropriate.  The assessment for best conventional
pollutant control technology  includes  these  same  factors  plus  an
evaluation  of  "...the reasonableness of the relationship between the
costs of attaining a reduction in effluents and the effluent reduction
benefits derived,  and  the  comparison  of  the  cost  and  level  of
reduction  of  such  pollutants from the discharge from publicly owned
treatment works to the cost and level of reduction of such  pollutants
from a class or category of industrial sources."

The  Agency  has  considered each of these factors in establishing the
proposed   effluent   limitations.    Factors   which    significantly
differentiate  groups  of  industry  facilities generally serve as the
basis for industry subcategorization.  Each subcategory then  develops
its own technologies representative of BAT, BCT, or BADT.

EPA   established  effluent  limitations  and  standards  (other  than
pretreatment standards) based on achievable values of three variables:
(1) total effluent flow  (gallons/day);  (2)  long-term concentration  of
each  pollutant  after BAT, BCT, or BADT treatment; and  (3)  short-term
variations in pollutant concentration after BAT, BCT or BADT treatment
which cannot be controlled by good operating practice.  It  should  be
noted  that  short-term variations in flow rate were not considered in
establishing effluent limitations.  These variations, in  contrast  to
final  effluent  concentrations,  are  controllable  by good operating
practice and design.  Flow  equalization   (collecting  effluent  in  a
large  tank or pond) is both an available technology  (see section VII)
and a good  operating  practice  since  it  minimizes  upsets  in  the
treatment system which can cause unnecessary  (controllable)  variations
in  final effluent concentration.  Flow equalization was a part of BPT
model technology, and costs and economic impacts of flow  equalization
were   considered   in   assessing  BPT.   Effluent  limitations  were
established by multiplying the achievable values of each variable.  In
general, an effluent limitation for a specific pollutant parameter  is
obtained as follows:
                                 87

-------
  Limitation = (Achievable Flow)  x (Achievable Concentration)
                             x (Achievable Variability)

The  Agency  analyzed  each  factor separately to determine whether it
significantly affects the ability of any group of refineries  to  meet
the   achievable  values  of  that  variable.   None  of  the  factors
significantly affect the  ability  of  different  refineries  to  meet
achievable  final  effluent  concentrations  of selected pollutants or
achievable concentration variabilities.  The only factor which affects
achievable  effluent  flow  was  factor  number   (2),   "the   process
employed."  Consideration  of  the  additional  "cost  reasonableness"
factor for establishment of BCT technology will be discussed later  in
this section.

Since  process  employed  was  found  to  be  a  significant factor in
establishing the  achievable  effluent  flow,  the  Agency  considered
subcategorizing based on processes employed.  Refineries, however, are
complex manufacturing facilities.  Over one hundred distinct processes
are  used  in the petroleum refining point source category.  Moreover,
sizes (throughputs) of the processes were  found  to  affect  effluent
flow.   It  is  not  practical to group refineries by both process and
size of process because each refinery would be a distinct subcategory.

The  Agency  ther.  considered  the   possibility   of   developing   a
mathematical model which would correlate achievable effluent flow with
a  relatively  small number of process variables.  Such a mathematical
model (flow model) would insure that  the  "process  employed"  factor
would be considered on an industry-wide basis.  Industry-wide effluent
limitations  could be developed without establishment of subcategories
containing only a very few facilities  (possibly one per subcategory).

Current BPT limitations are based on the approach  of  establishing  a
flow  model  to  account  for the factor "process employed"  (3).  Five
flow models were established to determine  achievable  flow  and  each
model  was  applicable  to  a  group of petroleum refineries (topping,
cracking, petrochemical, lube and integrated refineries).   Thus,  the
industry  was divided into five subcategories.  The flow model used as
a basis for BPT determined achievable flow based on two variables (one
related to the size of the plant and one related to the complexity  of
the plant).

For  the  current  flow  modeling effort, the Agency used the effluent
flows and the process characteristics reported in the  "1977  Survey".
The  Agency  reevaluated the BPT flow models based on the more current
data from the 1977 survey and found the BPT flow model to be very poor
in predicting the effluent  flows  which  had  been  achieved  by  the
industry in 1976.  Consequently, other flow models were explored.
                                 88

-------
FLOW MODELING EFFORT

Data Screening and Evaluation

The   data  from  the  1977  survey  were  reviewed  and  questionable
information was verified or corrected by subsequent telephone contacts
and additional mailings.  The follow up mailings focused primarily  on
the   interpretation   of   process   values   and   wastewater  flows
("Supplemental Flow Questions and  Verification  Report") .   The  flow
modeling  procedure  uses  only  these supplemental flow values in its
analysis.  Figure IV- 1 a plot of the wastewater flow values versus the
size of refinery, depicts the flow figures used in the analysis.

Regression Analysis

EPA has developed models of  refinery  wastewater  flows  based  on  a
statistical  analysis  of  the  verified  1977  EPA Petroleum Refining
Industry Survey data.  This analysis was performed  primarily  through
the use of multiple linear regression techniques.  With this approach,
an equation of the form
         Y = Ao +  -     AiXi     Equation  (1)
 (Note:  ^Z   means the summation from  1 to n.


       For example, if 3 variables were used  (n=3)

            Y = Ao + AIXI + A2_X2 + A3_X3_)

is  used  to  explain  the  relationship  between a dependent variable
 (wastewater flow in this case) and  a  set  of  independent  variables
 (such  as  process characteristics) .   Regression analysis assumes that
the  underlying  relationships  among  the  variables  are  linear  as
expressed in the above equation.

The  flow  modeling  analysis  begins  with  the  hypothesis  that the
petroleum refining industry effluent flow data can be modeled  by  the
relationship
         Y = Ao +      AiXi + Ei  Equation  (2)
where,
                                 89

-------
         Y = magnitude of the effluent flow

         Ao,Ai = constants to be determined by the regression
                  analysis

         Xi = characteristics of petroleum refineries and
               the petroleum refining industry

         Ei = random variable with a mean value of zero.

The independent variables are not restricted to representing a single,
unique physical characteristic; their functions take any form.  For an
industry-wide relationship, the Ei term in the above model assumes its
expected value of zero.

The  goal  of  the modeling procedure is to explain the variability of
wastewater flow among refineries  as  thoroughly  as  possible.   Each
physical  characteristic   (variable)   included in the model  (i.e., the
unit processes within a refinery) account  for  some  portion  of  the
total  flow.   Any  flow not attributable to the specific variables of
the model can be attributed to some  process  represented  by  the  Ei
variable.   The  larger  the  degree by which the model represents the
real world situation, the smaller  will  be  the  variability  of  the
random  variable  and  the  greater the accuracy of the model.  If the
magnitude of the wastewater flow were entirely explained  by  physical
characteristics, the model would need no random component.  Because an
infinite  amount  of  information is not available, however, the model
assumes only that all unknown factors will average  to  a  zero  value
over  the  entire  industry.   A  non-zero  expected  value  of  Ei is
indicative of a biased model and a failure of the modeling procedure.

BPT Model

Current BPT limitations for the  refining  industry  are  based  on  a
linear model of industry effluent flows.  This BPT model was developed
using  process and flow data from the 1972 EPA-API industry survey and
appears as:
         Y = Ao + A1X1 + A£X2    Equation  (3)

With components,

         Y = LogJJ) (total flow/capacity)

         Ao = Subcategory dependent constant

         A^,A,2 = Regression coefficient constants  (1.51 and
                  0.0738, respectively)
                                90

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         Xl^ = Refinery throughput

         X.2 = Sum of weighting factors for a particular
               refinery.

For the development of BPT regulations, the  equation  was  mathemati-
cally  transformed  from  the  standard slope-intercept representation
shown above to a form denoting deviation from  a  subcategory  average
value.  The  refinery  process  weighting  factors  are the normalized
coefficients of the regression model:

                   n
         Z = Ao * ^  AiXi       Equation  (4)
                  i=l

where

         Z = effluent flow

         Ao = regression constant

         Ai = regression constant  (weighting factor)
               corresponding to the ith petroleum refining
               process.

         Xi = throughput for process i.

BPT subcategorization was designed to give overall minimum variance to
the system; i.e., variance within each subcategory was  minimized  and
the differences between the subcategories were maximized.

Current Flow Model Development

The  development  of  the  BAT  effluent flow model differs in several
basic modeling assumptions from that of the BPT modeling effort.   The
primary  difference  is  the  wastewater quantity predicted by the two
models.

The BPT flow model identifies the dependent variable  (flow)  in  terms
of  gallons  of effluent discharged per barrel of raw input feedstock,
whereas the newly developed BAT model predicts  only  the  gallons  of
wastewater   generated   (not   necessarily   discharged.   The  total
wastewater generated from each refinery is the sum  of  the  wastwater
associated  with  each  in-plant  process.   The  flow  model does not
incorporate information on the reuse of wastewater.

Attempts  were  made  during  the  modeling  effort   to   develop   a
relationship  between  the  gallons of wastewater generated per barrel
unit of feedstock input and the process  capacities.   Such  endeavors
                                 91

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were  unsuccessful.   The Agency could develop no reasonable models by
which to identify a gallon per barrel wastewater flow.

From a theoretical viewpoint, the  gallons  per  barrel  figure  is  a
transformation of the total flow multiplied by the size of the primary
process.   Realistically, however, although some water is generated at
this stage of the refining chain, the refinery effluent  flow  appears
more  dependent on the configuration of the processes down stream from
the primary process.

Regression analyses using a  gallons  per  barrel  dependent  variable
produced  models which at best could explain only half the variability
of the effluent flow data.

Another major difference between the BPT and the BAT flow models is in
their forms.  The BPT model is an exponential multiplicative model  in
its  two  terms  of  size and complexity.  The BAT model is linear and
additive in its terms.

The decision not to use an exponential form for the present model  was
made  after  a  careful  study of the available facts.  It was closely
related to the more general decision not to perform any transformation
to the data at all.  Any transformation of data reduces the effect  of
some  of  the  data  points.   Although transformation at first appear
beneficial for this set of data, such an action  tend  to  deemphasize
the  larger  size  refineries,  even  though  it  is  the  larger size
refineries  for  which  so  few  data  points   exist.    Compromising
theoretical  statistical  purity  to  insured  that the effects of all
refinery sites were equitably considered.

The endeavors to  develop  a  viable  flow  model  progressed  through
several  distinct  stages, each one building on previous efforts.  The
statistical measure of "goodness of fit" also increased at each stage.

Initially, the model assumed that effluent flows could  be  determined
based on all the known sources of wastewater in refineries and all the
known  descriptive  characteristics  of  refineries.   This assumption
proved to be false.

Factors which impact wastewater generation is so numerous that data to
quantitatively describe their affect would be impossible to gather  or
to  analyze.   The  best  that can be hoped in flow modeling is that a
reasonable  approximation  of  what  occurs  in  a  refinery  can   be
formulated.

The  first  flow  model  attempted  to  identify  individual  refinery
characteristics slated  to  wastewater  production.   Because  nearly
every  refinery  characteristic  is correlated to some degree with the
magnitude of wastewater produced,  cause  and  effect  relations  were
                                 92

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extremely  difficult  to  separate from random relations.  Moreover, a
given characteristic had different effects  on  wastewater  generation
depending on the particular refineries under study.

The  result  of  this  stage  of the model development process was the
realization that many refinery characteristics do not  correlate  well
with  flow.   The  analysis  established  that  only  refinery process
characteristics should be included  in  the  model.   Because  process
wastewaters  account  for  only  70  percent  of  the  total  effluent
generated, the Agency had to accept the fact that a model based solely
on process information could not be 100 percent  accurate.   Remaining
variations would have to be included in the error term (Ei), and error
terms  from  the  resulting model would have to be analyzed for equity
among refineries.

The next model used only single ungrouped processes  as  the  modeling
factors.   A  variety  of  these  models were developed with differing
degrees of success.  Examples of these may be  found  in  the  earlier
draft  reports   (125).   The lack of real life physical correspondence
was the major drawback to these forms.  One  characteristic  of  these
models  was  that  almost  any  combination  of  processes  eventually
produced regression models with R2 values in the neighborhood of  .70.
R2  values (also known as correlation coefficients) measure the degree
to which the model explains the variation in  the  dependent  variable
 (flow).

After  considerable  experimentation  with  ungrouped  processes,  the
Agency next tried models based on processes grouped by  distinguishing
characteristics.

The  final  flow  model  is  a  compromise  among  perfect statistical,
regulatory, and  physical  factors.   This  model  contains  the  same
factors as the original BPT flow model, except for the size factor and
the coking effect.  The general form of the model is as follows:

    FLOW = industry average flow

         + Asphalt effect                 (Equation 5)
         + Crude effect
         + Cracking effect
         + Lube effect

The  regression analysis from which this model is derived indicated an
R2 of .749 with an overall F-distribution test statistic  of  166.   A
total  of  227  plants  possessed  valid  data  for the analysis.  The
independent model variable statistics are as follows:

-------
              Standard Error
                                        Regression Coef.
    Asphalt
    Crude
    Cracking
    Lube
             .02462
             .00112
             .00664
             .01073
 3.862
13.661
48.287
20.052
.04838
.00415
.04617
.04806
    The proposed form of the model for use in guidelines administration is:

Effluent Flow Model
FLOW = .568
                  .048A
                  .004 (C-59.2)
                  .046 (K-7.2)
                  .048L
       (Equation 6)
    The simplified form of this equation is as follows:

         FLOW = 0.004C + 0.046K + 0.048 (A + L).

    Constants are median values.
    Flow is in units of million gallons per day.
    A,C,K,L are in units of thousands of barrels per day throughput
    Constants are in units of million gallons per thousand
    barrels per day.

    Where,

    A = sum of asphalt processes
         Asphalt Production
         Asphalt Oxidizer
         Asphalt Emulsifying

    K = sum of cracking processes
         Hydrocracking
         Visbreaking
         Thermal Cracking
         Fluid Catalytic Cracking
         Moving Bed Catalytic Cracking

    C = sum of crude processes
         Atmospheric Crude Distillation
         Crude Desalting
         Vacuum Crude Distillation

    L = sum of lube processes
         Hydrofining, Hydrofinishing. Lube Hydrofining
         White Oil Manufacture
         Propane Dewaxing,  Propane Deasphalting,  Propane Fractioning,
           Propane Deresining
         Duo Sol, Solvent Treating, Solvent Extraction, Du©treating.
           Solvent Dewaxing, Solvent Deasphalt
         Lube Vac Twr,  Oil Fractionation,  Batch Still  (Naphtha Strip),
           Bright Stock Treating
                                94

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         Centrifuge and chilling
         MEK Dewaxing, Ketone Dewaxing, MEK-Toluene Dewaxing
         Deoiling (wax)
         Naphthenic Lubes Production
         SO£ Extraction
         Wax Pressing
         Wax Plant (with Neutral Separation)
         Furfural Extracting
         Clay Contacting - Percolation
         Wax Sweating
         Acid Treat
         Phenol Extraction
         Lube and Fuel Additives
         Sulfonate Plant
         MIBK
         wax Slabbing
         Rust Preventives
         Petrolatum Oxidation
         Grease Mfg. V. Allied Products
         Misc. Blending and Packaging

Use of the Flow Model

The flow model presented above (equation 6) predicts current  industry
flow  on  a  refinery  by  refinery  basis.   The  model  is  used for
regulatory purposes as representing the current wastewater  generation
flow rate of the industry.  This is analogous to using analytical data
(from  section  IV)   as representing current concentrations of various
pollutants in final effluent discharges.   If  additional  end-of-pipe
treatment  (such  as  activated  carbon) is applied as BAT, then lower
final effluent  concentrations  would  be  used  in  establishing  BAT
limitations.   Similarly,  if  flow  reduction  is  established as BAT
technology (see CONTROL AND TREATMENT TECHNOLOGY  section  VII),  then
correspondingly  lower  flows  than  those predicted by the flow model
would be used in establishing BAT limitations.

The flow model does not, and  is  not  intended  to,  exactly  predict
current flows from each refinery.  Some of these variations are purely
statistical  variations.  Much of the variation, however, is explained
by the fact that refineries discharging less effluent than  the  model
predicts  are  employing  flow  reduction  technology (see CONTROL AND
TREATMENT TECHNOLOGY Section VI)  which is not employed  by  refineries
discharging  more  effluent  than  the model predicts.  In considering
technology options for BAT and BCT, the Agency  calculated  compliance
costs  on  a  plant-by-plant  basis.   For  technology  options  which
included flow reduction, compliance costs were calculated for reducing
flow from actual flow  (1977) to the  flow  required  by  that  option.
Economic impacts also were assessed on a plant-by-plant basis.
                               95

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VO
                                             I
                                             I««
                                             I2V?
 »• 23 ?•
•32.1J 3     •
                                             0.0
                                                       3.30000  10"..60000  156.90000 209.20000 ?M.50000  313.BOOOO 366.10000 *18.40000 470.70000 523.00000
                                                                          Refinery Size (1000 bbJ/day)

                                                                                   FIGURE IV-1
                                                                  Process Wastewater Flow Versus Refinery Size

-------
                              SECTION V

                  SELECTION OF POLLUTANT PARAMETERS


INTRODUCTION

EPA  has  studied  petroleum  refinery  wastewaters  to  determine the
potential  presence  of  toxic,  conventional,  and   non-conventional
pollutants.   The  result  of  the study is provided in Section III of
this document.

The Settlement Agreement in Natural Resources Defense Council, Inc. v.
Train. 8 ERC 2120  (D.DoC. 1976), modified March 9, 1979, requires that
effluent limitations and standards be  established  for  each  of  the
sixty-five (65) toxic pollutants or classes of pollutants (Table II-1)
unless  the  Administrator  determines that it should be excluded from
rulemaking under Paragraph 8 of the subject Agreement.

POLLUTANTS FROM PETROLEUM REFINING INDUSTRY

EPA has conducted an extensive  sampling  and  analytical  program  to
determine  the  presence  of  toxic, conventional and non-conventional
pollutants in petroleum refinery wastewaters.   The  program  included
the  sampling  of  seventeen  (17) direct dischargers, six (6) indirect
dischargers, and two  (2) POTWs.  The American Petroleum Institute  has
split  samples  with  EPA  for  the  above  program at nine  (9) direct
discharge refineries, three (3) indirect discharge refineries and  one
(1)  POTW  sites.   The  analytical  results  from  the  EPA  and  API
laboratories are presented in Section III and Appendix 3.

The conventional and non-conventional pollutants analyzed  were  found
in  all  the  effluent streams.  The toxic pollutants were detected at
less frequent intervals.  Table V-1 lists the seventy-six  (76)  toxic
pollutants  that  were  not found in the treated effluents from direct
dischargers.  Of the  remaining  forty-seven  pollutants,  seven  were
found  in  the effluent of only one refinery and were uniquely related
to that refinery (not found in the  raw  wastewaters  from  any  other
plants).   These  seven  pollutants  and  the remaining pollutants are
listed in Table V-2 and V-3.  A pollutant is considered detected if it
occurs at a concentration higher than its concentration in the plant's
source water.

SELECTION OF REGULATED POLLUTANTS FOR DIRECT DISCHARGERS

The  pollutants  insufficiently  controlled  by  BPT  include  phenol,
chromium  (hexavalent  and  trivalent),  TSS,  BOD and oil and grease.
These pollutants were selected on the  basis  of  their  environmental
                                 97

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significance and/or the availability of treatment technology.  Reasons
for not further regulating the other pollutants are provided below.

Paragraph  8  of  the  Settlement Agreement (as modified) provides for
excluding toxic pollutants from regulations and standards.   Paragraph
8 (a) (iii)  of the Revised Settlement Agreement allows the Administrator
to  exclude from regulation toxic pollutants not detectable by Section
304(h) analytical methods or state of  the  art  methods.   Pollutants
listed   in  Table  V-1  are,  therefore,  excluded  from  regulation.
Paragraph 8(a)  (iii) also allows  the  Administrator  to  exclude  from
regulation  toxic  pollutants  detected  in  the effluent from a small
number of sources and uniquely related to those  sources.   The  seven
pollutants  in Table V-2 satisfy this criteria.  Pollutants which were
found in the treated effluent at only  one  refinery  but  which  were
detected  in  the untreated effluent of a number of facilities are not
considered uniquely related to one plant.

Paragraph 8(a)  (iii) also excludes  from  regulation  toxic  pollutants
which were detected but for which no known treatment technology exists
to  reduce their discharge, or which are effectively controlled by the
technology upon which  other  effluent  limitations  are  based.   The
Agency  believes  that  the  technology  upon  which  the proposed BAT
effluent limitations for phenol  (4AAP)  and  chromium  are  based  will
effectively control the organic and metallic toxic pollutants in Table
V-3  with  the  exception  of  cyanide.   Cyanide  with final effluent
concentration as high as  170  ppb  is  discharged  by  the  petroleum
refining  industry, but EPA is not aware of any end-of-pipe technology
which will reduce cyanide discharges beyond its  current  level.   The
Agency  plans  to  continue study of this problem to determine whether
cyanide discharges can be reduced by in-plant control.

SELECTION OF REGULATED POLLUTANTS FOR PRETREATMENT STANDARDS

Section 307(b)  of the Clean  Water  Act  requires  EPA  to  promulgate
pretreatment  standards  for  both  existing  and  new  sources  which
discharge their wastes into publicly  owned  treatment  works   (POTW).
These  pretreatment standards are designed to prevent the discharge of
pollutants which  pass  through,  interfere  with,  or  are  otherwise
incompatible  with  the  operation  of  POTWs.  In addition, the Clean
Water Act of 1977 adds a new dimension to these standards by requiring
pretreatment of pollutants, such as metals,  that  limit  POTW  sludge
management alternatives.

EPA  has sampled six indirect discharge plants and two POTWs API split
samples with EPA at half of these facilities.  Toxic pollutants  found
and  not  found  in the effluents from these refineries and POTW^ are
listed in Table V-4 and V-5, respectively.
                                98

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Ammonia and oil and grease at concentrations exceeding  100  mg/1  can
interfere with the operation of POTW's.  Chromium from refineries will
accumulate  in  POTW  sludges  and  will  limit  the sludge management
alternatives of the POTW.

Paragraphs 8(a) (i) and 8(a) (iii) of the Revised  Settlement  Agreement
allow  the  administrator to exclude pollutants from regulations under
pretreatment standards.   The  pollutants  listed  in  Table  V-5  are
excluded  from pretreatment regulations because they were not found in
the refineries' discharges to the POTW's.  Toxic pollutants other than
chromium are excluded from  regulation  because  they  are  controlled
adequately  by  existing  PSES  if  the  refinery  discharges  into  a
secondary POTW.  Refineries which route their wastes to primary  POTWs
require additional control.  Table V-6 lists those priority pollutants
which pass through primary POTWs.
                                  99

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                               TABLE V-1
                   Toxic  Pollutants Not. Detected In
                  Treated  Effluents  (Direct Discharge)
 1.   Organics
 acrolein
 acrylonitrile
 chlorobenzene
 1,1,1-trichloroethane
 1,1-dichloroe thane
 1,1,2—trichloroethane
 chloroethane
 2-chloroethylvinyl ether
 chloroform
 methyl chloride
 methyl bromide
 bromoform
 trichlorofluoromethane
 dichlorodifluoromethane
 chlorodibromomethane
 vinyl  chloride
 acenaphthene
 benzidine
 1,2,4-trichlorobenzene
 hexachlorobenzene
 hexachloroethane
 bis (chloroinethyl) ether
 bis (2-chloroethyl) ether
 2-chloronaphthalene
 2,4,6-trichlorophenol
 2-chlorophenol
 1,2-dichlorobenzene
 1,3-dichlorobenzene
2.  Pesticides

aldrin
dieldrin
chlordane
4,4'DDT
4,4'-DDE
4,4'-DDD
a-endosulfan-Alpha
b-endosulfan-Beta
endosulfan sulfate
endrin
 1,4-dichlorobenzene
 3,3'-dichlorobenzidine
 2,4-dinitrotoluene
 2,6-dinitrotoluene
 1,2-diphenylhydrazine
 4-chlorophynyl  phenyl ether
 4-bromophenyl phenyl  ether
 bis (2-chloroisopropyl)  ether
 bis (2-chloroethoxy) methane
 hexachlorobutadiene
 hexachlorocyclopentadien e
 isophorone
 nitrobenzene
 2-nitrophenol
 2,4-dinitrophenol
 4,6-dinitro-o-cresol
 N-nitrosodimethylamine
 N-nitrosodiphenylamine
 N-nitrosodi-n-propylamine
 pentachlorophenol
 butyl benzyl phthalate
 di-n-octyl phthalate
 3,4-benzofluoranthene
 benzo (k)fluoranthane
 acenaphthylene
 dibenzo(a,h)anthracene
 ideno(1e2,3-cd)pyrene
 2,3,7,8-tetrachlorodibenzo-
 p-dioxin (TCDD)
endrin aldehyde
heptachior
heptachlor epoxide
a-BHC-Alpha
b-BHC-Beta
r-BHC-Gamma
g-BHC-Delta
PCB-1242
PCB-1254
                                 100

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3.  Metals



None



4.  Others (Asbestos, UAAP Phenol)



    asbestos  (fibrous)
                                 101

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                              TABLE V-2
                      Toxic Pollutants Found in
                      Only One Refinery Effluent
                 (at concentrations higher than those
                 found in the intake water) and which
            are Uniquely Related to the Refinery at Which
                  it was Detected  (Direct Discharge)
1.  Organics

Carbon tetrachloride
1,1-dichloroethylene
1,2-dichloropropane
1,2-dichloropropylene
2,4-dichlorophenol
di-n-butyl phthalate
dimethyl phthalate

2.  Pesticides

None

3.  Metals

None

4.  Others (Asbestos, 4AAP Phenol)

None
                                102

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                              TABLE V-3

          Toxic Pollutants Detected in Treated  Effluents  of
          More Than One Refinery or Detected  in the  Treated
          Effluents of One Refinery but Not Uniquely Related
          to the Refinery at Which it Was Detected   (Direct
                              Discharge)
1.  Organics

Benzene
1,2-dichloroethane
1,1,2,2-tetrachloroethane
parachlorometa eresol
1,2-trans-dichloroethylene
2,4-dimethylphenol
ethylbenzene
fluoranthene
methylene chloride
dichlorobromometha ne
naphthalene
4-nitrophenol
phenol

2.  Pesticides
None
    Metals
bis(2-ehtylhexyl) phthalate
diethyl phthalate
benzo(a)anthracene
benzo(a)pyrene
chrysene
anthracene
benzo(ghi)perylene
fluorene
phenanthrene
pyrene
tetrachloroethylene
toluene
trichloroethylene
antimony  (total)
arsenic (total)
chromium  (total)
beryllium  (total)
cadmium (total)
copper (total)
cyanide (total)

4.  Others (Asbestos, 4AAP Phenol)

None
lead (total)
mercury (total)
nickel (total)
selenium (total)
silver
thallium (total)
zinc (total)
                                 103

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                              TABLE V-4

                     Toxic Pollutants Detected in
               Discharges to POTWs  (Indirect Discharge)
1.  Organics
benzene                           naphthalene
chlorobenzene                     N-nitrosodiphenylamine
1,2-dichloroethane                pentachlorophenol
1,1,1-trichloroethane             phenol
chloroform                        butyl benzyl phthalate
ethylbenzene                      di-n-butyl phthalate
methylene chloride                di-n-octyl phthalate
tetrachloroethylene               diethyl phthalate
toluene                           benzo(a)anthracene
acenaphthene                      chrysene
2,4-dimethylphenol                anthracene
2,4-dinitrotoluene                fluorene
1,2-diphenylhydrazine             phenanthrene
isophorone                        pyrene

2.  Pesticides

aldrin
4,4'-DDT
4,1•DDE
heptachlor epoxide
a-BHC-Alpha
b-BHC-Beta

3.  Metals

arsenic (total)
chromium (total)
copper (total)
lead (total)
mercury (total)
nickel (total)
selenium (total)
zinc (total)

4.  Others (Asbestos, 4AAP Phenol)

Not analyzed
                                104

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                              TABLE V-5
                   Toxic Pollutants Not Detected in
               Discharges to POTW  (Indirect Discharge)
1.  Organics
acrolein
acrylonitrile
carbon tetrachloride
1,1-dichloroethane
1,1,2-trichloroethane
1,1,2,2-tetrachloroethane
chloroethane
2-chloroethylvinyl ether
1,1-dichloroethylene
1,2-trans-dichloroethylene
1,2-dichloropropane
1,2-dichloropropylene
methyl chloride
methyl bromide
bromoform
di chlorobromomethane
trichlorofluoromethane
dichlorodifluoromethane
chlorodibromomethane
trichloroethylene
vinyl chloride
benzidine
1,2,4,-trichlorobenz ene
hexa chloroben zene
hexachloroethane
bis(chloromethyl) ether
bis (2-chloroethyl) ether
2-chloronaphthalene
2,4,6 -trichlorophenol
2.  Pesticides

dieldrin
chlordane
4,4'-ODD
a-endosulfan-Alpha
b-endosulfan-Beta
endosulfan sulfate
parachlorometa cresol
2-chlorophenol
1,2-dichlorobenzene
1,3-dichlorobenzene
1,4-dichlorobenzene
3,3'-dichlorobenzidine
2,4-dichlorophenol
2,6-dinitrotoluene
fluoranthene
4-chlorophenyl phenyl ether
4-bromophenyl phenyl ether
bis (2-chloroisopropyl) ether
bis(2-chloroethoxy) methane
hexachlorobutadiene
hexachlorocyclopentadiene
nitrobenzene
2-nitrophenol
4-nitrophenol
2,4-dinitrophenol
4,6-dinitro-o-cresol
N-nitrosodimethylamine
N-nitrosodi-n-propylamine
bis (2-ethylhexyl) phthalate
dimethyl phthalate
benzo(a)pyrene
3,4-benzofluoranthene
benzo(k)fluoranthene
acenaphthylene
benzo(ghi)perylene
dibenzo (a,h)anthracene
ideno(1,2,3-cd)pyrene
2,3,7,8-tetrachlorodibenzo-
 p-dioxin (TCDD)
g-BHC-Delta
PCB-1242
PCB-1254
PCB-1221
PCB-1232
PCB-1248
                                105

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endrin                            PCB-1260
endrin aldehyde                   PCB-1016
heptachlor                        toxaphene
r-BHC-Gamma

3.  Metals

antimony  (total)
beryllium  (total)
cadmium  (total)
silver (total)
thallium  (total)
cyanide  (total)

4.  Others  (Asbestos, 4 AAP Phenol)

Not analyzed
                                106

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                              TABLE V-6

             Toxic Pollutants Found to Pass Through POTW
           with Only Primary Treatment  (Indirect Discharge)

1.  Organics

benzene                           2,4-dimethylphenol
1,2-dichloroethane                naphthalene
1,1,1-trichloroethane             phenol
chloroform                        butyl benzyl phthalate
ethylbenzene                      di-n-butyl phthalate
methylene chloride                di-n-octyl phthalate
tetrachloroethylene               diethy1 phthalate
toluene

2.  Pesticides

U,4'-DDT
4,4'-DDE
a-BHC-Alpha
b-BHC-Beta

3.  Metals

arsenic (total)
chromium (total)
copper (total)
lead (total)
mercury (total)
nickel (total)
selenium (total)
zinc (total)

U.  Others  (Asbestos, 4AAP Phenol)
         Not analyzed
                                107

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                              SECTION VI

                   CONTROL AND TREATMENT TECHNOLOGY


INTRODUCTION

This  section  addresses  the  control and treatment technologies that
apply  to  petroleum   refining   wastewaters.    Petroleum   refinery
wastewaters vary in quality and quantity.  Nevertheless, they all were
readily  In  identifying  available treatment technologies, the Agency
assumed that each refinery had or would install treatment equipment to
comply with limitations based on best practicable  control  technology
currently  available   (BPT) (3).  The treatment technologies described
below are those which  can  reduce  further  the  discharge  of  toxic
pollutants  to  navigable  waters.   They  are  divided into two broad
classes -- in-plant source control and end-of-pipe treatment.

In-Plant Source Control

In-plant source control affords two major benefits  afforded  (1)  the
overall reduction of pollutant load that must be treated by an end-of-
pipe  system;  and  (2)  the  reduction or elimination of a particular
pollutant parameter before dilution in the main wastewater stream.

In  developing  an  in-plant  control  schemes  the  source  of   each
particular  pollutant  must  be identified, evaluated as to whether it
can be eliminated, or reduced.  This can be accomplished  by  sampling
the  wastewater at various points within the refinery sewer, beginning
at the end-of-pipe treatment system, and ending at the process  units.
This  procedure  produces  a profile of the refinery sewer showing the
origin and flow path of the pollutant in question.

Once the source of the particular pollutant is  identified,  the  next
step  determines if the pollutant:  (a) can be removed with an in-plant
treatment system;  (b)  can be eliminated by substitution, if  it  is  a
purchased  item;  or (c) can be reduced by the recycle or reuse of the
particular wastewater stream.  Discussions of each of  these  in-plant
treatment  options,  as  they  relate  to a particular waste stream or
pollutant parameter, are presented below.

In-Plant Treatment Options

All in-plant treatment options require the segregation of the  process
waste  streams  under consideration.  If there are multiple sources of
the particular pollutant or pollutants, they all  require  segregation
from  the  main wastewater sewer. However, similar sources can be com-
bined for treatment in one system. Sour waters illustrate  a  type  of
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wastewater  that  is  produced  at various locations within  a  refinery
complex, but that can be treated as one combined wastewater  stream.

Sour waters and cooling tower blowdown are the two waste   streams  for
which in-plant treatments are being practiced or are available.

Sour Waters.

Sour  waters  generally  result from water brought into direct contact
with a hydrocarbon stream.  This  occurs  when  steam  is  used  as  a
stripping or mixing medium, or when water is used as a washing medium,
as  in  the  crude  desalting  unit.   Sour  waters  contain sulfides,
ammonia, and phenols.

The most common in-plant treatment schemes  for  sour  waters  involve
sour  water  stripping,  sour  water oxidizing, or combinations of the
two.  Table VI-1 summarizes the  extent  of  this  technology  in  the
refining  industry.   The  operation  of sour water strippers  and sour
water oxidizers  has  been  discussed  at  great  length   in  numerous
technical publications  (3, 6, 18, 20, 24, 28, 48); there is  no need to
discuss  these  treatment  units  in  detail.   However,   it should be
emphasized that these systems can greatly reduce sulfides  and  ammonia
levels,  and  also  can  afford  some removal of phenols  (24).  A sour
water stripping study was undertaken in 1972 by the American Petroleum
Institute  (24).  The results of this survey showed that 17 out of  31
refluxed sour water strippers and 12 out of 24 non-refluxed  sour water
strippers   achieved   greater  than  99%  removal  of  sulfides.   An
additional nine refluxed and three non-refluxed units achieved greater
than 99% removal of sulfides and greater than 95% removal  of  ammonia.
The  data  thus  suggests  that refluxed columns afford better overall
removals of  both  pollutants.   It  should  be  noted  that  of  five
two-stage units reported, only one unit achieved high removals of both
parameters.   Six  out  of seven strippers operating with  flue or fuel
gases removed over 99% of the sulfides.  However, none of  these  units
achieved high ammonia removals.

The average effluent of all refluxed, non-refluxed, and flue gas units
which  achieved  greater  than  99%  sulfide  removal  was 6.7 mg/1 of
sulfide.  The average effluent from all units which  achieved  greater
than 95% ammonia removal was 62.5 mg/1 of ammonia.  These  averages are
based upon a wide range of influent and effluent values.

Existing  sour  water  stripper  performance  can  be  improved by  (a)
increasing the number of trays,  (b)  increasing  the  steam  rate;   (c)
increasing  tower  height;  and   (d)  adding a second column in series
(107).  All of these methods are available  already  to  the  refining
industry.
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Biological  treatment  to  remove total phenols is also a demonstrated
technology in this industry (H8).  Biological  treatment  of  stripped
sour  waters  may  prove  cost-effectiveness  for  the  removal of any
biodegradable organic priority pollutants that may originate  in  this
waste stream.

Phenol   removal  from  the  sour  water  waste  stream  can  also  be
accomplished by the addition of oxidizing agents, such as ozone   (51),
hydrogen  peroxide   (11),  chlorine,  chlorine  dioxide, and potassium
permanganate (113).

A recent research project has demonstrated that activated carbon  will
also removes phenolic compounds.  The experiment showed that activated
carbon  has a high affinity for phenolic compounds, so that relatively
short detention times are required.   Activated  carbon  treatment  in
sour  water  streams also may remove other organic priority pollutants
that may be present.  Refinery  No.  237  uses  activated  carbon  for
treatment   of  the  sour  water  waste  stream,  and  the  Agency  is
investigating this particular system further.

Cooling Tower Slowdown.

Removal of metals  (such as chromium and zinc)  and  phosphate  can  be
achieved by precipitation and clarification at a relatively high pH  (8
   10).   Hexavalent  chromium,  however, must be first reduced to the
trivalent  state  before  it  can  be  precipitated  and  removed   by
clarification.  This usually is accomplished by the addition of sulfur
dioxide,  ferrous  sulfate,  or  sodium  bisulfite.   The  pH  of  the
wastewater then rises with the addition of lime or  caustic  (lime  is
preferred  if phosphates are to be precipitated); clarification of the
wastewater stream follows.  Flocculants and flocculant aids,  such  as
ferric  chloride, alum, and polymers, can be added to increase removal
efficiencies.

Japan's Mitsubishi Petrochemical company has reported a new  treatment
technique  for  the  removal  of  heavy  metal ions (126).  The system
involves electrolytic coagulation in which electrical currents  causes
an  iron  electrode  to dissolve.  The iron combines with heavy metals
and added hydroxide ion to form a  sludge  that  can  be  precipitated
rapidly  from solution.  Magnets aid the settling process.  Mitsubishi
reports that the new treatment system can reduce Cr+* concentration to
less than 0.05 ppm in 2900 gallons of metal plating wastewater.   This
system  could apply to the treatment of cooling tower blowdown streams
at petroleum refineries.

None of the 259 refineries  in  the  1977  survey  indicated  in-plant
treatment   schemes   designed   specifically  for  chromium  removal;
treatment equipment vendors, however, indicate that several refineries
have installed such treatment.
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Chemical Substitutions

Chemicals are added to cooling tower recirculating  water  and  boiler
water  to  reduce  corrosion,  scaling,  and biological growth.   These
chemicals  usually  include  chromium,  zinc,  phosphates,  and    free
chlorine, as well as other potential pollutants.

Using  organic chemicals to replace for zinc and chromium solutions is
also a viable alternative  (53,54).  Molybdates are  also  a  practical
alternative   (55).    (Molybdates  are  compounds  containing the anion
MoOJ-t2-.)

Wastewater Reduction and Reuse

Reduction.  Reduction in  water  usage  sometimes  may  be  more  cost
effective  in reducing the quantity of wastewater discharge than water
reuse or recycle.  Good housekeeping  is  one  inexpensive  method of
reducing  wastewater  production.   It  may include:  (a) shutting down
pump gland cooling water lines on pumps that are out  of  service;  (b)
shutting  down  wash  down  hoses that are not in use;  (c) eliminating
leaks;  (d) using dry cleaning methods; and  (e) using  vacuum trucks to
clean  up oil spills.  Numerous other housekeeping procedures  commonly
are practiced throughout the industry.

Many new and modified refineries  incoporate  reduced water   use and
pollutant  loading  into  their  design.   Some of these modifications
include:

    1.   Substitution  of  improved  catalysts   that  require    less
regeneration.

    2.   Replacement of barometric condensers with surface  condensers
or air fan coolers.

    3.   Replacement of surface condensers with air fan coolers.

    4.   Newer hydrocracking and hydrotreating processes which produce
lower wastewater loadings than the older processes.

    5.   Increased use of improved drying, sweetening,  and  finishing
procedures  to  minimize  spent  caustics and acids,  water washes, and
filter solids requiring disposal.

    6.   Recycle of wastewwater at the process units,  to  reduce the
amount of wastewater leaving the process area.

A  major  process  change that, can reduce wastewater  production  is the
substitution of air cooling devices for water cooling systems.    Many
refineries  have  installed air cooling systems with  their new process
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installations, thereby reducing the additional  wastewater  production
associated with increased refinery complexity.

Of  the  78  refineries  for  which  data are available for comparison
between 1972 and 1976, the percentage use of air cooling  systems  has
increased  at  39  refineries,  has decreased at 26 refineries and has
rendered the same at 13 refineries.  Increasing  use  of  air  cooling
systems  can  reduce the quantity of cooling tower blowdown discharges
that require treatment.

Another method of wastewater reduction is the elimination  of  cooling
water  from  general  purpose  pumps   (117).  In certain instances the
elimination  of  water  can  increase  machinery  reliability,  reduce
capital  expenditures  for  piping and water treatment facilities, and
save operating costs guidelines are available for implementation of  a
well-planned,  step-by-step  program  of  deleting  cooling water from
pumps  and  drivers.   These   procedures   have   been   successfully
implemented on a full-scale basis  (117).

Reuse.   Many  of  the  streams,  such as treated sour waters, cooling
tower blowdowns, and utility blowdowns, are suitable for use  as  wash
waters and fire system water.  However, reuse of wastewaters for these
purposes    requires   investigation  on  a  plant-by-plant  basis  to
determine the technical and economic feasibility.

Wastewaters emanating from end-of-pipe BPT facilities are generally of
such quality that reuse can be  quite  attractive.  Uses  for  treated
refinery  wastewaters  include  make-up  to cooling towers, pump gland
cooling systems, wash-down waters, and fire water systems.

A number of articles in  recent  years  have  described  actual  reuse
practices at one refinery  (41, 57, 58).  This plant reuses most of its
treated  wastewater  as  make-up  to  the cooling tower and fire water
systems.  In practice, the cooling towers act as biological  treatment
units,  and  remove in excess of 99% of the phenols present (41).  The
refinery  reuses  approximately  4.5  million   gallons   of   process
wastewater  per day in their cooling towers; about 2.2 million gallons
of cooling tower blowdown per day are sand filtered and discharged  to
the  receiving stream.  The difference, in excess of 2 million gallons
per day, is evaporated in the cooling towers or in an impounding basin
(58).  Wastewater reuse began at this  refinery  in  1954.   Years  of
operating experience have confirmed that reuse water is a satisfactory
make-up  supply  to  cooling towers and does not require special water
conditioning or treatment.  Continued monitoring  has  confirmed  that
the  system  has  no  problems of corrosion, heat transfer, or cooling
tower wood deterioration.  The refinery  has  concluded  that  cooling
tower  reuse  is  an  economically  sound practice, paying significant
dividends in terms of both pollution abatement and water  conservation
(57) .
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Two  recent  articles discussed the reduction of wastewater generation
by the use of: (a)  side  stream  softening  to , reduce  cooling  tower
blowdown flow; and (b) reuse of properly treated wastewater as make-up
to a cooling tower system.

Reed,  et  al.  report  that  side stream softening can greatly reduce
cooling tower blowdown.  They conclude  that  by-pass  lime  softening
appears  to  be  a  realistic  technique  applicable  to  both new and
existing  cooling  tower  systems.   Cooling  water  systems  in  high
dissolved  solids  applications  can  be  expected  to  be  adequately
protected through  the  use  of  corrosion  inhibitors.   The  authors
present  a method for designing for zero blowdown applications and for
predicting  steady  state  conditions.   A  pilot  cooling  tower  was
operated with a recirculating water chemistry designed to simulate the
ultra-high  TDS levels, representative of conditions expected for zero
blowdown systems.  Low corrosion rates on mild steel and copper  alloy
specimens were reported after application of a proprietary synergistic
chromate   corrosion   inhibitor.   These  low  corrosion  rates  were
especially pertient to the application of  zero  blowdown  systems  at
existing  installations  having  considerable amount of mild steel and
copper plumbing and process equipment  (127).

Finelt and Crump (128) report  that  refiners  faced  with  increasing
fresh  water  costs  may direct their water management policies toward
the recirculation of treated water.  Properly treated  wastewater  can
be   recycled  as  make-up  to  the  cooling  tower  system.   At  new
refineries, it is possible that the recycle system could be  justified
economically over a non-recycle system.  There are a number of factors
to  be considered,  most notably the cost of fresh water, determing the
least costly system.  At existing well-operated  facilities,  only  at
very  high  fresh  water costs can the recycle system prove to be less
costly than a non-recycle system.   However,  application  of  recycle
technology  can  reduce effluent discharge by up to ninety percent and
possibly help to establish "zero discharge" facilities.

The use of sour  waters  as  make-up  to  the  desalter  is  a  proven
technology  in  this  industry.  This practice does remove some phenol
because the phenolics are extracted from  the  sour  water  while  the
crude  is  washed.    However,  the  removal  efficiency varies greatly
depending on a number of factors, and this treatment scheme may not be
a practical alternative for some  refineries   (48).   Certain  crudes,
particularly  California  crudes, may present problems in reusing sour
waters in the desalter because they produce emulsions in the  desalter
effluent.

Table  VI-2  identifies  those refineries with California crudes which
recycle; the table also lists the percent of crude capacity made-up of
California crudes and the percentage of  reused  sour  waters.   These
data  show  that  refineries  processing  California crudes do not use
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large percentages of  sour  water  in  the  desalter.   In  fact,  the
refineries  that use a large percentage of California crudes appear to
reuse less sour water than  those  refineries  that  process  a  small
percentage  of  California crude.  However, Table VI-3 shows that five
of the six plants in this analysis do reuse sour  water  elsewhere  in
the refinery.

Sour  water  stripper  bottoms  have  other  demonstrated  uses in the
petroleum refining industry (36).   These  include  reuse  as  cooling
tower  make-up  and  as  process  wash  water,  both  of  which afford
additional phenol removal due to either oxidation or extraction.   The
biological environment in most cooling systems is conducive to removal
of 90 percent or more of the phenols present  (36).

The  1977  EPA  Petroleum  Refining  Industry  Survey  shows  that  36
refineries reuse 100% of their treated sour waters  in  the  desalter,
while  an  additional  H3  plants reuse at least some portion of their
treated sour waters in the desalter.  In addition, 32 refineries reuse
treated sour waters in some other  process.   Of  these  plants,  four
reuse  100X of their treated sour waters as make-up to cooling towers.
Table VI-3 summarizes the extent of industry  reuse  of  treated  sour
waters.

The  American Petroleum Institute published a document entitled "Water
Reuse Studies" in August 1977  (150).  This document  presents  methods
for achieving zero discharge, including:

1.  Recycle  and  reuse  of  treated  effluent  as   well   as   other
    wastewaters;

2.  Recovery and reuse of condensate streams;

3.  Evaporation of wastewater with waste heat; and

t.  Use of brine concentrators to eliminate high TDS streams.

The API  report  concludes  that  for  grass  roots  refineries,  "(1)
engineering  concepts  are  available which indicate complete reuse of
refinery water  is  technically  possible  and   (2)  the  capital  and
operating costs appear favorable for complete recycle . . . ."(150).

The  recycle of treated effluent as cooling tower make-up or for other
uses  is  certainly  a  viable  treatment  alternative  and  must   be
considered  as an available BAT technology.  Significant reductions in
wastewater  generation  can  decrease  the  quantities  of  pollutants
discharged   to  navigable  waters.   In  some  cases  where  refinery
personnel already have significantly improved their present wastewater
management  system  (i.e.,  minimized  cooling  tower  blowdown) ,  the
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treated  effluent  to be recycled may require further treatment  (i.e.,
softening) prior to recirculation.

In order to determine an upper limit of how  much  treated  wastewater
can  be  reused  as cooling tower make-up, the amount of cooling tower
make-up  required  in  the  industry  on  a  plant-by-plant   basis  is
summarized  in  Table  VI-H.   The percentage of cooling tower make-up
water in the total wastewater discharged also is  shown.   This  table
has   been   derived   from   the   1977  idustry  survey  data  base.
Approximately half of the facilities  have  a  cooling  tower make-up
water  requirement  equaling or exceeding the total refinery  discharge
flow.

EPA analyzed the flow informations from the 1977 survey  to   determine
the  degree  of  flow  reduction achievable.  The petroleum refineries
were  divided  into  two  categories:  plants   presently   generating
wastewater equal to or less than their model flow; and those  with flow
rates  higher  than  the  model flow.  The average of the percent flow
reductions for all  refineries  meeting  their  model  flow   has  been
determined  to  be  52%.   36%  of  the  refinereies  have  wastewater
generation equal to or less than 52% of the model flow.   Table  VT-20
lists  the  refineries that are generating wastewater equal to or less
than their model flow.

Refineries with wastewater generation equal  to  or  less  than  their
model prediction and greater than 52% of the model flow were  anlayzed.
The average of the percent flow reduction for these refineries is 27%.
Approximately 50% of the industry is achieving this reduction.

In  order  to  check  whether  the "low flow" plants  (i.e. plants with
discharge flow rates at or below 0.48 of BAT model flow)  represent  a
special  segment of the industry, the data from these plants  have been
reviewed and  analyzed.   Table  VI-5  presents  the  capacities,  BPT
subcategories, and EPA regions for the 93 plants presently at or below
0.48 of their model flow.  Tables VI-6 through VI-8 summaries the data
included  in  Table VI-5.  These data show that the size, geographical
location and complexity  of  this  segment  is  very  similar to  the
industry as a whole.

END-OF-PIPE TREATMENT

This   document   defines  end-of-pipe  treatment  as  all  wastewater
treatment systems that follow an API separator or a similar   oil/water
separation   unit.    The   treatment  schemes  described  below  were
considered for application as BAT, BCT, and BADT in  conjunction  with
BPT treatment and water reuse and recycle.
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Biological Treatment

Biological  treatment is the basic process by which at most refineries
in meeting existing  BPT  guidelines.   Excellent  removal  of  oxygen
demanding  compounds  (as  measured  by  the  BOD5,  COD, and TOC test
methods) is being achieved at many refineries through the  application
of well-designed and well-operated biological treatment systems (146).
This  is  the first step toward compliance with future BAT guidelines,
regardless of their basis.  This will be particularly true  for  those
refineries  which  have  complied with BPT requirements by drastically
reducing flow while only minimal improving the treatment system.

Where it is necessary to upgrade present biological systems, there are
many options available.   These  include  compartmentalized  oxidation
ponds  to  provide  preliminary mechanical aeration; revamping aerated
lagoon systems into  activated  sludge  systems;  and  the  converting
standard  activated  sludge  systems  to  pure  oxygen systems.  Other
modifications can  improve  the  operating  efficiency  of  particular
biological  treatment  unit,  but  these  require  investigations on a
plant-by-plant basis.

The sampling data presented in Section III  indicate  that  biological
treatment  can  remove organic priority pollutants to low levels (i.e.
10-100 micrograms per liter).  These removals were obtained from  both
industrial and POTW samples as part of this study.  It should be noted
that the removal mechanisms have not been determined.  Removals may be
accomplished  by  air  stripping  and waste sludge settling as well as
biological degradation.

Filtration

Filtration, a polishing step  after  biological  treatment,  also  was
considered  as  part  of  the model BPT treatment technology (3).  The
survey results indicate that 27 of the 259 respondents use  filtration
as  part  of  their  existing treatment scheme, including those plants
where  filtration  precedes  biological  treatment.    Sixteen   other
refineries  plan  to  install  filtration  systems in the near future.
Table VI-9 lists those  refineries  that  have,  or  are  planning  to
install,  rapid  sand or dual media filtration systems. Filtration can
improve effluent quality by removing suspended solids and the BOD  and
COD  associated  with  suspended  material, and by removing carry-over
metals that already have been precipitated and flocculated. Filtration
can also improve overall treatment plant performance (130, 132, 133).

The removal of solids through filtration  techniques  can  reduce  the
effluent  variability of biological treatment systems.  One study  (30)
showed that  the  percentage  of  suspended  solids  removed  did  not
deteriorate  with  high  feed  content;  in fact, the percent removals
often increased with feed concentration.  Concentration  of  suspended
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solids  in  the  effluent  rose  during  these  situations, but  not  in
proportion to the feed increase.  Thus, one conclusion of  the   report
was  that  granular  media  filters  may  be  used to clarify refinery
wastewaters, including occasional surges.

Another study (99)  showed that filtration  of  refinery  effluent  was
able  to reduce the suspended solids to less than 5 mg/1 for "all  feed
concentrations" (8-91 mg/1 TSS),  further  supporting  the  fact  that
filters  can  reduce  the effluent variability of biological treatment
systems.

One petroleum refining company uses rapid sand filtration to treat its
biological  treatment  plant  influent   (150).   Biological  treatment
systems   presently   remove  some  suspended  as  well  as  dissolved
materials.  However, if filters are used prior to the biological  unit
to remove the suspended material not removed in primary treatment, the
biological  system can afford better removal of the dissolved organics
with less solids generation (50).  Another advantage of pre-filtration
is that it allows the biological system to operate at increased  sludge
ages (greater than 20-40 days).  High sludge ages can  produce   higher
treatment efficiencies, fewer system upsets, and less sludge.

Granular Activated Carbon

Granular  activated carbon has been used in the potable water industry
for many years and has been  used  to  remove  dissolved  organics  in
industrial  and  municipal wastewater treatment plants in recent years
(49).  Activated carbon systems  have  functioned  both  as  polishing
units  following  a  biological  treatment  system  and  as  the major
treatment process in a physical/chemical treatment system.

The granular activated carbon system considered here consists  of  one
or  more  trains  of  carbon  columns, each train having three columns
operated in series. The columns operate by rotating their positions  in
the train, so that the newly regenerated carbon would be in the  third
vessel,  whereas  the  vessel  with the most spent carbon would  be the
first vessel.  One possible piping and equipment  arrangement  showing
this  scheme is presented in Figure VI-1.  Smaller refineries may  only
require  one  or  two  vessels,   operated   manually,   without  the
sophisticated  piping  arrangement shown in Figure VI-1,  This simpler
system serves as the basis for EPA's development of installation costs
of this technology at refineries having low effluent flow rates.

EPA expects that all but the smallest systems  would  require  on-site
regeneration of carbon.  Figure VI-2 is a flow diagram of one possible
carbon  regeneration  system.    Some  instances may require filtration
prior to the carbon units  to  remove  suspended  solids  and  prevent
plugging of the carbon pores.
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One  refinery  (No.  168)  treats all of its wastewater with activated
carbon.  At this refinery, granular activated carbon has been used  as
the  main  treatment process, in that there is no biological treatment
system used for organic and BOD removal  before  the  adsorbers.   The
refinery  has  experienced operating problems with the system (many of
which have been mechanical in nature), and  now  plans  to  install  a
biological  treatment  facility  to  replace  the  carbon system.  The
carbon treatment facilities will be preserved in case they are  needed
to  meet  future  guidelines.   The  poor  performance  record at this
facility  should  not  be  considered  reflective  of  carbon  systems
operating as polishing units to biological treatment systems.

Powdered Activated Carbon

A new technology developed over the past several years consists of the
addition of powdered activated carbon to biological treatment systems.
The  adsorbant quality of carbon, which has been known for many years,
aids in the removal of organic materials in the  biological  treatment
unit   (144).   This  treatment  technique also enhances color removal,
clarification, and system stability, as well as BOD  and  COD  removal
 (115,  116).  Results of pilot testing  (59, 60) indicate that this type
of  treatment, when used as a part of the activated sludge process, is
a viable alternative to granular carbon systems.

One chemical manufacturing complex has installed a full-scale, 40  MGD
powdered  activated carbon system that started up during the spring of
1977  (61). This system, which includes  carbon  regeneration,  is  the
basis  for  the  cost analysis presented in section VII.  A simplified
flow  diagram is presented in Figure VI-3.  The  waste  sludge,  which
contains  powdered carbon, is removed from the activated sludge system
and thickened in a gravity thickener.  The sludge is then dewatered in
a filter press prior to being fed to the  regeneration  furnace.   The
regenerated  carbon  is washed in an acid solution to remove metals as
well as other inorganic materials.  Fresh carbon is added  as  make-up
to  replace  the carbon lost in the overflow from the activated sludge
process or in the regeneration system.

The powdered  activated  carbon  system  described  above  is  a  very
comprehensive  treatment system that includes operations which may not
be required at all installations.  The need for a filter press  system
or  acid  cleaning  system  as  well  as a carbon regeneration furnace
should be determined on a case-by-case basis, in that these  treatment
steps  may  not be required at every refinery.  Low metals content and
good sludge settleability may reduce the need for the filter press  or
acid  cleaning  systems  even  at refineries that would regenerate the
carbon on-site.

Several tests of powdered activated carbon added to petroleum refinery
activated sludge systems have been  reported.   Rizzo  reported  on   a
                               119

-------
plant test of carbon addition to an extended aeration treatment  at the
Sun  Oil  Refinery  in  Corpos  Christi, Texas  (150).  This test tried
three carbon dosages; 24 ppm, 19 ppm, and  9  ppm  were  tried.   Test
results  showed  that even the very small carbon dosages significantly
improved BOD, COD, and TSS removals,  as  well  as  producing  uniform
effluent quality, a clearer effluent, and elimination of foam.

Grieves,  et.  al.,  (153) reported on a pilot plant study at the Amoco
refinery in Texas City where the addition of activated carbon  to  the
activated sludge process was evaluated in 37.9 liter  (10 gallon) pilot
plant  aerators.   Significant  improvements in soluble organic  carbon
(53 percent), soluble  COD  (60  percent),  NH3-N   (98  percent),  and
pehnolics  were  observed  through  the  addition  of  50 mg/1 of high
surface area carbon.  Improvement  increased  with  increasing   carbon
dosage.

Exxon  researchers  tried  adding  activated  carbon  to  bench  scale
activated sludge units with somewhat less success  (154),  Their  tests
evaluated  three  carbon  dosages  which  produced aerator equilibrium
carbon levels of 25 to 2000 mg/1.  At aerator carbon levels  of  25  -
400  mg/1, no improvement was seen in the performance of the activated
sludge process.  However, since  this  represents  carbon  dosages  of
about  1-10 ppm, this result is not surprising, and not inconsistent
with most other studies.  This low dosage  is  usually  an  inadequate
amount of carbon, which gets lost or overwhelmed in the system.

At higher carbon dosages, giving aerator carbon levels of 1000 mg/1 or
more, Exxon got positive results.  In a field test, scale undisclosed,
Thibault,  et.  al., significantly improved effluent quality and noted
improvement in shock loading resistance leading to process  stability.
Increased removals of TOC and COD averaged 10 percent.

Another  powdered  activated  carbon scheme has been studied  (60, 145)
that uses very high sludge ages  (60 days or  more);  this  allows  the
carbon  to accumulate to high concentrations in the mixed-liquor, even
though only small make-up amounts  are  added  to  the  system.   This
approach  may eliminate the costly regeneration scheme described above
due to the low carbon addition rates, allowing  for  the  disposal  of
spent  carbon  with the sludge.  Considerable pilot work has been done
with this concept but no full-scale system is currently operating.

Pilot tests (62) also have shown that powdered activated carbon  can be
used  successfully  with  rotating  biological  contactors  (  RBC'S).
Refinery  No.  32,  has constructed a full-scale system based upon the
results of the  pilot  testing.   EPA  is  investigating  this   system
further.
                                120

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Metals Removal

Metals  such as copper, zinc, lead, arsenic and cadmium, may originate
from many sources within a refinery and may therefore requrie  end-of-
pipe  treatment.   The  development document published in March, 1974,
for  the  copper,  nickel,  chromium   and   zinc   segment   of   the
electroplating  industry   (114)  considered chemical precipitation and
clarification to be the best practicable treatment in that  industrial
category.   The  best  plants  in that industry obtained the following
long-term average effluent concentrations for selected metals:

         Cu             0.2 mg/1
         Ni             0.5 mg/1
         Cr«+           0.055 mg/1
         Cr(T)          0.3 mg/1
         Zn             0.3 mg/1
         CN             0.04 mg/1

The results of the RSKERL and  Burns  and  Roe  supplemental  sampling
programs  (see  section  III) show that BPT technology in the refining
industry achieves metal discharges similar to or lower than the values
shown  above;  therefore,  end-of-pipe  chemcial   precipitation   and
clarification  generally  will  not improve significantly the effluent
metals  concentrations  in  petroleum  refineries  over  existing  BPT
technology.   Further  reductions in the concentration of metals would
require advanced wastewater treatment schemes, such as  ion  exchange,
reverse osmosis, or activated carbon  (147).

With  regard  to chromium removal, since the chemical treatment scheme
described earlier is  applied  as  an  in-plant  measure,  the  actual
discharge concentration of chromium will be lowered by the dilution of
the  cooling  tower blowdown in the final effluent stream.  Therefore,
concentrations of total chromium on the order of  magnitude  of  0.02-
0.05  mg/1 may be achievable with this type of technology.  (0.02-0.05
mg/1 is based upon  a  dilution  to  10-25  percent  of  its  original
concentration  in  the  cooling tower blowdown stream, and a long-term
average concentration in the blowdown streams of 0.2 mg/1 as shown  in
the electroplating industry).

RSKERL Carbon Studies

The  Robert S. Kerr Environmental Research Laboratory (RSKERL) studied
carbon treatment at six refineries as part of their  overall  sampling
program.

The  granular  carbon  tests  used four columns operating in parallel.
Each  column  contained  a  different  type  of  carbon  to  determine
differences in performance.  One column contained previously exhausted
and  then  regenerated  carbon.   The  other  three  columns contained
                                 121

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different types of virgin carbon.   Field  tests  were  undertaken  to
determine  which  of  the  virgin  carbons had the highest TOC removal
capacity, using the isotherm testing method.  The effluents  from  the
"best"  virgin carbon and the "regenerated" carbon were then tested to
evaluate their removal capabilities.   The  inlet  wastewater  to  the
carbon columns was treated using multi-media filtration.

Tables  VI-10  and  VI-11  present the operating data, where available
prior to the preparation of this report, for the filter and two carbon
columns tested at the six refineries.  RSKERL is preparing a  detailed
report on the process operations at each refinery with a more detailed
discussion of the carbon testing program.

RSKERL  also  tested a powdered activated carbon system at four of the
six refineries.  The test unit consisted of a small  activated  sludge
pilot  unit  to  which  powdered  carbon  was  added on a batch basis.
Tables VI-12 and VI-13 present the  operating  data,  where  available
prior  to  the  preparation  of  this  report,  for the pilot powdered
activated carbon system.

It should  be  noted  that  these  pilot  tests  are  only  short-term
feasibility  studies,  due  to  the limited testing period and lack of
repeated carbon exhaustion and regeneration.  These  factors  tend  to
limit the usefulness of the tests as predictors of full-scale systems.
However, this information coupled with that being generated within the
petroleum  refining  industry   (60,62)  is  expected  to  be useful in
determining the potential for applicability  of  granular  carbon  and
powdered activated carbon systems to remove toxic pollutants.

Ultimate Disposal Methods

The  use  of  flow  reduction and recycle methods described above will
reduce the quantity of water  discharged  or  subject  to  end-of-pipe
treatment.  None of the above described techniques willl eliminate the
discharge   of   water.    Zero  discharge  of  water  is  technically
achievable,  however;  55  existing  refineries  have  reported   zero
discharge.   Table  VI-14  presents  information on the capacities and
disposal methods employed by these  55  refineries.   Out  of  the  55
plants,  32  use  evaporation  or  percolation  ponds, 10 use disposal
wells, five use contract disposal, two use  leaching  beds,  one  uses
surface spray, and six reported no wastewater generation at all.

In order to highlight the geographical and process distribution of the
zero discharges, the following breakdown is provided:
                                122

-------
    Distribution by
      EPA Region
                         Distribution by
                         BPT Subcateqorv
Region
Number of
Refineries

      1
      0
      0
      1
      1
     20
      2
     14
     14
      2
Subcategory

      A
      B
      C
      D
      E
Number of
Refineries
                                      Total
                   55

Percolation  and  evaporation ponds cbe an attractive disposal methods
when evaporation losses exceed rainfall.  These  ponds  can  be  sized
according to the annual flow, so that the inflow plus the incidentally
added  water (i.e., rainfall) are equal to percolation and evaporation
losses.  This technique is in operation at many  petroleum  refineries
in the continental United States.

The  petroleum  refinery  industry also practices deep-well injection.
This  method  can  be  recommended  only  with  the  stipulation  that
extensive studies be conducted to insure environmental protection.

Irrigation  or other similar land disposal techniques is a viable end-
of-pipe treatment alternative.  This can eliminate discharge of all or
a portion of process wastewaters to navigable streams.  One  petroleum
refinery (No. 26) already employs this or a similar technology.

The  various  ultimate  disposal  methods  discussed  above are viable
treatment  alternatives.   However,  their   application   is   highly
dependent  on  local  conditions   (i.e.,  rainfall,  availability of a
suitable  deep-well,  availability  of  land,  availability  of   land
suitable  for  irrigation).   Plants  which are not located in an area
with the above described conditions can also achieve  zero  discharge.
Technology  for  ultimate  disposal for these plants is based on force
evaporation.  Heat is used to  evaporate  the  water.   The  steam  is
condensed  and reused as make-up water to the refinery while the brine
(slurry)  stream is transformed into a solid state in  a  flash  dryer.
This  zero  discharge  treatment  scheme is described in detail in the
1977 American Petroleum Institute Reprot  (150).  The cost of this end-
of-pipe treatment scheme is related to the flow.  In costing this zero
discharge technology, the plant is assumed to  implement  the  various
recycle/reuse   scheme   discussed   earlier.    Although  the  forced
                                123

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evaporation system is not used currently in the refining industry,   it
is being used in power plants which have compatible flow rates.

EXISTING TECHNOLOGY

Existing  BPT  guidelines are based upon end-of-pipe treatment systems
consisting of biological treatment, followed by rapid sand  or   multi-
media filtration or an equivalent polishing step, and in-plant control
practices  widely  used  within  the  petroleum refining industry that
include the following:

    1.   Installation of sour water strippers to  reduce  the  sulfide
and ammonia concentrations entering the treatment plant.

    2.   Elimination of once-through  barometric  condenser  water   by
using  surface  condensers  or recycle systems with oily water cooling
towers.

    3.   Segregation of sewers so that  unpolluted  storm  runoff  and
once-through  cooling waters are not treated normally with the process
and other polluted waters.

    4.   Elimination  of  polluted  once-through  cooling  water,    by
monitoring  and  repair of surface condensers or by use of wet and dry
recycle systems.

The National Commission on Water Quality  had  a  contractor's   report
(65)  prepared in 1975 on the petroleum refining industry that included
a  status  of  the treatment technology and water usage of most  of the
refineries in the United States.  The data were obtained for the year
1973, and present a picture of the industry as it appeared at the time
the BPT guidelines were promulgated.

The  1977 EPA Petroleum Refining Industry Survey obtained data for the
calendar  year  1976.   Table  VI-15  presents  a  comparison  of  the
industry's   wastewater   treatment   practices   for  1973   (National
Commission Data) and 1976 (1977 survey).  The following is a  list   of
treatment processes included in Table VT-11:

    Corrugated Plate Separator      (Corr. Plate Sep.)
    Dissolved Air Flotation         (DAF)
    Other Flotation Systems         (OAF)
    Chemical Flocculation           (Chemical Floe,)
    Pre-Filtration
    Stabilization Pond              (Stab. Pond)
    Aerated Lagoon                  (Aerated Lag.)
    Activated Sludge                (Act, Sludge)
    Trickling Filter                (Trick.Filter)
    Rotating Biological Contactor   (RBC)
                               124

-------
    Other Organics Removal          (Other Org. Rem.)
    Filtration
    Polishing Pond                  (Pol. Pond)
    Carbon Adsorption               (Act. Carbon)
    Evaporation or Percolation Pond (Evap. or Perc. Pond)

Table  VI-16  summarizes  the treatment systems listed in Table VI-15,
showing the progress made by the industry  in  installing  end-of-pipe
treatment  technology.   The  treatment units shown in these tables do
not necessarily treat all of a particular refinery1s wastewaters,  and
many  treatment schemes may be pretreatment systems for discharge to a
POTW.

The word "none" where indicated in Table VI-15  refers  to  refineries
that  do  not  have any of the treatment operations considered in this
analysis. However, these plants may treat  their  wastewaters  through
gravity oil separation techniques.

A  definitive  list  of  refineries  that have filtration or activated
carbon operations is  significant.   Those  refineries  that  included
filtration  or  activated carbon in their responses to the 1977 survey
were screened to eliminate those systems  that  are  treating  only  a
minor portion of their wastewater, such as stormwater runoff or boiler
blowdown.   This  approach  has reduced the total number of refineries
listed as having these types of treatment to just those  plants  which
treat   a   significant   portion  of  their  wastewater  through  the
application of this technology.

Table VT-16 shows that there has been a marked increase in the  number
of refineries having BPT-type technology in-place in 1976.  The number
of  pretreatment operations, such as DAF, other flotation systems, and
chemical flocculation shows a  significant  increase,  indicating  the
importance of these unit operations in meeting BPT limitations.

Table  VI-15 also presents data on water usage, including once-through
cooling  water,  during  the  two  one-year  periods  surveyed.    The
comparison used water usage, rather than wastewater production because
data  on  wastewater  production were not available for the year 1973.
For those refineries with data available for both survey years,  there
was  an  overall flow reduction of approximately 16%.  This percentage
would  undoubtedly  be  greater  if  conditions   remained   constant.
However,  many  refineries have expanded their operations or increased
their complexity by adding additional process units between  1973  and
1976;  this  would  minimize  the  effect of water reduction on a unit
basis. Many of the flow reductions appear to result from  a  reduction
in the use of once-through cooling water.

Tables  VI-17  and VI-18 summarize the future modifications planned by
the survey respondents.   Table  VI-17  indicates  planned  wastewater
                                125

-------
reduction techniques along with expected flow reductions.  Table VI-18
presents  a  summary  of  future modifications to wastewater treatment
plants.

Effluent Concentrations

The effluent concentration achievable by BPT treatment technologies is
discussed in the 1974 Development Document.  The sampling results from
the 17 screening plants are in agreement with  the  original  findings
with  exception to phenol.  The concentrations and variability factors
used in the BPT regulations are:

                        Concentration       Variability Factors
                        	mq/1           daily       monthly

Phenol                         .1            3.5           1.7
Chromium  (total)               .25           2.9           1.7
Chromium  (hexavalent)          .02           3.1           1.4
BOD                          15              3.2           1.7
TSS                          10              3.3           2.1
O&G                           5              3.0           1.6

The screening  sampling  results  indicate  an  average  reduction  of
phenols  to  19  ug/1.   Additional  data are being gathered to better
define the variability factors for phenol at the 19 ug/1 level.

The  1974   development   document   concluded   that   the   influent
concentrations   do  not  affect  the  effluent  quality  of  the  BPT
wastewater treatment system.  This conclusion is indirectly  supported
by  the  screening  sampling  results.  The flow rate and the effluent
concentration from each screen sampling refinery were analyzed.

Table VI-19 presents a detailed summary of the discharge data from  16
screening plants; including the percentage of actual discharge flow to
model  flow,  as well as effluent concentrations for BOD, TSS, TOC and
Oil and Grease.  The table also presents analysis of the  correlations
of  these  factors.   These  data  show  that  there is no correlation
between discharge flow and final  effluent  concentrations  after  BPT
treatment.
                                126

-------
                                                                                    FIGURE VI-1

                                                                 Flow Diagram of a Granular Activated  Carbon  System
                                                                                                                                 Backwash  out
to
>J
                                                                                                                                           Effluent
                                                                                                                                              V
                                                        To other carbon  trains
                            Piping Explanation
                               Main Influent header (to 1st tank  In  series)
                               Main effluent header (from 3rd tank  in  series)
                               Influent header to 2nd tank in series
                               Influent header to 3rd'tank in series
                               Effluent header from 1st tank in series
(6)  Effluent from 2nd tank in  series
.7)  Connection between #3 and  #5  headers
 8)  Connection between #4 and  #6  headers
 9)  Backwash inlet header
,10) Backwash outlet header

-------
                                 Make-up carbon
to
00
                                                 Regenerated
                                                   Carbon
                                                   Holding
                                                    Tank
  r~    "i
fir)
  Carbon Adsorption
        Tanks
                                                                                     Furnace


                                                                                   FIGURE  VI-2

                                                                           Carbon Regeneration  Systeir
                                Spent Carbon
                                  Holding
                                   Tank

-------
                            Uastewater  Influent
to
10
                              Powdered
                              Activated
                              Carbon
                              Inlet
                              Carbon Make-up
                              __.	  |   	, fc~
                                                  Activated  Sludge
                                                      Units
                                                                        Treated Effluent
 Sludge
Thickener
                   Filter Presses
 Carbon
Regeneration
 Furnace
                                                                  Acid  Wash
                                                                   System
                                                                                     FIGURE VI-3

                                                                      Flow Diagram  of One PACT Treatment Scheme

-------
                    TABLE VI-1
               SOUR WATER TREATMENT
              IN PETROLEUM REFINERIES

REFINERY    SINGLE STAGE  TWO STAGE
 NUMBER      STRIPPING    STRIPPING    OXIDIZING      OTHER
    3                                      X
    8                                                   X
   10                                                   X
   13            X                         X
   15            X
   16            X
   18            X
   20            X
   24                                      X
   25            X                         X
   29            X                         XX
   30            X
   31                                                   X
   32            X
   33            X                         X
   36                                      X
   37            X
   38            X                         XX
   39            X
   40            X            X            X
   41            X            X            X
   42                                      x
   43            X                         x
   45            X
   46            X                         X
   49            X
   50                         x
   51            X            X
   53                                                   x
   55            X
   56                                      X            X
   57                                                   X
   59            X
   60                         X
   61            X
   62            X
   63            X                                      x
   64            X
   65            X
   67            X
   68            X
   70                                      X
   71            X
   72                                      X
   73            X
   74            X
   76            X
   77            X
   78                                      x
   80            X
   81            X
   83            X            X
                       130

-------
  TABLE VI-1 (Continued)
 SOUR WATER TREATMENT
IN PETROLEUM REFINERIES
REFINERY
NUMBER
84
85
36
< 87
88
94
96
98
102
103
104
105
106
107
108
109
111
112
113
114
115
116
117
121
122
124
125
126
127
129
130
131
132
133
134
139
142
143
144
147
149
150
151
152
153
156
157
158
159
160
161
162
163
165
SINGLE STAGE TWO STAGE
STRIPPING STRIPPING
X
X
X


X
X
X
X





X

X

X
X
X
X
X
X
X
X
X
X
X

X
X
X
X
X

X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
OXIDIZING









X



X





X



X





X



X




















                                        OTHER
               131

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 TABLE vi-1  (Continued)
 SOUR WATER TREATMENT
IN PETROLEUM REFINERIES
REFINERY
NUMBER
166
167
163
169
174
175
176
179
180
132
183
184
185
186
187
188
190
194
195
196
197
200
203
204
205
208
209
210
211
212
213
216
221
222
224
225
226
227
228
230
232
233
234
235
237
238
241
243
245
246
252
255
256
257
SINGLE STAGE TUO STAGE
STRIPPING STRIPPING OXIDIZING
X
X
X
X

X

X
y
X
X
X
X
X
X
X
X
X
X
X X

X
X
X
X
X X
X
X
X
X

X X
X
X
X
X
X
X
X
X
X X
X
X
X

XXX
X
X
X
X
X
X X
X
X
                                         OTHER
            132

-------
               TABLE VI-1  (Continued)
               SOUR UATER TREATMENT
              IN PETROLEUM REFINERIES

REFINERY    SINGLE STAGE  TUO STAGE
 NUMBER      STRIPPING    STRIPPING    OXIDIZING      OTHER
  258            X
  259            X
  261            X
  265            X
  309            X
                  133

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                           TABLE VI-2

                  Effect of California Crudes on
                       Reuse of Sour  Waters
Ref.  No.

13

32

37
38
40
41
State

CA

CA

CA



CA
                       Crude Source
            CA
            CA
L.A. Basin

California

San Joaquin Val, CA

Coalinga, CA

California

California

California

California

California

California

CA Midway Waxy

CA Mid Spec.
Percent
 Crude
Capacity

   17

   49

   39.6

   23.0

   28.1

   20.2

   15.7

    1.2

   20

   10

   35

   10
Percent
Sour Water
to Desalter

   26

   12.5

   17
                                                            Sr 30
                                                              60
                                                              25
                           134

-------
                  TABLE VI-3
             REUSE OF SOUR WATERS
                INDUSTRY STATUS

REFINERY            PERCENT              PERCENT
 NUMBER        REUSE IN DESALTER       OTHER REUSE
    2               100.00                 0.0
   13                26.00                13.00
   20                 0.0                 29.10
   24               100.00                 0.0
   29                 0.0                 30.00
   30                 0.0                UNKNOWN
   32                12.50                18.90
   37                17.00                17.00
   38               UNKNOWN                0.0
   40                60.00                22.00
   41                25.00                27.00
   49               100.00                 0.0
   51                10.00                20.00
   52               UNKNOWN                0.0
   53                 0.0                100.00
   55               100.00                 0.0
   57                 0.0                 28.50
   59                90.00                10.00
   60                48.00                15.00
   61                51.00                10.00
   62                70.00                 0.0
   65                55.60                25.40
   67               100.00                 0.0
   68                74.00                26.00
   71               100.00                 0.0
   72                 0.0                 59.00
   73                 0.0                100.00
   76               100.00                 0.0
   80                 0.0                100.00
   81                87.00                 0.0
   83               100.00                 0.0
   85                59.00                 0.0
   86               100.00                 0.0
   94               100.00                 0.0
   98                88.00                12.00
  104                10.00                 0.0
  111               UNKNOWN                0.0
  114                60.00                 0.0
  115                85.30                 0.0
  116                60.00                 0.0
  121                 0.0                  9.00
  122                58.00                 0.0
  126                 0.0                 30.00
  130                30.00                 0.0
  131                62.00                28.00
  132                 0.0                  6.00
  142               100.00                 0.0
  143               100.00                 0.0
  144               100.00                 0.0
  145                 0.0                100.00
  147               100.00                 0.0
  149               100.00                 0.0
  150               100.00                 0.0
  151                95.00                 0.0
                    135

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             TABLE VI-3  (Continued)
             REUSE OF SOUR WATERS
                INDUSTRY STATUS

REFINERY            PERCENT              PERCENT
 NUMBER        REUSE IN DESALTER       OTHER REUSE
  153                20.00                80.00
  155                35.00                 0,0
  156                50.00                50.00
  157                 0.0                  8.20
  159                50.00                 0.0
  160               100.00                 0.0
  161                90.00                10.00
  163               100.00                 0.0
  165               100.00                 0.0
  169                87.00                 0.0
  179               100.00                 0.0
  132                 0.0                 15.00
  1S3               100.00                 0.0
  134                66.00                 0.0
  186                80,00                 0.0
  187               100.00                 0.0
  138                73.00                27.00
  194                80,00                 0.0
  196                40.00                 0.0
  200               100.00                 0.0
  203                40.00                 0.0
  204               100.00                 0.0
  205               100.00                 0.0
  209               100.00                 0.0
  211               100.00                 0.0
  216                18.00                 0.0
  224               100.00                 0,0
  225               100.00                 0.0
  227                75.00                25.00
  228               100.00                 0.0
  230               100.00                 0.0
  232                60.00                40.00
  233                50.00                 0.0
  234               UNKNOWN                0.0
  241                35.00                 0.0
  243                99.99                 0.0
  252                80.00                 0.0
  256               100.00                 0.0
  257               100.00                 0.0
  258               100.00                 0.0
  259               100.00                 0.0
  265               100.00                 0.0
  305                20.00                80.00
                      136

-------
           TABLE SECTION VI-4

 COOLING TOWER MAKE-UP FLOW RATES
IN THE PETROLEUM REFINING INDUSTRY
REFINERY
NUMBER
1
2
3
4
6
7
8
9
10
11
12
13
13
15
16
17
18
19
20
21
22
23
24
25
26
29
30
31
32
33
35
36
37
38
39
40
41
42
43
44
45
46
48
49
50
51
52
53
54
55
56
57
58
59
MAKE-UP FLOW

0.059600
0.114800
0.0
NOT APP.
NOT APP.
0.107000
0.010000
0.025000
0.020000
2.909999
0.500000
7.303997
7.303997
0.084500
0.382100
0.018500
0.108000
0.013000
1.450000
0.298000
0.094500
NOT APP.
0.350000
0.867000
0.297000
3.419997
0.193000
> 0.0
4.969995
0.650000
NOT APP.
0.036000
6.808996
3.290996
0.165000
6.614997
6.621992
0.030000
3.769996
0.0
> 4.348996
1.462999
0.140500
0.650000
> 0.235000
NOT APP.
NOT APP.
0.050000
0.030000
NOT APP.
1.600000
9.699997
1.514149
1.825500
MAKE-UP FLOW
DIVIDED BY TOTAL
EFFLUENT FLOW
0.313684
2.125925
0.0
NOT APP.
NOT APP.
0.648485
2.000000
0.694444
0.400000
1.939999
0.723589
1.446336
1.446336
0.554099
1.179320
0.557229
0.473684
3.037382
0.759162
4.382351
1.049999
NOT APP.
1.166666
1.791321
1.993288
0.914438
0.814277
> 0.0
0.842372
1.633164
NOT APP.
1.090908
2.885168
1.073734
1.092714
0.848076
0.705969
0.874126
1.314045
0.0
> 1.363321
1.116793
0.231848
UNKNOWN
> 1.525973
NOT APP.
NOT APP.
0.200000
1.764706
NOT APP.
1.225115
0.941747
1.058845
1.659544
PERCENT COOLING
BY BTU BY
COOLING TOWERS
94.0000
100.0000
100.0000
0.0
0.0
70.1000
30.0000
UNKNOWN
UNKNOWN
94.0000
UNKNOWN
95.0000
31.5000
100.0000
72.0000
40.0000
UNKNOWN
100.0000
30.0000
UNKNOWN
73.0000
0.0
15.0000
58.0000
79.0000
75.0000
100.0000
UNKNOWN
76.8000
100.0000
0.0
98.5000
43.0000
80.0000
UNKNOWN
90.0000
4.5000
UNKNOWN
62.9000
95.0000
53.6000
50.0000
95.0000
65.0000
80.0000
0.0
0.0
98.0000
100.0000
0.0
81.0000
89.0000
99.0000
47.8000
            137

-------
     TABLE VI-4  (Continued)
 COOLING TOWER MAKE-UP FLOW RATES
IN THE PETROLEUM REFINING INDUSTRY
REFINERY
NUMBER
60
61
62
63
64
65
66
67
68
70
71
72
73
74
76
77
78
79
80
31
82
83
84
85
86
87
88
89
90
91
92
93
94
95
96
97
98
99
100
102
103
104
105
106
107
108
109
110
111
112
113
114
115
116
MAKE-UP FLOU
( MGD )
3.052498
4.599999
5.659997
1.355000
4.308998
2.484499
0.000050
8.829994
8.348999
0.0
0.359000
0.021000
0.468000
0.471500
1.933998
0.630000
0.075500
0.0
2.129998
0.776500
0.216000
2.929999
2.204995
5.394799
0.440950
NOT APP.
0.735000
0.0
0.017000
0.005000
> 6.552999
0.0
1.728000
0.0
19.014984
0.014040
4.289999
NOT APP.
NOT APF.
0.0
> 0.025000
8.384995
NOT APP.
2.250000
0.045000
0.126000
0.200000
NOT APP.
2.842497
0.302500
0.529500
0.320000
1.983199
0.864000
MAKE-UP FLOU
DIVIDED BY TOTAL
EFFLUENT FLOU
1.568117
1.742423
1.179166
0.496337
0.897708
0.690139
UNKNOWN
0.416706
1.717900
0.0
1.486542
0. 138158
0.605433
2.357499
0.348245
2.282607
0.111029
UNKNOWN
9.260860
0.641735
0.375000
1.197873
1 .304730
1,639756
1 .274422
NOT APP.
3.223682
0,0
0.377773
0.416667
> 0.587186
0.0
0.941176
0.0
1 .605995
UNKNOWN
1.656370
NOT APP.
NOT APP.
0.0
> 0.396825
1.128531
NOT APP.
1 .069391
1 .499999
2.863636
0.833333
NOT APP.
1,799048
1 .490147
0.957505
1.280000
0.708285
0.720000
PERCENT COOLING
BY BTU BY
COOLING TOWERS
60.0000
47.0000
74.0000
91.4100
66.0000
40.0000
100.0000
65.6000
74.4000
UNKNOWN
100.0000
10.0000
75.0000
95,0000
86.5000
59,0000
90.0000
UNKNOWN
85.4000
100.0000
100.0000
60.0000
75.0000
80.0000
97.0000
0.0
89,2000
28.0000
60.0000
UNKNOWN
56.0000
UNKNOWN
86.5000
100.0000
100.0000
UNKNOWN
39.4000
0.0
0.0
0.9000
UNKNOWN
71.0000
0.0
30.0000
100.0000
99.0000
7.6000
0.0
46.0000
35.0000
49.4000
78.0000
58.8000
40.0000
     138

-------
      TABLE VI-4  (Continued)
 COOLIN3 TOUER MAKE-UP FLOW RATES
IN THE PETROLEUM REFINING INDUSTRY
REFINERY
NUMBER
117
113
119
120
121
122
124
125
126
127
128
129
130
131
132
133
134
135
136
137
138
139
140
141
142
143
144
145
146
147
148
149
150
151
152
153
154
155
156
157
158
159
160
161
162
163
164
165
166
167
168
169
172
173
MAKE-UP FLOW
(MGD)
1.450000
0.036500
0.100500
0.175000
4.250000
3.323500
0.975999
0.766000
0.400000
0.090000
NOT APR.
0.066600
NOT APP.
0.330000
1.599999
5.160996
0.0
> 0 . 0
0.378000
0.0
0.466000
> 0.071000
0.222000
0.0
0.502500
0.030000
0.759500
0.004500
0.300000
1.695000
> 0.126500
0.740000
NOT APP.
4.150000
3.070000
5.792998
0.063000
0.391700
1.697997
4.119996
0.570800
0.199500
0.328000
2.114997
2.115499
2.732998
0.030000
0.595400
0.050000
3.864999
1.240000
6.794998
0.772000
0.0
MAKE-UP FLOW
DIVIDED BY TOTAL
EFFLUENT FLOW
1.435642
1.013887
0.670000
1.590908
0.944444
0.519297
2.054735
1.725224
0.061728
0.520231
NOT APP.
0.665999
NOT APP.
0.114583
0.156648
0.650819
0.0
UNKNOWN
1.321678
0.0
0.647222
> 5.071427
2.018181
0.0
0.317235
0.025000
1.161314
UNKNOWN
3.225806
2.942707
> 0 . 790625
0.627650
NOT APP.
1.044288
0.366348
1.489202
0.063000
2.266782
1.697997
2.049748
1 .041605
0.720216
1.874285
3.253841
0.863469
2.635486
1.363636
2.053102
0.454545
0.757843
0.430555
0.783737
0.839130
0.0
PERCENT COOLING
BY BTU BY
COOLING TOWERS
99.0000
30.0000
28.0000
30.0000
65.0000
97.0000
100.0000
60.0000
22.0000
99.0000
0.0
UNKNOWN
0.0
20.0000
10.0000
85 . 0000
62.0000
UNKNOWN
100.0000
100.0000
1.0000
99.9000
70.0000
100.0000
66.5000
2.0000
100.0000
100.0000
UNKNOWN
89.0000
100.0000
77.0000
0.0
61.7000
35.0000
63.0000
UNKNOWN
100.0000
60.0000
88.9000
71.5000
60.0000
100.0000
90.0000
UNKNOWN
88.0000
100.0000
49.8000
67.0000
70.0000
200.0000
90.0000
91.3000
UNKNOWN
            139

-------
     TABLE VI-4 (Continued)
 COOLING TOWER MAKE-UP FLOW RATES
IN THE  PETROLEUM REFINING INDUSTRY
REFINERY
NUMBER
174
175
1.76
177
17O
224
225
226
~) T"7
228
229
230
231
MAKE-UP FLOW
(MOD)
NOT APP.
10.787498
0.086000
0.028000
0.632700
1 .870998
20.876480
6.599497
2. 169648
4.675997
1.771500
2.574697
3.244994
. 4.653500
0.0
0.085000
2.545500
: 0.028000
0.0
11 .303490
0,0
16.445465
0.002000
0.017200
1 .694998
2. 156999
0.009500
10.209991
5.268191
2.818796
12.500000
0.180000
2.844998
0.413500
0. 137000
0.679049
1,763000
0.038880
0.0
0.0
16.502472
7.300000
1 ,939999
0.022000
0,0
0.860000
0,0
1 .679999
0.0
1 .483199
0.364500
0.113500
1.150000
NOT APP,
MAKE-UP FLOW
DIVIDED BY TOTAL
EFFLUENT FLOW
NOT APP.
0.364521
0.184986
0,036601
2.243616
0.676183
1.301526
1.031171
3.390075
3.438233
2.116487
1 .418566
4.203360
1.911087
0.0
2,560240
5.606828
0.198582
0.0
0.664911
0.0
0.888944
0,250000
UNKNOWN
2,769604
2.270524
95,000000
0.789026
1 .560205
1 ..'.56192
134.408600
2.535211
0.570140
1 .759574
3.512819
0.834726
2.507822
0.762353
0.0
0.0
0.808945
UNKNOWN
1.616665
0.916667
0,0
2.457141
0.0
1 .411764
0.0
1 . 167872
1 .752403
5.456731
1 .642857
NOT APP.
PERCENT COOLING
BY BTU BY
COOLING TOWERS
0.0
UNKNOWN
33.0000
75.0000
32.0000
98.7500
49.0000
70.0000
59.7000
75,0000
95.0000
71 .0000
60.0000
30.0000
UNKNOWN
70.0000
100.0000
100.0000
UNKNOWN
79,0000
UNKNOWN
91 .3000
100.0000
UNKNOWN
70.0000
69.0000
100.0000
65.0000
75.0000
90.6000
100.0000
90.0000
47,5000
40.0000
79.9000
UNKNOWN
65.0000
35.0000
UNKNOWN
UNKNOWN
78,0000
100.0000
63.0000
100.0000
99,5000
100.0000
UNKNOWN
97.9000
29.8000
80.0000
100.0000
100.0000
88.0000
0.0
             140

-------
                    TABLE VI-4  (Continued)
               COOLING TOWER MAKE-UP FLOW RATES
              IN  THE  PETROLEUM REFINING INDUSTRY
REFINERY
NUMBER
232
233
234
235
236
237
238
239
240
241
242
243
244
245
246
247
248
249
250
251
252
253
254
255
256
257
258
259
260
261
264
265
266
278
291
292
295
296
298
302
303
305
307
303
309
MAKE-UP FLOW
(MOD)
0.0
2.450000
0.0
2.149999
0.016000
0.016000
1.999999
0.055000
0.180000
0.324000
0.450000
0.524000
0.612000
0.707000
0.1B2500
0.558BOO
0.0
0.380000
0.0
NOT APP.
0.009000
0.0
0.0
0.0
0.040000
NOT APP.
0.792000
NOT APP.
NOT APP.
0.640000
0.0
1.296000
NOT APP.
0.0
0.506000
NOT APP.
0.610600
NOT APP.
> 0 . 0
NOT APP.
0.0
') 0.040000
> 0.0
> 0.0
> 0.720000
MAKE-UP FLOW
DIVIDED BY TOTAL
EFFLUENT FLOW
0.0
2.450000
0.0
1.433332
0.133333
0.571428
1.044931
0.436508
0.300000
0.490909
0.703125
3.119045
0.334426
1.178332
0.323009
2.696910
0.0
0.456731
UNKNOWN
NOT APP.
0.064748
0.0
UNKNOWN
0.0
0.109589
NOT APP.
0.792000
NOT APP.
NOT APP.
1.361701
0.0
1.169674
NOT APP.
UNKNOWN
3.563379
NOT APP.
2.361176
NOT APP.
> 0.0
NOT APP.
UNKNOWN
::• 0.363931
UNKNOWN
UNKNOWN
> 0.743801
PERCENT COOLING
BY BTU BY
COOLING TOWERS
2.5000
45.0000
UNKNOWN
83.0000
UNKNOWN
90.0000
84.5000
47.0000
UNKNOWN
100.0000
95.0000
69.0000
99.0000
99.6000
UNKNOWN
100.0000
100.0000
50.0000
UNKNOWN
0.0
90.0000
UNKNOWN
UNKNOWN
UNKNOWN
100.0000
0.0
40.0000
0.0
0.0
90.0000
UNKNOWN
UNKNOWN
0.0
UNKNOWN
90.0000
0.0
90.0000
0.0
100.0000
0.0
UNKNOWN
100.0000
UNKNOWN
UNKNOWN
100.0000
•>   DUE TO UNKNOWN MAKE-UP  FLOWS  FOR SOME COOLING TOWERS.
    THE NUMBER IS GREATER THAN  SHOWN
NOT APP. - NOT APPLICABLE BECAUSE OF 0.0 7. COOLING BY COOLING TOWERS

-------
                                TABLE VI-5

                         PROFILE OP PLANTS AT OR BELOW
                   48 PERCENT OF MODEL FLOW (LEVEL 2 PLANTS)
                                                 Crude           Fraction
Refinery        Region           BPT            Capacity           of
  No.             No.          Subcategory        (MBD)           Model Flow
  176              3              B               52.              .483
   98              6              B              202.3            .480
   62              5              D              295.0            .480
  144              8              B               49.9            .478
   33              9              A               44.0            .477
  185              6              B               75.0            .477
   53              4              A               14.0            .476
   15              9              B               32.0            .473
   86              4              B               25.0            .472
  113              5              B               42.0            .471
   37              9              E              103.0            .470
   60              5              B              195.0            .468
  305              6              A               13.              .467
  106              6              B              154.9            .464
    9              6              A                3.5            .458
  207              6              A               46.              .455
   23              9              A               16.              .452
  259              2              C              655.0            .451
  161              6              B               51.              .449
  119              4              A               11.              .444
   14              9              B               12.4            .439
   16              9              A               48.0            .438
  114              5              B               24.0            .432
  206              6              A               36.5            .431
   77              7              B               23.2            .430
    6             10              A               22.0            .427
  124              8              B               42.0            .404
    2              4              A               20.0            .399
   26              9              B               17.              .393
  158              6              B               54.6            .388
  233             10              B              100.              .372
  210              6              B               18.1            .361
  264              5              A               23.              .358
  298              1              A               15.              .349
  195              6              A               1.0             .332
  187              6              C              56.0             .332
   18              9              A              10.               .329
   90              6              A               2.2             .329
  125              8              B              56.               .322
  160              6              B              23.5             .312
   55              9              A              60.3             .311
    1              4              A              30.0             .310
  213              6              A              21.6             .301
  209              6              B              35.0             .299
   74              7              B              22.5             .297
  155              6              B              14.5             .295
  148              5              A              20.0             .285
                                      142

-------
                           TABLE  VI-5  (Continued)

                                               Crude           Fraction
                               BPT            Capacity           of
                            Subcategorv        (MBD)          Model Flow
"7              6              A               4.5             .283
147              5              B              65.0             .283
108              3              A              13.5             .279
 22              9              A              11.              .270
260              4              A               3.              .267
140              6              B              19.0             .253
 50              8              B              21.5             .251
202              6              A               3.5             .250
118              4              A               6.0             .248
179              6              B              26.              .244
243              5              B              42.0             .232
  8              9              A               5.0             .227
103              6              A              36.              .226
 25              9              B              53.8             .222
310              8              A               3.0             .217
191              6              B              53.5             .207
 36              9              A              17.0             .203
  3              4              A               1.2             .192
 54              4              A               3.              .179
 10              6              D               6.0             .174
237             10              A               5.0             .165
165              6              B              60.              .153
 17              9              A               9.5             .151
220              6              A              10.0             .149
 49              8              B              33.5             .141
 80              7              B              52.0             .139
 99              6              B              28.7             .136
107              3              A              17.              .096
 97              6              B              50.0             .085
254              8              A               1.              .083
229              8              B               5.6             .075
 19              9              A               2.5             .055
193              6              A               3.2             .050
218              6              A               6.0             .029
 31              9              A              12.              .029
141              6              A               4.0             .022
  4             10              A              13.0             .011
302              6              A               2.2             .010
248              8              A               1.              .003
135              6              A               2.5             .000
250              8              A               1.              .000
251              8              A               0.5             .000
278              4              A               3.              .000
296              6              A              10.0             .000
303              6              A               1.              .000
307             10              A               0.8             .000
308              8              A               0.1             .000
                                143

-------
                                 TABLE  VI-6


                   GEOGRAPHICAL BREAKDOWN OF LEVEL 2 PLANTS


                             PERCENT OF PLANTS
                            DISCHARGING LESS THAN               PERCENT OF
                               48 PERCENT OF                    PLANTS IN
EPA REGION                      MODEL FLOWS	             TOTAL INDUSTRY

    1                                II

    2                                14

    3                                36

    4                               11                               6

    5                                9                              13

    6                               37                              34

    7                                35

    S                               13                              12

    9                               17                              14

   10                                55
                             144

-------
                                TABLE VI-7
                SUMMARY OF CRUDE CAPACITIES FOR LEVEL 2 PLANTS
                           PERCENT OF PLANTS
                         DISCHARGING LESS THAN
                             48 PERCENT OF
                              MODEL FLOW
                          PERCENT OF  PLANTS
                                 IN
                           TOTAL INDUSTRY
  0-25

 25 - 100

100   200

    > 200
63

31

 3

 3
47

34

12

 7
                                145

-------
                                 TABLE VI-8
                  BPT" SUBCATEGORY BREAKDOWN OF LEVEL 2 PLANTS
                           PERCENT OF PLANTS
                          DISCHARGING LESS THAN            PERCENT OF PLANTS
                             48 PERCENT OF                         OF
SUBCATEGORY                  MODEL FLOWS                    TOTAL INDUSTRY
    A                             57                               38

    B                             38                               40

    C                             2                                9

    D                             2                                8

    E                             1                                4

    U                             0                                1
                               146

-------
             TABLE VI-9

Refineries that Utilize, or Plan to
    Utilize Filtration Systems
        Presently Installed

        12              134
        23              153
        44              168
        50              181
        53              187
        60              199
        92              201
        100             211
        107             219
        115             225
        118             227
        119             232
        120             255
        133
       Future Installations

         11             105
         32             122
         42             132
         44             152
         57             168
         67             204
         70             212
         102            232
                 147

-------
                                                                         TABLE VI-10
                                                                    ANALYTICAL  RESULTS

                                                                             FOR
                                              RSKERL GRANULAR ACTIVATED  CARBON  STUDY,  TRADITIONAL POLLUTANTS
                     Sample   - Day

                     Refinery B
                                            BOD-1
                                                       BOD- 3
                                                                 COD
                                                                          Concentration (mg/1)


                                                                         TOC     TSS     NH
                                                                                                  Cr
00
                     Refinery H
                       Filter influent
                                       -6
                                       -12
                                       -15
                       Filter effluent - 6
                                       -9
                                       -32
                                       -15
L6
L12
L12
L12
L6
L12
1,12
L12
                       Virgin carbon
                       effluent
                                        -6    L3
                                        -9    L6
                                        -12   L12
                                        -15     4
                                                                                                                   O&G
                                                                                                                           PH
Filter



Filter



Virgin
influent



effluent



carbon
effluent






-6
-9
-12
-15
-6
-9
-12
-15

-6
-9
-12
-15
L15
L30
10
L30
L15
L30
15
L30

L6
L12
L12
L12
L15
L30
L30
L30
L15
L30
L30
L30





120
110
110
100
99
120
100
84

16
31
13
16
53
43
37
40
45
45
37
33

17
11
9
10
22
36
32
26
12
34
28
10

4
4
6
4
22
15
16
12
22
15
16
11

44
16
16
12
L.
L.

L.
L.
.
L.
L.

L.
L.
L.
L.
02
02
02
02
02
02
02
02

02
02
02
02
.1
.5
.4
L.I
.1
.4
.3
.1

.1
.2
.1
.1
6
4
7
14
14
6
7
7

7
9
5
7
7.3
7.7
7.6
7.4
7.4
7.6
7.9
7.4

7.4
7.5
7.6
7.3
Reg. carbon
effluent






-6
-9
-12
-15
L6
L12
L12
L12




16
31
24
28
18
12
11
15
4
4
5
4
22
16
16
12
L.
L.
L.
L.
02
02
02
02
.2
.2
L.I
.1
17
4
6
5
7.3
7.5
7.4
7.3
24
35
40
39
20
31
32
33
12
12
12
15
40
13
21
15
36
14
18
8
10
6
10
8
5
4
5
15
4
1
3
7
2
2
4
7
5.
4.
3.
17
5.
4.
3.
2.
5.
3.
4.
2.
6
5
9

6
5
9
2
6
4
5
8
L.
L.
L.
L.

L.
L.
L.
L.
L.
L.

02
02
02
02
02
02
02
02
02
02
02
02
.1
.2
.2
.2
.1
.2
.1
.2
.2
.2
.2
.2
5
11
19
5
5
5
10
13
8
8
6
10
7
7
7
7
7
7
7
7
7
7
8
7
.5
.4
.5
.2
.4
.4
.7
.3
. 3
.5
.2
.4

-------
vo
Sample - Day
Refinery H - Cont'd
Reg. carbon effluent -6
-9
-12
-15
Refinery K
Filter influent -6
-9
-12
Filter effluent -6
-9
-12
Virgin carbon effl.-6
-9
-12
Reg. carbon effluent -6
-9
-12
Refinery M
Filter influent -6
-9
-12
Filter effluent -6
-9
-12
Virgin carbon effl.-6
-9
-12
Reg. carbon effluent-6
-9
-12
BOD-1

L3
L6
L12
L6

L30
L30
L6
L12
L12
L12
L6
L6
L6
L6
L6
120

L12
LI 2
L12
L6
L3
L6
L6
L3
L3
L6
L6
L6
                                                  BOD-3
                                                            COD
                                                             11
                                                             11
                                                             10
                                                             11
                                                            170
                                                             96
                                                            140
                                                             60
                                                             56
                                                             52
                                                              1
                                                             13
                                                             12
                                                             15
                                                             16
                                                             15
                                                             96
                                                             75
                                                            150
                                                             56
                                                             67
                                                             42
                                                             11
                                                             10

                                                             14
                                                              8
                                                             13
                                                                    TABLE VI-10 (Continued)


                                                                   Concentration  (mg/1)


                                                                    TOC
                                                                             TSS
                                                                                     NH
                                                                                             Cr
t-6

10
3
13
14
58
32
40
25
18
23
7
6
11
9
8
12
17
19
19
15
22
15
5
7

4
10
5

2
1
6
7
66
33
52
7
1
4
2
LI
2
2
1
LI
10
11
7
6
2
1
2
LI
LI
2
1
1
3
5.6
3.9
4.5
3.4
6.2
11
10
5.6
11
9.0
5.6
11
9.0
5.6
11
9.5
Ll.O
Ll.O
Ll.O
Ll.O
Ll.O
Ll.O
Ll.O
Ll.O

Ll.O
Ll.O
Ll.O

L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
L.02
       ,-2
                                                                                                               O&G
                42
                21
                42
                 5
                 a
                 6
                 6
                 9
                 5
                LI
                 8
                 7
                17
                14
                 5
                 9
                17
                10
                 9
                13
                 6
                10
                11
                 3
                        7.3
                        7.4
                        7.6
                        7.4
7.1
7.4
7.5
7.1
7.4
7.3
7.3
7.2
7.3
7.1
7.2
7.5
7.7
7.6
                                                                                                                        7.3

-------
                         Sample   -  Day
U1
O
                                               BOD-1
Refinery
Filter



Filter



Virgin


0
influent -6
-9
-12
-15
effluent -6
-9
-12
-15
carbon effl.-6
-9
-12
-15
Reg. carbon effluent -6
-9


Refinery
Filter


Filter


Virgin

-12
-15
P
influent -6
-9
-12
effluent -6
-9
-12
carbon ef f 1 . -6
-9
-12
Reg. carbon effl.-6
-9

-12
12
10
10
10
30
10
L15
L30
9
8
A
6
11
8
3
7
8
8
27
5
8
30
4
4
24
4
2
14
 BOD-3
 13
 10
  6
  8
 30
 L5
L15
L30
  8
  5
  3
 L6
 10
  5
  3
 L6
                                                                     TABLE Vl-10  (Continued)


                                                                     Concentration (mg/1)
                                                                                                      + 6
                                                                   COD      TOC      TSS
130
120
130
120
120
120
120
120
 61
 73
 80
                                                                    77
                                                                    88
                                                                    88
20
55
41
38
41
53
39
44
36
25
23
34

28
29
34
42
28
34
22
18
30
20
 6
16
52
24
 8
24
24
24
 6
                                                                                            NH
1.4
2.5
3.4
1.7
1. 4
2.5
2.2
2.8
 LI
2.5
3.4
2.5

2.5
2.8
12
                                                                                                    Cr
                                                                                                              -2
                                                                                                                      O&G      pH
18
 6
30
18
11
 7
13
12
25
12
16
 8
25
 6
16
7.9
8.2
8.2
8.4
7.9
8.2
8.6
8.0
8.0
8.2
8.3
7.7
7.8
8.2
8.5
8
8
27
5
8
30
4
4
24
4
2
14
4
4
23
4
9
23
4
L5
23
5
L5
6
85
100
120
110
160
110
69
81
56
28
81
68
22
54
37
20
70
44
16
52
25
14
70
19
23
16
11
11
21
11
13
7
4
11
7
4
5.9
7.0
10
5.3
7.0
13
5.3
7.0
9.5
5. 3
6.4
11
L.
L.
L.
L.
L.
L.
L.
L.
L.
L.
L.
L.
02
02
02
02
02
02
02
02
02
02
02
02
L.
L.
.
L.
L.

L.
L.
L.
L.
L.
L.
1
1
3
1
1
4
1
1
1
1
1
1
36
5
40
20
4
26
14
5
20
20
4
16
7
7
7
7
7
6
7
7
7
7
7
7
.2
.4
.3
.1
.3
.8
.3
.3
.1
.3
.4
.2

-------
                                      TABLE  VI-11

                               ANALYTICAL RESULTS  FOR RSKERL
                   GRANULAR ACTIVATED CARBON STUDY,  PRIORITY  POLLUTANTS
                                                  Concentration  (mg/1)
Sample - Day

Refinery B
  Filter influent   6
  Filter influent   9
  Filter influent   15
  Filter influent   Comp.
  Filter effluent   6
  Filter effluent   9
  Filter effluent - 15
  Filter effluent - Comp.
  Virgin carbon effluent   6
  Virgin carbon effluent   9
  Virgin carbon effluent - 15
  Virgin carbon effluent   Comp.
  Reg. carbon effluent   6
  Reg. carbon effluent   9
  Reg. carbon effluent - 15
  Reg. carbon effluent   Comp.

Refinery H
  Filter influent   6
  Filter influent   9
  Filter influent   15
  Filter influent   Comp.
  Filter effluent - 6
  Filter effluent - 9
  Filter effluent   15
  Filter effluent - Comp.
  Virgin carbon effluent   6
  virgin carbon effluent   9
  Virgin carbon effluent - 15
  virgin carbon effluent - Comp.
  Reg. carbon effluent - 6
  Reg. carbon effluent   9
  Reg. carbon effluent - 15
  Reg. carbon effluent   Comp.
L.02
 .01
 .12

 .02
 .01
 .12

L.02
 .01
 .01

L.02
 .01
 .04
L.02
L.02
L.02

L.02
L.02
L.02

L.02
L.02
L.02

L.02
L.02
L.02
                                                       Phenolics
 .024
 .024
 .012

 .022
L.01
L.01
 .017
 .019
 .014
L.0005
                    L.0005
                    L.0005
                                           L.0005
                    L.0005
                    L.0005
                    L.0005
                                           L.0005
 a Samples were not analyzed because filter influent contained lower limits  of
   detection.
                                   151

-------
                                  TABLE  VI-11  (Continued)
                                                  Concentration  (mg/1)
Sample - Day

Refinery K
  Filter influent
  Filter influent
  Filter influent
  Filter influent
  Filter influent - Comp.
  Filter effluent
  Filter effluent
  Filter effluent
  Filter effluent
  Filter effluent
  Virgin carbon effluent
  Virgin carbon effluent
  Virgin carbon effluent
  Virgin carbon effluent
  Virgin carbon effluent
  Reg.  carbon effluent
  Reg.  carbon effluent
  Reg.  carbon effluent
  Reg.  carbon effluent
  Reg.  carbon effluent

Refinery M
  Filter influent
  Filter influent
  Filter influent
  Filter influent
  Filter influent
  Filter effluent
  Filter effluent
  Filter effluent
  Filter effluent
  Filter effluent
  Virgin carbon effluent
  Virgin carbon effluent
  Virgin carbon effluent
  Virgin carbon effluent
  Virgin carbon effluent
  Reg.  carbon effluent
  Reg.  carbon effluent
  Reg.  carbon effluent
  Reg.  carbon effluent
  Reg.  carbon effluent
c
6
9
12
15
Comp.
6
9
12
15
Comp.
.uent 6
_uent 9
.uent 12
.uent 15
.uent Comp .
;nt 6
:nt 9
•nt 12
!nt 15
;nt Comp .
6
9
12
15
Comp.
6
9
12
15
Comp.
.uent 6
.uent 9
.uent 12
.uent 15
.uent Comp .
•nt 6
•.nt 9
int 12
:nt 15
:nt Comp.
:yanides
L.02
L.02
L.02
L.02
L.02

L.02


L.02

L.02


L.02

L.02
L.02
L.02
.10

.04
L.02
L.02
.09

L.02


.03

L.02


.02

Phenolics
.027
.018
.018
.031
.029
.017
.018
.029

L.012
L.012
L.012
L.01

L.012
L.012
L.012
L.01

L.012

L.012
L.010

L.012




L.012




L.012




Mercury
.0008
L.0005




.0013




.0016




.0008




L.0005




L.0005




L.0005
                                       152

-------
                                    TABLE VI-11  (Continued)
                                                  Concentration  (mg/1)
Sample - Day

Refinery O
  Filter influent - 6
  Filter influent - 9
  Filter influent - 12
  Filter influent - 15
  Filter influent - Comp.
  Filter effluent - 6
  Filter effluent - 9
  Filter effluent   12
  Filter effluent - 15
  Filter effluent - Comp.
  Virgin carbon effluent   o
  Virgin carbon effluent - 9
  Virgin carbon effluent - 12
  Virgin carbon effluent - 15
  Virgin carbon effluent - Comp.
  Reg. carbon effluent   6
  Reg. carbon effluent - 9
  Reg. carbon effluent - 12
  Reg. carbon effluent ~ 15
  Reg. carbon effluent - Comp.

Refinery f
  Filter influent   6
  Filter influent   9
  Filter influent - 12
  Filter influent   15
  Filter influent - Comp.
  Filter effluent - 6
  Filter effluent   9
  Filter effluent   12
  Filter effluent - 15
  Filter effluent   Comp.
  Virgin carbon effluent - 6
  virgin carbon effluent   9
  Virgin carbon effluent   12
  Virgin carbon effluent - 15
  Virgin carbon effluent   Comp.
  Reg. carbon effluent   6
       carbon effluent - 9
       carbon effluent   12
       carbon effluent   15
Reg.
Reg.
Reg.
Reg.
Cyanides
L.02
L.02
L.02
L.02

L.02
L.02
L.02
L.02

L.02
L.02
L.02
L.02

L.02
L.02
L.02
L.02

.05
.04
.04
.05

.05
.04
.04
.04

.05
.05
.05
.07

.04
.04
.05
.07
Phenolics
.038
.029
.025
.022

.039
.028
.023
.040

.005
L.005
L.005
L.005

L.005
L.005
.005
.007

.013
.028
.058
.090

.013
.016
.084
.092

L.005
L.005
L.005
.005

L.005
L.005
L.005
L.005
Mercury




L.0005




L.0005




L.0005




L.0005




L.0005




L.0005




L.0005




       carbon effluent - Comp.
                                                                             L.0005
                               153

-------

Sar^lc
Refinery B*
Filter l-.fLut-:it


Virgin CArbon etfluer.t

Reg. carix-:i cft'luont

Refinery H'
Filter ir.flue-.t

Vilttr e: fluent

Virgin carbon effluent

Reg. carbon effluent

Refinery K*


Virgin carbon effluent

Reg. carbon effluent

Refinery «•
Filter influent

Filter effluent

Virgin carbon effluent

Reg. carLon effluent

Refinery 0*
Filter influent

Filter effluent

Virgin carbo.-i effluer.t

Reg. carbon effluent

Refinery P*
Filter ii.fluc.it

Filter effluent

Virgin carbon effluent

Reg. carbon effluent


L..L
1
2
j
2
1
2
1
2

I
2
1
2
1
2
1
2

1
1
2
1
2
1
2

1
2
1
2
1
2
1
2

1
2
1
2
1
2
1
2

1
2
1
2
1
2
1
2

*~
LI
1.5
LI
LS
LI
1.5
LI
L5

LI
L5
U
IS
LI
L5
LI
LS

L5
LS
LI
LS
LI
LS

5
LS
5
LS
10
LS
7
L5

LI
L5
LI
L5
LI
LS
LI
LS

LI
L5
LI
LS
LI
LS
LI
LS

&
;
13
L3
2
L3
2
L3

U
L)
LI
L3
LI
L3
LI
L3

L3
L3
LI
13
LI
L3

LI
L3
LI
L3
LI
L3
LI
L3

LI
L3
LI
L3
LI
L3
LI
L3

LI
L3
LI
L3
LI
L3
LI
L3

fii.
5
LI
LI
L2
LI
1.2
LI

10
LI
L2
LI
L2
LI
L2
LI

LI
LI
L2
LI
L2
LI

7
LI
L2
LI
L2
LI
L2
LI

L2
LI
L2
LI
L2
1
L2
6

L2
1
L2
1
L2
4
L2
1

Cr
50
40
21
30
10
30
5

1C
L5
9
LS
L5
1.5
10
Lr'

196
23
10
10
20
10

100
24
60
17
50
8
60
10

30
110
20
100
L5
70
60
eo

LS
60
LS
50
LS
46
L5
40

Cu
I 6
I.S
LS
Ib
LS
9
1.5

10
32
10
14
L6
LS
7
L5

26
L5
L6
L5
L6
LS

20
LS
10
L5
10
L5
10
LS

L6
13
L6
9
L6
16
L6
14

L6
13
L6
11
L6
20
L6
20
r. ii. ,-m !„'
M
IS
L1S
L*
L1S
LS
1.15
LS
L15

L5
L15
L5
H5
L5
LI 5
1,5
L15

L15
L15
L5
L15
1.5
L15

e
us
9
LI 5
50
L1S
30
L15

LS
Lt5
LS
L15
L5
L15
LS
L15

L5
16
L5
16
LS
42
L5
L15
:-.,•!, lii "'I
— . -f ^ — —
rs.
L20
L1S
L15
L20
Lli
L20
L15

20
L1S
L~0
2C
L20
L15
L20
L15

L1S
115
L20
L1S
L20
L15

60
115
30
L15
70
LI 5
50
L15

L20
L1S
L20
L15
L20
L15
L20
LI 5

L20
L1S
L20
LI 5
L20
L15
L20
L15

?1-
too
rs
70
60
LbO
35
LGO
25

L60
15
Lf,0
20
L60
20
LfcO
20

210
85
1*0
30
L60
35

100
85
300
110
100
100
100
100

L60
L10
L60
L10
L60
17
L60
12

L60
17
L60
30
L60
27
LCO
30

ILl

L20
L20

L20

L20


L20

L20

L20

L20

L20
L20

L20

L20


L20

L20

L20

L20


L20

L20

L20

L20


L20

L20

L20

L20

£h

L25
1.25

L2S

L25


L25

L?5

L20

L25

1.25
L25

L2S

L25


L25

L25

L25

L25


L25

L25

L2S

L25


470

430

450

410
	 . 	
£«

62
56

50

SO


L20

L20

L20

L20

L20
L20

L20

L20


25

26

26

23


L20

L20

L20

L20


L20

L20

L20

L20
	
Tl

LI 5
L15

L15

L1S


L15

L15

111,

L15

LI 5
L15

US

L1S


LI 5

L1S

1,15

L1S


LI 5

L15

L15

US


L15

L15

L15

L15
        1  - EPA F.?cion V
KOTES:   L  - Less than
        •  - Ihc ?1-hoMr cor;)-?- itcs voru corrjxDsitcd Into one  sarnie for
                                                                   154

-------
                                                                        TABLE VI-12
                                                                   ANALYTICAL RESULTS
                                                                           FOR
                                               RSKERL POWDERED ACTIVATED  CARBON STUDY,  TRADITIONAL POLLUTANTS
Ul
Ul
Concentration (mg/1)

Sample -
Ref inery
Pilot



Pilot



Refinery
Pilot


Pilot


Refinery
Pilot


Pilot



Day
B
plant



plant



K
plant


plant


M
plant


plant





inf luent-6
-9
-12
-15
eff luent-6
-9
-12
-15

inf luent-6
-9
-12
eff luent-6
-9
-12

influent-6
-9
-12
ef fluent-6
-9
-12

BOD-1

170
110
110
160
L6
L12
L12
L12

110
80
L60
L6
L12
L12

95
63
16
8
13
L12

BOD- 3

160
110
110
220
L6
L12
LI 2
L12















COD

480
350
400
450
63
100
120
130

1400
480
840
76
36
48

280
360
260
84
95
140

TOC

160
58
98
120
28
20
32
39

450
110
200
29
12
19

78
87
66
17
21
32

TSS

22
28
36
56
30
42
58
94

860
150
280
30
6
14

22
32
24
58
35
62

NH,

7.8
3.9
6.7
3.9
20
15
22
16

6.2
5.6
10
2.2
3.4
2.0

19
20
16
10
15
11
+6
Cr

.09
.05
L.02
.06
L.02
L.02
L.02
L.02

.11
.02
.02
L.02
L.02
L.02

L.02
L.02
L.02
L.02
L.02
L.02
-2
S

.7
3.1
2.6
1.8
.8
2.7
.7
.8

2.7
1.8
2.5
.7
.6
.7

5.7
1.0
1.3
.7
.5
.7

O&G

24
38
23
16
6
5
14
12

240
470
98
10
11
13

19

36
28
12
9
Refinery P
Pilot


Pilot


plant


plant


influent-6
-9
-12
eff luent-6
-9
-12
180
130
200
14
5
10
160
110
170
6
6
16
340
460

140
190
150
90
160

28
45
56
68
78
40
140
58
50
8.1
10

3.6
4.2
13
L.02
L.02
L.02
.02
L.02
L.02
5.5
7.6
11
2.3
1.7
1.0
25
80
81
20
11
26
                                                                                                           S	    O&G     pH
                                                                                                                           8.9
                                                                                                                           9.3
                                                                                                                           8.4
                                                                                                                           9.2
                                                                                                                           8.2
                                                                                                                           7.8
                                                                                                                           7.8
                                                                                                                           7.8
                                                                                                                          7.3
                                                                                                                          7.1
                                                                                                                          7.4
                                                                                                                          7.7
                                                                                                                          7.5
                                                                                                                          7.5
                                                                                                                          8.7
                                                                                                                          8.3
                                                                                                                          8.8
                                                                                                                          5.6
                                                                                                                          5.8
                                                                                                                          5.8
                                                                                                                          8.2
                                                                                                                          8.2
                                                                                                                          8.3
                                                                                                                          7.0
                                                                                                                          7.7
                                                                                                                          7.6

-------
       TABLE VI-13
ANALYTICAL RESULTS FOR RSKERL
POWDERED ACTIVATED CARBON STUDY, PRIORITY POLLUTANTS

Sample - Day
Refinery B
Pilot plant influent
Pilot plant influent
Pilot plant influent
Pilot plant influent
Pilot plant effluent
Pilot plant effluent
Pilot plant effluent
Pilot plant effluent
Refinery K
Pilot plant influent
Pilot plant influent
Pilot plant influent
Pilot plant influent
Pilot plant influent
Pilot plant effluent
Pilot plant effluent
Pilot plant effluent
Pilot plant effluent
Pilot plant effluent
Refinery M
Pilot plant influent
Pilot plant influent
Pilot plant influent
Pilot plant influent
Pilot plant influent
Pilot plant effluent
Pilot plant effluent
Pilot plant effluent
Pilot plant effluent
Pilot plant effluent
Refinery P
Pilot plant influent
Pilot plant influent
Pilot plant influent
Pilot plant influent
Pilot plant influent
Pilot plant effluent
Pilot plant effluent
Pilot plant effluent
Pilot plant effluent
Pilot plant effluent



- 6
9
- 15
Comp .
- 6
- 9
- 15
Comp.

- 6
9
- 12
15
- Comp.
- 6
9
- 12
15
Comp.

- 6
9
12
15
Comp.
6
9
12
- 15
- Comp .

- 6
- 9
12
15
- Comp.
- 6
9
12
15
Comp.

Cyanides

.05
.06
.07

L.02
L.03
L.02


.01

L.02
.02

L.02


L.02


.01

.02
.28

L.02


.07


.05
.06
.05
.01

.02
L.02
L.02
.02

Concentration (mg/1)
Phenolics

24
18
31

L.010
L.010
L.010


.23
3.8
.95
.53

L.012
L.012
L.012
.014


6.0
6.4
6.2
5.2.

L.012
L.012
.018
L.010


39
42
80
58

.065
.039
.099
.027


Mercury




L.0005



L.0005





L.0005




.0006





L.0005




L.0005





L.0005




L.0005
   155

-------
                                                                              TABLE VI-13 (Continued)
tn
-vj
               Sample

               Refinery B*
                 Pilot plant influent

                 Pilot plant effluent
Refinery K*
  Pilot plant influent

  Pilot plant effluent
               Refinery M*
                 Pilot plant influent

                 Pilot plant effluent
               Refinery E>
                 Pilot plant influent

                 Pilot plant effluent
                                          Lab
*a
LI
L5
LI
LS
LI
L5
LI
LS
2
LS
LI
LS
LI
LS
Ll
LS
Be
Ll
L3
Ll
L3
2
L3
Ll
L3
2
L3
2
L3
Ll
L3
Ll
L3
Cd
L2
Ll
L2
Ll
L2
3
L2
Ll
L2
Ll
20
Ll
L2
7
L2
6
Cr
100
81
30
IB
2000
1700
70
49
500
393
60
33
700
620
70
110
Cu
L6
LS
L6
LS
400
370
20
a
20
17
9
LS
L6
14
L6
52
Hi
LS
L15
L5
15
20
27
L5
L15
10
L15
LS
L15
LS
16
LS
39
	 1 "
Pb
L20
L1S
L20
L15
100
65
L20
L15
L20
L15
60
L15
L20
L15
L20
L15
Zn
L60
30
L60
30
10000
1800
100
120
300
250
100
170
100
110
70
85
As

L20

L20

L20

L20

L20

L20

L20

L20
Sb

L25

L25

L25

L2S

L25

L25

430

410
Se_

L20

40

L20

L20

23

1.20

L20

L20
Tl

L15

L15

L15

L15

L15

L15

L15

L15
               LABS:
                       1 - EPA Region V
                       2 - RSKERL
               NOTES:
                       L - Leas than
                       * - The 24-hour composites were composited into one  sample for analysis.

-------
Refinery

C&H Refinery, Inc.
  Lusk, WY
                            TABLE VI-14
                                             *
                    Zero Discharge Refineries
      Capacity
(1000  bbl/stream  day)

          .05
Southwestern Refining Co., Inc.      .5
  LaBarge, WY

United Independent Oil Co.           .75
  Tacoma, WA

Yetter Oil Co.                      1.
  Colmer, IL

Dorchester Gas Producing Co.        1.
  Amarillo, TX

Mountaineer Refining Co., Inc.      1.
  LaBarge, WY

Glenrock  Refinery, Inc.             1.
  Glenrock, WY

Thriftway, Inc.                     1.
  Graham, TX

Sage Creek Refining Co.             1.
  Cowley, WY

Pioneer Refining, Ltd.              2.2
  Nixon,  TX

Oxnard Refinery                     2.5
  Oxnard, CA

Caribou Four Corners, Inc.          2.5
  Kirtland, NM

Kenco Refinery, Inc.                3.
  Wolf Point, MT

Kentucky Oil and Refining Co.       3.0
  Betsy Layne, Ky
Wastewater
Disposition

Evap/perc pone
                          No  wastewater
                          generated

                          No  wastewater
                          generated

                          Evap/perc  pond


                          Evap/perc  pond


                          Evap/perc  pond


                          Evap/perc  pond


                          No  wastewater
                          generated

                          No  wastewater
                          generated

                          Evap/perc  pond


                          Disposal well
                          No  wastewater
                          generated

                          Evap/perc  pond
                          do wastewater
                          generated
   This table includes all refineries whose production wastewater
   (excluding stormwater, ballast water, once-thru non-contact  cooling
   water, and sanitary wastewater) is not discharged directly via an
   UPDES permit nor is discharged to a  POTW.  This table  also includes
   those refineries which do not generate production wastewater.
                                  158

-------
                        TABLE VI-14  (Continued)
Refinery

Sabre Refining, Inc.
  Bakersfield, CA

Mid-Tex Refinery
  Hearne, TX

Bayou State Oil Corp.
  Shreveport, LA

Thriftway Co.
  Farmington, NM
      Capacity
(1000  bbl/stream day)

         3.5


         3.5


         4.


         4.
Southern Onion Refining Co.,        4.5
  Monument Refinery, Hobbs, NM

Arizona Fuels Corp.                 5.
  Fredonia, AZ

Tonkawa Refining Co.                5.
  Arnett, OK

Plateau, Inc.                       5.6
  Roosevelt, UT

Texas Asphalt and Refining Co.      6.0
  Euless, TX
Sunland Refining Corp.              7.
  Bakersfield, CA

Plateau, Inc.                       7.5
  Farmington, NM

Douglas Oil Co. of CA               9.5
  Santa Maria, CA

Gary Western Co.                   10.
  Fruita, CO

E-Z Serve, Inc.                    10.
  Scott City, KS

Husky Oil Co.                      10.8
  Cody, WY
Wastewater
Disposition

Contract
disposal

Recycle (7/1/77)
Disposal well,
Evap/perc pond

Evap/perc pond


Disposal well


Leaching bed
Disposal well

Evap/perc pond


Evap/perc pond


Evap/perc pond
Contract disposal

Evap/perc pond


Evap/perc pond


Disposal well
                          Evap/perc pond
                          Recycle

                          Evap/perc pond
                          Evap/perc pond
                          (7/1/77)
                                159

-------
                        TABLE VI-14 (Continued)
Refinery

Witco Chemical Corp.
  Oildale, CA

Newhall Refining Co., Inc.
  Newhall, CA

Atlantic Richfield Co.
  Prudhoe Bay, AK

Atlantic Terminal Corp.
  Newington, NH

Kern County Refinery, Inc.
  Bakersfield, CA

San Joaquin Refining Co.
  Bakersfield, CA

Texaco Inc.
  El Paso, TX

Shell Oil Co.
  Gallup, NM

Texaco, Inc.
  Amarillo, TX

Texaco, Inc.
  Casper, WY

Mohawk Petroleum Corp., Inc
  Bakersfield, CA

CRA, Inc.
  Phillipsburg, KS

Husky Oil Co.
  Cheyenne, WY
Southern Union Refining Co.
  Lovington Refinery, Hobbs, NM

Little America Refining Co.
  Evansville, WY

Chevron U.S.A. Inc.
  Bakersfield, CA
      Capacity
(1000  bbl/stream day)
11.
12.
13.
15.
17.
17.
17.
19.
20.
21.
22.
23.
24.
25.
i, NM
25.
26.










8
2
2
1

5

Wastewater
Disposition

Contract
disposal

Contract
disposal

Evaporation


Leaching bed


Surface spray
                          Evap/perc pond,
                          recycle

                          Evap/perc pond,
                          recycle

                          Evap/perc pond
                          Disposal well,
                          Evap/perc pond

                          Evap/perc pond,
                          recycle

                          Evap/perc pond


                          Evap/perc pond


                          Evap/perc pond


                          Disposal well


                          Evap/perc pond
                          Contract disposal,
                          recycle
                             160

-------
                        TABLE VI-14 (Continued)
Refinery

Navajo Refining Co.
  Artesia, NM

Champlin Petroleum Co.
  Wilmington, CA

Shell Oil Co.
  Odessa, TX

Lion Oil Co.
  Bakersfield, CA

Amoco Oil Co.
  Casper, WY

Sinclair Oil Corp.
  Sinclair, WY

Diamond Shamrock Corp.
  Sunray, TX

Cosden Oil and Chemical Co.
  Big Spring, TX
      Capacity
(1000  bbl/stream day)

        29.9
        32.
        35.
        40.
        44.5
        50.9
        53.5
        56.
Hawaiian Independent Refininery    60.3
  Ewa Beach, HI

Chevron U.S.A. Inc.                75.
  El Paso, TX
Wastewater
Disposition

Evap/perc pond


Disposal well


Evap/perc pond


Disposal well,
Evap/perc pond

Evap/perc pond,
recycle

Evap/perc pond


Disposal well
                          Evap/perc pond,
                          recycle

                          Disposal well,
                          Evap/perc pond

                          Evap/perc pond
                               161

-------
                    TA3LE  VI-15
Treatn*ent Oporf ttonfl and Waiter JJaaqe^ig?! and 1976
let.
NO.
001
002
Water unacio
Treatment Oprrntionn pillion n.il/nnv
1973
DAP
Act. Sludge

003 '
OD4 |
1
OCu* » Stab. Pond
s
0»
D09
010
Oil
012
013
014
DAF
Stab. Pond
AorateJ Lag.
Aerated Lag.
Stab. Pond
Stab. ronJ
Stab. Pond
DAF
DAF
X976
Corr. Plnte Sep.
DAF
Act. Sludge
Chemical Floe.
RBC
None

DAP
Aerated Lag.
DAF
Aerated Lag.

Aerated Lag.
roi. r»iij
Stab. Pond

Pro-Filtration
Stab. Pond
Chemical rloc.
DAP

1973
0.61
0.291



0.144
0.200

0.26
0.44
2.92
0.23
12.35
0.062
1976
1.07
0.186
0.125


0.144
0.243
10.0
0.09
0.14
3.52
0.72
10.96
O.H5
	 ~ NO.
-207 015
36 016
017
018

0.0 019
-22 020
021
022
69
023
6fl
024
-21
025
"213
026
11
027
-150
Treatment Operations Million Cal^'j.-v
1973
DAF
Filtration
None

None

None
DAP
Act. Sludgo
None


DAP
Aerated La?.
DAP
Nona

1976
Chemical Floe.
OAF
Hone
Chomical Ploc.
Evap. or Perc. Pond
Kono

Hunt*
Chemical Floe.
DAF
Act. Sludge
None
OAf
Filtration
Evap. or Pere. Pond
DAP
Aerated Lag.
Other Org. Rem.
DAF
Other Org. Rem.
Other Org. Rem.

1073






4.79



o.«



illi.
0.270
0.56
J.OC
0.60


4.51
0.22
0.11
.475
0.54
1.4
0.35

                                                                                                                     -54

-------
  TABLf V1-1S  (Continued)
«nd iM'.or Vmn'tu 3971 and 10T6
Kft.
Sis.
ozs
o;s
030
Treatment
1073

None
Hone
i
03 1 1 None
1
032
o:-3
034
035
036
037
033
039
040
DAF
.V*r.iteJ Lau.
Stab. Pond



Evap. or Tore. Pond
DAF
Act. Sludge
Corr. Plate Sep.
DAF
Evap. or Pere. Pond
Nonn
Onerationa
1976

OAF
Evap. or Pere. Pond
DAP
DAF
AC rote J Lag.
Stab. Pond


None
Evap. or Pare, pond
DAF
Aerated Lag.
id. i™.i
Corr Plate Sep.
DAF

Chi-mlr.il Floe.
DAP
Act. Sludge
Pthflrn On|t nnm.
Water Unnon
Million Gal/nav
1073




18.80
0.71



7.6
7.73

57. 0
1-170

>.5
}.33
).10
16.2


t.O
).12
r.6
i.34
1.35
11.2
X Bed. CSlk
IJOj.
041
042
043
044
14 04S
046
047
P48
049
0.0 050
18 051
052
20 053
Treatmen
022.
Aerated Lag.
Aeratad Lag.
Evap. or Pore. Pond
None

DAP
DAF

Stab. Pond
Evap. or Perc. Pond
Aerated Lag.
Aerated Lag.
Act. Sludge
Bvap. or Pere. Pond
None
t Oncrationa
lilt
Corr. Plate Sop.
Atratod Laq.
Stub. Pond
i-ol. -rorA
Chemical Ploc.
Aorat«d Lag.
Evjp, or Perc. Pond
DAF
Stab. Pond
Filtration
Evap. or Perc. Pond
Chemical Ploc.
DAP
OAF
Chemical Floe.
DAF

Evap. or Perc. Pond
Aoratod Lag..
hoi. fonii
DAP
Aerated Lag.
Stab. Pond
Filtration
Chemical Floe.
DAF
Act. Sludgo
Pol. lonl
Stab. Pond
f-ul. 1-uiil
f 1 1 l-.rnHnn
Watlr 'te»ii*
pillion Ral/o.iv
JV7J.




29.71
55.60

1.27
1.S1
0.40


1.25
r>T.
126.2
'J.l'J
4.96
2.72
/B.9
<4.

i
0.85
0.77
0.47
321.
j
1*
,.-,
0.11
^L




2.7
21

33
SO
-18


O'lf

-------
                                                                                                           TABU, VMS (Continued)
                                                                                     Treatment Ongrationa  »rd niter Uiaqn 1973 and J1978


Ret.
No,
054



055



056




057




OSS



059


060




061




062



053

OoJ


C65


066

Treatmen
1973
DAF



Nona



Aerated Lag.




Aerated Lag.




Kone



DAP
Aerated Lag.

PAP
Aerated Lag.
A..-I. Shul.jo
Filtration

DAF
Act. Sludge



Trick. Filter
£vap. or pore. Pond


Aerated Lag.
Stab. Pond

DAF
Act. Sludge

Act. Sludge




t Onerations
1976




Corr. Plate Sep.
Stab, pond
Pol. Fond
Evtvp. or Perc. Pond
DAF
Aerated Lag.
Pol. louil
Evnp. or Pore. Pond

Ac-rated Lag.
Pol. Pond



DAF



DAi'
Act. Sluilca

Chemical Floe.
DAP
Act.. Sludge
Filtration

Chemical Ploc.
DAF
Act. Sludge
I'ol. PonJ

Trick. Filter
Aerated Lag.
Pol. Pond

Aerated Lag.
!'ol. 1'oiU

DAF
Act. Sludge

Act. Sludge
Pol. Pond

Evap. or Perc. Pond
Water
Million
1973
0.08








4.24












51.27


4.84




12.09




13.4



7.97

27.89


4.06



Usaqe
ca 1/Dav
1976
.09



.18



.82




7.63




.73



.4


.2









.57



.79

4.8


.0


.001

% Had. _ ,
NoT*"
-13
067



068


-37
070




071




072


Questionable 073
Data

-7.4 074



075




076
29


077
-10
078
11

079
-23

080



1973

DAP
Aerated Lag.


Act. Sludge








DAF
Stab. Pond



Aerated Lag.
Stab. Pond

Aerated Lag.
Stab. Pond

Aerated Lag.



None




Stab. Pond



Evap. or Perc. Pond

Nona


Nona


Stab. Pond



1976

Chemical Floe.
DAF
Aerated Lag.

Act. Sludge



None




Chemical Ploc.
DAP
Aerated Lag.
Pol. fond

fi.-Tl-.-M KI.OC.
Aerated La.?.
Pol. Pond
Chemical Floe.
Aerated Lag.
lol. Iwl
Aerated Lag.
Pol. pijn-l







Chemienl Floe.
Aerated Lag.
I'ol. 1'cmd

Act. Sludge
lol. J-wid
Evuii, ur I'urc. 1-wA
Chemical Floe.





Stab. Pond

Million cal/Dav
1973
13.4.9
8.52

0.68
1.43
1.01
0.63
1.27
3.60
0.63

0.16
1.33
1976
U4.3
6.72
0.17
0.59

1.79
0.67

3.0
0.63
0.51

3.46
                                                                                                                                                                                                 13
                                                                                                                                                                                                 -e.j
                                                                                                                                                                                                 0.0
                                                                                                                                                                                                  -160

-------
            TABLE VMS (Continued)
tiMint Qparatlena t\id M«»«r Uaami 1073 nirt 107ft
Water 'Jaaie
Kef.

081



032

OE3



084




085



086


087

088

089

090

091

092



o-n

Treatment
1223

Chemical Floe.
Aerated Lag.
Stab, pond

None

OAF



AurAted Lag.
Stab. Pond



Nona



DAF


Nona

OAF

Evap. or Perc. Pond



None

DAP
Othor Org. Rem.




Onorntione
1976

Aerated Lag.
Pol. Fond


trap, or Peru. Pond

DAF



OAF
Act. Sludge
Pol. Fond


Chemical Floe.
CAP
Act. Sludge

Chemical ploe.
OAF

Evap. or Pvro. Pond

Stab. Pond

Evap. or Pere. Pond

Aerated Lag.

'.'one

. PAP
Act. Sludge
Aerated Lie.
Pol. fond
NOIIO

Water inam
Million Onl/»nv
1973

2.50





4.63



3.54




11.0



0.35


0.42



0.31



0.032

321.5





1976

1.58





4.86



3.84




10.43



0.47


1.0

1.16

0.19

0.031

0.012

278.8





Kef.
X Bed. BOjL
094
37


095

096
-S.O


097
-a. s


098

5.2


099
-34

100
-138
101

102
39
103

104
63

13
105



106
Treatnon
i2Zl
Act. Sludge
Aerated Lag.


None

Corr. Plate Sep.
Auratod Lag.






Aerated Lag.







Filtration

Aerated Lag.

Aerated Lag.



Aerated Lag.



Aorated Lag.



Stab. Pond
Operation* Million nul/9av
1976
Corr. Plate Sep.
DAF
Act. Sludge
Pol. Fund
Stab. Pond
hoi. l-ond
Corr Plate Sep.
Chumical ploc.
DAP
Act. Sludge
None



OAF
DAP
Aorated Lag.
Stab Fund

DAF
Aerated Lag.
Poi. J-o,,d
Filtration



Aetated Log.

Aerated Lag.

Corr. Plate Sep.
Aerated Lag.
Stab. Pond

Chemical Floe.
OAF
Ai-rntml Mitj.

Auriitcd l.uf).
1973
4.59



0.60

90.52







31.27











17. »



24.88



71.0



5.7t
1S76
1.6





34.64



D.034



26.56




121.


0.19



91.1

0.27

21.34



14.



1.59
JL
22





62







15











-!•



14



-18



:o

-------
               TABLE  VI-15 (Continued)
Trpati»jnt-Qporat:loni_ j
Water Usage . wntlir '"""i"
Pet, T^.»t^»n r,n.,.^<™. ...TTr: — __.,..- .. . Hot. Treatm^n ; Operations Million onl/niv •< P«d.
KOj.
107




108

109


1973
None




DAF

OAF
Act. Sludge
Trick. Filter
j

110

111

112
Stab. Pond



Filtration
i

H 113
(Ti
CTi

1U
115


116
117


118



119




120




Aerated Lag.



Aoratcd Lag.
Act. Sludge


Aerated Lag.
PAF
Aerated Lag.
Stab. Pond
None



Filtration




None



1976
Filtration




OAF

Chemical Floe.
DAF
Act. Sludge
Trick. Filter
Pol, Pond


Chemical Floe.
DAF
Aerated Lag.


Aerated Lag.
Pol. Poni


Aerated Lag.
Pre-Filtratlon
Act. Sludge
Pol. roiul
Stab. Pond
OAF
Aerated Lag.
lol. Foul
Aerated Lag.
Filtration


Aerated Lag.
Filtration



Aoratcd Lag.
ri H mil on


1973
0 .39




0.31

83.25




1.22



0.75


1.14



0.72
5.05


2.06
2.01


0.13



1.17




1.35



1976
D.39




D.34

6.22




.0

.8

.51


.90



.59
3.92


2.77
2.10


0.94



D.23




1.29



fj n.uuj^ u
0.0 121




-9.7 I22

20 I24




18 "5



32 126


21 127



IB 128
22 129


-34 "0
-4.5
131

-623
132


-35
133



17
IJ'I


1973
Corr. Piste Sop.
DAF
Aerated Lag.
Stab. Pond

Aerated Lag.

None




Aerated Lag.
Stab. Pond


Aorated Lag.
Stab. Pond

DAF
Aorated Lag.
Stnb. Pond


Evap. or Perc. Pond


None

Stab. Pond


Act. Sludge
Aerated Lag.


Stab. Pond




Mini). Point


i22£.
Corr. Plate Sep.
DAF
Aerated Lag.
Other Org. Hem
Pol. lonl
Aerated Lag.

Chotiical Floe.
DAK
Stab. Pond


Aerated Lag.
Othor Org. Rem.
Pol. I-ool

J.crat"d Lag.
lol. :-oml

Chemical Floe.
DAF
A"r.1tc.-) Lag.
J'ol. r-o.-l'l
Evop. or I'orc Pond
Aerntcd L-ig.
EvGp. or Pore, pond
i-'ol. ior.i
None

OAF
noc

OAF
Activated Sludge


DAF
Act. Sludge
Trick. Filter
Filtration

Ac4« 6loidl£€
Filtration

127JL
34,5




12.03






1.J3



33.0


0.31







3.13

74.01


174.5



35.28




II. 1.4


l-ni,
4.0




5.

.87




.28



0.8


.25



.01
.15


2.67

>d.f>


iSl.S



19.3




..'Jl



59




Cueat ionable
Data





-4.1



-24


1-,







15

24


-4.0



45




-i.O



-------
IAIII i  Vi V*
                                       .''.to
r*_f-_f j_
i»
136
'.57
j
139
139
140
i«l
142
143
144
145
146
147
Tr'>.-ilmfnt. rmr-r.-ttirjnti Million Cal/lj.iv
1073


Nona
(tone
Stab. Pond


DAP
DAP
Aerated Lag.

Stab. Pond
DAP
1076

Corr. Plate Sep.
None
Evap. or Pere. Pond
Evap. or Perc. Pond
Evap. or Perc. Pond
Evap. or Pore. Pond
Chemical Ploc.
DAP
Chemical Floe.
DAP
Aerated Lag.
l-ol. l'or/1
None
Stab. Pond
Chemical Floe.
DAP
Act. Sludge
1221







18.35
28.85
45.02

).32
1.40
JJiii

.6
.06
.03
.ice
.5
).03
21.67
13.7
L.77
1.014
1.3
.94
•**»* %£
148
149
150
151
152
153
154
-18 I55
-17 I56
Questionable l57
Data
158
6.3 «»
-39 "0
Troutmcn
1973
DAP
Aerated Lag.
Aoratod Lag.
DAP
Aerated Lag.
DAP
Aerated Lag.
Act. Sludge
Trick. Filter
Aerated Lag.
Stab. Pond
Aerated Lag.
Stab. Pond
Aerated Lag.
Other Organic* Rem.
Act. Sludge
Stab. Pond
None
DAP
Act. Sludge
Filtration
oiior.ii... — Million 1.1 !/:>.r/
1076
DAP
Corr. Plate Sep.
Aerated Lag.
Corr. Plate Sep.
Act. Slud.je
Chemical Ploc.
DAP
Aerated Lag.
rol. Fond
DAP
Act. Sludge
Other Organic* Rem.
Filtration
Stab. Pond
Pol. Pond
Stab. Pond
rol. roini
Chemical Ploc.
DAP
Aerated Lag.
Pol. 1'ond
Act. Sludge
Aoratod Lag.
Other Organic* Rem.
Act. Sludge
Pol. Foul
Stab, pond
Pol. Pond
Checlcal Ploc.
OAF
Act. Sludge
Stab. Pond
ro). I'on.l
KvKI'i OP roil;, Inn.l
1073

1.78
04.44
6.50
122.1
5.43
0.31
0.59
2.47
7.65
1.40
0.75
0.53
1-J/o
1.47
1.92
.0.14
7.59
14. OS
4.7
3.05
0.65
2.37
7.33
1.49
0.69
0.65
_*-£

-176
,9
-17
"4
13
-174
-10
4.0
4.2
-6.4
8.0
-23

-------
                                                                                                             TABLE VI-15  (Continued)
                                                                                                Treatment Qporjittptia and  Ualer UsJere 1973 and 1976
;c/
l'^76
0',. «
.86
.15

.<>3
.91
7.5

4.53

..nr.
1.4
».1J
!.3S

% f.

14
-79
49

0.0
11
-3.0

12

-IJ.O

-18


-------
1AHLI VI-1S (Continued)
M..
168
169
150
191
192
193
194
133
196
197
193
199
200

i-vn
None
None
DAP
Aerated Lag.
DAF

None
Aerated Lag.
Stab, pond
None
DAP
Act. Sludge
Stab. Pond
None
Hone
i^vo
Corr. Plate Sep.
Aerated Lag.
lol. lw«l
Aerated Lag.
Pel. Fond

Bvap. or Pere. pond
None
Aerated Lag.
I'ol. Fond
None
Corr. Plated Sep.
Chemical ploc.
DAF
Act. Sludge
Stab. Pcnd
Aerated Lag.
I'ol. fond
Pre-Piltratlon
Aoratod Lag.
Filtration
None
Wnl.n.r.
Ml II It. »'
1-J73
6.22
0.05
0.40


0.039
44.25

130.0

2.00

Mnn'jn
lll.l/ll.iy
1976
i.23
D.03
0.12
2.89
0.035
0.059
32.7
0 1 0011
16.36
>.012
>.OS
1.43
— *. fr
16 201
4U 202
70 203
204
205
-36 206
26 207
208
64 209
210
211
212
29 213
1-roatmen
1973
DAP
Aerated Lag.

DAF
Act. Sludge
Act. Sludge
DAP
Aerated Lag.
Stab. Pond
Evap. or Pere. pond
None
Trick. Filter
Act. Sludge
Stab. Pond
Evap. or Pere. Pond
DAP
Aerated Lag.
DAP
Act. Sludge
DAP
t Onerfttlona
1976
chemical Floe.
DAP
Act. Sludge
Filtration

Chemical Floe.
DAP
Chemical Floe.
DAF
Act. 'Sludge
Pol. Pond
DAF
Aerated Lag.
Pol. Pond

Nona
Corr. Plate Sep.
Act. Sludge
Trick. Filter
Stab, pond
DAF
Stab. Pond
Pol. Ford
Evap. or Pero. Pond
Nona
Chemical Floe.
DAF
Act. sludge
Aerated Lag.
Filtration
DAF
Act. Sludtje
OAF
Aornt.nl Lag.
Stab. l-ond
Pol, '.liitl
WnLur t.*>:aue
Million c:il'n.w
i2Z3.
2.02

52.4

12.66
0.05

15.25

1.25
3.57

£976
!.9
).004
29.14
3.07
9.05
9.14

3.2
9.76
1.98
J.14
r. Bod.
-44

44

29
-180

-52

-58


-------
TABLE VI-15 (Continued)
Ij.-f .

J!4
215
= «
218

2»
22)
m
222
223
224
225
226
Treatmon
1973
Evnp. or Perc. pond
Evap. or Perc. Pond
Act. Sludge
Aerated Lag.
Evap. or Perc. Pond

Aerated Lag .
Evap. or Pore. Pond
Act. Sludgo
Stab. Pond

3AF
DAP
Stab. Pond

1976
Eva p. or Pore. Pond
Evap. or Perc. Pond
Chcmicnl Floe.
Act. Sludgo
Aerated Lag.


Aerated Lag.
I'ol. 1-ond
Filtration

Other Organic* Rom.
Aerated Lag.
Pol. Pond
Nona
Chemical Ploc,
DAP
DAP
Filtration
Stab . Pond
Pol. Pond
Water
Mi 1 lion
1973


672.




14.33


0.40

0.04
tlsnqo
1976


53.24
0.68

3.45
0.087
8.15
0.89

0.413
2.52
O.OB4

* ReA'' f^-
227
223
Questionable 229
Data
230

231
232
43 233
234
239
-3.3 "6
237
-110 23B
ilJ!)
Trcatiren
1973
Stab. Pond
Evap. or Perc. Pond
Nona
Stab. Pond


Aornted Lag.
Filtration
DAF
Act. Sludge
Stab, pond
DAF
Act. Sludge
Trick. Filter
Act. Sludge
Filtration
Corr. Plate Sep.
Trick. Filter
Act. Sludge
t'ULrrtLluil
Stab. Pond
: Operations
1976
OAF
RISC
I'ol'. lijnii
mirutlon
Stab. Pond
I'ol. Foivl
Evap. or Perc. Pond
Stab. Pond


Chemical Floe.
Filtration
Act. Sludge
Trick. Filter
Pol. i-onii
DAF
Act. Sludge
Trick. Filter
Pol. honi
Act. Sludge
Trick. Filter
fol. Pond

Corr. Plate Sep.
OAF
Act. Carbon
Act. Sludgo
Trick. Filter
Aerated Lag.
Stab. Pond
1- 	 i.n.l
Curr I'iattt Sep.
nnc
I'ol. 1-oml
Million

2.56
0.48

1.80


72.22
5.59
2.30
4.40
0.13

3.72
0.23
Gul/oav

2.59
0.55
0.15
1.5


^3.65
3.75

3.*»
0.15
0.038
4.2
0.216
                                                                                                17
                                                                                                 -15

-------
               TABLE VMS (Contlnutd)
ITMtmnt Oniratlemi «nd »«t«r U.«a« im Mid MM
wntnr u«i.n. water Usaoe
ss±
240
241

242


243

Treatment Opflratione Million Rni/n^u
1973
None
Other Organlca Res.

None


Aerated Lag.
Evap. or Perc. Pond
t
i
244

I

245


2 -1C-


247
-S3



149


250



251

252

Stab. Pond


MF
Stab. Pond
Svap. or Perc Pond
Evap. or Perc. Pond




PAP
Evap. or Perc. Pond

Evap. or Perc. Pond





Stab. Pond
1976

Act. Sludge
Tol. Pbni
None


Aerated Lag.
I'd. Fond


Evap. or Perc. Pond


Corr Plat. Sep.
rol? fond
Evap. or Pere. Pond
Aerated Lag.
Evap. or Perc. Pond
!'ol. Fond
Evap. or Perc. Pond
Evap. or Perc. Pond



OAF
Evap. or Fere Pond







Stab. Pond
1973
1.58
2.47

0.95


O.S6









2.16
















0.24
1976
1.34
0.96

0.86


0.77



3.19





2.84


0.84













0.32
-*-ESS*. JJOj.
IS 253
61 254

9.5 255


10 256



257


250


-31 259


260
261





264

265




-33 266
Vreatmen
i2Zi
Evap. or Pare. Pond









DAP
Aerated Lag.

Aerated Lag.





Hone













None
. 9pf ration* Hi IK on rol/mv
1V76
Evap. or Pere. Pond
Nona

Pre-Flltration
Aera'cod Lag.
l-ol. fond
Corr. Plate Sep.
Stab. Pond


Stab. Pond


DAP
Act. Sludge
f-ol. l'on-1
OAF
Act. Sludge

Aerated Lag.
DAP
TrieX. Filter
RBC
Evap. or Pore, Pond




Corr. Plate Sep.
DAP
Act. Sludge
Stab. Pond
Pol. Pond
None
1973



















0.25













0.94
1976

1.0

0.13


0.04



99. S


1.96


21.55


1.0






3.0

2.07




O.B3
* r*4.



















-300













12

-------
                                                                                            TABLE VI-15 (Continued)
                                                                                Tr»»tn»nt Oryrationii and W*U-r Usarin 1973 and 1976
                                      Treatmen   Operations
               278
               282
               .263
               284
to
                                                        1976
  Water usage
Million Gal/pay   % Red.
££3U
No.
                                                                                                           295
                                                                                                           £97
                                                                                                           298
                                                                                                           299
                                                                                                           300
                                                                                                           301
                                                                                                           302
                                                                                                           303
                                                                                                           30U
                                                                                                           305
                                                                                                           306
                                                                                                           307
                                                                                                                                  Treatment  Qperationa
                                                                                                                               1973
                                                                                                                                             Ev»l>. or Perc. Pond
                                                                                                                                                                      Watoi^Usaoe^
                                                                                                                                                                    Million Gal/p.TV   %  Rgd.
                                                                                                                                                                     1073.

-------
                                                                                          TABLE VMS (Continued)
                                                                               Tteatiimt Op«r«tioM ana Matir u»« 1»TJ i
Treatment Operations
                                 107]
                                              Cli«nicul Floa.
                                              Act.
                                              Aerated
u>
                                                      1076


                                              Evap. or Pere. ?ond
  Hntar  Unacie
Million  onlAlav   X Raf.
 1973   [   197fi  '
                                                                                                                                                                  water
                                                                                                         Rat.
                                                                                                         U2,.
   Tr«at««n
1973.
Poorattonft
       A176
                                                                                                                                                                Million cal/sav
                                                                                                                                                                                   S Red.

-------
                      TABLE VI-16
            Summary of Treatment Technologies
Prefiltration

Activated Sludge

Trickling Filter

Aerated Lagoon

Stabilizat

Rotating B

Other Orga:

Filtration

Polishing Ponds

Activated Carbon
For 1973 and 1976
•stems Number of
1973
'late Separators 4
icculation 1
.r Flotation 56
lion Systems 1
in Unknown
.udge 30
.Iter 7
ion 63
in Pond 4 4
i logical Contactor 0
.cs Removal 4
10
mds Unknown
irbon 1
or Percolation Ponds 26
Refineries
1976
20
46
68
15
6<
50
10
73
35
5
10
23 (
75
2
37
(1)  Two refineries have both prefiltration and post filtration,
     so that a total of only 27 refineries had filtration systems
     in 1976.
                            174-

-------
           TABLE VI-17



PLANNED WASTEWATER FLOW REDUCTIONS
Refinery
No.
3
7
9
11
12
13
18
22
i
31
35
39
40
42
44
45
46
50
53
57
59
Expected Flow
Reduction (MGD)
-
0.115
0.023
0.72
0.0014
-
0.0462
0.021
0.050
1.89
-
1.2
5.0
0.230
1.93
0.450
0.052
0.100
6.0
0.11
Effective
Date
1978
1977
-
1977
1977
-
1977
1978
1977
-
1978
-
1979
1977
1977
1977
1978
1977
1930
Reduction Technique
Upgrade piping and installing air
coolers
Stripping steam to crude unit
In plant modifications
Better cooling tower controls and
waste water supervision
Recycle
Cascading of sour water
Sour water stripper effluent to
desalter or cooling towers
(50-50)
Recycle
Haste water to cooling tower
Replace once -thru condensers with
recycled water
Reuse
Discontinue selected quench
streams
Recycle
Recycle cooling tower water and
boiler blowdown
Stripped sour water to desalter
Stripped sour water to cooling
towers and recycle cooling water
and desalter water
Sour water used for desalting
Reuse and increase cooling water
cycles
Recycle cooling water and control
blowdowns
Water management within refinery
           175

-------
                            TABLE VI-17

                   PLANNED WASTEWATER
                            (Continued)

                            FLOW REDUCTIONS
Refinery
  No.

  63
  64
Expected Flow
Reduction (MGD)

    0.240
              2.37
Effective
  Date

  1977
                             1983
67
71
72
74
76
77
78
82
87
88
90
92
96
102
106
107

0
0

0

0

0
0
0
0
2
0
0
0
-
.04
.020
-
.5
-
.063
-
.00001
.16
.002
.270
.1
.417
.259
.04
-
1977
1977
1977
1978
1977
_
1982
1977
1977
1978
1978
1977
-
1977
1977
 113
              0.072
                             1977
       Reduction Technique

Reroute cooling tower blowdown
and new storm water handling
facilities

Closed system for pump cooling;
eliminate once-thru cooling;
cooling cycles increase via acid
injection

Recycle and make-up for firewater

Storm water segregation

Larger cooling capacity for lower
blowdown rates

Improved condensate recovery

Fin fan air condensing

Runoff to be used as cooling tower
make-up
Stripped sour water used as de-
salter make-up

Treated sour water to desalter

Switch to Fin fan cooling

Reuse of wastewater in gas hand-
ling system

Non-refinery runoff eliminated

Closed loop cooling loops and
some recycle

Cooling towers replacing once-thru
cooling

Treated wastewater for firewater
system

Recycled treated wastewater

Stormwater segregation

Recycle wastewater effluent to
cooling tower make-up

Reduce once-thru cooling and tower
blowdown
                                 176

-------
                          TABLE VI-17

                 PLANNED WftSTEWftTER
         (Continued)

         PLOW REDUCTIONS
Refinery
No.
115
117

122
132
138
144
150
152

153
156
162
163
169
172
Expected Flow
Reduction (MGD)
0.08
0.200

0.700
0.7
0.538
0.08
0.072
0.4

1.0
0.216
1.0
0.166
1.55
0.156
Effective
Date
1978
1977

1977
1978
-
1977
1978
1978

1977
1977
1977
1977
1977
1977
Reduction Technique
Recycle process wastewater to cok
cooling
Pump gland cooling to cooling
towers
Coker recycle water system
Uncontaminated stream segregation
Recycle to cooling towers
Two series desalter
Segregated once-thru pump gland
cooling and plant wastewater con-
servation program
Firewater use reduction and me-
chanical pump seal replacement
Recycle treated wastewater to
cooling towers
Cooling tower cycle increases
(blowdown decreases)
Recycled wastewater to process
units
Segregation of uncontaminated
runoff
Reuse of process water
Replacement of barometric conden-
173
181
            0.180
            3.0
         ser with surface condensers and
         treated sour water recycle to
         desalter

1977     Segregate uncontaminated runoff
         and replace barometric condenser
         with on-contact condensing system

1978     Reduce boiler blowdown via better
         control; Increase cooling tower
         cycles; Cascade boiler  blowdown
         from high pressure boilers to low
         pressure boilers;  Use boiler blow-
         down as desalter water; Use clarifier
         overflow and regeneration water
                      177

-------
                          TABLE VI-17 (Continued)

                   PLANNED WASTEWATER FLOW REDUCTIONS
Refinery  Expected Flow
  No.     Reduction (MGD)
181 Cont'd.
  182



  183

  184


  185


  187

  191

  194




  196



  200

  202

  207


  208
  210
0.94



0.080

0.144


0.837


0.72

0.140

3.0




9.



0.022



0.0005
             Effective
               Date
1977



1977

1978


1981


1977

1979

1977




1983



1977

1977

1977


1980
              0.003
       Reduction Technique

from condensate polisher as  cool-
ing tower make-up; Recycle filter
backwash to clarifier; Reuse coke
cutting water and coke drum  cool-
water in delayed coking units;
Reuse treated wastewater in  fire-
water system

Treated wastewater used as utility
water and greater reuse of stripper
bottoms

Recycle desalters effluent

Steam condensate collection  &
reuse

Effluent reuse and solar evapora-
tion

Recycle effluent to cooling  towers

Sour water stripper

Replacement of barometric conden-
sers; Utilization of recycled fire
waters in cat cracker; Cooling
tower blowdown atomation

Recyle of waotewater to cooling
tower and segregation of storm
waters

Stripped sour water to desalter

Total recycle

Increase heat recovery at reformer
to reduce cooling requirements

Increase cooling tower cycles;
Reuse of boiler blowdown;  Recovery
of condensate; Recycle demineral-
izing regenerants to fire system;
reuse appropriate water as cooling
water

Boiler blowdown and stripped sour
water to be used in desalter
                             178

-------
                           TABLE VI-17

                  PLANNED WASTEWATER
                           (Continued)

                           FLOW REDUCTIONS
Refinery
  No.

  216
  220


  227


  229



  231
Expected Flow    Effective
Reduction  (MC.n)    Date
    4.56




    1.0


    0.0432


    0.0125



    0.300
1977




1977


1978


1978



1977
232
236
240
242
247
249
252
254
259
265

0.
0.
0.
0.
14.
0.
0.
0.
0.
-
026
37
36
652
4
016
500
072
537
-
1977
1977
1977
-
1977
1977
-
1977
-
  298
       Reduction Technique

Reuse of effluent, stormwater and
sludge blowdown decant as intake
and activated sludge effluent as
service water intake

Condensate from tower over heads
to desalter feed

Sour water treatment to reduce
volume requiring stripping

Strip ammonia from cat cracking
condensate to release water for
desalter

Once-thru cooling to become cool-
ing towers

Program being developed

Contact cooling to non-contact
cooling

Contact cooling to non-contact
cooling

Non-contact cooling water segrega-
tion

Find market for spent phenolic
caustic

Reroute cooling tower blowdown
to spray pond

Additional wastewater evaporation
                            Recycle boiler blowdown

                            Ballast water bottoms, desalter
                            water, and zealite regeneration
                            brine to disposal well

                            Install water softeners to reduce
                            cooling tower blowdown
                             179

-------
                          TABLE VI-17 (Continued)

                  PLANNED WASTEWATER FLOW REDUCTIONS

Refinery  Expected Flow    Effective
  No.     Reduction (MGD)    Date            Reduction Technique

  308           -            —       Study underway

  309         0.15           1978     Replacement of two vacuum jet
                                      ejecters on solfolane unit with
                                      vacuum pumps.
                            180

-------
                               TABLE VI-18

              FUTURE WASTEWATER TREATMENT MODIFICATIONS

Refinery
  No.                             Modifications

   3        Steam stripper  to be added

  10        DAF unit to be installed

  11        Sour waters to be stripped; Separator effluent to equal-
            ization, pH adjustment, flocrulation, DAF, bio-reactors,
            clarification and filtering

  15        API effluent to CPI and then to detention pond

  16        DAF unit to be installed

  25        API sludge handling system to be installed

  32        Replace stabilization with bio-disc, and effluent to pass
            through clarifier carbon and filtration

  37        DAF sludge thickener to be installed

  38        Chemical floculation and DAF unit to be added

  39        Final effluent to be used as boiler feed water

  40        DAF effluent to equalization, activated sludge, and clari-
            fication

  42        Detention pond effluent to oxidation pond, then percolation
            ponds;Clarifier effluent to filter before recycle to cool-
            ing tower

  44        Desalter effluent to separate separators; Two CPI and sand
            filter at deep well; two stage sour water stripper; Warm
            lime treatment for boiler and cooling water; Equipment for
            SS  removal or wet scrubbers blowdown

  45        Tie in to POTW

  46        Segregated streams to trickling filter where effluent
            to combine with DAF effluent to activated sludge and
            clarifier

  50        Separate stabilization pond for sludge recirculation

  51        Additional foul water stripping;  IAF for ballast water

  57        Activated sludge unit with pre-and post-filtration to
            be added along with surge pond

  62        DAF units being added
                               181

-------
                            TABLE VI-18 (Continued)

              FUTURE WASTEWATER TREATMENT MODIFICATIONS

Refinery
  No.                             Modifications

  67        Activated sludge plant to be added

  70        Segregate process and non-process wastewater and add
            oil to skimmer and filter

  71        Segregate storm water; New API units and equalization
            pond;  Increase lagoon aeration

  72        Total renovation of barometric recycle water system

  74        Possible addition of pH adjustment, chemical flocu-
            lation, and DAF

  76        Equalization after API; Two new DAF units; Activated
            sludge unit; Final clarifier

  77        Adding DAF, equalization, pH adjustment, activated sludge
            unit,  and clarification

  78        Add sour water stripper  effluent  and  coker  effluent
            to desalter

  83        New equalization, bio-discs, and clarifiers after DAF,
            and sludge to be treated and digested

  86        Storm water surge basin

  87        All sour water to be evaporated

  88        Adding two additional oil separators, and by-passing off-
            property water

  90        Segregation of storm  sewers and boiler blowdowns, and
            installation of bio-discs

  92        Aerated lagoons to be converted to activated sludge;
            Biological treatment of storm runoff and ballast water;
            Cooling towers will be replaced by once-thru cooling water

  95        Adding API separator

  97        Adding activated sludge plant

  98        Storm water segregation  and overall plant modifications

 102        New activated sludge plant including pH adjustment,
            chemical flocculation and settling, DAF unit,  two
            parallel sludge reactor tanks and clarifiers,  and final
            dual media filters;  Also partial effluent recycle
                               182

-------
                          TABLE VI-18 (Continued)

             FUTURE WASTEWATER TREATMENT MODIFICATIONS

Refinery
  No.                            Modifications

  104       New impounding basin before aerated lagoon

  105       Areated lagoon to be converted to activated  sludge basins
            and to be followed by sand filters

  106       Storm water segregation

  107       Tie in to POTW

  110       Boiler blowdown, sour water, desalter condensate, water
            treatment system blowdown, and spent caustic to be routed
            to new separator and into city sewer

  114       Tie in to POTW

  115       Storm water segregation; Separator effluent  to pH adjustment,
            equalization, chemical floculation, DAF unit, activated
            sludge and clarification

  120       Additional API separators and enlargement of aeration ponds;
            Activated carbon to be added if necessary

  121       Plant source control programs

  122       Stormwater segregation; Extra aerators to aeration basins;
            Mixed media filter for final effluent; Some recycle of
            final effluent to cooling water

  124       Storm water retention pond

  125       DAF unit to be installed

  127       Baffles added to final polishing pond

  132       Water treatment systems blowdown to clarifier; Segregate
            once-thru cooling water and  un -contaminated runoff;
            Additional sour water stripper to allow reuse of stripped
            sour water; Effluent from separator, stripper, and clarifier
            to go to equalization, activated sludge, and filtration

  142       Tie in to POTW

  143       Tie in to POTW

  150       Bio-discs to be added

  151       Additional ammonia removal facilities; Bio-discs studies
            on aerated lagoon effluent
                              183

-------
                          TABLE VI-18 (Continued)

              FUTURE  WASTEWATER TREATMENT MODIFICATIONS

 Refinery
   No.                        Modifications

   152        Downflow sand  filter  to  be  added prior to final discharge

   154        API  separator  to be added with new holding pond

   163        API  effluent  to  equalization pond with skimmer, four stage
             bio-disc unit, two  parallel clarifiers,  and final pond-
             ing  with skimmers

   1.65        Storm water runoff retention basin

   163        Oily process wastewater, stripped sour water,  and con-
             taminated runoff to receive  pH adjustment,  oil water
             separation, sand filtration,  equalization, nutrient
             addition,  bio-disc treatment,  and final clarification;
             ballast  water  to be held, fed to an IAF unit,  passed
             through  cooling  water guard basin and  discharged

   172        Adding IAF, equalization, bio-discs, and  clarification

""'173        API  effluent to  equalization,  chemical addition, DAF,
             activated sludge,and  clarification

   175        To join  regional treatment  plant

   177        Installation  of  bio-discs  and clarifiers

   181        API  effluent to  primary  clarifiers before equalization

   182        Expanded reuse of stripped  sour water;  Increased rainfall
             collection and retention facilities;   All wastewater to
             POTW

   184        Addition of chemical  f locculation, DAF  units,  and cooling
             towers,  and modification of aeration basin and clarifier

   185        Add  secondary  treatment, effluent reuse,  and,  in 1981,
             solar evaporation

   187        Larger API separator

   190        Increase lagoon  size

   194        Improve  API and  polishing pond

   199        Additional API separator

   204        Modify DAF for recycle pressurization;  Aerators in equali-
             zation pond; Dual media  filters for bio-treator effluent;
             Improve  chlorination;  Better storm water  segregation
                             184

-------
                          TABLE VI-18 (Continued)

             FUTURE WASTEWATER TREATMENT MODIFICATION

Refinery
  No.                       Modifications

  205       Sour water stripping systems; Larger API separator; Pond-
            ing or biological systems

  208       Existing two parallel plate interceptors and three API
            separators to be replaced by five CPI units

  212       Sand filtration for plant effluent

  216       Aerated lagoon to be converted to activated sludge;  New
            contaminated runoff impoundment facilities; Sour water
            oxidizer to be replaced by single stage stripper

  219       Storm sewer effluent treatment to be improved;  New CPI
            and equalization basin to be installed;  Filter backwash
            to be dewatered in settling ponds and supernatant sent
            back to treatment plant intake

  221       Equalization before aeration, and storm water segregation

  222       Increase surge pond size; Chemical Floculation and
            clarification to be added; Effluent recycle facilities
            installed

  230       IAF provided for Atl separator and equalization basin
            enlarged for grit removal

  232       Storm water retention, activated sludge, aid filtration
            under construction

  236       New system to include API separator, holding tank,CPI,
            aerated equalization basin, four stage bio-disc unit, and
            final clarifier

  240       New oil-water separator and existing pond to be sub-
            divided into primary settling, aeration, and final settling

  241       New parallel separator to combine with old separator  and
            go to two parallel DAF units, activated sludge pond,
            clarifier, and final chlorination

  242       Adding equalization basin after API separators, then
            chemical floculation, DAF, activated sludge, and final
            clarification

  246       Total impoundment for all but once-thru cooling water

  225       New API separator Additional treatment pond, DAF, new
            aeration basin, and phenolic treatment
                              185

-------
                         TABLE VI-18  (Continued)

              FUTURE WASTEWATER TREATMENT MODIFICATION

Refinery
  No.                              Modification

  256       Additional CPI to operate in parallel with existing one;
            Continuous solids removal to be added prior to API
            separator;  Equalization basin capacity to be increased

  257       Additional API separator, air flotation unit, and aerated
            lagoon

  298       New system including primary separator, DAF, and secondary
            separator
                              186

-------
                               TABLE VI-19
                      REFINER* FLOW VS. FINAL EFFLUENT
                    CONCENTRATION FOR 17 SCREENING PLANTS
Percent of
Refinery Actual Discharge
Code Flow
A
B
C
D
E
F
G
H
I
J
K
L
H
N
0
P
Q
Slope
Intercept
(Correlation)
to BPT Flow
40.8
37.8
36.7
49.7
143.3
.96
121.7
72.5
69.4
58.0
89.4
173.9
35.0
69.1
121.3
4
28.0



Average
BOO,
mg/1
< 2.5
18.5
41.0
125.0
< 9.5
27.0
<12.5
<. 4.5
<' 12.0
6.0
< 8.5
•* 7.5
<-12.0
9.0
•C51.0
rf 5.0
25.0
- .11
31.27
.03
Average
TSS,
ng/1
37.0
22.0
19.0
62.0
14.5
103.0
56.0
9.0
8.0
13.5
24.0
27.5
11.5
45.0
25.0
6.5
30.0
- .15
42.40
.08
Average
TOC,
mq/1
11.0
43.0
39.0
220.0
10.0
92.5
60.0
19.5
31.5
30.0
40.5
16.5
16.0
34.5
46.0
23.5
68.5
- .31
70.96
.08
Average
Oil and Grease,
mg/1
*
34.0
9.0
*
*
*
16.5
20.0
6.0
13.0
21.5
*
13.0
*
it
*
41.0
- .11
26.03
.09
Note:  * - NO DATA
                              187

-------
                                                                     TABLE VI-20

                                                         REFINERIES INCLUDED IN THE DEVELOPMENT
                                                          OF WASTEWATER FLOW REDUCTION FACTORS
   Refineries Meeting Model Flow Only
                                                 Refineries Meeting Level 1 Only
Refinery
Code No.
127
2131
239
21V
/8
129
204
v2
V »t-:j
88
1£|Q
131
l.-.A
1M
245
104
1'Ob
-1 81
0 153
0 :M 9
14V
115
23 A
186
84
110
265
13
112
2OO
45
i)8
41
;~,9
24
189
96
257
tiv
11

1 - R
0.004B32
0.010/^.2
o.ouiijoa
0.022324
0.024390
0.043977
0.046543
0.073705
0.0/8091
O.OfilS30
0. 10694A
0. 109219
0. 110032
0.113357
0,113475
0. 114422
0.118^16
0. 120256
0. 122688
0.135170
0. 143167
0. 151155
0.154930
0.160188
0.165102
0.166667
0.170161
0.197342
0. 197578
0.211340
0.211372
0.221726
0.237844
0.240990
0.247366
0 . 250000
0.257829
0,259934
O. 260304
0.264403
Notes:  1. Of the 262 refineries included in the
           project data base, 175 refineries are
           known to have generated wastewaters
           in 1976 at a rate less than their model
           flows based upon crude throughputs.
Refinery
1 - R Code No.
0.1' 6 5/99
O , ' Y'V'*'' 1
o!''7 (''j/''
0.277283
0, 277396
0.291450
0.29 7861
0.302376

•,'.310503
.313123
.325362
0.331140
0.338431
0.357085
0.365553
0.369167
0.371728
0.382311
0.396491
0,399538
0.400000
0.407621
0.407631
0.419953
0.422332
0.432812
0.438513
0.444599
0.451475
0.452902
0.457237
0.462064
0.463856
0.473802
0.477875
0.479167
0.483395
0.490506
0.496587
0.502878
0.510246


Wastewater Generated in 1976
Model Flow based upon Crude
Throughput in 1976
176
98
62
144
33
185
53
15
86
113
37
60
305
106
9
207
23
259
161
119
14
16
114
206
77
6
124
2
26
158
233
210
264
298
195
187
13
90
125
160
55
1
213
209
.74
155
148
                                                             R =
R^ for Level  1 = 0.73
R2 for Level  2 = 0.48
                                                                                                           Refineries Meeting Level 2
                                                 I  -  R
                                               0.516635
                                               0.519890
                                               0.520057
                                               0.522209
                                               0.522553
                                               0.523294-
                                               0.523628-
                                               0.526985
                                               0.527967
                                               0.529121
                                               0.530348
                                               0.532319
                                               0.533266
                                               0.536462
                                               0.542311
                                               0.544872
                                               0.548148
                                               0.548640
                                               0.551402
                                               0.555687
                                               0.561105
                                               0.562280
                                               0.568072
                                               0.569444
                                               0.569981
                                               0.572893
                                               0.595636
                                               0.600592
                                               0.607326
                                               O,612115
                                               0.628336
                                               0.638883
                                               0.641834
                                               0.650538
                                               0.667500
                                               0.666071
                                               0.670520
                                               0.671052
                                               0.678214
                                               0.687500
                                               0.68EI612
                                               0.690352
                                               0.699307
                                               0.701322
                                               0.703493
                                               0.705220
                                               0.715018
Refinery
Code No.
137
147
108
2*-*
260
140
50
202
118
179
243
8
103
25
310
191
36
3
54
10
237
165
17
220
49
80
99
107
97
254
229
19
193
218
31
141
4
302
248
135
250
251
278
296
303
307

1 - R
0,716590
0.717381
0.720812
0.729892
0.733088
0.746777
0.748891
0.750000
0.752066
0.755548
0.768034
0.772727
0.774355
0.778185
0.783333
0.792902
0.795792
0.807692
0.820523
0.826075
0.835294
0.846560
0.848736
0.850649
0.858620
0.861077
0.864288
0.903723
0.915076
0.916667
0.925180
0.945128
0.949884
0.970833
0.971374
0.978270
0.989423
0.990476
0.997499
1.000000
1.000000
1 .000000
1.000000
1.000000
1.000000
l.OOOOOO

-------
                             SECTION VII

              COST, ENERGY AND NON-WATER QUALITY ASPECTS


INTRODUCTION

This  section  addresses  the costs, energy requirements and non-water
quality  environmental  impacts  associated  with  the   control   and
treatment  technologies  presented  in  Section VI.  As such, the cost
estimates represent the incremental  expenditures  required  over  and
above  the  capital  and operating costs associated with attainment of
BPT effluent limitations.  These differential costs, therefore, relate
to specific control and treatment alternatives that could be necessary
to comply with BAT limitations.

The cost estimates presented do not include land costs;  the  cost  of
land  is  variable  and  site  dependent  and cannot be estimated on a
national basis.  However, the amount of land required is indicated for
each of the major end-of-pipe treatment schemes.  It should  be  noted
that  these  land  requirements  are  minimal  compared  to  the  land
requirements for refinery process equipment and land at  the  refinery
for  wastewater  treatment  systems  exists  in most cases.  All costs
presented in this section are based upon January 1977 values.

The cost data presented in this  section  are  based  on  flow  rates.
basis.  The  following  table  outlines the cost basis used for calcu-
lating the  major  capital  and  operating  costs  presented  in  this
section:

                             Table VII-1

                              COST BASIS

Item                                    Unit Cost


1.  Tank Steel                          $1.40 - 2.00/pound
2.  Tank Lining                         $3.00 - 4.00/ftz
3.  Carbon, granular (capital cost)     $31.00/ft3
H.  Carbon, granular (operating cost)   $0.61/lb
5.  Carbon, powdered (operating cost)   $0.31/lb
6.  Electricity                         $0.04/kilowatt hr.
7.  Manpower                            $10.00/hr

Capital  costs  for major equipment items such as clarifiers, filters,
carbon regeneration furnaces,  solids  dewatering  filters,  activated
carbon,  and  large  pumps were obtained from equipment manufacturers.
Other costs such as the unit cost of tank steel, piping, small  pumps.
                                189

-------
etc.  were  derived  from  the  contractor's   (Burns and Roe)  in-house
experience and expertise in  the  design  and  construction   of  major
facilities.

The depreciation factor and the cost of capital have not been included
in  these  cost  presentations  but will be considered  in the economic
impact analysis.

COST AND ENERGY REQUIREMENTS OF TECHNOLOGIES CONSIDERED

Biological Treatment.  Cost analyses  developed  for  BPT  regulations
were  based  on  activated sludge or equivalent BPT systems  (3).  Very
limited number of  refineries  may  need  to  upgrade   their   existing
biological treatment systems inorder to comply with BAT limitations.

One  method  of  upgrading  a  biological  unit  is  to install a raw
wastewater equalization system  (143).  Table  VTI-2  presents capital
and  operating  costs  for this type of modification.   These  costs are
based upon 12 hours detention and  include  the  necessary  pumps  and
controls for equalization of flow as well as pollutant  loading.

EPA  assumes  the tanks are manufactured by placing a steel shell on a
concrete pad.  Costs are included for pumping the wastewater  either to
or from the equalization tank.  It is assumed either that  pumping  is
not  required  on  both  sides  of  the  tank,  or there is one set of
existing pumps to supply the second pumping requirement.

Another method of improving the performance of a biological   treatment
system  is to install a biological roughing unit.  Rotating biological
contactors (RBC's)  are an applicable treatment alternative for use  as
a roughing system.

Tables   VII-3   and   VII-U   present   equipment  sizes  and  energy
requirements, as well as capital and operating costs  for  RBC  units.
This  study  assumes  that  this treatment alternative  will be used if
aerated lagoons or oxidation ponds are used as  the  basic  biological
treatment  process.   The  use  of aerated lagoons and  oxidation ponds
implies that the refinery has sufficient land to install this type  of
wastewater treatment system.

It  also  is  assumed  that  the  RBC  units  will precede the present
biological  system.   Clarifiers,  or   additional   sludge   handling
capabilities,  will  not  be  required,  since  the  amount   of solids
carry-over from the RBC units to the present lagoons is assumed to  be
the  same  order  of  magnitude as that presently entering the lagoons
from the raw wastewater.

Refineries with activated  sludge  or  trickling  filter  systems  can
improve   their   effluent  quality  with  powdered  activated  carbon
                                190

-------
treatment.  Powdered activated carbon may also  improve  the  effluent
quality  of  trickling  filter  systems.   Tables  VII-5 through VII-7
present cost data for powdered activated carbon systems  that  do  not
include  the  cost  of sludge handling in the analysis.  However, when
carbon regeneration is used in  conjunction  with  powdered  activated
carbon  treatment, the sludge produced in the biosystem is incinerated
as the carbon is regenerated, thus  eliminating  the  sludge  disposal
costs associated with this requirement.  An analysis was undertaken to
determine  when  the  use  of  carbon  regeneration  would become cost
effective when sludge handling is included as  a  cost  factor.   This
analysis  is  included  in  Table  VII-8.  Tables VTI-9 through VII-11
present cost data for powdered activated carbon systems based upon the
inclusion of sludge handling costs.

Table VII-10 includes the costs  for  purchase  of  solids  dewatering
systems,  whereas  Table  VII-11  includes operating costs with sludge
disposal shown as  a  credit  for  the  systems  that  include  carbon
regeneration.

The  powdered activated carbon costs described above are based upon an
80 mg/1 dosage rate.  This number is based upon one year of  operating
data at the DuPont Chambers works facility.

Filtration.   Filtration  was  also  discussed  in  Section  VI.   BPT
regulations were based, in  part,  on  granular  media  filtration  or
polishing  ponds   (3).   Many  refineries do not include filtration or
other polishing techniques in their present systems, even though  that
technology  was  included  in  the  model  BPT  technology.  It may be
necessary for certain refineries to install granular media  filtration
to  comply with BAT limitations.  Tables VII-12 and VII-13 include the
associated cost data for tertiary filtration systems.

Granular Activated Carbon.  Table VII-14 presents the equipment  sizes
and  energy  requirements  used  to estimate the capital and operating
costs for granular activated carbon systems.  The sizes are based upon
the design concept described in Section VI, with the system consisting
of tanks that can be shipped in one piece,  thereby  minimizing  field
construction.   This results in an unusually large number of tanks for
the larger systems.  In reality, a more  cost-effective  design  (with
cost  savings on the order of 5 to 15%) for a given refinery could use
field constructed steel tanks, concrete tanks, or  other  construction
techniques  determined  on a piant-by-piant basis.  The use of similar
sized, shop fabricated tanks allows for uniformity in cost estimating,
especially in regard to the development  of  construction  and  design
engineering  estimates.   This approach also results in a conservative
(e.g., larger)  estimate, and is considered preferable when considering
general industry-wide costs.
                               191

-------
Table VII-15 presents the capital costs for the  systems  outlined  in
Table  VII-1U.   Table  VII-16 provides the operating costs, excluding
depreciation,  for  these  granular  activated  carbon  systems.   The
capital  costs  for  carbon  regeneration  systems  are  based upon an
equipment manufacturer's quotations.

The manhour estimates used in carbon  regeneration  calculations  were
based on the following: Manpower requirements for the operation of the
granular  carbon  adsorbers  were  obtained  from  the  EPA Technology
Transfer Series, Carbon Adsorption Manual  (64); the manpower estimates
for operating powdered carbon feed systems were assumed to be half  of
those  for  the  granular  systems.   The  estimates presented in this
reference for the operation of carbon regeneration systems  appear  to
have  significant errors (on the order of  5 to 10 times too large), so
that they were not used in this analysis.  Based on  other  experience
in  operating a system of this type, it is estimated that one operator
around the clock would be required  for  the  operation  of  a  carbon
regeneration system, and this value has been used in the analysis.

One equipment supplier leases carbon adsorption systems.  Plants would
pay  a  yearly  operating cost with no initial investment other than a
foundation for  and  piping  to  the  equipment.   This  supplier  has
suggested the following rental cost estimates for the two smallest
systems:

I.   380 M3/day  (O.lxlO6 gal/day)    -  $75,000 - $100,000/year
     Foundation and Hook-up         -  $5,000
II.  3800 M3/day (l.OxlO6 gal/day)    - $450,000/year
     Foundation and Hook-up         -  $15,000

These  estimates  are  based  upon  a lease agreement for a minimum of
three years and include the carbon adsorbers, with  installation,  all
granular  carbon required,  and carbon regeneration services.  Manpower
for the operation of the carbon columns is not included.

Powdered Activated Carbon.   Powdered activated  carbon  treatment  can
also  be  used  for  the  removal of organic toxic pollutants, but may
require higher carbon dosages.   Tables  VII-17  thru  VII-19  present
costs for powdered activated carbon systems based upon a carbon dosage
of  150  mg/1.   Tables  VII-20  thru  VII-23 present the analyses and
associated results when the costs for sludge hauling and recognized.

Low Flow Rate Systems.  Table VII-24 presents  capital  and  operating
costs  for the systems discussed above at  a design flow rate of 10,000
gal/day.
                                192

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In-Plant Control

Chromium Removal.  The treatment technology described in Section VI is
the  basis  for  estimating  the  costs  of  chromium  removal.   Most
refineries  also  can  take  advantage  of the reducing environment in
refinery sewers and the removal capabilities  of  secondary  treatment
systems.

Table  VII-25 presents cooling tower blowdown rates for the refineries
that responded to the 1977 EPA  Petroleum  Refining  Industry  Survey.
The  flow rates have been used as the design basis for chromium treat-
ment systems.  Table VTI-26 presents equipment cost bases  and  energy
requirements  for  selected flow rates from Table VII-25; Table VII-27
presents the capital and operating costs for these same systems.

Flow Reduction.  Section VI describes a  number  of  in-plant  control
measures  designed  to  reduce  or  elminate wastewater flow.  Many of
these  measures,  however,  require  a  plant-by-plant  evaluation  to
determine  their  usefulness.  In  addition, the costs associated with
their implementation are for the most part site dependent,  making  an
accurate  estimation  of representative costs on a national basis very
difficult.

The Agency has selected one in-plant flow reduction measure,  however,
that  can be applied at most refineries in the country, and whose cost
can be readily estimated on a national  scale.   This  flow  reduction
scheme  consists  of the recycling of treated refinery wastewaters for
use in such process related applications  as  cooling  tower  make-up,
pump gland cooling water, wash down water, and fire system water. This
wastewater  could  be  reused  once, and then returned to the refinery
wastewater collection system for end-of-pipe treatment. The amount  of
wastewater  that  can  be  recycled  in  this  manner  depends on many
factors, including the number of cooling  towers  in  the  plant,  the
salinity  of  the wastewater to be recycled, etc.  EPA has chosen this
wastewater reduction technique for estimating purposes because  it  is
both  definable and representative of the costs that would be incurred
by other similary effective in-plant control measures.

Table VII-28 presents the capital and operating  costs  per  mile  for
recycling  various  amounts of treated wastewater.  Figure VTI-1 shows
this data in curvilinear form, projecting the  cost  values  in  Table
VII-28 over a wide range of pumping distances.

Determining  the  costs  incurred  at  a  particular refinery requires
information on the distance between the treated wastewater  collection
point and the actual point of reuse.  Since this data is not generally
available,  it  is  necessary  to  estimate  based upon refinery size.
Figure VII-2 presents a curve of refinery size vs.  pumping  distance.
This  figure  is presented to permit an estimate of the cost for reuse
                               .193

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of treated wastewater.  EPA expects that  the  costs  developed   using
Figures   VII-1  and  VII-2  will  be  higher  than  the   actual   cost
experienced at most refineries.  This is because the distances derived
from Figure VII-2 probably will be higher than  the  actual  distances
involved at most petroleum refineries.

Treatment  of_  Recycled  wastewater.   In some cases, particularly for
cooling tower make-up, the recycled wastewater may  require  treatment
for  the  removal  of  calcium  and  magnesium hardness.   This type of
treatment may involve the use of  lime  or  lime-soda  ash softening,
followed  by  filtration.  Table VII-29 presents the capital costs for
softening systems that correspond to the flow rates utilized in   Table
VII-28.   Operating  costs  cannot be readily determined on a national
basis because they are  heavily  dependent  on  the  concentration  of
calcium  and  magnesium  in  the  recycled wastewater.  Lime costs can
range from roughly $0.025/1000 gal. of treated water, for  an  influent
hardness  of  100  mg/1  (as CaCO_3) , to $0.12/1000 gal. for an influent
hardness of 500 mg/1  (as CaC<33).  These costs can  vary  depending  on
the  desired  effluent  quality  and  on  the  influent water quality,
especially in regard to alkalinity.

NON-WATER QUALITY ASPECTS

Solid Wastes

In general, the treatment systems  described  in  Section  VI  produce
relatively  small amounts of solid waste with regard to large powdered
activated carbon  systems,  the  sludges  may  be  incinerated,   which
actually  reduces  or  eliminates  the  solid wastes produced by  these
biological  treatment  facilities.   For  smaller  powdered  activated
carbon  systems  that  do  not  include regeneration, the  inclusion of
powdered carbon in  the  sludge  has  been  shown  to  improve  sludge
settleability  (61),  so  that the volume of sludge requiring disposal
should not increase significantly, and in fact, may decrease.

Sludge  is  produced  from  lime  softening  systems  and   from   the
application  of  chromium removal techniques.  The Agency  anticipates,
however, that only a limited number of refineries would require   these
types  of  treatment.   The  cost of handling this sludge  has not been
included in the  cost  estimates  presented  in  this  section.   These
sludges   would   require   land   disposal,   because  they  are not
biodegradeable.  However, the cost and environmental  impact  of  this
type  of  disposal  is  assumed  to  be  minimal  on a national basis,
especially when compared to the large quantities of  sludges  produced
by  BPT type technology. The cost and environmental impact on a plant-
by-plant basis cannot be determined, because the quantity  of sludge is
heavily dependent on the hardness of the water being  treated  and  on
the chromium concentration in the wastewater.
                                194

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Air Pollution

The  carbon  regeneration  furnaces  associated with both granular and
powdered activated carbon systems will produce airborne  contaminants.
However,  the  equipment costs and operating requirements presented in
this  section  for  regeneration  systems  include  after-burners  for
hydrocarbon  and  carbon  monoxide removal and air scrubbing equipment
for particulate removal.

COSTS AND EFFECTIVENESS OF TECHNOLOGY OPTIONS

EPA  is  presently  considering  six  regulatory  options  for  direct
dischargers  and  two  regulatory  options  for  indirect dischargers.
Plant-by-plant costs for two of the six direct discharge  alternatives
and both of the indirect discharge alternatives are presented below.

Direct Discharge Options

Costs are presented in Table VTI-30 for the following options:

    Option  1  -  Set  BAT  regulations  based  upon  BPT  end-of-pipe
treatment with an average reduction in effluent flow of 27% (refer  to
discussion on reuse in Section VI).

    Option  2  -  Set BAT regulations based upon 52% pollutant loading
reductions.  This level of reduction can  be  achieved  via  52X  flow
reduction   (refer  to  discussion  on  reuse  in  Section  VI)  or  a
combination of limited flow reduction and end-of-pipe  treatment  such
as   powdered  activated  carbon  or  rotating  biological  contactors
(RBC's).  Cost for this option is based upon 27% flow reduction  (same
as  Option  1)   with  biological  enhancement using powdered activated
carbon or rotating biological contactors.

The following general assumptions have been  made  in  developing  the
costs:

    1.   In order to comply with a given BAT  option,  it  is  assumed
that  the  refinery must reduce its flow and install a "model" end-of-
pipe treatment system.  Refineries already having  these  technologies
or  planning  to  install  them have no costs.  It is assumed that all
refineries have some type of biological treatment already in place.

    2.   Although there are many methods to reduce  flow,  recycle  of
treated  wastewater  is  easily definable in terms of developing costs
and will be the assumed technique  for  each  refinery  that  requires
effluent  reduction.  Although a given refinery may choose a different
method, the costs allocated are expected to be conservatively high.
                               195

-------
    3.   Although a refinery may  choose  to  upgrade   its   biological
treatment  system  in other ways, rotating biological contactors  (RBC)
and powdered activated carbon can be readily priced as  add-on  systems.
Costs for these systems also are expected to  be  conservatively  high
estimates.

    it.   Although the costs are based on  one  approach to  achieving
effluent  quality,  there  are  many  alternatives  available  to this
industry.  A given refinery may choose to  add  sophisticated  end-of-
pipe  treatment  systems,  rather  than reduce flow.  Alternatively, a
refinery may choose to drastically reduce its flow and  install minimal
end-of-pipe treatment.  However, in order  to  produce  conservatively
high  costs  within  a  reasonable manhour expenditure, the  costs rely
heavily on end-of-pipe treatment alternatives, which can  be  directly
defined.   The  cost  procedures  include  reducing  flow  to  Option 1
requirements only.  Beyond this, sophisticated  end-of-pipe  treatment
 (biological  polishing  with  RBC's or powdered activated carbon) were
used  to  represent  the  costs  associated  with  meeting   Option   2
requirements.

    5-   Effluent flow is considered to be the flow indicated  in  the
NPDES  permit.   All  other forms of disposal  (i.e., evaporation, deep
well, etc.), except indirect discharge, were considered flow reduction
techniques.

    6.   Some refineries discharge partly  to  POTW's   and   partly  to
surface  waters.   Only  those  plants  that  directly  discharge  the
majority of their wastewaters were included  in  this   analysis.   For
these  plants,  the  wastewater discharged to a POTW was assumed to be
included with the direct discharge flow.

The costs were developed using a model technology for each   regulatory
option, as follows:

Option        Flow Reduction      End-of-Pipe Treatment Reqd

   1            27%                    Bio Treatment

   2            52%                     activated carbon or  RBC's

The  costs  for each refinery were generated by adding  those treatment
operations that did not exist in 1976, and were not listed as  planned
for  the  future,   Since biological treatment is essential  to meeting
the BPT guidelines? this level of treatment was assumed to  exist  at
all  direct  discharging refineries, whether or not they were  in-place
or were planned for the future.

Therefore, a plant was assumed to be meeting BPT with their  system  as
it   existed   in  1976,  with  the  inclusion  of  planned  treatment
                                196

-------
improvements.    Costs  were  then  calculated  for  those   additional
treatment  techniques  necessary  for completing the "model treatment"
train.

Planned flow reductions also were included in this analysis where they
were applicable to the costs  for  meeting  the  BAT  limitations.   A
detailed  description  of  those  flow reductions considered and those
ignored are presented in the March 1979 Cost Manual (151).

The energy requirements for meeting these two options are as follows:

    Option    Industry Energy Requirements, Kwh/yr

       1                 5,500,000
       2                 5,800,000

These estimates were calculated using four model  plant  sizes,  which
represent  four  equal segments of the direct discharge segment of the
industry, as follows:

                          Capacity,         Discharge Flow Rate,
    Model Plant            BBL/day               10« gal/day

         1                10,000                    0.052
         2                50,000                    0.3
         3                65,000                    0.86
         4               200,000                    5.1

Each model plant represents approximately 20 plants in its size range.

Estimates of the additional sludge generated by these technologies are
as follows:

                             Sludge Generation, Pounds
         Option              of Dry Solids Per Year

            1                           0
            2                      31,000,000

The estimate for Option 2 is based upon the installation  of  powdered
activated carbon at all plants.  This allows for a conservatively high
estimate  since plants that choose to use RBC's will only have a minor
increase in sludge generation.

Indirect Discharge Options

There are two indirect discharge  options  being  considered  by  EPA.
These are as follows:
                               197

-------
    Option  1  - Set standards based upon the treatment of chromium in
the cooling tower blowdown stream.

    Option 2 -  Set  standards  equal  to  BPT  end-of-pipe   treatment
technology, namely flow reduction, equalization, biological  treatment,
and filtration.

Table  VI1-31  presents  the  costs  associated with meeting Option 1.
Where the cooling tower blowdown rate was not known, it was  assumed to
be one-fourth of the total effluent flow.  The analysis also included
the cost of combining the effluents from multiple tower installations.
The costs presented for recycle of treated effluents  (Table  VII-28 and
Figure  VII-1)  were  used  to  obtain the estimates for the necessary
pumps and piping.

Table VII-32 presents the costs  associated  with  meeting   Option  2.
Costs  for the installation of in-plant control measures were assigned
to plants whose wastewater flow was greater than their calculated  BPT
flow.  These costs were obtained from the National Commission on Water
Quality  (20), which included the following control measures:

    Sour Water Stripping
    Conversion of Barometric Condensers
    Collection and Treatment of Contaminated Storm Water
    Collection and Treatment of Contaminated Ballast Water
    Spent Caustic Neutralization, Oxidation, or Disposal
    Reuse of Sour Water in Desalter
    Reuse of Coker Cutting Water

The  costs  presented in this document were updated to January 1977 by
using a correction factor of 1.184.  This factor  is  based   upon  the
Engineering News-Record index.

Costs   for   end-of-pipe   treatment  were  obtained  from   the  1974
development document (3), using alternatives B and C, as follows:

    B.   Biological treatment, consisting of activated  sludge  units,
         thickeners, digestors, and dewatering facilities.

    C.   Granular media filtration, consisting of filter  systems  and
         associated equipment.

These  costs also were corrected to January 1977 values using a factor
of 1.22 derived from the Engineering News-Record index.

Industry-wide energy consumption and sludge generation estimates  have
been  prepared for Option 1, chromium removal.  These estimates are as
follows:
                               198

-------
    Energy consumption, Kwh/yr - 1,900,000
    Sludge generation, pounds per year - 2,200,000

EPA developed these costs by estimating  the  values  for  each  plant
requiring chromium removal.

New Sources

The  Agency expects that grass roots refineries built in the next five
years will be in the size of 150,000 bbls/day, with at  least  topping
and  cracking  processes.   It  is  assumed  that such a refinery will
generate a flow of 3,340,000 gallons per day.   Based  upon  the  flow
rate,  the costs over BPT for meeting BAT Option 2 for this model size
plant include:

    Capital Costs       $615,000
    Operating Costs     $284,000

EPA has not calculated the costs for eliminating wastewater discharge.
However, the API publication "Water Reuse Studies"(150)  has  presented
such  costs  for  a 150,000 barrel per day grass roots refinery.  This
document estimates an additional investment, over BPT, of $9.5 million
with  an  annual  cost  of  $3.5  million,  including   interest   and
depreciation  (1977 dollars).

Effectiveness of Guidelines

Tables  VII-33 and VII-34 present the estimated pollutant removal from
BPT to the two BAT options  for  the  direct  discharging  refineries.
Pollutant  removals for BOD, TSS, Oil and Grease, chromium (hexavalent
and total), and phenol are presented.

Option 1 for pretreatment standards requires the removal  of  chromium
from  cooling  tower  blowdown to a daily maximum level of 1 mg/1.  In
addition, the Agency is proposing a maximum concentration of 100  mg/1
for  oil  and  grease and ammonia.  However, the data collected during
this study indicate that  these  values  are  of  the  same  order  of
magnitude   found   in   raw   refinery   wastewater;  therefore,  the
effectiveness of these limitations cannot be quantified.

Proposed NSPS for the model size plant of 150,000 bbls/day will remove
2.46 Ibs/day phenol, 3.9 Ibs/day hexavalent chromium, 6 Ibs/day  total
chromium, 308 Ibs/day total syspended solids, and 381 Ibs/day BOD.
                                199

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N>
O
o
                    Vl
                    uJ
I
                    r
                    D
                    Q.
                                   zoo
                        4        4>OO       &OO


                             CAPITAL  COST
                                                                          looo
                                                                          |OOO
                                                                                              1400
                                                                                                        1600
                                                                                                                  I BOO
                                                                FIGURE VII-1
                                                   Pumping Capital Cost vs.  Pumping Distance

-------
N>

O
uJ

f
  •«l»
ol
VJ


I
A

vff




I
                                          too
                                                    2.00
                                                               300
                                                400        soo



                                                    ,   \OOO
                                                                                               6,00
                                                                                                          700
                                                                      FIGURE VII-2



                                                           Refinery  Size vs.  Pumping  Distance

-------
to
o
to
                                                                                TABLE  VII-2


                                                                          RAW  WASTEWATER  EQUALIZATION SYSTEMS

                                                                              CAPITAL AND OPERATING COSTS
                                                                                                  Capital Cost, Dollars
Description


Detention tank, 12 hours detention,
steel shell on concrete pad
Pumps, and associated controls,
installed
Subtotal
Piping^ installed (15%)
Total Installed Cost
Engineering
Contingency
Total Capital Cost
2
Land Requirements, ft

Pumping
Maintenance (3% of Capital Cost)
Total Annual Cost
380 /day
(0.1 x 10°)
gal/d
$ 30,000

8,000

$ 38,000
5,700
$ 43,700
6,650
6,650
$ 57,000
585

$ 140
1,700
$ 1 ,840
3800 3/day 19
(1.0 x 10B)
gal/d
$ 116,000

30,000

$ 146,000
22,000
$ 168,000
26,000
26,000
$ 220,000
5,780
Annual
$ 1,400
6,600
$ 8,000
,000 3/day
(5 x 106)
gal/d
$ 346,000

87,000

$ 433,000
65,000
$ 498,000
75,000
75,000
$ 648,000
28,200
Operating
$ 7,000
19,500
$ 26,500
38,000 3/day
(10 x 10B)
gal/d
$ 595,000

149,000

$ 744,000
117,000
$ 861 ,000
129,500
129,500
$1,120,000
57,600
Costs, Dollars
$ 14,000
33,600
$ 47,600
76,000 3/day
(20 x 10B)
gal/d
$1,020,000

255,000

$1,275,000
192,000
$1,467,000
221 ,500
221,500
$1,910,000
113,000

$ 28,000
57,300
$ 85,300
                               Note:   The Depreciation factor has been omitted from this  analysis  due  to  the  fact  that  it will be  included

                                      separately in the Economic Impact Analysis  Supplement.

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                                                                                 TABLE  VII-3
to
o
10
                                                                     ROTATING  BIOLOGICAL CONTACTORS (RBC's)
                                                                              AS ROUGHING SYSTEMS
                                                                              EQUIPMENT COST BASIS
                                                                            AND ENERGY REQUIREMENTS
Equipment Size
Description

Design Percent Removal
of BOD
Number of Units
Shaft Lengths, each
Total Square Feet of Surface Area
Manpower Requirements, hours
Power Requirements, kwh/yr
380 m3/day
(0.1 x 10 )
gal/d
50
1
15
75,000

500
33,000
3800 Pi3/day
(1.0 x 10 )
gal/d
50
6
20
630,000
Annual
750
294,000
19,000 m3/day 38
(5 x 10 )
gal/d
50
24
25
3,200,000 6,
Operating and Energy
1,000
1,180,000 2,
,000 o>3/day
(10 x 10 )
gal/d
50
48
25
400,000
Requirements
1,500
360,000
76,000 "»3/day
(20 x 10 )
gal/d
50
96
25
12,800,000

2,000
4,720,000

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                                                                                      TABLE VII-4

                                                                            ROTATING BIOLOGICAL CONTACTORS (RBC's)
                                                                                      AS ROUGHING FILTERS
                                                                                  CAPITAL AND OPERATING COSTS
                                                                                                       Capital  Cost,  Dollars
tO
o
Description

RBC Units, Steel Shell,
Fiberglass Cover
Piping
Total Equipment Cost
Installation (50%)
Total Constructed Cost
Engineering
Contingency
Total Capital Cost
Land Required, ft^
Power
Labor
Maintenance (3% of Total Capital Cost)
380 ra3/dav
(0.1 x 10°)
gal/d
$ 46,000
5,000
51 ,000
25,500
76,500
11,750
11,750
$100,000
420

$ 1,500
5,000
3,000
3800 ra3/day
(1.0 x 10°)
gal/d
$340,000
35,000
375,000
187,500
562,500
84,750
84,750
$732,000
2,800

$ 12,000
7,500
22,000
19,000 ra3 /day 38
(5 x 10°)
gal/d
$1,590,000
160,000
1,750,000
875,000
2,625,000
397,500
397,500
$3,420,000
13,500
Annual Operating
$ 48,000
10,000
103,000
,000 ro /day
(10 x 10°)
gal/d
$3,170,000
317,000
3,487,000
1,744,000
5,231,000
784,500
784,500
$6,800,000
27,000
Costs*
$ 95,000
15,000
204 ,000
76,000 ro3/day
(20 x 10°)
gal/d
$6,340,000
634,000
6,974,000
3,487,000
10,461,000
1,569,500
1,569,500
$13,600,000
54,000

$ 190,000
20,000
408,000
                                    Total Annual Cost
$  9,500     $ 41,500
$  161,000     $  314,000     $   798,000
                                    Note:   The depreciation factor has been omitted from this analysis due to the fact that it will be included separately
                                           in the  Economic Impact Analysis Supplement.

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                                                                                       TABLE  VII-5
to
o
(J\
                                                                                 PONDERED ACTIVATED CARBON
                                                                                   EQUIPMENT COST BASIS
                                                                                  AND ENERGY REQUIREMENTS
                                                                                    80 mg/1 DOSAGE RATE
                                                                                                  Equipment Size
Description

Powdered Carbon Feed Tanks (2 each)
Capacity, gallons (Based on feed
concentration of one pound
carbon/gallon water)
Feed Rate pounds/day

380m /day
(0.1 x 10 )
gal/d
700
67

3800m /day 19
(1.0 x 10C)
gal/d
7,000
670
Annual Operating
,000 m /day
(5 x 10 )
gal/d
35,000
3,350
and Energy
38,000 in/day
(10 x 10 )
gal/d
70,000
6,700
Requirements
76,000m /day
(20 x 10 )
gal/d
140,000
13,400

                                 Manpower Requirements, hours

                                 Miscellaneous Power Requirements,
                                 kWh/yr
                                                                            400
                                                                                          540
                                                                                                          940
                                               1,240


25,000        50,000         125,000         200,000
  1,940


375,000

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                                                                              TABLE VII-6

                                                                        POWDERED ACTIVATED CARBON
                                                                              CAPITAL COSTS
                                                                           80 mg/1 DOSAGE RATE
to
                        Total Capital Cost
                                                                                     Capital  Costs,  Dollars
Description

Powdered Carbon Feed System
Piping
Total Equipment Cost
Installation (50%)
Total Constructed Cost
Engineering
Contingency
380 m3/dav
(0.1 x 10 )
gal/d
510,000
1,000
11,000
6,000
17,000
9,000
9,000
3800 m /day
(1.0 x 10 )
gal/d
530,000
3,000
33,000
16,500
49,500
10,000
10,000
19,000 m /day
(5 x 10 )
gal/d
545,000
4,500
49,500
24,800
74,300
11,350
11,350
38,000 m /day
(10 x 10 )
gal/d
560,000
6,000
66,000
33,000
99,000
15,500
15,500
76,000 ™ /day
(20 x 10 )
gal/d
5100,000
10,000
110,000
55,000
165,000
25,000
25,000
                                                               535,000
                                                                             569,500
                                                                                             597,000
                                                                                                            5130,000
                                                                                                                             5215,000
                        Land Requirements,  ft
                                                                   100
                                                                                 200
                                                                                                 900
                                                                                                               1,300
                                                                                                                                1,700

-------
                                                                                       TABLE VII-7



                                                                                POWDERED ACTIVATED CARBON

                                                                                 ANNUAL OPERATING COSTS

                                                                                   80 mg/1 DOSAGE RATE
                                                                                             Annual Costf Dollars
Description

Carbon Hake-Up
Miscellaneous Power Requirements
Labor ($10/manhour)
Maintenance (3% of total Capital Cost)
380 m /day
(0.1 x 10 >
gal/d
$ 7,400
1,000
4,000
1,000
3800 m 3/day
(1.0 x 10 )
gal/d
$74,000
2,000
5,400
2,000
19,000m /day
(5 x 10 )
gal/d
$370,000
5,000
9,400
3,000
38,000m 3/day
(10 x 10 )
gal/d
$740,000
8,000
12,400
4,000
76,000"! /day
(20 x 10 )
gal/d
$1,480,000
15,000
19,400
6,600
to
o
•J
                                Total Annual Cost                       $13,400      $83,400        $387,400        $764,400        $1,521,000
                                The depreciation  factor has been omitted from this analysis due to the fact that it will be included separately
                                in the Economic Impact Analysis Supplement.

-------
to
o
00
                                                                                      TABLE VI1-8

                                                                               POWDERED ACTIVATED CARBON
                                                                             COMPARISON OF OPERATING COSTS
                                                                          CARBON REGENERATION VS. THROW-AWAY
                                                                                 80 mg/1 DOSAGE  RATE
                                                                                                  Regenerated
Item


Capital Cost
Carbon Make-Up
Furnace Power
Miscellaneous Power
Labor
Maintenance ( 3% )
(15%)
Depreciation (27%)
Total Annual Cost

Capital Cost
Carbon Make-Up
Labor
Maintenance ( 3% J
Miscellaneous Power
Depreciation (27%)
Total Annual Cost
Cost for Sludge Dewatering
Annual Cost with Sludge Dewatering
Cost for Land Disposal
Annual Cost with Land Disposal
380 m3/day
(0.1 x 10")
gal/d
$735,000
5 2,200
5,000
1,000
91,600
1,000
105,000
200,000
$405,800

5 35,000
5 7,400
4,000
1,000
1,000
9,500
$ 22,900
5 20,000
$ 42,900
4,000
5 46,900
3800 m3/day
(1

$1
5






$

$
5




$
5
$

$
.0 x 10 )
gal/d
,000,000
22,000
19,000
2,000
93,000
2,000
140,000
270,000
548,000

39,500
74,000
5,400
2,000
2,000
17,600
101,000
76 , 000
177,000
40,000
217,000
19,000 m /day
(5 x 10 )
gal/d
$1,650,000
$ 110,000
44 , 000
5,000
97,000
3,000
233,000
446,000
$ 938,000
Non-Regenerated
$ 97,000
$ 370,000
9,400
3,000
5,000
26,200
$ 413,600
$ 137,000
$ 550,000
200,000
$ 750,000
38,000 m3/day
(10 x 10 )
gal/d
$2,300,000
$ 220,000
76,000
8,000
100,000
4,000
328,000
621,000
$1,357,000

$ 130,000
$ 740,000
12,400
4,000
8,000
35,100
$ 799,500
$ 226,000
$1,025,000
400,000
$1,425,000
76,000 m /day
(20 x 10 )
gal/d
$3,250,000
$ 440,000
132,000
15,000
108,000
6,600
455,000
878,000
$2,034,600

$ 215,000
$1,480,000
19,400
6,600
15,000
58,000
$1,579,000
$ 335,000
$1,914,000
800,000
$2,714,000

-------
                                                                                       TABLE VII-9
                                                                                 POWDERED ACTIVATED CARBON
                                                                                   EQUIPMENT COST BASIS
                                                                                  AND ENERGY REQUIREMENTS
                                                                            INCLUDING COSTS FOR SLUDGE DISPOSAL
                                                                                    80 rog/1 DOSAGE RATE
                                                                                                      Equipment Size
N>
o
10
Description


Powdered Carbon reea Tanks (2 each)
Capacity, gallons (Based on feed
concentration of one pound
carbon/gallon water)
Feed Rate, Ib/d
Sludge handling and/or regeneration
system, Ib/d dry solids

Carbon make-up Ib/d
furnace power requirements
Fuel, Btu/h
Connected np
380 m /d 3800 m /d
(0.1 x 10°) (1.0 x 10 )
gal/d gal/d
700 7,000



67 670
290 2,900

Annual
67 670

N.A. N.A.
N.A. N.A.
19,00001 A3 38
(5 x 10 )
.gal/d
35,000



3,350
14,600

Operating and Energy
3,350

N.A. 2
N.A.
,OOOm-3/d
(10 x 10 )
gal/d
70,000



6,700
29,000

Requirements
2,000

,500,000
100
76,000 » /d
(20 x 10 )
gal/d
140,000



13,400
58,000


4,000

4,500,000
140
                                 Manpower requirement, hours
                                                                            400
                                                                                          540
                                                                                                          940
                                                                                                                       10,000
                                                                                                                                       10,700

-------
                                                                                TABLE VII-10
to
M
O
                                                                            POWDERED ACTIVATED CARBON
                                                                                  CAPITAL COSTS
                                                                       INCLUDING COSTS FOR SLUDGE DISPOSAL
                                                                               80 mg/1 DOSAGE RATE
                                                                                                    Capital Costs, Dollars
Description (0.
Powdered Carbon Feed System
Solids Dewatering System
Regenerated Carbon Acid Nash
System
Subtotal
Piping (10%)
Total Equipment Cost
Installation (50%)
Total Constructed Cost
Engineering
Contingency
Subtotal
Activated Carbon Regeneration
System (Installed)
Contingency (For Utility
Hook-up , etc . )
Engineering for Carbon
Regeneration System
Total Capital Cost
Land Requirements, ft
380 p3/d
1x10 gal/d)
? 10, 000
—

10,000
1,000
11,000
5,500
16,500
9,000
9,000
35,000
—
535,000
100
3800 m3/d
(1.0x10 gal/d)
$30,000
—

30,000
3,000
33,000
16,500
49,500
10,000
10.000
69,500
—
$69,500
200
19,000 m3/d
(5x10 gal/d)
$45,000
—

45,000
4,500
49,500
24,800
74,300
11,350
11,350
97,000
—
$97,000
900
38,000 m3/d
(10x10 gal/d)
$60,000
397,000
40,000
497,000
49,700
546,700
273,400
820,100
119,950
119,950
1,060,000
900,000
190,000
150,000
$2,300,000
3,000
76,000 m3/d
(20x10 gal/d)
$100,000
585,000
60,000
745,000
74,500
819,500
410,000
1,229,500
185,250
185,250
1,600,000
1,200,000
250,000
200,000
$3,250,000
4,500

-------
                                                                                   TABLE VII-11
                                                                              PONDERED ACTIVATED CARBON
                                                                               ANNUAL OPERATING COSTS
                                                                         INCLUDING CREDIT FOR SLUDGE DISPOSAL
                                                                                 80 mg/1 DOSAGE RATE
ro
                                                                                                      Annual Cost, Dollars
Description


Carbon Make-Up
Furnace Power
Miscellaneous Power Requirements
Labor (510/manhour)
Sludge Disposal Credit
Maintenance
380 m3/day
(0.1 x 10 )
gal/d
$7,400
	
1,000
4,000
—
1,000
3800 m3/day
(1.0 x 10 )
gal/d
$74,000
	
2,000
5,400
	
2,000
19,000 m3/day
(5 x 10 )
gal/d
$370,000
	
5,000
9,400
	
3,000
38,000 m3/day
(10 x 10 )
gal/d
$220,000
76,000
8,000
100,000
(-1400,000
332,000
76,000 m3/day
(20 x 10 )
gal/d
$440,000
132,000
15,000
108,000
<-)800,000
461,600
                              Total Annual Cost
                                                                      $13,400
                                                                                   $ 83,400
                                                                                                   $387,000
                                                                                                                   $336,000
                                                                                                                                  $ 356,000
                              Note:
                               The depreciation factor has been omitted from this analysis due to the fact that it will be included separately
                               in the Economic Impact Analysis Supplement.

-------
                                                                                     TABLE VII-12
                                                                                   TERTIARY  FILTRATION
                                                                      EQUIPMENT  COST  BASIS AND  ENERGY REQUIREMENTS
NJ
Equipment Cost Basis
Description
Filter Description
(all units are
automatic and
air scoured)
Bed depth, ft
Operation type
Media type
Pumping,
kWh/yr
Labor,
Manhours/year
380 m3/ day
(0.1 X 106gal/d)
2 units
5' diam. , steel
4
Gravity
Dual media

3,440
400
3800m 3/day
(1 X 106gal/d)
2 units
11' diam., steel
4
Gravity
Dual media
Annual Operating
34,400
500
19,000 .niVday
(5 X 106gal/d)
1 unit, 4-35'square
cells, concrete
4
Gravity
Dual media
38,000 ntVday
(10 X 106gal/d)
1 unit, 4-47 'square
cells, concrete
4
Gravity
Dual media
76,000 mVday
(20 X 106gal/d)
2 units, 47' square
cells, concrete
4
Gravity
Dual media
and Energy Requirements
172,000
600
344,000
700
688,000
800

-------
                                                                                TABLE VII-13
to
H
W
                                                                              TERTIARY  FILTRATION
                                                                           CAPITAL AND  OPERATING COSTS
                                                                                          Capital  Cost,  Dollars
Ascription

Filtration Units Installed
Interconnecting Piping, Installed
Pumps, Installed
Total Installed Cost
Engineering
Contingency
Total Capital Cost
Land Requirement, ft2
Pumping
Labor
Maintenance (3% of Capital Cost)
Total Annual Cost
Note: The Depreciation factor has
380 m3/dav
(0.1 x 10°)
gal/d
$ 25,000
3,000
5,000
33,000
6.000
6,000
$ 48,000
200

$ 140
4.000
1,400
$ 5,540
3800 m3/day
(1.0 x 10")
gal/d
$100,000
10.000
15,000
125,000
20,000
20.000
$165.000
700
Annual
$ 1 ,400
5.000
5,000
$ 11,400
19,000 m /day
(5 x 10°)
gal/d
$250.000
25,000
42,000
317.000
49,000
49,000
$415,000
5,000
Operating Cost,
$ 7,000
6,000
12,500
$ 25,500
38,000 m3/day
(10 x 10°)
gal/d
$350,000
35,000
60,000
451 .000
69,500
69,500
$590,000
9,000
Dollars
$ 14,000
7,000
18,000
$ 39,000
been omitted from this analysis due to the fact that it will
76,000m3/day
(20 x 10 }
gal/d
$600,000
60,000
100,000
770.000
115,000
115,000
$1,000,000
18,000

$ 28.000
8,000
30,000
$ 66,000
be included
                                   separately in the Economic Impact Analysis Supplement.

-------
                                                                            TABLE VII-14
                                                                    Granular Activated Carbon
to
                     Description
Activated Carbon Units

Carbon, ft3 Total

Automatic Controls Included

Furnace size, Ib/d
      of carbon
                    Carbon Make-up,  lb/d
                       (10% make-up)

                    Furnace Power Require-
                      ments
                        Fuel, Btu/hr
                        Connected  hp

                    Pumping Power Require-
                      ments  kWh/yr

                    Manpower Requirements,
                      hours
380 m3/day
(0.1x106 ga]/d)
Three-4'diam.
x 13' high
281
1 No
N.A.
125
N.A.
N.A.
Equipment Cost Basis
and Energy Requirements
Equipment Size
3800 nrVday 19,000 m3/day 38,000 m3/day 76,000 m3/day
(l.OxlO6 gal/d) (5xl06 gal/d) (IQxlO6 gal/d) (20xl06 gal/d)
Three-H1 diam. Nine-12' diam. Fifteen-121 diara. Thirty-121 diam.
x 18' high x 25' high x 30' high x 30' high
2800 14,000 28,000 56,000
Yes Yes Yes Yes
1250 6,250 12,500 25,000
Annual Operating and Energy Requirements
125 625 1,250 2,500
500,000 800,000 1,500,000 2,800,000
40 50 60 80
                                11,400


                                 2,100
114,000


  9,800
570,000


 10,500
1,140,000


   11,500
2,280,000


   12,500

-------
                                                                                      TABLE VII-15
ro
                                                                             GRANULAR ACTIVATED CARBON
                                                                                   CAPITAL COSTS
                                                                                                     Capital Costs,  Dollars
Description


Activated Carbon Units
Pumping S Misc. Equip. (10%)
Piping (10%)
Total Equipment Cost
Installation (5O%)
Total Constructed Cost
Engineering
Contingency
Subtotal
Activated Carbon Regeneratior
Contingency (For utility hook-
Engineering for Carbon Regeneration
System
380 ™3/day
(0.1 XlO )
gal/d
$50,000
5,000
5,000
60,000
30,000
90,000
40,000
20,000
150,000



3800 m3/day
(1.0 XlO )
gal/d
$325,000
32 , 500
32,500
390,000
195,000
585,000
85,000
80,000
750,000


50,000
19,000 03/day
(5 X10°)
gal/d
$1,500,000
150,000
150,000
1,800,000
900,000
2,700,000
400,000
400,000
3,500,000


50,000
38,000 m3/day
(10 XlO )
gal/d
$2,600,000
260,000
260,000
3,120,000
1,560,000
4,680,000
710,000
710,000
6,100,000


80,000
76,000 m3/day
(20 XlO )
gal/d
$5,000,000
500,000
500,000
6,000,000
3,000,000
9,000,000
1,350,000
1,350,000
11,700,000


100,000
                                   Total Capital Cost
                                                                      $150,000    $1,160,000
                                                                                                 $4,100,000
                                                                                                                 $6,920,000
                                                                                                                                $12,700,000
                                   Land Requirements, ft
                                                                           300
                                                                                       1,500
                                                                                                      3,500
                                                                                                                      5,500
                                                                                                                                     12,000

-------
                                                                               TABLE VII-16
                                                                        GRANULAR ACTIVATED CARBON
                                                                         ANNUAL OPERATING COSTS
NJ
                              Total Annual Cost
                                                                                               flnnual  Costs,  Dollars
Description

Carbon Make-Up
Furnace Power
Pumping
*
Labor (510/manhour)
Maintenance (3% of total
Capital Cost)
380 ,,,3/day
(0.1 X106)
gal/day
528,000
	
500
21,000
4,500
3800 m3/day
(1.0 X106)
gal/day
528,000
19,000
5,000
98,000
35,000
19,000 m3/day
(5 X106)
gal/day
5i37,000
27,000
25,000
105,000
123,000
38,000 m3/day
(10 X106)
gal/day
5275,000
46,000
50 , 000
115,000
208,000
76,000 ™3/day
(20 X106)
gal/day
5550,000
82,000
100,000
125,000
381,000
                                                                 $54,000
                                                                             5185,000
                                                                                             5417,000
                                                                                                            5694,000
                                                                                                                           51,238,000
                              NOTE:  The depreciation factor has been omitted from this analysis due to the fact that it will  be included
                              separately in the Economic Impact Analysis Supplement.
                                 The manpower requirements were obtained from the "Process Design Manual for Carbon Adsorption,
                                 Environmental Protection Agency Technology Transfer Series, October 1973.   Labor includes operation,
                                 maintenance, and laboratory personnel requirements.

-------
                                                                                TABLE VII-17
                                                                         POWDERED ACTIVATED CARBON

                                                                EQUIPMENT COST BASES AND ENERGY REQUIREMENTS

                                                                            ISO mg/1 DOSAGE RATE
                                                                                               Equipment Size
to
H1
•J
Description (0.
Powdered Carbon Feed Tanks
(2 each) Capacity, gallons
(Based on feed concentration
of 1 Ib carbon/gal water)
Feed Rate Ib/d
Sludge Handling and/or
Regeneration System,
Ib/d dry solids
Carbon Make-Up Ib/d
(25% make-up)
Furnace Power Requirements
Fuel, Btu/h
Connected hp
380 m3/d
, 1x10 gal/d)
1,000
125
335
Annual
125
N.A.
N.A.
3800 m3/d
(1.0x10 gal/d)
10,000
1,250
3,350
Operating and Energy
1,250
N.A.
N.A.
19,000 m3/d
(5x10 gal/d)
43,000
6,250
16,700
Requirements
6,250
N.A.
N.A.
38,000 m3/d
(10x10 gal/d)
87,000
12,500
33,500
12,500
N.A.
N.A.
76,000 m3/d
(20x10 gal/d)
175,000
25,000
66,700
8,350
4,500,000
140
                                Manpower Requirements, hours     400
                                                                                   540
                                                                                                     940.
                                                                                                                      1,240
                                                                                                                                      10,700

-------
                                                                                TABLE VII-18
N>
H
00
                                                                          POWDERED ACTIVATED CARBON

                                                                                CAPITAL COSTS

                                                                            150 mg/1 DOSAGE RATE
                                                                                               Capital Costs, Dollars
380 m3/d 3800 m3/d
Description (0.1x10 gal/d) (1.0x10 gal/d)
Powdered Carbon Feed System 515,000 545,000
Solids Dewatenng System
Regenerated Carbon Acid Wash
System — —
Subtotal 15,000 45,000
Piping (10%) 1,500 4,500
Total Equipment Cost 16,500 49,500
Installation (50%) 8,500 24,500
Total Constructed Cost 25,000 74,000
Engineering 9,000 13.000
Contingency 9,000 13,000
Subtotal 43,000 100,000
Activated Carbon Regeneration
System (Installed)
Contingency (For Utility
Hook-up, etc.)
Engineering for Carbon
Regeneration System
19,000 m3/d 38,000 m3/d 76,000 m3/d
(5x10 gal/d) (10x10 gal/d) (20x10 gal/d)
565,000 590,000 5150,000
615,000
60,000
65,000 90,000 825,000
6,500 9,000 83,000
71,500 99,000 908,000
35,500 49,500 454,000
107,000 148,500 1,362,000
16,500 22,250 207,500
16,500 22,250 207,500
140,000 193,000 1,777,000
1,300,000
280,000
200,000
Total Capital Cost            $ 43,000        $ 100,000


Land Requirements, ft              100              800
                                                                                                  5140,000


                                                                                                     2,000
5193,000


   3,000
53,557,000



     4,500

-------
                                                                                 TABLE VII-19

                                                                           PONDERED ACTIVATED CARBON
                                                                            ANNUAL OPERATING COSTS
                                                                             150 tng/1 DOSAGE RATE
                                                                                                   Annual Cost,  Doliar3
to
H»
vo
Description
Carbon Hake-Up
Furnace Power
Miscellaneous Power
Requirements
Labor ($10/man-hour)
Maintenance
Total Annual Cost
380 m3/d
(0.1x10 gal/d)
$13,900
--
1,000.
4,000
1,000
$19,900
3800 m3/d
(1.0x10 gal/d)
$139,000
—
2,000
5,400
2,000
$149,400
19,000 m3/d
(5xl06gal/d)
$694,000
—
5,000
9,400
3,000
$711,400
38,000 m3/d
(10x10 gal/d)
$1,388,000
—
8,000
12,400
4,000
$1,412,400
76,000 m3/d
(20x10 gal/d)
$ 825,000
132,000
15,000
108,000
491,000
$1,571,000
                                Note:

                                The  Depreciation factor has been omitted from this  analysis due  to the  fact  that it will  be  included separately
                                in the  Economic  Impact Analysis  Supplement.

-------
                                                                            TABLE VII-20
to
NJ
O
                                                                                PACT
                                                                    COMPARISON OF OPERATING COSTS
                                                                 CARBON REGENERATION VS. THROW-AWAY
                                                                        150 mg/1 DOSAGE RATE
                                                                                                      Regenerated
Description (0
Capital Cost
Carbon Make-up
Furnace Power
Miscellaneous Power
Labor
Maintenance (3%)
(15%)
Depreciation (254)
Total Annual Cost
380 m /d
.1x10 gal/d)
$743,000
4,130
5,000
1,000
91,600
1,000
105,000
200,000
5407,730
3800 m /d
(1.0x10 gal/d)
51, 035, 000
41,300
19,000
2,000
93,000
2,000
140,000
280,000
$577,300
19,000 m /d
(5x10 gal/d)
$1,743,000
207,000
44,000
5,000
97,000
3,000
240,000
471,000
$1,067,000
38,000 m /d
(10x10 gal/d)
$2,463,000
413,000
76,000
8,000
100,000
4,000
343,000
665,000
$1,609,000
76,000 m /d
(20x10 gal/d)
$3,557,000
825,000
132,000
15,000
108,000
6,000
485,000
961,000
$2,532.000
Non-Regenerated
Capital Cost
Carbon Make-up
Labor
Maintenance (3*)
Miscellaneous Power
Depreciation (27%)
Total Annual Cost
Cost for Sludge Dewatering
Annual Cost with Sludge
Dewatering
Cost for Land Disposal
5 43,000
13,900
4,000
1,000
1,000
11,600
$ 31,500
25,000
$ 56,500
5,000
$100,000
139,000
5,400
2,000
2,000
27,000
$175,400
95 , 000
$270,400
50,000
$140,000
694,000
9,400
3,000
5,000
37,800
$749,200
171,000
$920,200
250,000
$193,000
1,388,000
12,400
4,000
8,000
52,100
$1,464,500
282,000
$1,746,500
500,000
$322,000
2,775,000
19,400
6,600
15,000
87,000
$2,903,000
419,000
$3,322,000
1,000,000
                            Annual Cost with Land
                            Disposal
S 61,500
                                                                           $320,400
                                                                                            $1,170,200
                                                                                                               $2,246,500
                                                                                                                                 $4,322,000

-------
                                                                          TABLE VI1-21

                                                                    POWDERED ACTIVATED CARBON
                                                          EQUIPMENT COST BASES AND ENERGY REQUIREMENTS
                                                               INCLUDING COSTS FOR SLUDGE DISPOSAL
                                                                      150 mg/1 DOSAGE RATE
to
10
Description (0.
Powdered Carbon Feed Tanks
(2 each) Capacity, gallons
(Based on 'feed concentration
of 1 Ib carbon/gal water)
Feed Rate Ib/d
Sludge handling and/or
Regeneration System,
Ib/d dry solids
Carbon Make -Up Ib/d
(25% make-up)
Furnace Power Requirements
Fuel, Btu/h
Connected hp
380 m3/d
. 1x10 gal/d)
1,000
125
335
Annual
125
N.A.
N.A.
3800 m3/d
(1.0x10 gal/d)
10,000
1,250
3,350
Operating and Energy
1,250
N.A.
N.A.
Equipment
19,000 m3/d
(5x10 gal/d)
43,000
6,250
16,700
Requirements
2,100
1,300,000
80
Size
38,000 m3/d
(10x10 gal/d)
87,000
12,500
33,500
418
2,500,000
100
76,000 m3/d
(20x10 gal/d)
175,000
25,000
66,700
8,350
4,500,000
140
                          Manpower Requirements, hours
                                                           400
                                                                             540
                                                                                             9,700
                                                                                                               10,000
                                                                                                                                10,700

-------
                                                                               TABLE VII-22
Ml
to
NJ
                                                                         POWDERED ACTIVATED CARBON

                                                                               CAPITAL COSTS

                                                                    INCLUDING COSTS FOR SLUDGE DISPOSAL

                                                                           150 mg/1 DOSAGE RATE
                                                                                              Capital Costs, Dollars
Description (0.
Powdered Carbon Feed System
Solids Dewatering System
Regenerated Carbon Acid Wash
System
Subtotal
Piping (10%)
Total Equipment Cost
Installation (50)
Total Constructed Cost
Engineering
Contingency
Subtotal
Activated Carbon Regeneration
System (Installed)
Contingency (For Utility
Hook-up, etc.)
Engineering for Carbon
Regeneration System
Total Capital Cost
2
Land Requirements, ft
380 m3/d
1x10 gal/d)
$15,000
—

15 , 000
1,500
16,500
8,500
25,000
9,000
9,000
43,000
—
543,000
100
3800 m3/d
(1.0x10 gal/d)
$ 45,000
—

45 , 000
4,500
49 , 500
24,500
74 , 000
13,000
13,000
100,000
—
5100,000
800
19,000 m3/d
(5x10 gal/d)
5 65,000
250,000
20 , OOP
335,000
34 , OOP
369,000
185,000
554,000
82,000
82,000
718,000
750,000
160,000
115,000
51,743,000
2,000
38,000 m3/d
(10x10 gal/d)
5 90,000
415,000
40,000
545,000
55,000
602,000
300,000
900,000
131,500
131,500
1,163,000
950,000
200,000
150,000
52,463,000
3,000
76,000 mJ/d
(20x10 gal/d)
5150,000
615,000
60,000
825,000
83,000
908,000
454,000
1,362,000
207,500
207,500
1,777,000
1,300,000
280,000
200,000
53,557,000
4,500

-------
tSJ
10
                                                                                 TABLE VII-23

                                                                          POWDERED ACTIVATED CARBON
                                                                           ANNUAL OPERATING COSTS
                                                                    INCLUDING CREDIT FOR SLUDGE DISPOSAL
                                                                            150 mg/1 DOSAGE RATE
                                                                                                  Annual Cost, Dollars
Description
Carbon Make-up
Furnace Power
Miscellaneous Power
Requirements
Labor ($10/man-hour)
Sludge Disposal Credit
Maintenance
Total Annual Cost
380 m3/d
(0.1x10 gal/d)
$13,900
—
1,000
4,000
—
1,000
$19,900
3800 m3/d
(1.0x10 gal/d)
$139,000
—
2,000
5,400
—
2,000
$148,400
19,000 m3/d
(5x10 gal/d)
$207,000
55,000
5,000
97,000
(-)250,000
243,000
$357,000
38,000 m3/d
(10x10 gal/d)
$413,000
95,000
8,000
100,000
(-)500,000
347,000
$463,000
76,000 m3/d
(20x10 gal/d)
$825,000
165,000
15,000
108,000
(-) 1,000, 000
491,000
$604,000
                                Note:

                                The Depreciation factor has been omitted from this analysis due to the fact that it will be included separately
                                in the Economic Impact Analysis Supplement

-------
                         TABLE VI1-24
              SUPPLEMENTAL  ECONOMIC COST INFORMATION
                    CAPITAL AND OPERATING COSTS
            FOR  10,000 GALLON PER DAY TREATMENT SYSTEMS
Treatment System
Equalization
Rotating Biological
Contactors
Filtration
Powdered Activated
Capital Cost,
Dollars
$ 12,000
50,000
35,000
35,000
Annual Operating
Dollars*
$ 400
6,100
3,000
4,300
Cost




  Carbon

Granular Carbon              60,000                   10,000
Note:  The depreciation factor has been omitted from this  analysis due to
       the fact that it will  be included separately in the Economic Impact
       Analysis Supplement.
                              224

-------
                                TABLE VII-Z5
                      COOLING TOWER  SLOWDOWN RATES
                      PETROLEUM REFINING INDUSTRY
                       (MILLION GALLONS PER DAY)
REFINERY
 NUMBER
   i
   2
   3
   1
   6

   8
   9
  10
  11
  12
  13
  15
  16
  17
  IS
  19
  20
  21
  24
  25
  26
  29
  30
  31
  32
  33
  35
  36
  37
  38
  39
  40
  41
  42
  43
  44
  45
  46
  48
  49
  50
  51
  52
  53
  54
  55
  56

SLOWDOWN
0.008000
0.014400
UNKNOWN
NOT APR.
NOT APR.
0.030000
UNKNOWN
0.001440
0.015000
1.794998
0.002000
1 .014999
0.028200
0.069300
0.005000
0.021440
•0.001500
0.320000
0.011250
0.010500
NOT APP.
0.065000
0.167000
0.074500
0.330000
0.033200
10.000000
0.840000
0.110000
NOT APP.
0.005500
1.834998
0.702000
0.060000
UNKNOWN
1.013998
0.012000
0.550000
UNKNOWN
0.816999
0.145000
0.141000
0.170000
0.025500
NOT APP.
NOT APP.
0.035500
UNKNOWN
NOT APP.
0.650000
REFINERY
NUMBER
57
58
59
60
61
62
63
64
65
66
67
68
70
71
72
73
74
76
77
78
79
80
31
82
83
84
85
86
87
38
89
90
91
92
93
94
95
96
97
98
99
100
102
103
104
105
106
107
108
109

SLOWDOWN
6.300000
0.268600
50.167191
0.850250
1.400000
1.024999
0.298500
1.000999
0.943500
UNKNOWN
3.229999
2.447998
UNKNOWN
0.095500
0.022000
0.138200
0.157000
0.826000
0.198000
0.015000
> 0.0
0.370000
0.242000
6.000000
1.014999
UNKNOWN
2.539797
0.147700
NOT APP.
0.072500
UNKNOWN
0.007000
0.003600
2.023998
0.021040
0.432000
UNKNOWN
6.011999
0.008354
0.775000
NOT APP.
NOT APP.
UNKNOWN
0.005000
2.589997
NOT APP.
0.524000
0.010000
UNKNOWN
0.185000
REFINERY
NUMBER
110
111
112
113
114
115
116
117
118
119
120
121
122
124
125
126
127
128
129
130
131
132
133
134
135
136
137
138
139
140
141
142
143
144
145
146
147
148
149
150
151
152
153
154
155
156
157
158
159
160
 SLOWDOWN

 NOT APP.
 1.106499
 UNKNOWN
 0.109000
 0.128000
 0.520600
 0.288000
 0.500000
 0,011500
 0.031000
 0.022500
 0.740000
 1.562500
 0.135000
 0.113500
 0.120000
 0.025000
 NOT APP.
 0.066600
 NOT APP.
 0.120000
 0.750000
 1.830997
 UNKNOWN
 UNKNOWN
 0.0
 0.0
 0.153000
 0.006000
 0.055500
 0.0
 0.110000
 UNKNOWN
 0.143500
 UNKNOWN
 UNKNOWN
 0.490000
 0.055000
 0.150000
 NOT APP.
 1.504999
 1.779999
 3.806998
 0.050000
34.663391
 0.564000
 0.925000
 0.066710
 0.066000
 0.042000
                                  225

-------
                         TABLE VII-25  (Continued)

                      COOLING TOWER BLOUDOUN RATES
                      PETROLEUM REFINING INDUSTRY
                       (MILLION GALLONS PER HAY)
REFINERY
 NUMBER
 161
 162
 163
 164
 165
 166
 167
 168
 169
 172
 173
 174
 175
 176
 177
 179
 130
 181
 182
 183
 184
 185
 186
 187
 188
 189
 190
 191
 192
 193
 194
 195
 196
 197
 199
 200
 201

BLOUDOUN
1.128999
0.356250
0.641500
0.015000
0.168000
0.025000
1.189999
0.620000
1.659999
0.149000
UNKNOUN
NOT APR.
4.360797
0.002600
0.014000
0.149200
0.386000
5.218994
1.85849B
0.340650
0.521320
0.322000
0.515399
0.983000
1.005500
0.0
0.005000
0.485000
0.011000
UNKNOUN
2.987994
UNKNOUN
3.507991
0.000500
0.006500
0.395000
0.483000
REFINERY
NUMBER
202
203
204
205
206
207
208
209
210
211
212
213
214
21E
216
218
219
220
221
019
224
225
226
227
228
t>T>O
230
231
232
233
234
235
236
237
238
239
240

BLOUDOUN
UNKNOUN
2.034996
1.536595
0.345550
2.500000
0.036500
0.859999
0.095000
0.014500
0.279100
0.374000
0.012960
UNKNOUN
UNKNOUN
2.420487
1.000000
0.565000
0.012000
UNKNOUN
0.200000
UNKNOUN
0.711000
UNKNOUN
0.388500
0.122000
0.008500
0.370000
NOT APP.
UNKNOUN
0.307000
UNKNOUN
0.230000
> 0.0
0.750000
0.325000
UNKNOUN
0.072000
REFINERY
NUMBER
241
242
243
244
245
246
247
248
249
250
251
252
253
254
255
256
257
258
259
260
261
264
265
266
278
291
292
295
296
298
302
303
305
307
308
309

 BLOUDOUN

 0.109500
 0.305000
 0.125000
31.500000
 0.931000
 0.042500
 0.556700
 UNKNOUN
 0.015000
 UNKNOUN
 NOT APP.
 0.001500
 UNKNOUN
 UNKNOUN
 UNKNOUN
 0.000800
 NOT APP.
 0.633500
 NOT APP.
 NOT APP.
 0.200000
 UNKNOUN
 0.259000
 NOT APP.
 UNKNOUN
 1.259999
 NOT APP.
 0.158000
 NOT APP.
 0.0
 NOT APP.
 UNKNOUN
 0.010000
 UNKNOUN
 0.0
 0.302000
        >   DUE TO UNKNOUN VALUES IN ONE OF THE COOLING TOUERSr
            THE VALUE IS GREATER THAN SHOUN
        NOT APP. - DUE TO A ZERO RESPONSE TO PERCENT COOLING
            BY COOLING TOUERS
                          226

-------
ro
10
                                                                                         TABI£ VII-26


                                                                                  Chromium Removal Systems

                                                                        Equipment Cost Basis and Energy Requirements
Description
Detention Tank, gallons
Mixer, hp
Nixing Requirements. kWh/yr
3.8,m3/day
(lxlOJ gal/d)
32
0.25
1,650
Solids Contact Clarifier, diam 8
S02 Feed Rate, lb/d
Acid Feed Rate, lb/d
Caustic Feed Rate, lb/d
Pumping Requirements, kWh/yr
Manpower Requirements, h/yr
0.4
0.2
2
23
520
38 ra3/day
(IxloVl/d)
320
0.25
1.650
8
4
2
20
230
520
380,m3/day
(lxlOD gal/d)
3.200
1.5
9,900
15
40
20
200
2,300
520
3800 m3/day
(1x10° gal/d)..
32.000
15
99,000
45
400
200
2,000
23,000
1.040
19,000 m3/day
(5xl06 gal/d)
160.000
80
528.000
100
2,000
1,000
10,000
115,000
2.080

-------
                                                                                           TABLE  VI1-27
N>
to
CD
                                                                                    Chromium Removal Systems
                                                                                   Capital and Operating Costs

                                                                                              Capital Costs, Dollars
Description

Detention Tank
Chemical Feed Systems
Automatic Controls
Solids Contact Clarifier
Pumps
Total Equipment Cost
Installation (50%)
Total Constructed Cost
Engineering
Contingency
Total Capital Cost
3.8,m3/day
(1x10 gal/day)
$ 100
5,000
--
25,000

30,100
15,000
45,100
6,950
6,950
$59,000
38.m3/day
(1x10^ gal/day)
$ 1,000
15,000
10,000
25,000

51,000
25,500
76,500
11,750
11,750
$100.000
380,-m3/day
(lx!0s gal/day)
$ 5,000
30,000
10,000
35,000

80,000
40,000
120,000
17,500
17,500
$155,000
Annual Operating Costs,
S02
Acfd
Caustic
Mixing
Pumping
Labor
Maintenance (33i of
Total Capital Cost)
Total Annual Cost
*Note: The depreciation
i 16
4
130
70
Negligable
5,200
1,780

$ 7,200
factor has been
$ 160
40
1,300
70
10
5,200
3,000

$ 9,780
omitted from this
$ 1 ,600
400
13,000
400
100
5,200
4,800

$ 25.500
analysis due to the
3800 m3/day
(IxlO6 gal/day)
$20,000
40,000
10,000
80,000

150,000
75,000
225,000
37,500
37,500
$300,000
Dollars*
$ 16.000
4,000
130,000
4,000
1,000
10,000
9,000

$174,000
fact that it will
19,000 m3/day
(5x10 gal/day)
$50,000
45,000
10,000
155,000

260,000
130,000
390,000
60,000
60,000
$510,000

$ 80,000
20,000
620,000
21 ,000
5,000
20,000
16,000

4782,000
be included
                                            separately in the Economic Impact Analysis Supplement.

-------
Description
                   TABLE  VII-28

Wastewater Recycle - Capital  and Operating  Costs

                      Capital  Costs.  Dollars  -  Per Mile

         2.3 m3/hr  16 m3/hr  80 m3/hr  160 m3/nr  320 m3/hr  800 m3/hr
        (10 gpm)   (70 gpm)  (350 gpm) (700 gpm)   (1400  gpm)  (3500 gpm)
Piping:
  Piping,installed,per mile
  Misc. Costs (15%)
  Total Constructed cost,
    per mile
  Engineering (15%)
  Contingency

Piping-total capital costs
  per mile
         $32,000   $53,000   $100,000  $135,000   $175,000   $243,000
           5.000     8.000     15.000    20.000     26.000     36.000

          37,000    61,000    115,000   155,000    201,000    279,000
           6,000     9,000     18,000    23,000     30,000     42,000
           7.000    10.000     17.000    22.000     29.000     42.000

         $50,000   $80,000   $150,000  $200,000   $260,000   $363,000
Pumps:
  Pumps and associated
  equipment installed (10%
  of piping cost)	
           5,000     8,000     15,000    20,000      26,000     37,000
Total capital costs per mile   $55,000   $88,000   $165,000  $220,000   $286,000    $400,000
(Minimum pumping costs
  regardless of distance)
           5,000     6,000     12,000    18,000      24,000     40,000
                                       Annual Operating Costs,  Dollars  -  Per Mile

Pumping costs per mile,           $100     $ 700      $2600     $4500     $ 9200    $24,300
  per year
Maintenance (1.5% of capital       800      1300       2500      3300      4300      6,000
  costs) per mile.per year	
Total Annual operating cost
            $900
$2000      $5100     $7800    $13,500     $30,300
Note:  The Depreciation factor has been omitted from this  analysis  due  to  the  fact  that
       it will be included separately in the Economic Input Analysis  Supplement.
                                         229

-------
                                      TABLE VI1-29

                          Water Softening  of Recycled Wastewater


                                                 Capital  Costs. Dollars


Description                   2.3  m3/hr  16 m3/hr  80 m3/hr  160 m3/hr  320 m3/hr  800 m3/hr
	(10  gpm)   (70 qpm)  (350 gpm) (700 gptn)  (1400 gpm) (3500 gpm)
Solids Contact Clarlfier      $ 25,000
(Diameter, ft)                  (8)

Chemical Feed System(s)          5,000
             30,000  $ 45,000  $  65,000    $ 80,000   $125,000
             (11)       (23)       (32)       (45)       (72)

              7,000    10,000    15,000     25,000     50,000
Filter Unit
(Diameter, ft)
Subtotal
Auxiliary Equipment
Total Capital Cost
Installation(50%)
Total Constructed Cost
Engineering
Contingency
15,000
(3)
45,000
5,000
50,000
25,000
75,000
15,000
15,000
25,000
(8)
62,000
8,000
70,000
35,000
105,000
20,000
20,000
30,000
(11)
85,000
10,000
95,000
50,000
145,000
25,000
25,000
40,000
(15)
120,000
15,000
135,000
70,000
205,000
30,000
30,000
80,000
(two-151
units)
185,000
20,000
205,000
100,000
305,000
45,000
45,000
150,000
(three-201
units)
325,000
35,000
360,000
180,000
540,000
80,000
80,000
Total Capital  Costs
$105,000   $145,000   $195,000   $265,000   $395,000   $700,000
                                       230

-------
                   TABLE VII-30







CAPITAL AND OPERATING COSTS BY REFINERY NUMBER
REFINERY
NUMBER

1
2
3
6
7
9
10
11
12
13
19
20
24
30
32
37
38
40
41
43
46
49
50
51
52
53
54
56
57
59
60
61
62
63
64
65
67
68
70
*

Capital
Colts
0
0
0
0
0
0
0
0
0
No cost
No cost
0
0
180,000
0
0
No cost
435,000
0
0
0
0
0
865,000
0
0
0
195,000
530,000
0
0
0
0
0
235,000
370,000
2,610,000
385,000
12,500

ECONOMIC COSTS, DOLLARS
OPTION 2 Level 1
Annual Operating
Coats
0
0
0
0
0
0
0
0
0
- considered presently indirect
- insignificant flow
0
0
10,500
0
0
considered presently indirect
17,975
0
0
0
0
0
567,000
0
0
0
14,300
91,000
0
0
0
0
0
16,000
27,000
275,000
39,000
8,500

OPT
Capital
Costs
50,000
50,000
35,000
85,000
70,000
52,000
70,000
60,000
441,000
discharger only

75,000
240,000
230,000
4,000,000
1,600,000
discharger only
555,000
6,400,000
2,100,000
60,000
120,000
565,000
3,140,000
240,000
35,000
35,000
1,100,000
630,000
75,000
75,000
80,000
100,000
1,900,000
310,000
470,000
5,860,000
485,000
160,000

ION 2 LEVEL 2
Annual Operating
Costs
21,500
9,000
5,000
8,000
7,000
6,200
7,000
67,000
27,000


150,000
16,000
34,500
192 ,000
84,000

528,000
290,000
102,000
73,000
10,000
34,000
904,000
16,000
18,000
11,000
62,000
653,000
84,900
145,000
-:05,000
373,000
49 ,000
209,000
309,000
635,000
415,000
26,500

                 231

-------
          TABLE VII-30 (Cont.)
CAPITAL AND OPERATING COSTS BY REFINERY NUMBER
ECONOMIC COSTS, DOLLARS
REFINERY
NUMBER


71
72
73
74
76
77
80
81
83
84
85
87
88
89
90
91
92
93
94
96
97
98
99
100
102
103
104
105
106
107
108
109
110
112
113
114
115
116
117

OPTION 2
Capital
Costs
0
0
No Cost - will
0
180 , 000
0
0
160,000
0
0
0
125,000
0
0
0
0
480,000
0
228,000
0
0
0
0
0
230,000
0
0
305,000
0
No Cost - Will
0
0
No Cost Will
160,000
0
No Cost Will
0
0
355,000

Level 1
Annual Operating
Costs
0
0
Discharge to POTW in
0
11,400
0
0
9,100
0
0
0
8,400
0
0
0
0
30,900
0
12,400
0
0
0
0
0
13,600
0
0
22,200
0
Discharge to POTW in
0
0
Discharge to POTW in
9,700
0
Discharge to POTW in
0
0
8,600

OPTION
Capital
Coats
200,000
35,000
Future
170,000
1,430,000
40,000
90,000
1,040,000
85,000
75,000
95,000
220,000
175,000
77,000
60,000
35,000
2,810,000
35,000
303,000
/, 480, 000
35,000
1,600,000
83,000
35,000
305,000
78,000
1,100,000
380,000
1,100,000
Future
35,000
40,000
Future
330,000
330,000
Future
90 , 000
900,000
945,000

2 LEVEL 2
Annual Operating
Costs
15,000
17,000

13,000
77,400
28,000
9,000
57,100
192,000
139,000
264,000
17,400
13,000
9,000
7,000
4,000
367,000
6,000
157,000
343,000
11,000
80,000
8,000
9,500
32,600
8,000
180,000
203,000
60,000

8,000
25,000

22,700
21,000

216,000
48,000
42,600
               232

-------
TABLE VII-30  (Cont.)
REFINERY
NUMBER

118
119
120
121
122
124
125
126
127
129
131
132
133
134
142
143
144
146
147
149
ISO
151
152
153
154
155
156
157
158
159
160
161
162
163
165
167
168
169
172
173

Capital
Costs
0
0
0
0
520,000
0
0
260,000
0
120,000
0
740,000
660,000
350,000
No cost -
No cost -
0
125,000
0
170,000
0
330,000
630,000
0
0
0
0
0
0
0
0
0
0
0
0
575,000
0
720,000
185,000
160,000
OPTION 2 Level 1
Annual Operating
Costs
0
0
0
0
83,500
0
0
25,200
0
8,300
0
108,000
135,000
34,000
will discharge to POTW in future
will discharge to POTW in future
0
8,300
0
11,400
0
18,500
118,000
0
0
0
0
0
0
0
0
'
0
0
0
59,000
0
96,300
14,100
9,700
OPTION
Capital
Costs
55,000
115,000
100,000
3,100,000
4,920,000
365,000
340,000
4,660,000
150,000
220,000
90,000
3,070,000
785,000
450,000


113,000
220,000
40,000
970,000
52,000
3,030.000
745,000
100,000
700,000
95,000
475,000
75,000
40,000
225,000
35,000
275,000
75,000
700,000
234,000
675,000
80,000
845,000
23,500
200,000
2 LEVEL 2
Annual Operating
Costs
6,500
10,000
9,000
151,000
288,000
23,000
21,500
236,000
12,000
17,300
236,000
454,000
735,000
348,000


10,000
17,300
51,100
53,400
81,000
151,000
730,000
300,000
40,000
9,000
28,500
161,000
49,000
15,500
20,500
18,000
198,000
42,000
16,100
455,000
228,000
765,000
79,100
52,700
    233

-------
TABLE VII-30 (Cont.)
REFINERY
NnMBER

174
175
176
177
179
180
181
183
184
186
189
190
194
196
197
199
201
204
205
208
210
211
212
213
216
219
221
222
226
227
230
231
232
233
234
235
236
237
238

Capital
Costs
135,000
NO COSt
0
175,000
0
315,000
980,000
0
0
0
0
0
750,000
1,280,000
0
125,000
0
268,000
270,000
0
0
0
0
0
0
0
300,000
155,000
0
0
0
No cost
0
0
0
0
0
0
243,000
OPTION 2 Level 1
Annual Operating
Costs
8,300
- will discharge to POTW in future
0
12,300
0
28,100
106 , 000 j
0
0
0
0
0
44,500 10
193,000 4
0
8,300
0
18,700
16 , 400 1
0
0
0
0
0
0 3
0
22,300
9,800
0
0
0
will discharge to POTW in future
0
0
0
0
0
0
17,500
OPTION 2
Capital
Costs
565,000

285,000
225,000
225,000
390,000
,540,000
420,000
75,000
75,000
53,000
60,000
,100,000
,380,000
50,000
197,000
60,000
358,000
,970,000
100,000
35,000
60,000
50,000
73,000
,250,000
850,000
390,000
430,000
65,000
60,000
520,000

60,000
60,000
60,000
75,000
35,000
35,000
318,000
LEVEL 2
Annual Operating
Costs
34,300

19,000
77,300
15,800
245,000
448,000
24,900
100,000
146,000
6,200
6,400
541,000
549 ,000
6,000
15,300
30,000
283,000
101,000
390,000
5,000
69,000
61,000
7,000
358,000
48,000
281,000
27,800
7,000
96,000
31,000

90,000
85,000
85,000
120,000
13,000
6,000
168,000
  234

-------
TABLE VII-30 (Cont.)
REFINERY
NUMBER

239
240
241
242
243
252
255
256
257
258
259
260
261
265
266
292
295
309

Capital
Costs
0
0
0
0
0
0
0
0
0
0
0
0
180,000
0
130,000
No cost
170,000
220,000
OPTION 2 Laval 1
Annual Operating
Costs
0
0
0
0
0
0
0
0
0
0
0
0
10,300
0
8,300
- insignificant flow
10,800
473,000
OPTION
Capital
Costs
35,000
40,000
45,000
40,000
145,000
115,000
115,000
285,000
1,400,000
60,000
75,000
58,000
228,000
48,000
190,000

210,000
265,000
2 LEVEL 2
Annual Operating
Costs
16,500
24,500
40,000
28,000
11,500
10,000
10,000
19,000
72,000
84,000
169,000
6,300
50,300
51,000
66,300

35,800
513,000
 235

-------
NJ
U>
                                                                                        TABLE VII-31


                                                                               CAPITAL AND OPERATING COSTS


                                                                              INDIRECT DISCHARGE - OPTION 1
Cooling
Refinery Tower
Code Slowdown
No . gal/day
8
13
14
16
18
21
23
25
29
31
33
38
45'
58
73
78
1,250**
1,020,000
7,700
69,300
21,500
11,300
Does Not
167,000
325,000
10,000
110,000
702,000
817,000
269,000
139,000
15,000
Chromium Removal, $ Piping Cost, $
Capital Annual Capital Annual
Cost operating Cost Cost Operating Cost
63,000
300,000
94,000
143,000
115,000
102,000
Have Cooling
172,000
207,000
100,000
156,000
265,000
280,000
194,000
165,000
108,000
7,JOO * *
17b,000 320,000 11,000
8,000 20,000 400
20,000 45,000 900
12,500 30,000 400
10,000 * *
Tower +
40,000 60,000 1,600
70,000 150,000 4,200
9,800 *
28,000 5u,OuO 1,100
130,000 160,000 5,000
150,000 200,000 6,500
60,000 90,000 2,500
35,000 60,000 1,300
10,000 35,000 500
Total Cost, $
Capital Annual
cost Operating Cost
63 . 000
620,000
114,000
188,000
145,000
102,000

232,000
357,000
10u,000
206,000
425,000
480,000
284,000
225,000
143,000
7,300
186,000
8,400
20,900
12,900
10,000

41,600
74,200
9,800
29,100
135,000
157,000
62,500
36,300
10,500

-------
                                                                                         TABLE VII-31 (Cont.)
NJ
U)
Refinery
Code
No.
78
79
86
107
110
111
114
128
130
142
143
145
148
166
175
182
188
Cooling
Tower
Blowdown
gal/day
15,000
No
148,000
10,000
No
1,110,000
Chromium Removal, $
Capital Annual
Cost Operating Cost
108,000 10,000
Cost - Unknown Flow
166,000 35,000
100,000 10,000
Cooling Tower +
310,000 188,000
Piping Cost, S Total
Capital Annual Capital
Cost Operating Cost Cost
35,000 500 143,000

45,000 1,100 211,000
* * 100,000

160,000 5,600 470,000
Cost, $
Annual
Operating Cost
10,500

36,100
10,000

194,000
Non Chromium Treatment ++
No
No
110,000
Cooling Tower +
Cooling Tower +
156,000 28,000


60,000 1,400 216,000


29,400
Non Chromium Treatment ++
1,000** 59,000 7,200
* * 59,000
7,200
Non Chromium Treatment ++
25,000
4,360,000
1,860,000
1.010,uOO
118,000 12,000
487,000 628.000
370,000 285,000
300,000 175,000
* * 118,000
485,000 34,200 972,000
630,000 28,700 1,000,000
200,000 7,000 500.000
12,000
662,000
314,000
182,000

-------
                                                                                      TABLE VII-31 (Cont.)
N)



00
Refinery
Code
No.
193
195
200
203
206
207
220
224
225
228
229
231
264
291
305
TOTAL
Cooling
Tower
Slowdown
gal/day
130**
Chromium
Capital
Cost
59,000
Removal, 5 Piping Cost, 5
Annual Capital Annual
Operating Cost Cost Operating Cost
7,200 * *
Total
Capital
Cost
59,000
Cost, $
Annual
Operating Cost
7,200
No Cooling Tower +
395,000
2,040,000
2,000
36,500
220,000
382,000
70,000
126,000
80,000 65,000 2,000
308,000 680,000 31,800
8,000 * *
15,000 40,000 700
285,000
1,062,000
70,000
166,000
82,000
340,000
8,000
15,700
Non Chromium Treatment ++
Non Chromium Treatment ++
Non Chromium Treatment ++
122,000
8,500
No Cooling
No Cooling
126,000
11,600**
5
166,000
98,000
Towers +
Towers +
162,000
103,000
,916,000
30,000 50,000 1,000
9,400 * *


30,000 40,000 800
11,300 * *
2,633,000 3,675,000 150,000
216,000
98,000


202,000
103,000
9,591,000
31,000
9,400


30,800
11,300
2,783,000

-------
                                                                                       TABLE VII-31 (Cont.)
                                            *  These Refineries have only one cooling  tower  and  so piping  cost is  excluded.



                                            **  Actual Cooling Tower blowdown data were not available;  the  blowdown rate is assumed to be

                                               25% of total wastewater generated.


                                            +  These Refineries do not have any  cooling towers.


                                            ++  These Refineries do not use Chromium in the cooling towers.
to
w
vo

-------
       TABLE VII-32





 CAPITAL AND OPERATING COSTS





INDIRECT DISCHARGE -  OPTION 2
Refinery
Code No.
8
13
14
16
18
21
23
25
29
31
33
38
45
58
73
78
79
86
107
110
111
114
128
130
Capital
Costs , $
No Cost
5 , 800 , 000
315,000
826,000
495,000
373,000
315,000
375,000
4,650,000
247,000
1,090,000
4,350,000
3,900,000
1,900,000
915,000
1,390,000
No Cost
800,000
255,000
250,000
2,450,000
683,000
277,000
1,310,000
Annual Operating
Costs, S
- Insignificant Flow
626,000
51,400
136,000
58,000
62,500
60,200
54,500
521,000
54,700
152,000
455,000
419,000
159,000
84,100
119,000
Unknown Flow
104,000
57,900
56,700
211,000
103,000
29,700
421,000
    240

-------
 TABLE VI1-32  Continued
Refinery
Code No.
142
143
145
148
166
175
182
188
193
195
200
203
206
207
220
224
225
228
229
231
264
291
305
Capital
Costs, $
2,450,000
2,190,000
247,000
493 , 000
273,000
13,300,000
7,000,000
3,660,000
247,000
247 , 000
1,150,000
13,800,000
437,000
375,000
258,000
655,000
2,220,000
710,000
242,000
1,110,000
250,000
250,000
277,000
Annual Operating
Costs, $
211,000
174,000
54 , 700
111,000
96,900
2,360,000
781,000
340,000
54 , 700
54,700
106,000
1,510,000
95,800
92,500
56,700
112,000
177,000
112,000
25,400
378,000
55,500
51,200
29,700
241

-------
                                             TABLE VII-33


                            EFFECTIVENESS OF BAT OPTIONS FOR DIRECT DISCHARGERS
                                    POUNDS REMOVED FROM BPT TO LEVEL 1

Refinery
  Mo.           BOD         TSS         Oil & Grease        Chromium (Hex.)        Chromium  (Total)        Phenol

   1              67          56             21                  .074                    1.12                1.29
   2              27          22              8                  .030                    0.45                0.33
   3              12          10              4                  .013                    0.20                0.14
   6              32          26             10                  .035                    0.53                0.80
   7              58          48             18                  .064                    0.97                0.64
   9               44              1                  .004                    0.07                0.10
  10              33          27             10                  .036                    0.55                0.58
  11             213         175             67                  .234                    3.55                3.41
  12              24          20              8                  .026                    0.40                0.49
  19              22          19              7                  .024                    0.37                1.33
  20             344         283            108                  .378                    5.73                5.84
  24             101          83             32                  .111                    1.68                1.05
  30              49          41             16                  .054                    0.82                0.40
  32             502         414            158                  .551                    8.37                7.06
  37             560         461            176                  .615                    9.33              10.05
  40             970         799            304                 1.065                   16.17              13.81
  41            1720        1417            540                 1.889                   28.67              25.29
  43             390         321            122                  .428                    6.50                5.37
  46             502         414            158                  .551                    8.37                6.74
  49               210                  .002                    0.03                1.08
  50               00              0                  .000                    0.00                0.00
  51             741         610            232                  .814                   12.35                9.42
  52               00              0                  .000                    0.00                0.00
  53              50          41             16                  .055                    0.83                0.82
  54               54              1                  -DOS                    0.08                0.12
  56               000                  .000                    0.00                0.00
  57             116          95             36                  .127                    1.93                4.08
  59             104          85             32                  .114                    1.73                2.29
  60             553         456            174                  .607                    9.22                7.67
  61             659         542            207                  .724                   10.98                9.58
  62            3250        2677           1020                 3.569                   54.17              34.30
  63              67          56             21                  .074                    1.17                3.54
  64             267         220             84                  .293                    4.45                4.19
  65             502         414            158                  .551                    8.37                6.85
  67            2400        1976            753                 2.635                   40.00              28.42
  68               00              0                  .000                    0.00                0.00
  70              19          16              6                  .021                    0.32                0.22
  71               00              0                  .000                    0.00                0.00
  72              41          33             13                  .045                    0.68                0.55
  74              36          30             11                  .040                    0.60                1.10
  76             337         278            106                  .370                    5.62               4.09
  77               00              0                  .000                    0.00                0.00
  80              55          46             17                  .060                    0.92                2.11
  81             114          94             36                  .125                    1.90                1.98
  83             271         224             85                  .298                    4.52                5.62
  84              36          30             11                  .040                    0.60                1.98
  85             336         277            105                  .369                    5.60                6.47
  87              11           9              3                  .012                    0.18                0.09
  88              75          62             24                  .082                    1.25               0.77
  89              13          11              4                  .014                    0.22                0.17
  90               11              0                  .001                    0.02                0.23
  91               97              3                  .010                    0.15                0.07
  92            3030        2495            951                 3.327                   50.50              31.49
  93              12          10              4                  .013                    0.20                0.11
  94             108          89             34                  .119                    1.80                2.58
  9G            3050        2511            957                 3.349                   50."1              36.64
  97               97              3                  .010                       j                1.10
  93             491         404            154                  .539                    o.ia                7.80
  99               97              3                  .010                    0.15                0.67
 100              16          14              5                  .018                    0.27                0.18
 102             130         107             41                  .143                    2.17                1.93
 103              55          46             17                  .060                    0.92                0.61
 104             390         733            279                  .977                   14.83              15.17
 105               44              1                  .004                    0.07                2.15
 106             262         216             82                  .288                    4.37                7.08
 108             100          83             32                  .110                    1.67                1.54
 109               00              0                  .000                    0.00                0.00
 112              24          20              8                  .026                    0.40                0.22
 113              86          70             27                  .094                    1.43                1.32
 115            1043         859            327                 1.145                   17.38                9.80
 116             311         256             97                  .341                    5.18                4.28
 117              86          70             27                  .094                    1.43                1.15
 118              71          58             22                  .078                    1.18                0.69
 119             122         100             38                  .134                    2.03                1.14
 120              46          38             15                  .051                    0.77                0.49
 121             793         653            249                  .871                   13.22              10.18
                                                  242

-------
                            TABLE VII-33  - Continued
Refinery
No.
122
124
125
126
127
129
131
132
133
134
144
146
147
149
150
151
152
153
154
155
156
157
158
159
160
161
162
163
165
167
168
169
172
173
174
176
177
179
180
181
183
184
186
189
190
194
196
197
199
201
204
205
208
210
211
212
213
216
219
221
222
226
227
230
232
233
234
235
236
237
238
239
240
241
242
243
252
255
256
257
258
259
260
261
265
266
292
295
309

BOD
644
144
155
48
4
0
629
810
660
18
0
0
190
3
0
781
198
35
34
10
63
392
51
0
0
0
853
0
186
604
377
390
83
8
18
75
49
51
486
710
58
185
526
11
16
4905
1490
9
21
0
3
65
960
27
291
32
33
1710
49
0
0
8
33
54
52
294
517
114
9
40
10
20
29
61
23
12
2
43
25
293
1482
1691
0
64
614
9
2
10
211

T5S
530
119
127
40
4
0
518
667
544
15
0
0
157
2
0
644
163
28
28
9
52
322
42
0
0
0
703
0
153
498
310
321
68
6
15
62
41
42
400
584
48
152
434
9
14
4039
1227
7
17
0
6
53
791
22
240
26
27
1408
41
0
0
6
27
44
43
242
426
94
7
33
9
16
23
51
19
10
1
36
21
241
1220
1392
0
53
505
7
1
9
174

Oil £ Creaae
202
45
48
15
1
0
197
254
207
6
0
0
60
1
0
245
62
11
11
3
20
123
16
0
0
0
268
0
58
190
118
122
26
2
6
24
16
16
152
223
18
58
165
3
5
1539
467
3
7
0
2
20
301
8
91
10
10
536
16
0
0
2
10
17
16
92
162
36
3
13
3
6
9
19
7
4
0
14
a
92
465
530
0
20
192
3
0
3
66

Chromium (Hex.)
.707
.158
.170
.053
.004
.000
.691
.889
.725
.020
.000
.000
.209
.003
.000
.858
.217
.038
.037
.011
.069
.430
.056
.000
.000
.000
.937
.000
.204
.663
.414
.428
.091
.009
.020
.082
.054
.056
.534
.780
.064
.203
.578
.012
.018
5.386
1.636
.010
.023
.000
.009
.071
1.054
.030
.320
.035
.036
1.878
.054
.000
.000
.009
.036
.059
.057
.323
.568
.125
.010
.044
.011
.022
.032
.067
.025
.013
.002
.047
.027
.322
1.627
1.857
.000
.070
.674
.010
.002
.011
.232

Chromium (Total)
10.73
2.40
2.58
0.80
0.07
0.00
10.48
13.50
11.00
0.30
0.00
0.00
3.17
0.05
0.00
13.02
3.30
0.58
0.57
0.17
1.05
6.53
0.85
0.00
0.00
0.00
14.22
0.00
3.10
10.07
6.28
6.50
1.38
0.13
0.30
1.25
0.82
0.35
8.10
11.83
0.97
3.08
8.77
0.18
0.27
81.75
24.83
0.15
0.35
0.00
0.13
1.03
16.00
0.45
4.85
0.53
0.55
28.50
0.82
0.00
0.00
0.13
0.55
0.90
0.87
4.90
8.62
1.90
0.15
0.67
0.17
0.33
0.48
1.02
0.38
0.20
0.03
0.72
0.42
4.88
24.70
28.18
0.00
1.07
10.23
0.15
0.03
0.17
3.52

Phenol
6.59
1.92
2.00
1.97
0.33
0.00
8.14
15.17
7.75
3.81
0.00
0.00
3.90
1.17
0.00
9.36
5.76
4.21
0.60
0.60
1.92
5.74
1.70
0.00
0.00
0.00
9.88
0.00
3.48
7.73
6.53
7.19
1.02
0.37
0.75
1.95
0.84
1.41
5.49
16.34
1.23
3.86
5.77
0.09
0.16
34.19
.20.25
0.08
0.17
0.00
3.44
2.81
15.85
0.30
3.39
1.42
0.37
26.99
2.66
0.00
0.00
0.12
1.34
1.22
1.90
4.17
5.23
4.04
0.18
0.56
1.81
0.52
0.60
1.30
0.56
0.88
0.25
0.50
0.81
5.72
12.72
16.45
0.00
0.72
6.56
0.10
0.02
0.07
1.41
51325
                         16048
                                             56.356
                                                                   855.48
                                243

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                   TABLE VII-34
EFFECTIVENESS OF BAT OPTIONS FOR DIRECT DISCHARGEES
              POUNDS REMOVED FROM BPT TO LEVEL 2
Refinery
No.
1
2
3
6
7
9
10
11
12
19
20
24
30
32
37
40
41
43
46
49
50
51
52
53
54
56
57
59
60
61
62
63
64
65
67
68
70
71
72
74
76
77
80
81
83
84
85
87
86
89
90
91
92
93
94
96
97
98
99
100
102
103
104
105
106
108
109
112
113
115
116
117
118
119
120
121
122
124
125

BOD
120
37
16
69
74
8
56
338
45
29
570
124
54
738
961
1433
2600
566
717
70
26
1025
11
81
11
69
324
205
804
987
4050
263
420
724
3190
262
25
32
58
91
454
30
165
192
514
147
605
12
92
19
15
9
3750
14
225
4080
75
778
47
21
197
71
1470
138
600
156
10
28
133
1224
449
122
85
143
57
1104
790
206
216

TSS
99
31
14
57
61
6
46
278
37
23
469
103
44
608
792
1180
2141
466
590
58
21
844
9
67
9
57
267
169
662
813
3335
216
346
597
2627
216
21
26
48
75
374
25
136
158
424
121
498
10
75
16
12
7
3088
11
185
3360
62
641
38
17
162
58
1211
114
494
128
9
23
110
1008
369
100
70
117
47
909
651
169
178

Oil & Grease
38
12
5
22
23
2
17
106
14
9
179
39
17
231
302
449
816
177
225
22
8
321
3
25
3
22
102
64
252
310
1271
82
132
227
1001
82
8
10
18
29
143
9
52
60
161
46
190
4
29
6
5
3
1176
4
71
1280
24
244
15
7
62
22
461
43
188
49
3
9
42
384
141
38
27
45
18
346
248
64
68
                          Chromium (Hex.)    Chromium (Total)     Phenol

                               .132                2.00            1.36
                               .041                0.62            0.34
                               .018                0.27            0.15
                               .076                1.15            0.84
                               .081                1.23            0.66
                               .009                0.13            0.10
                               .061                0.93            0.61
                               .371                5.63            3.57
                               .049                0.75            0.52
                               .032                0.48            0.26
                               .626                9.50            6.12
                               .136                2.07            1.08
                               .059                0.90            0.41
                               .810               12.30            7.36
                              1.005               16.02           10.56
                              1.573               23.88           14.40
                              2.855               43.33           26.41
                               .621                9.43            5.59
                               .787               11.95            7.01
                               .077                1.17            1.17
                               .029                0.43            0.63
                              1.125               17.08            9.78
                               .012                0.18            0.37
                               .089                1.35            0.86
                               .012                0.18            0.13
                               .076                1.15            1.19
                               .356                5.40            4.35
                               .225                3.42            2.42
                               .883               13.40            7.98
                              1.084               16.45           10.00
                              4.447               67.50           35.32
                               .289                4.38            3.79
                               .461                7.00            4.39
                               .795               12.07            7.13
                              3.503               53.17           29.42
                               .288                4.37            4.68
                               .027                0.42            0.23
                               .035                0.53            0.57
                               .064                0.97            0.57
                               .100                1.52            1.17
                               .499                7.57            4.24
                               .033                0.50            0.57
                               .181                2.75            2.24
                               .211                3.20            2.08
                               .564                8.57            5.93
                               .161                2.45            2.12
                               .664               10.08            6.81
                               .013                0.20            0.09
                               .101                1.53            0.79
                               .021                0.32            0.18
                               .016                0.25            0.25
                               .010                0.15            0.07
                              4.118               62.50           32.40
                               .015                0.23            0.11
                               .247                3.75            2.73
                              4.480               68.00           37.95
                               .082                1.25            1.19
                               .854               12.97            8.17
                               .052                0.78            0.72
                               .023                0.35            0.19
                               .216                3.28            2.01
                               .078                1.18            0.63
                              1.614               24.50           15.90
                               .151                2.30            2.32
                               .659               10.00            7.51
                               .171                2.60            1.61
                               • Oil                0.17            0.58
                               .031                0.47            0.22
                               .146                2.22            1.38
                              1.344               20.40           10.03
                               .493                7.48            4.40
                               .134                2.03            1.19
                               .093                1.42            0.71
                               .157                2.38            1.17
                               .063                0.95            0.50
                              1.212               18.40           10.58
                               .867               13.17            6.78
                               .226                3.43            2.00
                               .237                3.60            2.08
                 244

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                                           TABLE VII-34 - Continued


 Refinery
 N°-            B°D          TSS      Oil s Grease      Chromium  (Hex.)    Chromium (Total)     Phenol
 126             153          126            48               ^68 	     	Til	      2.10
 127
 129
 131            881          725           276               .967               14.68            8.46
 132           1430         1177           448              1.570               23.83           15.96
 133            873          719           274               .959               14.55            8.02
 134
0.40            0.35
0.08            0.10
                                                                                 4.22            4.11
 144              66           54            21               .072                1.10            1.23
 146               541               .005                0.08            0.08
 147             358          295           112               .393                5.97            4.11
 149              75           62            24               .082                1.25            1.26
 150              79           65            25               .087                1.32            1.39
 151            1043          859           327              1.145               17.38            9.69
 152             479          394           150               .526                7.98            6.11
 153             288          237            90               .316                4.80            4.53
 154              58           48            18               .064                0.97            0.64
 155              43           36            14               .047                0.72            0.64
 156             158          130            49               .173                2.63            2.04
 157             590          485           185               .648                9.83            6.00
 158             137          112            43               .150                2.28            1.80
 159              27           22             8               .030                0.45            0.47
 160              20           16             6               .022                0.33            0.48
 161               321               .003                0.05            0.94
 162            1119          922           351              1.229               18.65           10.22
 163              99           82            31               .109                1.65            1.68
 165             328          271           103               .360                5.47            3.66
 167             841          693           264               .923               14.02            8.03
 168             632          520           198               .694               10.53            6.85
 169             682          562           214               .749               11.37            7.56
 172             112           93            35               .123                1.87            1.05
 173              28           23             9               .031                0.47            0.39
 174              58           48            18               .064                0.97            0.80
 176             167          137            52               .183                2.78            2.06
 177              82           68            26               .090                1.37            0.38
 179             119           98            37               .131                1.98            1.50
 180             628          518           197               .690               10.47            5.67
 181            1450         1195           455              1.592               24.17           17.28
 183             112           93            35               .123                1.87            1.30
 184             351          289           110               .385                5.85            4.07
 186             669          551           210               .735               11.15            5.96
 189              12           10             4               .013                0.20            0.09
 190              19           16             6               .021                0.32            0.16
 194            3370         2776          1057              3.700               56.17           32.24
 196            2140         1763           672              2.350               35.67           21.07
 197              10            9             3               .011                0.17            0.08
 199              23           19             7               .025                0.38            0.17
 201              88           73            28               .097                1.47            1.63
 204             223          184            70               .245                3.72            3.72
 205             216          178            68               .237                3.60            3.00
 208            1560         1285           489              1.713               26.00           16.61
 210              35           28            11               .038                0.58            0.31
 211             382          315           120               .419                6.37            3.50
 212             109           90            34               .120                1.82            1.52
 213              42           35            13               .046                0.70            0.38
 216            2690         2215           844              2.954               44.83           28.03
 219             198          163            62               .217                3.30            2.85
 221              69           57            22               .076                1.15            2.62
 222               541               .005                0.08            0.16
 226              12           10             4               .013                0.20            0.13
 227             104           85            32               .114                1.73            1.43
 230             109           90            34               .120                1.82            1.29
 232             151          125            48               .166                2.52            2.03
 233             435          358           136               .478                7.25            4.35
 234             630          519           198               .692               10.50            5.37
 235             323          266           101               .355                5.38            4.30
 236              17           14             5               .019                0.28            0.19
 237              59           48            18               .065                0.98            0.59
 238             120           99            38               .132                2.00            1.94
 239              44           36            14               .048                0.73            0.55
 240              54           44            17               .059                0.90            0.63
 241             118           98            37               .130                1.97            1.38
 242              49           41            16               .054                0.82            0.60
 243              63           52            20               .069                1.05            0.95
 252              17           14             5               .019                0.28            0.26
 255              56           46            17               .061                0.93            0.51
 256              66           54            21               .072                1.10            0.87
 257             532          439           167               .584                8.87            6.02
 258            1663         1370           522              1.826               27.72           12.95
 259            2020         1664           634              2.218               33.67           16.87
 260               110               .001                0.02            0.31
 261              83           68            26               .091                1.38            0.75
 265             770          634           241               .845               12.83            6.75
 266              11            9             3               .012                0.18            0.10
 292               210               .002                0.03            0.02
295              10            9             3               .011                0.17            0.07
 309             211          174            66               .232                3.52            1.41

•total        73172        60265        22950            80.289             1219.54          744.16


                                              245

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                             SECTION VIII

                                 BAT


The   factors   considered  in  assessing  best  available  technology
economically  achievable   (BAT)  include  the  age  of  equipment  and
facilities  involved, the process employed, process changes, non-water
quality environmental impacts  (including energy requirements), and the
costs of application of such technology   (Section  304(b) (2)(B)).   In
general,  the  BAT technology level represents, at a minimum, the best
economically achievable performance of plants of various ages,  sizes,
processes or other shared characteristics.  Where existing performance
is  uniformly  inadequate,  BAT  may  be  transferred from a different
subcategory or category.  BAT may include process changes or  internal
controls, even when not common industry practice.

The  statutory  assessment  of  BAT  "considers"  costs,  but does not
require a balancing of costs against effluent reduction benefits.   In
developing the proposed BAT, however, EPA has given substantial weight
to  the reasonableness of costs.  The Agency has considered the volume
and nature of discharges, the volume and nature of discharges expected
after application of BAT, the general  environmental  effects  of  the
pollutants,  and  the  costs  and  economic  impacts  of  the required
pollution control levels.

Despite this expanded consideration of costs, the primary  determinent
of  BAT  remains  effluent reduction capability.  Effluent limitations
for the petroleum refining industry are expressed as mass limitations,
i.e., restrictions on the total quantity of pollutants  which  may  be
discharged.   Since the total mass of pollutants in an effluent stream
depends on both the total  effluent  flow  and  the  concentration  of
pollutants  in  that  flow, the six options considered for BAT include
various combinations of flow reduction  and  improved  performance  of
waste treatment technology-

BAT OPTIONS CONSIDERED

OPTION  ONE  -  Require  effluent limitations based on an average flow
reduction from model flow of 27 percent achieved through greater reuse
and recycle of wastewater.  This option would not  require  additional
end-of-pipe  treatment  since  limitations  would  be  based  upon the
performance of BPT end-of-pipe technology; phenol  (UAAP)  limitations,
however,  would be based on a long term achievable concentration of 19
ug/1.   (See Section III) .

This level of flow is now achieved by 50 percent of the facilities  in
the  industry.   $19.3 million additional investment would be required
                                247

-------
with  an  annual  cost  of  $7.7  million   including   interest    and
depreciation.

OPTION  TWO  -  Require  effluent  limitations  based on an  average 52
percent flow reduction achieved through greater reuse and  recycle  of
wastewater.   This  option  would  not  require additional end-of-pipe
treatment since limitations would be based on the performance  of   BPT
end-of-pipe  technology.   Mass  limitations  on  4AAP phenol would be
based on the 19 ug/1 currently achieved by industry.

This option was based on an average of the  flows  of  all   refineries
which  are  achieving flows lower than those predicted by the proposed
flow model.  This produces limitations based on flows now achieved  by
38  percent  of the industry; an average reduction of 52 percent would
be required throughout the industry.

Although precise costs have not yet been calculated for  this  option,
EPA  has  concluded,  based  on  its  technological  evaluation of  the
industry, that the costs for Option Two  approximate  those  projected
for Option three below.  $113.0 million additional investment would be
required  with  an annual cost of $48.7 million including interest  and
depreciation.  This amounts to $0.0002 per gallon of product.

In order to confirm its assessment of costs EPA intends to conduct  an
engineering  field  survey  of  the  costs associated with Option Two.
This survey will be completed and a report  prepared  prior  to  final
promulgation  of  these regulations.  EPA will publish a notice in  the
Federal Register when the report is available to the public.

OPTION THREE - Require effluent limitations based on a combination  of
OPTION   ONE   flow  reduction  and  improved  end-of-pipe   treatment.
Improved end-of-pipe treatment was evaluated with the use of powdered
activated  carbon   (PAC).  This combination of treatment produces mass
limitations equivalent to those produced by flow reduction alone under
Option Two.

$113.0 million additional investment would be required with  an  annual
cost  of  $48.7  million  including  interest  and depreciation.  This
amounts to $0.0002 per gallon of product.

OPTION FOUR - Require  mass  limitations  based  on  Option  Two  plus
segregation and separate treatment of cooling tower blowdown.  Cooling
tower  blowdown  would  be treated for metals  (reduction of  hexavalent
chromium to  trivalent  chromium,  pH  adjustment,  precipitation   and
clarification).   Limitations for other process streams would be based
on treatment in existing BPT treatment systems.

Treatment of segregated streams may  remove  more  toxics  than  would
biological  treatment  of  a  combined,  more  dilute,  waste  stream.
                               248

-------
Potential  contamination  of  biological  sludges  by  cooling   tower
biocides  (generally  containing  chromium and zinc) would be reduced.
pemoval of organic toxic pollutants in the biological treatment system
may be increased since  the  wastewater  would  not  be  diluted  with
cooling tower water prior to treatment.

EPA  has not made a detailed cost analysis for this option.  While the
cost of metals treatment can be estimated,  the  cost  of  segregating
cooling  tower blowdown from other process streams cannot be estimated
with available data.  The engineering  survey,  described  above   (See
Option  2)  also  will  collect data on the technical requirements and
cost of cooling water segregation.

OPTION FIVE - Require effluent limitations based on  Option  One  flow
reductions  plus  the  addition  of granular activated carbon (GAC) to
control residual toxic organic pollutants dissolved in the  wastewater
discharged from Option 1 technology.

Although  results  of  the Agency study were inconclusive  (see Section
V), it can be generally stated that toxic pollutant removal  increases
with  the  use  of  GAC.   This  removal,  however, appears to be only
marginally better than with PAC  (Option Two) and the cost  of  GAC  is
much greater than PAC.

EPA  estimates  that  this  option  would  require  direct discharging
refineries to incur an annualized cost of $363 million.

OPTION SIX - Prohibit discharge from existing refineries.  This  could
be  achieved by further reuse and recycle, evaporation, or reinjection
of  wastewaters.   Fifty-five   existing   refineries   already   have
eliminated discharge.

This  is  a demonstrated technology, but costs were not calculated for
this option.  While additional costs for building a  new  refinery  to
eliminate discharge can be calculated  (150), the costs of retrofitting
an  existing refinery are highly site specific,  costs, however, would
be significantly higher than costs  for  applying  any  of  the  other
options.

BAT  SELECTION  AND DECISION CRITERIA - EPA has selected Option Two as
the basis for proposed effluent limitations.  This option was selected
because it was best supported by available data and because it reduces
total pollutant discharges  through  the  use  of  proven  technology.
Since  this  level  represents the average of the best in the industry
EPA believes that it demonstrates reasonable further progress  towards
the  clean  Water  Act's  goal  of the elimination of the discharge of
pollutants.  Further, these limitations are also  technologically  and
economically  achievable  through  the use of Option Three.  Thus, all
facilities have several ways to achieve  this  limitation.   They  may
                                 249

-------
meet  it  totally  through  flow reduction or through a combination of
flow reduction and improved treatment.

Available data  show  that  existing  treatment  already  reduces  the
concentration   of   4AAP  phenols  to  19  ug/1   (See  Section  III).
Consequently mass  limitations  on  phenols  will  be  based  on  that
achievable  concentration.  In order to validate this decision, EPA is
presently requesting, under section 308 of the Act, that approximately
37 refineries believed to have installed  BPT  model  technology  send
data  to  EPA  for  further  evaluation  of  what constitutes a proper
achievable concentration  of  4AAP  phenols  based  on  BPT  treatment
technology.   That  data  also will allow EPA to determine whether the
variability factors used to establish daily and  monthly  fluctuations
should  be  changed  as  a  result  of the lower concentrations.  Mass
limitations  on  all  other  pollutants  are  based  on  those   final
concentrations already part of the BPT limitations (3):

Option  Four  still remains a serious candidate for the basis of final
regulations.  EPA has data establishing  that  greater  quantities  of
metals and toxic organics can be removed when introduced into separate
treatment systems at higher concentrations.  EPA has only limited data
on  the  costs  required to segregate flows from cooling towers.  This
matter is presently under study.

Option Five was not selected because GAC allows only  slightly  better
pollutant  removal than PAC (Option Three) and because the cost of GAC
is considerably higher than the cost of PAC.

Option Six was not selected because, in the  Agency's  judgement,  the
costs  of  retrofitting  to  eliminate discharge on a uniform national
basis would be significantly higher than the selected option and would
result in a substantial number of plant closures.  Nevertheless,  this
option  still remains a serious candidate for any subsequent revisions
of BAT limitations, especially  for  certain  sizes  and/or  types  of
plants.

The  following derivation presents the development of mass limitations
for phenol, based upon Option 2, from  the  flow  model  discussed  in
Section IV.

1) Mass = Flow x concentration x variability (equation 1)
    BAT Mass = .48 x Mass (based on average 1976 industry flow)

2) Flow (see Section IV)  = 0.004C + O.OU6K + O.OU8(A+L)  (equation 2)
         where     Flow = million gallons per day
                   C = summation of the crude oil and fed natural gas
                        liquids to the atmospheric distillation, vacuum
                        distillation, and crude desalting  (in units of
                        1,000 bbls/day)
                               250

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                   K = summation of the petroleum liquids fed to the
                        catalytic cracking processes  (in unit of
                        1,000 bbls/day)
                   A = summation of the petroleum liquids fed to the
                        asphalt processes  (in units of 1,000 bbls/day)
                   L = summation of the petroleum liquids fed to the
                        lube processes  (in units of 1,000 bbls/day)

3)  Concentration and variability factor
         phenol =  19 ug/1     (concentration)
                    1.7   (variability factor for 30 day averages)

4)  Sample Calculation
         Mass = Flow x concentration x variability factor x .48

                =  .004C + .046 K + .048  (A+L) x .019 mg/1
                   x 1.7 x  8.34 x .48
         Mass  (Ibs of phenol)  = (0.0005C) +  (0.0060K) + (0.0062(A+L)

The  following  example  presents  the derivation of a phenol effluent
limitation for typical refinery.

                                       Refinery X Y Z

    Refinery                             Refinery
    Processes                     Capacity 1000 bb/day

Atmospheric Crude Distillation              100
Vacuum Crude Distillation                    75
Desalting                                    50

    total crude processes(C)                225

FCC                                          25
Hydrocracking                                2.0

    Total cracking processes(K)              45

Asphalt Production                            5
Hydrofining                                   3
Wax processing                              	1

    Total asphalt and lube processes  (AL)     9

Using the equation given in item 4 above:

Average of daily values for 30 consecutive days of
phenol discharge, (Ibs/day) =  .0005  (225)  +  .0060  (45) +
                              6.2 x 10-3  (9) =  .nn
                                251

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                              SECTION IX

                                 BCT


The  1977  amendments  added  Section   301(b) (4) (E)   to   the   Act,
establishing  "best  conventional  pollutant control technology"  (BCT)
for discharges of conventional  pollutants  from  existing  industrial
point  sources.   Conventional pollutants are those defined in Section
304(b)(4)  - BOD, TSS, fecal coliform, and  pH  -  and  any  additional
pollutants   defined   by  the  Administrator  as  "conventional."  On
July 30, 1978,  EPA  designated  oil  and  grease  as  a  conventional
pollutant (44 Fed. Reg. 44501).

BCT  is  not  an additional limitation; rather it replaces BAT for the
control of conventional pollutants.  BCT requires that limitations for
conventional  pollutants  be  assessed  in  light  of  a  new   "cost-
reasonableness" test which involves a comparison of the cost and level
of reduction of conventional pollutants from the discharge of publicly
owned  treatment  works   (POTW)  to the cost and level of reduction of
such pollutants from a class or category of industrial sources.  As  a
part  of  its  review  of  BAT for certain "secondary" industries, the
Agency has promulgated a methodology for this cost test.  (See  44  FR
50732, August 29, 1979).  The Agency compares industry costs with that
of  an "average" POTW with a flow of 2 mgd and costs  (1977 dollars) of
$1.18 per pound of pollutant removal (BOD and TSS).

EPA applied this methodology to the costs  for  removing  conventional
pollutants  in  the petroleum refining industry and concluded that BCT
limitations based on a 52 percent reduction in total effluent flow  by
greater recycle and reuse of wasterwaters  (BAT Option Two, See section
IX)   or  a  52  percent  reduction  in  pollutants  discharged  by  a
combination  of  flow  reduction   and   powdered   activated   carbon
enhancement  of  activated  sludges  (BAT Option three) are reasonable.
This is based upon a cost of depreciation and interest of  25  percent
of  capital  costs.   At this level, the total annualized cost for BCT
technology is $48.7 million and EPA projects that 123.3 million pounds
of BOD and TSS will be removed throughout the industry by  Option  Two
technology   (See  Tables VII-30 and VIII-32).  Based on these figures,
the cost to pollutant reduction ratio for  Option  Two  is  $1.00  per
pound  of  BOD  and  TSS removed  (compared to a POTW cost of $1.18 per
pound  of  BOD  and  TSS).   Therefore,  EPA  proposes  BCT   effluent
limitations at the proposed BAT (OPTION TWO) level.
                                 253

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                              SECTION X

                                 NSPS


The  basis  for  new source performance standards  (NSPS) under Section
306 of the Act is the best  available  demonstrated  technology.   New
plants  have  the  opportunity  to  design the best and most efficient
petroleum refining processes and  wastewater  treatment  technologies;
Congress  therefore  directed  EPA  to  consider the best demonstrated
process  changes,  in-plant  controls,   and   end-of-pipe   treatment
technologies  capable  of  reducing  pollution  to  the maximum extent
feasible.

NSPS OPTIONS CONSIDERED

OPTION  ONE  -  Require  performance  standards  based  on  the   same
technology  proposed  for  BAT  (see Section IX), including wastewater
flow control by recycle and reuse of wastewaters after BPT  treatment.
As discussed under BAT Option Two, application of this technology will
ensure  a  high  degree  of  removal  of  toxic  pollutants.   Similar
reductions in pollutant mass discharge can be achieved by  BAT  Option
Three.

OPTION TWO - Require performance standards based on granular activated
carbon   (BAT  Option  Five).   As discussed under BAT Option Five, GAC
allows somewhat better pollutant removals than NSPS Option One, but is
considerably more expensive.

OPTION THREE - Require a performance standard to eliminate  discharge.
Unlike BAT Option Six, there is no cost of retrofitting to comply with
such a requirement.  No discharge of refinery wastes is a demonstrated
technology;  EPA  has  identified  fifty-five  refineries which do not
discharge.  The American Petroleum Institute   (API)  has  published  a
technical  report   (150)  which  evaluates the technologies capable of
eliminating discharge of refinery wastes.  The water reuse schemes and
end-of-pipe technologies described in the API Report are being used in
the refining industry,  used  by  other  industries,  or  successfully
tested  on  a pilot scale.  The report also calculates the costs to be
expected if those technologies were designed into a new refinery  (i.e.
without the need to retrofit existing equipment).  This  option  would
require  a new source of the size and configuration likely to be built
in the 1980's to incur additional investment over BPT of $9.5  million
with   an   annual   cost  of  $3.5  million  including  interest  and
depreciation (1977 dollars).

NSPS SELECTION AND DECISION CRITERIA - EPA has selected  Option  Three
as  the  basis  for  proposed  new  source  performance standards.  No
discharge is a  demonstrated  technology  in  the  petroleum  refining
industry  and,  based on available data, can be economically achieved.
Consequently, EPA believes that the Act requires that option Three  be
the basis for NSPS.
                                255

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                              SECTION XI

                        PRETREATMENT STANDARDS


Section  307(b)   of  the  Act  requires EPA to promulgate pretreatment
standards for both existing sources  (PSES) and new sources   (PSNS)  of
pollution  which  discharge their wastes into publicly owned treatment
works (POTWs).  These pretreatment standards are designed  to  prevent
the discharge of pollutants which pass through, interfere with, or are
otherwise incompatible with the operation of POTW's.  In addition, the
Clean  Water  Act  of  1977 adds a new dimension to these standards by
requiring pretreatment of pollutants, such as heavy metals, that limit
POTW sludge management alternatives.  The legislative history  of  the
Act  indicates  that pretreatment standards are to be technology based
and, with respect to toxic pollutants, analagous to BAT.   The  Agency
has  promulgated  general  pretreatment  regulations which establish a
framework for the  implementation  of  these  statutory  requirements.
(See 43 Fed. Reg. 27736 June 26, 1978).

    A  determination  of  which  pollutants may pass through or be in-
compatible with POTW operations, and thus be subject  to  pretreatment
standards, depends on the level of treatment employed by the POTW.  In
general,  more  pollutants  pass  through  or  interfere  with  a POTW
employing primary treatment (usually physical separation by  settling)
than  one  which  has  installed  secondary  treatment   (settling plus
biological stabilization) (See Section IV).

Section 301(b)(1)(B)  of the Act requires most POTW's to have installed
secondary treatment by July 1, 1977.  There are, however,  two  groups
of  POTW's which have not yet met this requirement.  One group remains
subject to the obligation and contains POTW's which are  scheduled  to
install secondary treatment within the next few years.  A second group
of  POTWs  will  be  exempt  from the requirement to install secondary
treatment.  Under Section 301(h) of the  Act,  POTWs  which  discharge
into  marine waters may, under certain circumstances, receive a waiver
from this requirement.  EPA has proposed regulations dealing with  the
issuance of section 301 (h)  waivers.  43 Fed. Reg. 301 Vol. 44 No. 117,
Friday,  June 15, 1979.

OPTION ONE - Establish pretreatment for all refineries based on metals
removal (pH adjustment, precipitation, and clarification) and existing
PSES  controls.    Metals  removal  would  be required only for cooling
tower blowdown,  since that is the major source of the heavy metals  of
concern  —  chromium  and zinc.   (Under this option, organic priority
pollutants would  pass  through  primary  POTWs  which  have  not  yet
complied  with  Section  301(b)(1)(B) of the Act and those POTWs which
are granted waivers under Section 301(h)).
                               257

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The regulation would require  the  53  affected  indirect   discharging
refineries  to  incur  $9.6  million additional investment  with  annual
costs of $5=2 million including  interest  and  depreciation.    A new
indirect  discharging refinery of the size and configuration  likely to
be built in the 1980's  would  incur  additional   investment   of  $0.3
million  with  annual  costs  of  $0.2  million including interest and
depreciation.

OPTION TWO - Establish two pretreatment standards.    Pretreatment for
those  refineries  discharging  into  POTWs  which have  been granted
waivers  under  Section  301 (h)  would  be  based  on  concentrations
achievable  after  application  of  BPT  technology.  Pretreatment for
other indirect discharging refineries would be the same as  Option 1.

The cost of this option cannot be specifically calculated since   there
are  no  POTWs  which  have been granted waivers under section 301 (h).
Costs were developed, however, for each indirect discharging   refinery
to install biological treatment  (See Section VI).

SELECTION  OF  PRETREATMENT TECHNOLOGY AND DECISION CRITERIA  - EPA has
selected Option Two as the basis for pretreatment  standards.   Based on
its sampling and analysis program, EPA has determined that  pollutants
found in petroleum refining wastes after present PSES treatment  do not
pass  through  secondary  POTWs  and  that  only metals limit  the POTW
sludge management alternatives  (See Section III).   Consequently,  for
metals  only,  EPA  is proposing additional pretreatment standards for
indirect dischargers whose wastes  go  to  POTWs   employing  secondary
treatment.

The  Agency  additionally proposes that this limitation apply  to those
indirect dischargers whose wastes  go  to  a  primary POTW which is
scheduled to install secondary treatment.  Although EPA has determined
that  petroleum refining wastes pass through primary  POTWs, the  Agency
believes that it would  be  improper  to  require  industrial  sources
discharging into such POTWs to install treatment systems which will be
unnecessary  when  the POTWs come into compliance  with the  requirement
of secondary treatment.

EPA is, however, proposing specific pretreatment   standards  based on
application  of  BAT  technology  for those indirect  dischargers whose
wastes go to POTWs which have  been  granted  301(h)  waivers.   Since
POTWs  with  301 (h)  waivers  will  remain  at primary treatment,  only
specific limitations on indirect dischargers will  ensure   that   their
wastes  do  not  pass  through into waters of the  United States.   Such
standards, however, will apply only where a valid  301(h)   waiver has
been  granted.   Those  sources  discharging  into a POTW  which has a
pending application for  a  301(h)  waiver  will   be  subject  to the
generally  less  stringent  pretreatment  standards based on  secondary
treatment in the POTW  until  such  time  as  the  waiver   is  finally
approved.
                                258

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                             SECTION XII

                           AC KNOWLEDGEMENTS
This  document  is based largely on a contractor's report, the purpose
of which was to present the technical  data  base  developed  to  meet
EPA's  requirements for further development and review of BAT effluent
limitations for new  source  performance  standards  and  pretreatment
standards for the petroleum refining point source category.  Burns and
Roe  of  Paramus,  New  Jersey, under contract to EPA, submitted their
report in December of 1977 (125).

The following members of  the  Burns  and  Roe  technical  staff  made
significant  contributions  to  the  overall  project  effort  and the
development of this report:
    Arnold S. Vernick, P.
    Paul D. Lanik, P.E.
    Barry S. Langer, P.E.
    Roy Ehlenberg
    Tom H. Fieldsend
    Gary C. Martin
    Gerald Smit, P.E.
Project Manager
Project Engineer
Project Engineer
Systems Designer
Environmental Engineer
Civil Engineer
Operations Research Specialist
Acknowledgment  is  made  to  all  Environmental   Protection   Agency
personnel  contributing to this effort, including Robert W. Dellinger,
William A. Telliard, Dennis C. Ruddy, Martin P. Halper, Jaye  Swanson,
Harold Coughlin, W. Lamar Miller, Carl J. Schafer, Robert B. Schaffer,
Effluent Guidelines Division; Leon H. Myers, John E. Matthews, Fred M.
Pfeffer,  Thomas  E.  Short,  Jr., Ph.D., Robert S. Kerr Environmental
Research Laboratory; Jeff Gaba, Office  of  General  Counsel;  Michael
Callahan,  Monitoring and Data Support Division; Martin Wagner, Office
of Planning and  Evaluation;  Louis  DuPuis,  Gary  Liberson,  Maurice
Owens,   Charles   Cook,  and  Henry  Kahn,  Office  of  Analysis  and
Evaluation;  George  Keeler,  Office  of  Research  and   Development;
Madeleine  Nawar  and  Gregory Kew, Office of Water Enforcement; T. N.
Hushower, Office of Water Supply; W. L. Polglase,  Emission  standards
and  Engineering  Division;  Gerald  Fontenot,  Region  VI; and Harvey
Lunenfeld, Region II.

We would also like to thank David G. Hutton and Francis L. Robertaccio
of E.I. DuPont de Nemours and Company for their assistance and  review
relative to powdered activated carbon bio-enhancement technology.

The  assistance  of all personnel at EPA Regional Offices and at state
environmental departments  who  participated  in  the  data  gathering
efforts is greatly appreciated.

The assistance of Mrs. S. Frances Thompson of Burns and Roe and of Ms.
Kaye  Starr,  Ms.  Nancy  Zrubek,  and Ms. Carol Swann of the Effluent
                                 259

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Guidelines Division in the typing and preparation of  this   report  is
specifically noted.

Ryckman, Edgerly, Tomlinson, and Associates are acknowledged for their
assistance in the sampling and analysis phase of this study.

The  efforts  of personnel employed at the petroleum refineries listed
in Table III-2 of this report  are  appreciated  with  regard to  the
furnishing  of  data  via  the  1977  EPA  Petroleum Refining Industry
Survey.   In  addition,  the  representatives  of  the  following  oil
companies  are  acknowledged for their assistance during U.S.  EPA and
contractor visits:

    Amoco Oil Company, Yorktown, VA
    B.P. Oil, Inc., Marcus Hook, PA
    Chevron, U.S.A., Inc., Perth Amboy, NJ
    EXXON Company, U.S.A., Linden, NJ
    Getty Refining and Marketing Co., Delaware City, DE
    Mobil Oil Corporation, Paulsboro, NJ
    Sun Oil Co., Marcus Hook, PA
    Texaco, Inc., Westville, NJ

The refineries that were included in the  RSKERL  and  Burns   and  Roe
supplemental  sampling  programs,  as  listed  below, are specifically
noted:

    Asamera Oil  (U.S.) Inc., Commerce City, CO
    Atlantic Richfield Co., Philadelphia, PA
    Clark Oil and Refining Corporation, Hartford, IL
    Coastal States Petrochemical Co., Corpus Christi, TX
    Continental Oil Company, Ponca City, OK
    EXXON Company, U.S.A., Baytown, TX
    EXXON Company, U.S.A., Benicia, CA
    EXXON Company, U.S.A., Billings, MT
    Getty Refining and Marketing Company, El Dorado, KS
    Gulf Oil Company, Philadelphia, PA
    Hunt Oil Company, Tuscaloosa, AL
    Mobil Oil Corporation, Augusta, KS
    Phillips Petroleum Company, Sweeny, TX
    Quaker State Oil Refining Corporation, Congo, WV
    Shell Oil Company, Anacortes, WA
    Sun Oil Company, Toledo, OH
    Texaco, Inc., Lockport, IL

The American Petroleum Institute and its contractor. Brown  and  Root,
Inc.,  are  also  acknowledged  for  their  efforts  relative  to this
project.
                                 260

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                             SECTION XIII

                             BIBLIOGRAPHY


1.       American Petroleum Institute, "Petroleum Industry  Raw  Waste
         Load Survey", December, 1972.

2.       American Petroleum Institute, "Disposal of Refinery Wastes  -
         Manual,  Volume of Liquid Wastes", Washington, DC, 1969.

3.       "Development Document for Effluent Limitations Guidelines and
         New Source Performance  Standards  for  Petroleum  Refining",
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H.       Bush, Kenneth E., "Refinery Wastewater Treatment and  Reuse",
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5.       Wigren,   A.  A.  and  Burton,  F.  L.,  "Refinery  Wastewater
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6.       Armstrong, T.  A.,  "There's  a  Profit  in  Processing  Sour
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7.       Easthagen, J.H., et al., "Development of Refinery Waste Water
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8.       Aqueous  Wastes  from  Petroleum  and  Petrochemica1  Plants,
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9.       Klett,  R. J., "Treat  Sour  Water  for  Profit",  Hydrocarbon
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10.      Brunet,  M. J. and  Parsons,  R.  H.,  "Mobil  Solves  Fouling
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11.      "Phenols  in  Refinery  Waste  Water  Can  be  Oxidized  with
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         January 20, 1975.

12.      Short,  Thomas  E.,  Jr.,  et  al.,  "C&ntrolling  Phenols  in
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13.      Congram, Gary E., "Refiners Zero In On Better Desalting", The
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14.      Beychock,  M.   R.,   "Wastewater   Treatment",   Hydrocarbon
         Processing, pp. 109-112, December, 1974.
                                261

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15.       Swing, R. C., "Modern  Waste-Treatment  Plant   on   Stream  in
         Texaco  Refinery",  The  Oil  and  Gas  Journal,   pp.   66-69,
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16.       "New Ion-Exchange System Treats Sour Water", The Oil  and  Gas
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17.       Pollio, F. X. and Kunin, R., "Ion Exchange Resins  Treat  Sour
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18.       Melin,  G.  A.,  et  al.,  "Optimum  Design  of Sour    Water
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19.       Contrell, A., "Annual  Refining  Survey",  The  Oil  and  Gas
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20.       Gantz, Ronald  G.,  "API  -  Sour  Water  Stripper Studies",
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21.       Short,   T.E.,   et   al.,   "Petroleum   Refining  Phenolic
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22.       Norwood, B. E., "Application of Biological  Trickling   Filter
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         Exposition and Conference, April 4 and 5, 1968.

23.       Congram, Gary E., "Biodisk  Improves  Effluent-Water-Treating
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24.       "1972 Sour Water Stripping  Survey  Evaluation",   Publication
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25.       Annessen, R. J. and Gould,  G.  D,,  "Sour  Water   Processing
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26.       Brown 6 Root, Inc., "Analysis of the 1972 API-EPA   Raw  Waste
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27.       Diehl, Douglas S., et al., "Effluent  Quality   Control  at a
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28.       "Sour  Water  Stripping  Project",  Committee   on  Refinery
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                               262

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         by  Environmental  Services  Department, Bechtel Corporation,
         API publication No. 946, June, 1975.

29.       "Petroleum Refining Industry, Technology and Costs of  Waste-
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30.       "Granular Media Filtration  of  Petroleum  Refinery  Effluent
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31.       "Economics of Refinery Waste Water  Treatment",  prepared  by
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32.       "Economic  Impact  of  EPA's  Regulations  on  the  Petroleum
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33.       Mitchell,  G.  E.,  "Environmental   Protection   -   Benecia
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34.       Ewing, Robert C., "Shell  Refinery  Uses  Pollution-Abatement
         Units", The Oil and Gas Journal. March 8, 1971.

35.       Aalund, Leo A., "Cherry Point Refinery  -  A  Story  of  Air,
         Water, and Fuel", The Oil and Gas Journal, January 24, 1972.

36.       Maguire, W. F., "Reuse Sour Water Stripper  Bottoms",  Hydro-
         carbon Processing, pp. 151-152, September, 1975.

37.       "State   and   Local   Pretreatment   Programs,   -   Federal
         Guidelines",  January,  1977,  U.S.  Environmental Protection
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38.       "Refinery Effluent  Water  Treatment  Plant  Using  Activated
         Carbon", June, 1975, EPA, EPA-660/2 - 75-020.

39.       "Assessment of Hazardous Waste  Practices  in  the  Petroleum
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40.       "Report to Congress - Disposal  of  Hazardous  Wastes",  U.S.
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                                 263

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41.       Elkin, Harold F., "Biological Oxidation 6 Reuse   of   Refinery
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42.       Elkin, Harold  F.,  et  al.,  "Biological   Oxidation   of  Oil
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43,       Mohler, E. F.,  et  al.,  "Experience  with Reuse  and  Bio-
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44.       Wiley,  Morris  A.,  "Chromium  Analysis",  API   Proceedings,
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45.       "Coastal Water Research Project", Southern  California  Coastal
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46.       "Environmental Effect of Disposal of Municipal Wastewater  in
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47.       Donaldson, W. T., "Trace Organics  in  Water",   Environmenta1
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48.       "Draft  Supplement  for  Pretreatment  to   the   Development
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49.       Davis, John C., "Activated  Carbon:  Prime  Choice  to  Boost
         Secondary  Treatment",  Chemical Engineering, April 11, 1977,
         pp. 81-83.

50.       Grutsch, J. F. and Mallatt, R. C., "A New Perspective  on  the
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         Facilities", Proceedings of the Open Forum  on  Management  of
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51.       Gould, J. P. and Weber,  W.  J.,  "Oxidation  of Phenols  by
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52.       Zogorski, J. S=, and Faust,  S.  Do,  "Removing   Phenols  via
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         May, 1977.

53.       Gesick, J. A., "A Comparative Study of  Non-Chromate   Cooling
         Water  Corrosion  Inhibitors",  presented   at the 35th Annual
                                264

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         International Water Conference of the Engineers'  Society  of
         Western Pennsylvania f October 31, 1974.

54.       Zecher, D. C., "Corrosion  Inhibition  by  Surface  -  Active
         Chelants.",   The  International  Corrosion  Forum,  Toronto,
         Canada, April 14-18, 1975.

55.       Robitaille, D. P. and Bilek, J. G., "Molybdate  Cooling-Water
         Treatments", Chemical Engineering, December 20, 1976.

56.       Bush, K.  E.,  "Refinery  Wastewater  Treatment  and  Reuse",
         Chemical Engineering. April 12, 1976.

57.       Mohler, E.  F.,  Jr.,  and  Clere,  L.  T.,  "Development  of
         Extensive  Water  Reuse  and  Bio-Oxidation  in  a  Large Oil
         Refinery",  Complete  Water  Reuse,  American  Institute   of
         Chemical Engineers, Library of Congress Catalog No. 73-87964,
         based  on  papers  presented  at  the  National Conference on
         Complete Water Reuse, April 23-27, 1973.

58.       Mohler, E. F., Jr., and Clere, L. T., "Sun Oil Develops Water
         Reuse Program", The Oil and Gas Journal, September 10, 1973.

59.       Crame,  L.  W.,  "Activated  Sludge  Enhancement:    A  Viable
         Alternative  to  Tertiary  Carbon Adsorption", Proceedings of
         the  Open  Forum  on   Management   of   Petroleum   Refining
         Wastewater, June 6-9, 1977.

60.       Grieves, C. G., et al., "Powdered Activated  Carbon  Enhance-
         ment  of  Activated  Sludge  for  BATEA  Refinery  Wastewater
         Treatment", Proceedings of the Open Forum  on  Management  of
         Petroleum Refinery Wastewater, June 6-9, 1977.

61.       Heath, H. W., Jr.,  "Combined  Powdered  Activated  Carbon  -
         Biological  ("PACT")  Treatment  of HO MGD Industrial Waste",
         presented to Symposium on Industrial Waste Pollution  Control
         at A.C.S. National Meeting, March 24, 1977.

62.       Dehnert, J. F., "Case History - The Use of Powdered Activated
         Carbon with a Biodisc-Filtration  Process  for  Treatment  of
         Refinery Wastes", Proceedings of the Open Forum on Management
         of Petroleum Refinery Wastewater, June 6-9, 1977.

63.       Zanitsch,  R.  H.,  and  Lynch,  R.  T.,   "Granular   Carbon
         Reactivation:  State-of-the-Art",  Proceedings  of  the  Open
         Forum on Management of Petroleum Refinery Wastewater, June 6-
         9, 1977.

64.       Process Design Manual for  Carbon  Adsorption,  Environmental
         Protection Agency Technology Transfer, October, 1973.
                                265

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65.      Ford, D. L., and Tischler, L. F., "Meeting BPT Standards  for
         Refinery    Wastewater    Treatment",     Industrial    Wastes,
         July/August, 1977.

66.      "Proceedings of the 1972 National Conference  on  Control  of
         Hazardous  Material Spills", University of Houston,  March  21-
         23, 1972.

67.      "Spill  Prevention   Techniques   for   Hazardous    Polluting
         Substances",  U.S.  Environmental Protection Agency,  prepared
         by Arthur D. Little, Inc., Contract No. 14-12-927,   February,
         1971.

68.      "Industrial Process Profiles for Environmental  Use:   Chapter
         3.    Petroleum   Refining   Industry",   U.S.  Environmental
         Protection Agency, prepared by Radian  Corporation,   Contract
         No. 68-02-1319, January, 1977.

69.      Rizzo,  J.  L.  and  Shepard,  A.  R.,  "Treating  Industrial
         Wastewater  with  Activated  Carbon",  Chemical  Engineering,
         January 3, 1977.

70.      Dewalle, F.B., et al»,  "Organic Matter  Removal  by   Powdered
         Activated  Carbon  added  to Activated Sludge", Journal  Water
         Pollution Control Federation, April, 1977.

71.      Thibault,  G.  T.,  et  al.,  "PACT  Performance  Evaluated",
         Hydrocarbon Processing, May, 1977.

72.      Lanouette, Kenneth H. and Paulson, Edgar  G.,  "Treatment  of
         Heavy  Metals in Wastewater9', Pollution Engineering,  October,
         1976.

73.      "Petroleum Refineries in the United States and Puerto Rico",
         Mineral  Industry  Surveys,  U.S. Department of The  Interior,
         Bureau of Mines, Washington, DC, January  1, 1977.

74.      "Petroleum Refineries in the United States and Puerto Rico",
         National Petroleum Refiners Association,  Washington,  DC, July
         22, 1977.

75.      "Sampling and Analysis  Procedures for Screening of Industrial
         Effluents  for  Priority  Pollutants",  U.S.    Environmental
         Protection Agency, Cincinnati, OH, April, 1977.

76.      "Preliminary Industry Profile Data", Burns and Roe   submittal
         to  EPA,  Effluent  Guidelines  Division,  Petroleum Refining
         Point Source Category,  December 30, 1976.

77.      "Worldwide Directory,   Refining  and  Gas Processing,  1976-
         1977", Oil and Gas Journalg 34th Edition  1976.
                                 266

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78.       "S-l,  Analysis of Self  Reporting  Data  from  Refineries  to
         Determine Compliance with July 1, 1977 Effluent Limitations",
         Burns  and Roe submittal to EPA, Effluent Guidelines Division,
         February 22,  1977.

79.       "S-2,  Selection of Refineries for RSKERL  Sampling  Program",
         Burns  and Roe submittal to EPA, Effluent Guidelines Division,
         February 22,  1977.

80.       "Analytical  Variability  of  Five   Wastewater   Parameters,
         Petroleum Refining Industry", Prepared by the Robert S.   Kerr
         Environmental   Research   Laboratory,   U.S.   Environmental
         Protection Agency, EPA-600/2-76-234, September, 1976.

81.       "Economic Analysis of Interim  Final  Pretreatment  Standards
         for  the  Petroleum  Refining  Industry",  U.S. Environmental
         Protection Agency, EPA 440/1-77-002, April, 1977.

82.       Askins, W., and Wilcox, D.  R.,  "Tertiary  Treatment  of  an
         Organic  Chemicals  Plant Effluent", Proceedings of the Ninth
         Mid-Atlantic Industrial Waste Conference, August 8-9, 1977.

83.       Talbot, R.S., "A New Redox Method  for  Complete  Removal  of
         Chromium  from  Wastewater",  Proceedings  of  the Ninth Mid-
         Atlantic Industrial Waste Conference, August 8-9,  1977.

84.       "Injections Pep Up Cat Crackers", Chemical  Week,   April  13,
         1977.

85.       Schwartz, R.  D., and McCoy, C.J., "The Use of Fluid Catalytic
         Cracking Catalyst in Activated Sludge Wastewater  Treatment",
         Journal  Water  Pollution Control Federation, Vol. 48, No. 2,
         February, 1976.

86.       Ford,  D. L.,  "Putting Activated Carbon in Perspective to 1983
         Guidelines",  Industrial Water Engineering, May/June, 1977.

87.       Congram, G. E., "Biodisk Improves  Effluent  -  WaterTreating
         Operation", The Oil and Gas Journal, February 23,  1976.

88.       "From Refinery Wastes to  Pure  Water",  Prepared  by  Hydro-
         technic Corporation, New York, NY, undated.

89.       Siegal, B. A., and Barrel, R. C., "Community Metabolism in  a
         Refinery  Holding  Pond",  Journal  Water  Pollution  Control
         Federation, Vol. 48, No. 10, October, 1976.

90.       Baird, R., et al., "Behavior of Benzidine and Other  Aromatic
         Amines   in  Aerobic  Wastewater  Treatment",  Journal  Water
         Pollution Control Federation, July, 1977.
                                267

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91.      Reed, J. L., "Outlook  for  Refinery  Capacity",   Hydrocarbon
         Processing, June, 1977.

92.      Maclean,  W.  D.,  "Construction  Site  Selection   -    A.U.S.
         Viewpoint", Hydrocarbon Processing, June,  1977.

93.      Jenkins, D. M. and Sheppard, W. J., "What  Refinery Pollution
         Abatement Costs", Hydrocarbon Processing,  May, 1977.

9U.      Hatch,  L.  F.,  and  Matar,  S.,   "From   Hydrocarbons   to
         Petrochemicals", Hydrocarbon Processing, June, 1977.

95.      Becker, K.P. and  Wall,  C.F.,  "Fluid  Bed   Incineration  of
         Wastes", Chemical Engineering Progress, October  ,1976.

96.      "Putting   Powdered   Carbon   in   Wastewater     Treatment",
         Environmenta1   Science  and  Technology,  Vol.  11,  No.  9,
         September, 1977.

97.      Puckorius, P., "New Cooling-Water-Systems  Treatment", The Oil
         and Gas Journal, July 5, 1971.

98.      Nicholas, G.W., and  Sopocy,  D.M.,  "Evaluation   of  Cooling
         Tower Environmental Effects", Combustion,  November, 1974.

99.      Kempling,  J.C.  and  Eng,  J.,  "Performance of   Dual-Media
         Filters-2", Chemical Engineering Progress, April,  1977.

100.     Porter, J.W. et  al.,  "Zero  Discharge  of   Wastewater  From
         Petroleum  Refineries",  Presented at the  National Conference
         or. Complete Water Reuse, April 23-27, 1973.

101.     Lindsay, J.T. and Pratter, B.V., "Solving  Petroleum Refinery
         Wastewater   Problems",   Journal   Water  Pollution  Control
         Federation, August, 1977.

102.     Neff, B.,  "The  Development  of  Petroleum   Refinery   Liquid
         Effluent  Controls",  Presentation  to  members  of the U.S.
         Environmental Protection Agency by  Water  Pollution  Control
         Directorate, Environment Canada, March 3,  1977.

103.     "Status Report on  Abatement  of  Water  Pollution From  the
         Canadian  Petroleum  Refinery Industry-1975", Water Pollution
         Control Directorate, Environment Canada, Report  No. EPS-3-WP-
         76, December, 1976.

104.     "Economic  Analysis   of   Proposed   Effluent   Guidelines",
         Petroleum  Refinery  Industry,  U.S. Environmental Protection
         Agency, EP -230/1-73-020, September, 1973.
                                268

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105.      Huber, L.J., "State  and  Development  in  Refinery  Effluent
         Purification",  Proceedings  of  the  Ninth  World  Petroleum
         Congress. 1975.

106.      Statistical    Package  for  the  Social   sciences.   Second
         Edition, McGraw-Hill Book Company, 1970.

107.      Beychok,  Milton  R.,   "State-of-the-Art   in   Sour   Water
         Stripping,"  Proceedings  of  the Open Forum on Management of
         Petroleum Refinery Wastewater, June 6-9, 1977.

108.      "Screening Survey for Priority Pollutants, Petroleum Refining
         Industry"  prepared  by  the  Robert  S.  Kerr  Environmental
         Research Laboratory, U.S. EPA, Draft Report, September, 1977.

109.      Watkins, J.P., "Controlling Sulfur Compounds in Wastewaters,"
         Chemical Engineering, October 17, 1977.

110.      Paulson, E.G., "How to Get Rid of Toxic  Organics,"  Chemical
         Engineering, October 17, 1977.

111.      Ford, D.L., and Elton, R.L., "Removal of Oil and Grease  from
         Industrial  Wastewaters,"  Chemical  Engineering, October 17,
         1977-

112.      Lanouette,   K.H.,   "Heavy   Metals    Removal,"    Chemical
         Engineering, October 17, 1977.

113.      Lanouette, K.H., "Treatment  of  Phenolic  Wastes,"  Chemical
         Engineering, October 17, 1977.

114.      "Development Document for Effluent Limitations Guidelines and
         New Source Performance  Standards  for  the  Copper,  Nickel,
         Chromium, and Zinc Segment of the Electroplating Point Source
         Category,"  March 1974, D.S. Environmental Protection Agency,
         EPA-440/1-74-003-a.

115.      Grulich, G., et al., "Treatment of  Organic  Chemicals  Plant
         Wastewater  with  DuPont  PACT  Process,"  Presented at AIChE
         Meeting, February, 1972.

116.      Button, D.G., and Robertaccio, F.L., U.S.  Patent  3,904,518,
         September 9, 1975.

117.      Bloch, Heinz P., "Improve Safety and Reliability of Pumps and
         Drivers," Hydrocarbon Processing, pp. 97-100, January, 1977.

118.      Natural Resources Defense Council, et al., v. Train, 8 E.R.C.
         2120  (D.D.C. 1976).

119.      Thibodeaux, L.J., and Millican, J.D., "Quantity and  Relative
         Desorption  Rates  of  Air-Strippable  Organics in Industrial
                                269

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         Wastewater," Environmental Science and Technology,  Vol.   11,
         No. 9, September, 1977.

120.      Knowlton, H.E., "Biodisks Work in Waste-Water Treating,"   Oil
         and Gas Journal, October 3, 1977.

121.      Kunz, R.G., et al., "Cooling  Water  Calculations,"  Chemical
         Engineering, August 1, 1977.

122.      "Environmental Considerations of Selected  Energy  Conserving
         Manufacturing  Process Options:  Vol. IV.  Petroleum Refining
         Industry  Report,"  U.S.  Environmental  Protection   Agency,
         EPA-600/7-76-034d, December, 1976.

123.      Dellinger,  Robert  W.,  "Incorporation   of   the   Priority
         Pollutants  into  Effluent  Guidelines  Division  Documents,"
         presented at  the  open  Forum  on  Management  of  Petroleum
         Refinery Wastewater, Tulsa, Oklahoma, June 7, 1977.

124.      "S-3, Selection of Refineries for B S R Supplemental Sampling
         Program," Burns and Roe submittal to EPA, Effluent Guidelines
         Division, March 18, 1977, revised May 4, 1977,

125.      "Data Base for the Review of Effluent Limitations  Guidelines
         (BATEA),  New  Source Performance Standards, and Pretreatment
         Standards for the Petroleum Refining Point Source  Category,"
         Burns and Roe Industrial Services Corporation, Paramus, N.J.,
         December, 1977.

126.      "Electrolytic Coagulation Cleans Waste Water,"  Chemical   and
         Engineering News, January 23, 1978.

127.      Reed, D.T., Klen, E.F.,  and  Johnson,  D.A.,  "Use  of  Side
         Stream    Softening   to   Reduce   Pollution,"   Hydrocarbon
         Processing, November, 1977.

128.      Finelt, S. and Crump,  J.R.,  "Pick  the  Right  Water  Reuse
         System," Hydrocarbon Processing, October, 1977.

129.      Telliard, William A., "Rationale for the Development  of   BAT
         Priority Pollutant Parameters," May 24, 1977.

130.      Grutsch, J.F. and Mallatt, R.C., "Optimizing  Granular  Media
         Filtration," Chemica1 Engineering Progress, April, 1977.

131.      Lash, L., "Scale-up  of  Granular  Media  Filters,"  Chemical
         Engineering Progress, April, 1977.

132.      Brody, M.A., et al. ,  "Performance  of  Dual-Media  Filters,"
         Chemical Engineering Progress, April, 1977.
                                270

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133.      Mahler,  E.F.,  Jr.,  "Removing  Colloidal  Solids  Via  Upflow
         Filtration,"  Chemical Engineering Progress, April, 1977.

134.      Bardone, L.,  et a_l.,  "Costs of  Reducing  SO2.  Emissions  and
         Improving  Effluent   Water Quality from Refineries," Concawe,
         Report NR.,  March, 1977.

135.      Heath, H.W.,  Jr.,  "Chambers Works Wastewater Treatment  Plant
         Removal   of   Organic  and  Organo-Nitrogen  Compounds  From
         Wastewater,"    Unpublished   Report   to   Robert   S.   Kerr
         Environmental  Research  Laboratory,   November, 1976 - April,
         1977.

136.      Hakansson,  H.,  et   al.,  "Petroleum  and   Petrochemicals,"
         Swedish  Water  and   Air Pollution Research Laboratory, B346,
         Stockholm, January,  1977.

137.      Matthews, J.E., et aJL., "Acute  Toxic  Effects  of  Petroleum
         Refinery  Wastewaters  on Redear Sunfish," Office of Research
         and Development, U.S. Environmental Protection  Agency,  EPA-
         600/2-76-241, October, 1976.

138.      Pendleton, H.E.,  Ph.D.,  "Petroleum  and  the  Environment,"
         Pollution Engineering, September, 1977.

139.      Dickerman, J.C., et  al.,  "Industrial  Process  Profiles  for
         Environmental  Use:    Chapter 3 Petroleum Refining Industry,"
         U.S.  Environmental   Protection  Agency,   EPA-600/2-77-023C,
         January, 1977.

140.      "Industry's Challenge on Benzene", Business Week, August  22,
         1977.

141.      Gubrud,  A.E.,  Remarks  at  the   "Federal   Water   Quality
         Association  Conference  on  Toxic  Substances  in  the Water
         Environment," April  28, 1977.

142.      Weiss,  F.T.,  "Fates,  Effects  &  Transport  Mechanisms  of
         Pollutants in the Aquatic Environment", Prepared for the Open
         Forum on Management  of Petroleum Refinery Wastewater, June 7,
         1977.

143.      Kuserk, F.,  "Texaco  Has the Right Answer for Cleaner Refinery
         Effluents," New Jersey Effluents, October, 1977.
                                271

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144.     DeWalle, F.B., et al., "Organic Matter  Removal   by  Powdered
         Activated  Carbon  Added  to Activated Sludge," Journal  Water
         Pollution Control Federation, April,  1977.

145.     Grieves, C.G., "Powdered  Carbon  Improves  Activated Sludge
         Treatment," Hydrocarbon Processing, October, 1977.

146.     Ford,  D.L.  Sr.,  et  al.,  "Meeting   BPT   Standards   for
         Intermediate  and  Secondary  Refinery Wastewater Treatment,"
         Industrial Wastes, September/October, 1977.

147.     Hannah, S.A., et al., "Removal of Uncommon  Trace  Metals  by
         Physical  and  Chemical  Treatment  Processes," Journal  Water
         Pollution Control Federation, November, 1977.

148.     "Electron Microscopic Analysis of Water Samples for Asbestos"
         prepared by GCA Corporation, GCA/Technology  Division,   Final
         Report, December 1977-

149.     Analysis of Petroleum Refinery Effluents for Organic  Priority
         Pollutants" prepared by  Midwest  Research  Institute,   Draft
         Final Report, March  1978.

150.     Water  Reuse  Studies.,  American  Petroleum  Institute,  API
         Publication 949, August, 1977.

151.     U.S. EPA and  Burns  &  Roe,  "Cost  Manual  for  the Direct
         Discharge  Segment of the Petroleum Refining Industry,"  March
         1979.

152.     Rizzo, Joyce A., "Case History:  Use  of  Powdered  Activated
         Carbon in an Activated Sludge System", Paper Presented at the
         First  Open  Forum   on Petroleum Refinery Wastewaters, Tulsa,
         OK, Jan. 1976.

153.     Grieves, C. G., M. K. Stenstrom, J.D. Walk, and J.F.  Grutsch,
         "Effluent Quality Improvement by Powdered Activated Carbon in
         Refinery Activated Sludge Processes", Paper Presented at API
         Refining Department, 42nd Midyear Meeting, Chicago, Illinois,
         May 11, 1977.

154.     Thibault, G.T., K.D. Tracy and J.B, Wilkinson, "Evaluation of
         Powdered Activated Carbon Treatment for  Improving  Activated
         Sludge   Performance",   Paper   Presented  at  API  Refining
         Department, 42nd Midyear Meeting, Chicago, IL, May  11, 1977-

155.     Flynn, B.P., "Startup of 38 MGD Powdered Activated  Carbon   -
         Activated Sludge  (PACT) Treatment System at DuPont's  Chambers
         Works",  paper  Presented  at the 50th Annual Water Pollution
         Control Federation conference, Philadelphia, PA,  October  3,
         1977-
                                272

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156.     Robertaccio,  F.L.,   "Combined  Powdered  Activated  Carbon  -
        Biological Treatment:  Theory and Results",  Paper Presented at
        Second   Open  Forum  on  Management  of  Petroleum  Refinery
        WastewatERS,  Tulsa,  OK, June 8f 1977.

157.     Spady, Ben, and Alan D.  Adams,  "Improved  Activated  Sludge
        Treatment with Carbon", Deeds £ Data,  Water Pollution Control
        Federation, January 1976.
                                273

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                             SECTION XIV

                      GLOSSARY AND ABBREVIATIONS
Glossary
Act:  The  October  18, 1972 Amendments to the Federal Water Pollution
Control Act, P.L. 92-500.

Administrator; Administrator  of  the  U.S.  Environmental  Protection
Agency, whose duties are to administer the Act.

Appendix  A  Pollutants;  Those pollutants listed in Appendix A of the
Settlement Agreement of June 7, 1976  (see Table III-l).

Best Available Technology  Economically  Achievable   (BATEA  or  BAT) ;
Treatment required by July 1, 1983 for industrial discharge to surface
waters as defined by Section 301  (b)  (2)  (A) of the Act.

Best  Practicable  Control  Technology Currently Achievable (BPCTCA or
BPT|; Treatment required by July 1, 1977 for industrial  discharge  to
surface waters as defined by Section 301  (b)  (1)  (A) of the Act.

Best  Available Demonstrated Technology  (BADT); Treatment required for
new sources as defined by Section 306 of the Act.

Catalyst; A  substance  which  can  change  the  rate  of  a  chemical
reaction, but which is not itself involved in the reaction.

Cluster  Analysis; A statistical procedure which solves the problem of
separating objects into groups  so  that  each  object  is  more  like
objects in the same group than like objects in other groups.

Cross-check  Editing; The determination of a value's validity based on
the occurrence of a value of some other variable.

Data Validation; An operation performed to  insure  the  accuracy  and
reliability of raw input information.

Dependent  Variable;  A  variable  whose value is a function of one or
more independent variables.

Deterministic Variable; A variable whose values are purely  determined
to be a function of physical facts.

Discriminant  Analysis;  A  statistical  procedure to assign an entity
whose population identity is  not  known  to  a  population  of  known
characteristics.

Dummy  Variable;  A  symbol representing the statistical encoding of a
qualitative value.
                                 275

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Economics Survey: Survey to be mailed by the Office  of  Analysis  and
Evaluation  of  EPA  to  the  petroleum refining industry, pursuant to
Section 308 of the Act.  Data on  the  economic  status  of  petroleum
refineries will be requested.

End-of-Pipe Treatment  (control): Those treatment technologies that are
used after gravity oil separation.

Flow  Model;  A  mathematical  model  of the effluent wastewater flow,
developed through the use of multiple linear regression techniques.

Forward  Stepping  Multiple  Linear  Regression;  A  multiple   linear
regression procedure in which the order that the independent variables
enter  into  the regression model is determined by the respective con-
tribution of each variable to explain the variability of the dependent
variables.

Independent Variable; A variable whose value is not dependent  on  the
value of any other variable.

In-plant  Control; Those treatment techniques that are used to reduce,
reuse, recycle, or treat wastewater prior to end-ofpipe treatment.

Linear Regression; A method to fit a line through a set of points such
that the sum of squared vertical deviations of the point  values  from
the  fitted line is a minimum, i.e. no other line, no matter how it is
computed, will have a smaller sum of  squared  distances  between  the
actual and predicted values of the dependent variable.

Listvdse  Deletion  of Missing Data: A procedure to handle the absence
of some of the information in a regression analysis by eliminating any
data point with absent information from all calculations.

Magnitude of Entry Editing; The determination of  a  value's  validity
based  solely on size of the figure, and is a test typically performed
on raw input data.

Mathematical Model; A quantitative equation  or  system  of  equations
formulated  in  such  a way as to reasonably depict the structure of a
situation and the relationships among the relevant variables.

Mean Value; The statistical expected or average figure.

Multicollinearity; A regression analysis situation in  which  some  or
all of the independent variables are very highly intercorrelated.  The
presence of this situation may cause model development to be extremely
difficult or impossible.

Multiple  Linear  Regression: A method to fit a plane through a set of
points such that the sum of squared distances between  the  individual
observations  and  the estimated plane is a minimum.  This statistical
                                276

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technique is an extension of linear regression in that more  than  one
independent variable is used in the least squares equation.

Normalized  Coefficients;  Regression  constants  whose magnitudes are
referenced to some value.

Pairwise Deletion of Missing Data; A procedure to handle  the  absence
of some of the information in a regression analysis by eliminating the
data point from only those calculations which use the absent figures.

Portfolios  Aj.  B;  The  two  sections  of the 1977 U.S. EPA Petroleum
Refining Industry Survey (see "The Survey").

Priority Pollutants; Those pollutants included in Table III-3.

Probabilistic  Variable;  A  symbol  whose  values  vary   with   some
likelihood   of   occurrence   distribution.   The  values  cannot  be
determined "a priori".

Process Conf iqurat ion; A numerical measurement of a refinery's process
complexity; developed for use in calculating BPT guidelines  for  this
industry.

Process  Factor;  A  factor  based upon process configuration, used in
calculating a petroleum refinery's BPT limitations.

Random Process; A procedure which varies according to some probability
function.

Random Variable : A variable whose values occur according to the  dis-
tribution of some probability function.

Regression  statistics;  Values generated during a regression analysis
which identify the significance, or  reliability,  of  the  regression
generated figures.

Regression Model: A mathematical model, usually a single equation, de-
veloped through the use of a least squares linear regression analysis.

Residuals; The differences between the expected and actual values in a
regression analysis.

Settlement  Agreement  of_  June  2j.  1976;  Agreement between the U.S.
Environmental  Protection  Agency   (EPA)  and  various   environmental
groups,  as  instituted  by  the  United States District Court for the
District of Columbia,  directing  the  EPA  to  study  and  promulgate
regulations for a list of chemical substances, referred to as Appendix
A Pollutants.

Significance;  A  statistical measure of the validity, confidence, and
reliability of a figure.
                               277

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Size Factor; A factor, based upon a petroleum refinery's size, used in
calculating a petroleum refinery's BPT limitations.

Sour Waters; Those wastewaters containing sulfur  compounds,  such  as
sulfides and mercaptans.

Statistical  Stability;  A  condition  whereby if a process were to be
repeated over time, differences  would  occur  due  solely  to  random
processes.

Statistical Variance; The sum of the squared deviations about the mean
value  in  proportion to the likelihood of occurrence.  A measure used
to identify the dispersion of a set of data.

The 1977 EPA Petroleum Refining Industry Survey (The Survey); A survey
mailed pursuant to Section  308  of  the  Act  to  274  refineries  on
February 11, 1977, and an additional 23 refineries on August 12, 1977.
The  survey was issued in two sections, referred to as Portfolio A and
Portfolio  B,  and  requested  data  on  various  aspects  of  process
operations, wastewater production, and wastewater treatment.

Tolerance Limits; Numerical values identifying the acceptable range of
some variable.

Traditional Pollutant Parameters; Pollutant parameters considered, and
used, in the development of BPT guidelines.  These parameters include,
but are not limited to BOD, COD, TOC, TSS, and  ammonia.
                                278

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Abbreviations
API:
BATEA (BAT) :
bbl(Bbl) :
BPCTCA (BPT) :
B 6 F:
DMR:
EPA:
gal:
MGD:
mg/L:
POTW:
RETA:
RSKERL:
8 & A:
SPSS:
ug/1:
American Petroleum Institute
Best Available Technology Economically Achievable
Barrel
Best Practicable Control Technology Currently Available
Burns and Roe
Discharge Monitoring Report
U.S. Environmental Protection Agency
Gallon
Million gallons per day
Milligrams per liter
Publicly Owned Treatment Works
Ryckman, Edgerley, Tomlinson and Associates
Robert S. Kerr Environmental Research Laboratory
Surveillance and Analysis
Statistical Package for the Social Sciences
Micrograms per liter
                                  279

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        APPENDIX 1
 Petroleum Refinery Industry

      Survey Form and
Supplemental Flow Question
            281

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                                                                 CODE NO.	

                            PETROLEUM REFINING INDUSTRY SURVEY

                     FOR REVISION OF "BEST AVAILABLE TECHNOLOGY" (BAT)
           EFFLUENT LIMITATIONS GUIDELINES AND NEW SOURCE PERFORMANCE STANDARDS

                                        PORTFOLIO A

NOTES

(1)   Portfolio A is to be mailed within 30 days of receipt and Portfolio B within
     60 days of receipt to:

                                   Robert B.' Schaffer, Director
                                   Effluent Guidelines Division
                                   U.S. Environmental Protection Agency (WH-552)
                                   Washington, D.C. 20460

(2)   All flow rates requested in this survey are annual average values  (for calendar
     year 1976) and in units of million gallons per day (MGD), unless otherwise specified.

I    GENERAL INFORMATION
     A.   Name of Refinery_

     B.   Street Address
     C.   Refinery Contact_
     D.   Telephone Number
II   REFINERY PROCESS DATA

     Definitions for Following Table:

     1.   "First Generation Petrochemicals" are compounds such as BTX, olefins, Cyclohexane,
          etc. which are produced through processes normally associated with refineries such
          as isomerization or distillation.

     2.   "Second Generation Petrochemicals" are compounds such as alcohols, ketones,
          cumenes, styrenes, etc. which are produced through more complex chemical
          reactions.

     3.   "Treating and Finishing Processes" should include only those processes that
          are used to upgrade the intermediate or final product streams, or other
          product streams that are blended to result in final products.
                                         282

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PORTFOLIO A (continued)
                                                                CODE NO.	
II   REFINERY PROCESS  DATA  (Continued)

     Please include a  simple process block flow diagram of the refinery operations
     with the completed survey form.
     Indicate which of the processes listed below are utilized at your refinery, and
     the respective process rates for the period 1/1/76 - 12/31/76.

                                    A. 1976 Stream       B.  Calendar Day    Year Process
     Process                           Day Capacity         Rate 1976 Avg.    Installed
                               Units: 1000 bbl/day    Units:  1000 bbi/day
     1.  Atmospheric Crude
         Distillation               	      	   	
     2.  Crude Desalting            	      	
     3.  Vacuum Crude  Dis-
         tillation                  ____^________      _______________   	
     4.  Vi screaking                	      ______________   	
     5.  Thermal Cracking           	      _____________   	
     6.  Fluid Catalytic
         Cracking                   __________      	   	
     7.  Moving Bed Catalytic
         Cracking                   	      ^^^^^^^^^^^^   	
     8.  H2SO4 Alkylation
     9.  HF Alkylation
     10.  Hydrocracking
     11.  Hydroprocessing
     12.  Catalytic Reforming
     13.  Catalytic Polymerization
     14.  Aromatic Petrochemicals
     15.  Delayed Coking
     16.  Fluid Coking
     17.  Isomenzation
     18.  Asphalt Production
     19.  Ammonia Petrochemicals
     20.  Alkylate Production
     Lube Oil Processes
     21.  Hydrofining, Hydro-
         finishing, Lube Hydro-
         fining
     22.  White Oil Manufacture
                                             283

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PORTFOLIO A (continued)                                         CODE N0._
                                     A.  1976  Stream        B. Calendar Day    Year Process
 Process                                Day Capacity         Rate  1976 Avg.    Installed
          Oil Processes         Units:  100° bbl/day    UnitS: 10°°
     23.  Propane Dewaxing, Propane
          Deasphalting, Propane
          Fractioning, Propane De-
          resining                   	
     24.  Duo Sol, Solvent Treat-
          ing, Solvent Extraction,
          Duotreating, Solvent De-
          waxing, Solvent Deasphalt  	
     25.  Lube Vac Twr, Oil Fraction-
          ation. Batch Still  (Naptha
          Strip), Bright Stock Treating
     26.  Centrifuge & Chilling      	
     27.  MEK Dewaxing, Ketone Dewaxing,
          MEK-Toluene Dewaxing       	
     28.  Deoiling (wax)             	
     29.  Naphthenic Lubes           	
     30.  SO  Extraction             	
     31.  Feed Preparation           	
     32.  200°F Softening Point
          Unfluxed Asphalt           	
     3 3.  Compounding                	
     34.  Wax Pressing               	
     35.  Wax Plant  (with Neutral
          Separation)                	
     36.  Furfural Extracting        	
     37.  Clay Contacting -
          Percolation                	
     38.  Wax Sweating               	
     39.  Acid Treat                 	
     40.  Phenol Extraction          	
     Treating & Finishing
     41.  Bender Treating            	
     42.  Petreco Locap Gasoline
          Sweetening                 	
                                            284

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PORTFOLIO A (continued)
             ~~                                                CODE NO.
                                     A.  1976 Stream      B. Calendar Day    Year Process
 Process                                Day Capacity         Rate 1976 Avg.    Installed
     Treating s Finishing       Units:  100° "hi/day   Units: 1000 bbl/day
     43.  Asphalt Oxidizer           	
     44.  Caustic or KOH Treating,
          For example:   Caustic or
          KOH Treating for (1),
          H2S (2), Mercaptan (3),
          Cresylic Acid (4)  Naphenic
          Acid (5), PWS MEA for COS
          Removal, etc.              	      	   	
     45.  Hater Wash                 	      	   	
     46.  Mercapfining, Pentane
          Mercapfining               	      	   	
     •17.  Merox Treating (i.e.
          Liquid-Liquid Extraction,
          Liquid-Liquid Sweetening,
          and Fixed Bed              	      	   	
     48.  C  & C  Scrubbing,
          Girbitol Treating          	      	   	
     49.  Linde                      	      	   	
     50.  Doctor Treating            	      	   	
     51.  Sulfuric Acid Treating     	      	   	
     52.  Unisol Treating            	      	   	
     53.   SO2 Treating
     54.   Hydro Treating
     55.   Perco (copper chloride).
          Copper Slurry
     56.   Inhibitor Sweeting
     57.   KCr
     58.   Clay Treating, Bauxite
          Treating
     59.   Hypochlorite Sweetening
     60.   Salt Brightening or
          Drying
     61.   Sulfinol
     62.   Unclassified Treating
          and Finishing
                                        285

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PORTFOLIO A (continued)                                           CODE NO._
                                     A. 1976 Stream       B.  Calendar Day    Year Process
 Process                                Day Capacity         Rate 1976 Avg.     Installed
                                Units: 1000 bbl/day   Units:  1000 bbl/day
     Petrochemicals
     63.  Isobutane Production
     64.  Carbon Black
     65.  Heptane
     66.  Sulfolane
     67.  OxoAlcohol
     68.  Napthalene
     69.  Butadiene
     70.  Aliphatics
     71.  Cumene
     72.  Paraxylene Charge
     73.  Xylene Fractionation
     74.  Polypropene, Polyiso-
          butylene, Poly Feed
          Preparation, Trimer-
          Tetramer
     75.  Phenol, Oxonation Addi-
          tives Mfg., Polystyrene
          Resin, Lube Oil De-
          pressant
     76.  Detergents Alkylate
     77.  Cresylic Acid
     78.  Styrene
     79.  Naphthenic Acid
     80.  Alpha Olifins
     81.  Nitric Acid
     82.  Phthalic Anhydride
     83.  Butyl Rubber
     84.  Polyproplene
     85.  Cyclohexane
     86.  Solvent hydrotreater
     87.  HHU
     88.  Unclassified Petrochem
                                            286

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PORTFOLIO A (continued)                                               CODE NO
                                     A.  1976 Stream       B. Calendar Day    Year  Process
  Process                                Day Capacity         Rate 1976 Avg.     Installed
                                 Units:  1000 bbl/day   Units: 1000 bbl/day
      Other Processes
      89.   Asphalt,  Asphalt  Oxi-
           dizing, Asphalt Emulsi-
           fying                    	      	   	
      90.   Sulphur Recovery,  Sulphur
           Production
      91.   Hydrogen, Reformer Feed
           Prep, Steam Methane  Re-
           former, Partial Oxidation 	      	   	
      92.   Gas Plant	
      93.   DEA Treating             	
      94.   CO  Recovery
      95.   Furfural
      96.   Dubbs Pitch
      97.   Solvent Decarbonizing
      98.   Hydrodemethylation
      99.   Catalyst Manufacture
     100.   Gasoline Additives
     101.   Linear Paraffins
     102.   Butadiene Concentration
     103.   Nonene
     104.   Ammonia Plants
     105.   Other
                                             287

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                                                                   CODE NO.	
PORTFOLIO A (continued)
     C.   Description of Feedstocks Processed
                                                                              All
                                        #1          #2          #3           Others
     1.   Nitrogen content,  *       	   	   	   	
     2.    Sulfur content,  %
     3.    API Gravity
     4.    Source (Country  or U.S.
          geographical Region)
          Type (e.g.  asphaltic,
          napthenic,  paraffinic,  gas)
          Percent of  yearly crude
          capacity                  	
          Trace metals content,  %
          a.   Antimony              	
          b.   Beryllium             	
          c.   Cadmium
          d.   Chromium
          =.   Copper                 	
          f.   Lead                  _
          g.   Mercury               	
          h.   Nickel                 _
          i.   Selenium              	
          j.   Silver                 _
          k.   Thallium              	
          1.   Zinc
          Product  Yield  (% of  1976 Feedstock  Intake)
          1.   Leaded  gasoline       	
          2.   Unleaded gasoline     	
          3.   Naptha  jet  fuel       	
                                           288

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PORTFOLIO A  (continued)
                                                                     CODE NO.
Ill  IN-PLANT TREATMENT
     A.   Crude Vacuum Unit:
          1.   Barometric  condenser.annual average flow, MGD
     B.   Sour Water
          1.  Treated Sour Water, annual average flow, MGD
              Method of Treatment                Check Method Used
              a.  Single stage stripping               	
              b.  Two stage stripping
              <.-.  Oxidizing
              d.  Others (List)
                                                            Annual  Average Flow,  MGD
          3.  Sour Water Sources
              a.  Condensate from catalytic cracking        	
              b.  Condensate from petroleum coking          	
              c.  Condensate from hydrocracking             	
              d.  Condensate from other hydroprocessing	
              e.  Desalter water                            	
              f.  Crude unit condensate                     	
              g.  Flare drum knock-out                      	
              n.  Other
                  Total Sour Water Flow
          4.   If certain sour water streams are not treated,  list them,  and  describe dis-
              position (e.g.  discharged,  reused, etc.)	
(1)   Removal  of hydrogen sulfide carried out by steam stripping in  a  single  stage with
     or  without the removal  of ammonia.
(.1)   Removal  of hydrogen sulfide and ammonia carried  out  separately.   Hydrogen  sulfide
     is  removed in the first stage followed  by ammonia removal  in the second stage.
                                               289

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PORTFOLIO A (continued)


III  B.   5.   Disposition of Treated Sour Waters
               a.  Desalter make-up
               b.  Other reuse  (describe)
                 CODE NO.
           Percent
               c.  Non-recycled  (e.g. sent to:  tr
                   discharged, POTW, etc.)                   	
               Are sour water treatment units to be upgraded in the future?  Explain and
               describe.  Give expected completion date.
     D.
     C.   Spent Caustic Disposition

          1.  Sulfidic
               a.  Amount oxidized
               b.  Amount neutralized
               c.  Amount sold
               d.  Other, explain
          2.
               Phenolic
               a.  Amount sold
               b.  Acid oil sold
               c.  Other, explain
Annual Average Flow in Gallons per Day
          Use the spaces below for descriptions of additional in-plant treatment systems
          existing at your refinery.  (Attach additional sheets, if necessary).
                                              290

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PORTFOLIO ft (continued)

IV   PLANT WATER MANAGEMENT
     A.  Intake Haters
         1.  Fresh water-
             river/lake
         2.  Brackish or salt
         3.  Well
         4.  Recycled treated
             wastewater
         5.  Municipal supply
         6.  Municipal sewage
             effluent
         7.  Rainwater
         8.  Other
       CODE NO.
                                  Annual Average
                                    Flow, MGD
Where Used
  (process)
Treated
Prior to use?
  Yes/No.
         9.  For those intake waters treated prior to use:
             a.   Average total annual discharge of blowdowns  from  these treatment systems
             b.   Describe treatment systems by intake source:
     B.    Wastewaters

          1.   Refinery process wastewaters
          2.   Ballast water
          3.   Storm water treated in the  main  treatment
              system
          4.   Water treatment  systems blowdown
          5.   Boiler blowdowns
Annual Average Flow,  MGD
                                          291

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PORTFOLIO ft (continued)
                      —
IV   B.   6.  Other wastewaters from non-refinery production operations  (e.g. catalyst
              manufacturing).  List sources and give flow rates
     C.   Utilities
          1.  Do you produce your own steam?  (yes/no)	
          2.  Do you produce your own electricity?  (yes/no)
     D.   Cooling Service
          1.  Cooling Water Uses
              Estimate your refinery's percent by volume of cooling water in each cate-
              gory.   (Total in each category should add up to 100%.)
              a.  Pump Gland Cooling                                         Percent
                  (1)  Closed cycle cooling system                           	
                  (2)  Once-thru segregated discharge  (i.e. not in
                       process sewer                                         	
                  (3)  Once-thru non-segregated (i.e. in process sewer)      	
                  (4)  Others (List)
                                                    Total                     100%
               b.  Compressor Cooling
                   (1) Closed cycle cooling system                           	
                   (2)  Once-thru segregated discharge (i.e. not in
                        process sewer)                                       	
                   (3)  Once-thru non-segregated discharge  (i.e. in
                        process sewer)                                       	
                   (4)  Others (List)
                                                     Total                    100%
                   Once-Through, if applicable
                   (1)  Segregated                                           	
                   (2!  Non-segregated                                       	
                                                     Total                    100%
                                           292

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PORTFOLIO A (continued)                                              CODE N0'-
IV   D.  2.  Cooling Towers (1)                        Summer             winter
             a.  Source of make-up water
             b.  Make-up water flow rate, MGD
             c.  Make-up water quality
                 (1)  Chlorides, mg/1                  	    	
                 (2)  TDS, mg/1                        	    	
                 (3)  Sulfates, mg/1                   	    	
                 (4)  Silica, mg/1                     	    	
                 (5)  Hardness, as CaCO , mg/1         	    	
             d.  No. of cycles of concentration        	    	
             K.  Corrosion inhibitor(s) used
                 (1)  Type                             	    	
                      Concentration                    	    	
                 (2)  Type                             	    	
                      Concentration
                 (3)  Type                             	    	
                      Concentration                    	    	
             f.  Slowdown rate, MGD                    	    	
             g.  Slowdown quality                      	    	
                 (1)  Chlorides, mg/1                  	    	
                 (2)  TDS, mg/1                        	    	
                 (3)  Sulfates, mg/1                   	    	
                 (4)   Hardness, as CaCO ,  mg/1
             h.  Cooling range,A F
             i.  Recirculation rate, MGD
             j.  Evaporation rate, MGD
(1)   Note:   One copy of this sheet should be used for each cooling tower.   Therefore,
     an adequate amount of copies of this sheet should be made before data is  entered
     on the original.   All copies should then be included with your response.
                                            293

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PORTFOLIO A (continued)
IV   D.   3. Overall Summary
             a.  Once-through water
             b.  Recycled, using cooling towers
                 or ponds
             c.  Air cooling
                                                       Flow, MGD
                                                         N.A.
                                                                   CODE NO.
% of Total
Cooling (by BTU)
          1. Are any wastewater flow reduction techniques planned or under construction?
             a.  Yes	
             b.  No	
          2. If the answer to 1 is yes.
             d.  What is expected flow reduction, MGD	
             b.  When will these changes become effective, (give date)
             c.  Describe technology planned
                                            294

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PORTFOLIO A (continued)                                                                          CODE NO.	

V    EFFLUENT DISCHARGE INFORMATION
     A.  Wastewater Monitoring, Direct Dischargers and Dischargers to Publicly Owned Treatment Works.
                                                                                                           Grab or
                                           Sampling                      Parameters                       Composite
                                           Frequency    	Measured	          Sample
         1.  Intake Hater
             a.  Fresh water river/lake    	    	        	
             b.  Brackish or salt          	    	        	
             c.  Well                      	    	        	
             d.  Treated Wastewater -
                 recycled                  	    	        	
             e.  Municipal supply          	    	        	
             f.  Municipal sewage
                 effluent                  	    	        	
             g.  Rainwater                 	    	        	
             h.  Other
          2.   Discharges
              a.   Main treatment plant
              b.   Other non-stormwater
                  discharged

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PORTFOLIO A (continued)
                                                                                                 CODE NO.
     B.    Wastewater Effluent Limitations - Direct Dischargers  (NPDES Values) and Dischargers  to Publicly
          Owned Treatment Works.  (Pretreatment Limitations)
          Final July 1, 1977 - BPT Limitations (in pounds and/or concentration units   - give units  )  for main waste-
          water treatment system.
          1.   Parameter
              (1)  Oil & Grease
              (2)  BOD
              (3)  COD
              (4)  TOC
              (5)  TSS
              (6)  Phenolic
                  Compounds
              (7)  Chromium,
                  Total
              (8)  Chromium,
                  Hex.
              (9)  Ammonia
              (lO)Sulfides
              (11)Others
                                   a- Daily
                                     Average
-  Daily
Maximum
               c.Other
d.Dec. 1975
  DMR* Daily
  Avg. Values
e.Dec.  1976
  DMR* Daily
  Avg.  Values
              (12)
              (13)
          * EPA Discharge Monitoring Report Form

-------
PORTFOLIO A  (continued)
                                                                   CODE MO._
V    C.   Additional Information
          1.  If your refinery is a direct discharger, please give your:
              a.  NPDES permit number	
              b.  NPDES permit expiration date
                  Refuse Act/NPDES application number
              d.  Permitting authority receiving compliance data
              e.  Give process configuration factor* used for permit development

          2.  Are wastewaters discharged to the same water body used for process intake
              waters?  If yes, are discharges upstream or downstream of  process  intake  waters?
              a.  Yes	          op	          Down	
              b.  No	
              c.  If yes, which wastewaters?
          3.  Are "net discharge" values used in the NPDES permit limitations?
              a..  Yes	
              b.  No	
          4.  If your refinery is an indirect discharger, please give name of the muni-
              cipal sewage authority receiving your wastewater.
               *Ref:  Federal Register (40 CFR Part 419)
                                            297

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PORTFOLIO A (continued)                                          CODE NO.	

  VI   WASTEWATER TREATMENT

       A.   Attached is a block diagram showing most of the effluent treatment unit
            operations utilized in oil refineries.  Please use this diagram to indicate
            those treatment processes used in your facility.  Use lines with arrows
            to explain your refinery system.  For clarity, cross out those boxes not
            applicable.  Join all other boxes with lines indicating system connections.
            In addition, please include any available flow diagrams that can'supplement
            this information.

       B.   Additional Clarifications

            Please use the following page to present a narrative that will supplement
            the attached block flow diagram.  This narrative should include a sequential
            listing of the applicable waste treatment processes, including flow rates
            where available  and number and letter designations, as listed on the
            block diagram.  The narrative should also present clarifications where
            the block diagram cannot adequately describe your system.  Also describe
            all processes indicated as "other" on flow diagram.

            An example of a typical response is as follows:

                 Intake water

                      I.   Water from Lake Michigan (l.a.) is used for segregated,
                           once-thru cooling (2.a.)  at a rate of 3.0 MGD.

                      II.  Hater from a municipal supply  (I.e.) goes to all process
                           uses (0.8 MGD).  Other miscellaneous uses of municipal
                           supply total 0.02 MGD.

                 Industrial wastewater

                      I.   Segregated, once-thru cooling water (2.a.) is discharged
                           directly (3.0 MGD) to Lake Michigan (9.b.).

                      II.  Boiler blowdown (2.d.) at 0.04 MGD, blowdown from water
                           treatment system  (2-j.) at 0.03 MGD, sour water (2.i.) at
                           0.02 MGD, and contaminated runoff (2.g.) go to one API
                           separator (4.b.).

                      III. Oily process water (2.e.)  at 0.02 MGD and ballast water
                           (2.f.)  are discharged to another API separator (4.c.).

                 All wastewater from the two API separators are then combined in an
                 equalization basin (5.<=.)r fed to a dissolved air flotation unit
                 (6.b.), and discharged to a stabilization pond (7.d.).

                 Sanitary sewage (0.02 MGD) is treated in an activated sludge unit
                 (10.b.), and then pumped to the stabilization pond  (7.d.).

                 Effluent from the pond is discharged directly to Lake Michigan
                 (9.b.) at a rate of 1.30 MGD.
                                             298

-------
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-------
PORTFOLIO A  (continued)                                         „__ „_
^—^—^—~~———~                                              NO.
  VI   B.    Additional Clarifications
                                           300

-------
 PORTFOLIO A (continued)

                                                                   CODE NO.	

VI   c.   Future Modifications

          Please use the following spaces to describe wastewater  treatment plant
          modifications presently under construction or planned for the  future.
          Include flow rates, detention times,  and expected  operational  dates.
          In addition, please use the code numbers on the  block diagram  in your
          description.
                                       301

-------
                                                                CODE NO.
                            PETROLEUM REFINING INDUSTRY SURVEY

                     FOR REVISION OF "BEST AVAILABLE TECHNOLOGY" (BAT)
           EFFLUENT LIMITATIONS GUIDELINES AND NEW SOURCE PERFORMANCE STANDARDS

                                        PORTFOLIO B
NOTES
(1)   Portfolio B is to be mailed within 60 days of receipt to:

                             Robert B.  Schaffer, Director
                             Effluent Guidelines Division
                             U.S. Environmental Protection Agency (WH-552)
                             Washington, D.C.  20460

I    GENERAL INFORMATION
     A.   Name of Refinery_

     B.   Street Address
     C.   Refinery Contact_

     D.   Telephone Number
II   ADDITIONAL POLLUTANT INFORMATION

     Part of our scope of work, as specified in the U.S. District Court settlement
     agreement of June 7, 1976 (8 E.R.C 2120 D.D.C. 1976),  requires that we obtain
     analytical data and other information on the presence and removal of the priority
     pollutants included in Table IIA.  The questions listed in this portfolio are
     general in nature, and are meant to serve as a guide for future contacts to obtain
     more detailed information.
                                        302

-------
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                                                         303

-------
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304

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                                                                305

-------
                                                                  CODE N0._
II B.  Priority Pollutant #	
       Priority Pollutant Name
Directions;    For each substance that you have analyzed for in wastewater (i.e.
               for each substance checked in Column 3 in Table IIA) please fill
               out one copy of this page.  DUPLICATE THIS SHEET FOR EACH SUBSTANCE
               AS REQUIRED BEFORE ENTERING ANY INFORMATION ON THE ORIGINAL.

               Please indicate yes/no to the following questions:

a.   Is plant data available on the removal efficiency by biological treatment for
     this substance?

b.   If yes, please indicate treatment type, e.g. bench scale, pilot, or full scale.
c.   Is plant data available on the removal efficiency by sorption type treatment
     systems (e.g. carbon, clay, sludge, etc.) for this substance?	
d.   If yes, please indicate treatment type, e.g. bench scale, pilot, or full scale.
e.   Is plant data available on the removal efficiency of this substance by air or
     steam stripping processes (or any system which includes removal to the atmosphere,
     e.g. DAP)?	

f.   If yes, please indicate treatment type, e.g. bench scale, pilot, or full scale.
g.   Is plant data available on the removal efficiency by solvent extraction processes
     for this substance?	

h.   If yes, please indicate treatment type, e.g. bench scale, pilot, or full scale.
i.   Is plant data available on the removal efficiency by any other process for this
     substance?                      Specify process

j.   If yes, please Indicate treatment type, e.g. bench scale, pilot, or full scale.


k.   Is plant data available regarding health affects (acute or chronic) of this
     substance?

1.   Specify the analytical procedure
-------
Supplemental Flow Question
            307

-------
                          SUPPLEMENTAL FLOW QUESTION

The following data request does not relate to economics directly,  but is added
here because of comments made by the American Petroleum Institute  that your
responses to Question IV.B.of Portfolio "A" of the 1977 Petroleum  Refining
Industry Survey need further clarification.  This is a follow-up to the original
308 questionnaire sent to refineries in February or August of 1977 by Mr.
Robert B. Schaffer, Director of the Effluent Guidelines Division.

Please submit your completed response (page 3) within 14 days to:

                    Robert W.  Del linger (WH-552)
                    Effluent Guidelines Division
                    U.S. Environmental Protection Agency
                    401  M. Street S.W.
                    Washington, D.C. 20460

Wastewater Discharge Data

The attached figure includes a block flow diagram depicting various possible
wastewater flows present at petroleum refineries.  Please fill  in  the annual
average dry weather flow, for calendar year 1976, for each flow line applicable
to your refinery.  Do not supply additional data sheets.  The units for these
flow rates should be presented in million gallons per day only.If your
refinery has multiple streams of each type, the total of these  streams should
be used; i.e., assume your system is similar to the simplified  block flow
diagram attached.

Excluded Selected Wastewaters

It should be noted that the flow rates asked for may not correspond to actual
streams in the refineries.  For example, the physical influent  to  your end-of-
pipe treatment system may include storm water or ballast water. However,  the
flow rates to be reported should not include storm water, ballast  water,
sanitary wastewater, once-through non-contact cooling water, other non-refinery
related wastewater, nor any raw (untreated) wastewater reused within the
refinery complex.

The following definitions apply to each flow line:

1.   Total Refinery Wastewater Excluding Selected Wastewaters - Excluding the
selected wastewaters above, this "flow line" includes non-segregated cooling
water, cooling tower blowdown, boiler blowdown, oily process water, sour water
water treatment system blowdown and "other refinery-related wastewaters".  It
includes all of the above mentioned wastewaters regardless of disposition.

Oily process water by implicacion includes all wastewaters generated at the
refinery and which are not covered under any other above-mentioned specific
categories (i.e., sour water).   Oily process water includes, but  is not
limited to, such wastewaters as contact process water, non-sour process con-
densates, vent scrubber water, tank drains, flare seal water blowdown, lab-
oratory drains, maintenance shop drains, hydrotest waters, maintenance de-
contamination waters, pad wash waters, fire waters and system test waters, and
barometric condenser water blowdowns.  The above "other refinery-related waste-
waters" would include, but are not limited to, wastewaters from blowdown from
air pollution control equipment and wastewaters originating at the wastewater
treatment plant.  Additionally, this stream is based on net flow and includes
                                   308

-------
each wastewater only once.  For  example,  if  the  sour water stripper blowdown is
used in the desalter then only the  desalter  water would be included to avoid
double accounting  the  sour water.

2.   Untreated Refinery Hastewaters  Excluding Selected Wastewaters to POTW
Excluding the selected wastewaters  listed on page 1, this flow line includes
untreated (by an EOPS) refinery  wastewater that  is discharged to a POTW
(Publicly Owned Treatment Works). For  the purpose of this  survey , oil/water
separation is considered an end-of-pipe treatment but sour water stripping is
not.

3.   Untreated Refinery Wastewater  Excluding Selected Wastewaters to Other
Disposal - Excluding the selected wastewaters listed on pace 1. this flow line
includes untreated (by EOPS)  refinery  wastewater that is not disposed of via an
NPDES permit, nor  discharged  to  a POTW.  This type of discharge includes deep
well disposal,~Tand application, contract disposal, evaporation, percolation,
etc.

4.   Wastewater Treatment Influent  Excluding Selected Wastewaters - Excluding
the selected wastewaters listed  on  page 1, this flow line includes the dry
weather refinery wastewater flow which receives end-of-pipe treatment.  Please
note that flow line 4  should  equal  flow line 1 les.s flow lines 2 and 3.

5.   Recycled Treated  Wastewater Excluding Selected Wastewaters - txcluding
the selected wastewaters listed  on  page 1, this flow line includes that portion
of the dry weather, end-of-pipe  treatment effluent that is recycled for use in
refinery operations.

6.   Treated Wastewater Excluding Selected Wastewaters to POTW - Excluding the
selected wastewaters listed on page  1, this  flow line includes that portion of
the dry weather, end-of-pipe  treatment effluent which is discharged to a POTW.

7.   NPDES Discharge Excluding Selected Wastewaiers - Excluding the selected
wastewaters listed on  page 1, this  flow line includes that portion of the dry
weather end-of-pipe treatment effluent which is a direct discharge under an
NPOES permit.

8.   Treated Wastewater Excluding Selected Wasiewaters to Other Disposal   -
Exc1uding the selected wastewaters  listed on page 1, this flow line includes
that portion of the dry weather, end-of-pipe treatment effluent which is not
covered in flow lines  6 and 7.   This type of disposal includes deep well
injection, land application,  contract  disposal, evaporation, percolation, etc.

Please review the  attached example,  which is given in two steps, before answering
the questions.  Step 1 (pages 4  and  5) is a  calculation of required flow rates
and Step 2 (page 6) is essentially  the example summary answer sheet that upon
completion would be transmitted  back to EPA.

NOTE:  The main purpose of the attached example is to clarify the above.defini-
tions.  In Step 2  of the example it  may become apparent that only certain
flows are needed to determine the required flow rates.  J_t should be noted
that the calculation procedure would vary from refinery to refinery because
"the required flow  rates could be obtained by either additions or subtractions
oTVarious requireTTTows.  Thus for each refinery one should determine what
flows are required to  answer the gTven questions.  We do not require that you
submit your work sheets; you  need only submit the completed summary
page (page 3).
                                 309

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Refinery Name_
                                               Location
                                                             (dty,  state)
                       Recycled Treated Wastewater
\
Ref 1 nery

i ^ ^
To PC
2
TW Tc
0
3
Otl
SPO!

Refinery
EOPS
rer
al


\
To PC
•c
TV NPDE
01SC
nisonsal
7
S
harge
Flow
Line
Number

  1
Flow Line Identification
(a)
                                                   Annual  Average
                                                    Dry Weather
                                                        Flow
                                                   Calendar Year
                              (million gallons/day)
                                                                  etc)
         Total Refinery Wastewater Excluding
         Selected Wastewaters

         Untreated Production Wastewater
         Excluding Selected Wastewaters to
         POTW

         Untreated Refinery Wastewater
         Excluding Selected Wastewaters to
         Other Disposal

         Specify Other Disposal	
         Uastewater Treatment Influent
         Excluding Selected Wastewaters

         Recycled Treated Wastewater
         Excluding Selected Wastewaters

         Treated Wastewater Excluding
         Selected Wastewaters to POTW

         NPDES Discharge Excluding
         Selected Wastewaters

         Treated Wastewater Excluding
         Selected Wastewaters to Other
         Disposal
         Specify Other D1sposal_
 In addition, please Indicate the source
 and flow rate for pump gland cooling water
          Source
  (a)  These flow lines are aa defined in the narrative.
  (b)  Refinery EOPS refers to any end-of-plpe Wastewater treatment
      systen  (including oil water aeparacion).
  (c)  Indicate whether flow value la measured, estimated, or
      calculated (To be considered a calculated flow, the calculation
      muat be based on all measured flow*.).
  (d)  Please  fill in all flow lines; i.e.. Indicate zeros where applicable.
                                   310

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                                    Calculation of Uastewater Flows at XYZ Refining Company:
Flow Line Identification
                                       Uastewater  Included or  Excluded
Annual Average Dry
Weather Calendar Year
1976 Flow, Million
Gallons per Day
1.
2.
3.
4.
Total refinery wastewater
excluding selected waste-
waters
Untreated refinery waste-
waters excluding selected waste-
waters to a POTW
Untreated refinery wastewater
excluding selected wastewaters
to other disposal
Wastewater treatment influent
excluding selected wastewaters
Wastewater Balance
Total wastewater influent to EOPS
Ballast water
Storm water
Untreated refinery wastewaters to a POTW
Untreated refinery wastewater to other disposal
Total
Boiler blowdowns
Water treatment systems blowdown
Total
Spent caustic wastewaters
Air pollution control equipment blowdowns
Total
Total wastewater treatment influent
Ballast water
Storm water
Total
Flow Lines
1
-2
-3
-4
Difference should equal 0.0
5.97 (M ]
-0.05 {M ,
-0.02 (tr
+0.9 (M
+0.303 (M;
77TT»3 (E;
0.2 (M)
0.7 (M)
i
0.9 (C)3
0.003 (M
0.3 (M
07303 (M)
5.97 (M
-0.05 (M
-0.02 (E
~579tT(E)
7.103
-0.9
-0.303
-5.9
0.0
«
Measured
Estimated
Calculated based on measured flows
If dry weather flows are known, storm water contributions  can  be  ignored.

-------
                                        Step  1  Calculation of Wastewater flows at XYZ Refining Company (continued)
U>
M
NJ
                  Flow  Line  Identification
                                                     Wastewater Included or Excluded
  Annual  Average  Dry
  Weather Calendar  Year
  1976  Flow,'Million
  Gallons per  Day	
                  5.    Recycled wastewater  excluding selected
                       wastewaters

                  6.    Treated wastewater excluding selected
                       wastewaters  to POTW

                  7.    NPOES Discharge excluding selected
                       wastewaters
     Treated wastewater, excluding selected
     wastewaters to other disposal
                                                     Recycled treated wastewaters
                                                     Treated wastewaters discharged to a POTW
                                                     Total wastewater discharged to stream
                                                     Ballast water plus storm water
                                                                      Other disposal of treated wastewaters
          1.98   (E)


          0.0


          3.97   (M),
         - .047  (E)
total     T3T (E)

          0.0
                                                                                                                                  1
                                                                                                                         1.98
                                                                                                                        +0.0
                                                                                                                        +3.92
                                                                                                                        +0.0
Wastewater Balance                                   Flow Lines

                                                           5
                                                          +6
                                                          +7
                                                          +8

                                                        Total
                                                          -4
                                                     Difference should be close to 0.0

                                                     (May not be exactly 0.0 because of losses
                                                      in EOPS, such as blowdowns and evaporation)

_]_/ A measured flow of 2.0 million gallons of treated effluent is recycled per day.Some storm water and ballast water
are recycled with the treated effluent.  This equals (2.0/5.97)(0.05 + 0.02) = .0235 million gallons per day.   Therefore,
the estimated value of 2.0 - .0235 or 1.98 is shown.  If dry weather flows are known, and no ballast water is  discharged
to the treatment system, this calculation is unnecessary.
2/ Based on calculation of that portion of ballast and storm water that is recycled.  Ballast water olus storm water
equals 0.07 - 0.0235 = 0.0465 or 0.047-

-------
Refinery Name XVg
                                EXAMPLE
                                              Location
                                                            (city, state)
                       Recycled  Treated Wastewater
1






1 . *


1


2


,!

Refinery
EOPS










ifi
•*• a uuier
fHsoosal

7
Flow
Line
Number

  1
                     To  POTW  To Other
                             Disposal
                                                        To  POTW
                                                                 NPDES
                                                                 Discharge
                 Flow Line  Identification
                                         'a'
                                         Annual  Average
                                          Dry Weather
                                              Flow
                                         Calendar Year

                                            1976
                                     (million gallons/day)
                                                                        Flow Basisl
Total Refinery Wastewater  Excluding
Selected Wastewaters

Untreated Production  Wastewater
Excluding Selected  Wastewaters to
POTW

Untreated Refinery  Wastewater
Excluding Selected  Wastewaters to
Other Disposal

Specify Other Disposal ejey-ioe-i/

Wastewater Treatment  Influent
Excluding Selected  Wastewaters

Recycled Treated Wastewater
Excluding Selected  Wastewaters

Treated Wastewater  Excluding
Selected Wastewaters  to  POTW

NPOES Discharge Excluding
Selected Wastewaters

Treated Wastewater  Excluding
Selected Wastewaters  to  Other
Disposal

Specify Other Disposal     —
                                                    7-103
                                                    0.303
                                                    I-1&
                                                    0.0
                                                     0.0
In addition,  please Indicate  the source
and flow rate for pump  gland  cooling water
          Source
                                            l-o
 (a)  Thaaa Clow Llnef  are  a«  dtflnvd In ch« aamciva.
 (b)  Refinery EOPS refers  Co  any end*of-pipe westevacer creacmenc
      •yacea (Including oil water separation).
 (c)  Indicate whether  flow value la measured, estimated, or
      calculated (To be considered a calculated flow, the calculation
      must be based on  all Masured flows.).
 (d)  Pleaae fill In all flow  lines; i.e.. Indicate zeros where applicable
    fe*il*if
                                   rteuee,
                              313

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              APPENDIX 2
EPA Regional Surveillance and Analysis

  Sampling Survey, Analytical Results
        for Priority Pollutants
                    315

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Refinery 1
             EPA REGIONAL SURVEILLANCE AND ANALYSIS SAMPLING SURVEYS
                   ANALYTICAL RESULTS FOR PRIORITY POLLUTANTS*
                            (Concentrations in ug/1)
     A.  Intake water (all Day 1 grab samples)

         1.  Volatile organics
             a   Preserved:
             b.   Unpreserved:
                                 chloroform
                                 chloroform
                                 methylene chloride
               29

               531
             L 10
         2.   Semivolatile organics:   not detected
         3.   Metals:
                                   L  5
                                   L  5
                        antimony
                        arsenic
                        beryllium  L  5
                        cadmium    L 10
                        chromium
                        copper
                                   L  5
                                   L 10
lead
nickel
selenium  L  5
silver    L  5
thallium  L
zinc
L  5
L  S
   1
L 10
         4.   Phenolics
         5.   Cyanide:

         6.   Mercury:
         7.   Asbestos:
                                   L  2
                                   L 0.5
                                   not sampled
     B.   Wastewater treatment system influent

         1.   Volatile organics (Day 1 grab  sample/Day 2  grab sample)
             b.   Unpreserved:
             a.  Preserved:        benzene                     NA /165
                                   ethylienzene                NA/L 10
                                   methylene chloride          NA/L 10
                                   toluene                     NA/L 10
                                   vinyl chloride              NA/L 10

                                   benzene                     27/230
                                   1,1,2,2,-tetrachloroethane  L 10/ND
                                   chloroform                  L 10/L 10
                                   1,2-trans-dichloroethylene  L 10/L 10
                                   ethylbenzene                L 10/17
                                   methylene chloride          32/ND
                                   tetrachloroethylene         L 10/14
                                   toluene                     43/180
(1)  L  - Less than
(2)  NA - Not analyzed
(3)  ND - Not detected

*  Sampling and analysis conducted for volatile organics,  semivolatile
   organics and metals as listed on Table  III-4, unless noted.  Only
   detected priority pollutants are reported.
                                 316

-------
         2.   Semivolatile organics:  (48 hour composite sample/blank)

             acenaphthene                         11/ND
             naphthalene                          47/ND
             phenol                               37/ND
             bis(2-ethylhexyl)  phthalate          17/ND

         3.   Metals:  (48 hour composite sample/blank)
antimony
arsenic
beryllium
cadmium
chromium
copper
L 5/L 5
L 5/L 5
L 5/L 5
L 10/L 10
L 5/L 5
14/L 10
lead
nickel
selenium
silver
thallium
zinc
46/L 5
L 5/L 5
L 5/L 5
L 5/L 5
C. 8/L 1
130/L 10
         4.   Phenolics:         37
            (composite of 2 daily grab samples)

         5.   Cyanide:         L  2
            (composite of 2 daily grab samples)

         6.   Mercury:         2/L 0.5
            (48 hour composite sample/blank)

         7.   Asbestos:        not sampled

     C.   Wastewater treatment system effluent

         1.   Volatile organics (Day 1 grab sample/duplicate/blank)

             a.  Preserved:   methylene chloride       L 10/L 10/L  10

             b.  Unpreserved: methylene chloride       L 10/L 10/L  10

             Volatile organics (Day 2 grab sample/duplicate)

             c.  Preserved:   methylene chloride       L 10/L 10
                              toluene                  ND/L 10

             d.  Unpreserved: methylene chloride       L 10/L 10
                                                               4
         2.   Semivolatile organics:  (48 hour composite sample)

             bis(2-ethylhexyl)  phthalate     11
             phenol                          76
(4)   Sample bottle containing blank for semivolatile  organics was broken
     and contents were lost.
                                  317

-------
3.  Metals:  (48 hour composite sample/blank)
    antimony
    arsenic
    beryllium
    cadmium
    chromium
    copper
L  5/L  5
L  5/L  5
L  5/L  5
L 10/L 10
L  5/L  5
L 10/L 10
lead
nickel
selenium
silver
thallium
zinc
12/L  5
L  5/L  5
L  5/L  5
L  5/L  5
L 10/L  1
19/L 10
4.  Phenolics       113
    (composite of 2 daily grab samples)

5.  Cyanide:            3
    (composite of 2 daily grab samples)

6.  Mercury:          L 0.5/L 0.5
    (48 hour  composite sample/blank)
7.  Asbestos:
                     not sampled
                          318

-------
Refinery 83

     A.  Sour water stripper influent  (all Day 1 grab samples)

         1.  Volatile organics
             benzene
             toluene
             ethylbenzene

         2.  Semivolatile organics

             phenol
             2,4 Dimethylphenol
             naphthalene
             bis(2-ethylhexyl)phthalate
             fluorene
             phenanthrene and/or anthracene
             di-n-butyl-phthalate

         3.  Metals

             copper
             silver
             zinc

         4.  Phenolics

         5.  Cyanide

         6.  Mercury

         7.  Asbestos

     B.  Sour water stripper effluent (all Day

         1.  Volatile organics

             benzene
             toluene
             ethyl benzene

         2.  Semivolatile organics

             phenol
             2,4-dimethylphenol
             naphthalene
             bis(2-ethylhexyl)phthalate
             acenaphthene
             fluorene
             phenanthrene and/or anthracene
             di-n-butyl-phthalate
        G  4840
        G  7000
           3030
        42000
          100
         5410
        L 50
        L 50
         210
        L 50
        70.0
         8.1
        70.0

          NA

          14

           2

    not sampled

1 grab samples)
        G 4840
        G 7000
          1750
          7000
           230
           700
        L  100
        L  100
        L  100
           700
        L  100
(5)   G  x - Detected greater than x

(6)   Values for copper should be viewed with caution due to new piping
     on sample tap.
                                319

-------
         3.   Metals

             cadmium                                     1
             chromium                                  11
             copper                                    150
             lead                                     130
             zinc                                     630
             arsenic                                    50

         4.   Phenolics                                  NA

         5.   Cyanide                                    120

         6.   Mercury                                    ND

         7.   Asbestos                             not sampled
                                                 Q
     C.   Intake water #1 (all Day 1 grab samples)

         1.   Volatile organics                         ND

         2.   Semivolatile  organics (grab sample/duplicate/blank)

             bis(2-ethylhexyl)phthalate                 10/40/L 10
             di-n-butyl-phthalate                    L 10/L 10/ND

         3.   Metals

             zinc                                       7

         4.   Phenolics                                  13

         5.   Cyanide                                    ND

         6.   Mercury                                   0.7

         7.   Asbestos                             not sampled
                                                 9
     D.   Intake water #2 (all Day 1 grab samples)

         1.   Volatile organics (arab sample  fU/duplicate)

             methylene  chloride                      L 10/L 10
             chloroform                              150/80
             bromodichloromethane                     30/20
             dibromochloromethane                   L 10/L 10

         2.   Semivolatile  organics (grab sample)

             bis(2-ethylhexyl)phthalate                 10
             di-n-butyl-phthalate                    L 10

(7)   Values  for metals  should be  viewed  with caution due to new copper
     line on sample tap, with cadmium, brass and  galvanized fittings.

(8)   Well water intake.

(9)   Municipal water  intake.
                                   320

-------
    3.  Metals

        copper                                     30
        zinc                                       80

    4.  Phenolics                                  NO

    5.  Cyanide                                    NA

    6.  Mercury                                   0.4

    7.  Asbestos                              not sampled

E.  Wast-B^ater treatment system influent

    1.  Volatile Organics  (Day 1 grab sample/Day 2 grab sample)

        chloroform                                10/10
        bromodichloromethane                    t, 10/L 10
        trans-l,3-Dichloropropene                 10/10
        toluene                                  340/430
        ethylbenzene                              20/20

    2.  Semivolatile organics (Day 1, 24 hour composite samples)

        phenol                                     910
        chlorophenol                                50
        2,4-dichlorophenol                        L 10
        pentachlorophenol                           40
        naphthalene                                230
        bis(2-ethylhexyl)phthalate               L 100
        fluorene                                 L 100

    3.  Metals (Day I/Day 2 grab samples - Day I/Day 2, 24 hour
        composite samples)

        chromium (hex)                       NA/138-55/98
        copper                               NA/40-130/30
        lead                                 NA/6-27/18
        zinc                                 NA/480-1700/530
        arsenic                              NA/NA-35/ND
        cadmium                              NA/NA-1.7/1.2
        chromium (total)                     NA/2600-3600/1200

    4.  Phenolics (Day I/Day 2 grab sample)    11700/6050

    5.  Cyanide
        (Day 1 grab sample/Day 2 grab sample)      16/36

    6.  Mercury (Day 2 grab sample)                0.6

    7.  Asbestos                               not sampled
                             321

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F.  Wastewater treatment system effluent

    1.  Volatile Organics (Day 1 grab sample/Day 2 grab sample)

        methylene chloride                        L 10/ND
        chloroform                                L 10/L 10
        toluene                                   L  5/L  5

    2.  Semivolatile Organics (Day 1, 24 hour composite samples)

        2,4 dimethylphenol                         L 10
        pentachlorophenol                          L 20
        bis(2-ethylhexyl)phthalate                 L 10
        fluorene                                   L 10
        phenanthrene and/or anthracene               80
        di-n-butyl-phthalate                       L 10

    3.  Metals (Day I, 24 hour composite sample/Day 2, 24 hour
        composite sample/Day 2 grab sample)

        chromium                               320/370/480
        copper                                   20/ND/20
        lead                                      6/ND/ND
        zinc                                   570/480/620

    4.  Phenolics
        (Day 1 grab sample/Day 2 grab sample      75/125

    5.  Cyanide
        (Day 1 grab sample/Day 2 grab sample)       8/3

    6.  Mercury (Day 2 grab sample)                0.5

    7.  Asbestos                               not sampled
                               322

-------
Refinery 131

     A.  Intake water #1   (all grab samples)

         1.  Volatile organics

             1,1,1-trichloroethane                      6.2
             chloroform                                11.6
             1,2-transdichlorethylene                  47.0
             ethyIbenzene                               0.3
             methylene chloride                         0.3
             dichlorobromomethane                       3.5
             chlorodibromomethane                       1.0
             tetrachloroethylene                        0.3
             toluene                                    0.02
             trichloroethylene                          0.03

         2.  Semivolatile organics

             bis(2-ethylhexyl)phthalate                 2.8

         3.  Metals

                                                        6.0
                                                        0.6
                                                        0.1
                                                      250.0

                                                        9.5

                                                         ND

                                                         NO

                                                    not sampled

                        12
     B.  Intake water #2   (all grab samples)

         1.  Volatile organics

             1,1,1-trichlorethane                      2.0
             1,1-dichloroethylene                      0.7
             ethyIbenzene                              0.1
             methylene chloride                        3.7

         2.  Semivolatile organics                     ND

(10)   Municipal water intake.  9% of total intake flow.

(11)   Sample blanks at Refinery 131 analyzed for all semivolatile organic
      samples.  No parameters detected for sample blank analysis.

(12)   Well water intake.  1% of total intake flow.

4.
5.
6.
7.
copper
lead
nickel
zinc
Phenolics
Cyanide
Mercury
Asbestos
                                 323

-------
         3.   Metals

             antimony                                   4"514
             beryllium                                  0.5
             copper                                      1•0
             lead                                      12.0
             nickel                                      1.0
             zinc                                       7.0

         4.   Phenolics                                  ND

         5.   Cyanide                                    ND

         6.   Mercury                                    0.3

         7.   Asbestos                               not sampled

     C.   Intake water #3

         1.   Volatile organics  (grab samples)

             chlorobenzene                              0.05
             1,2-dichloroethane                         2.10
             1,1,1-trichlorethane                       2.60
             chloroform                                15.30
             1,1-dichloroethylene                       0.10
             methylene chloride                        27.00
             bromofonn                                  0.80
             tetrachloroethylene                         2.30
             trichloroethylene                           2.30

         2.   Semivolatile organics  (24  hour  composite  samples)

             bis(2-ethylhexyl)phthalate                 35

         3.   Metals

             antimony                                  ^^1/1
             beryllium                                   4
             cadmium                                    10
             chromium                                   61
             copper                                      59
             lead                                      180
             nickel                                      54
             zinc                                      130

         4.   Phenolics (grab  sample)                     8.6

         5.   Cyanide (grab sample)                        ND

         6.   Mercury (24 hour composite sample)          0.3

         7.   Asbestos                               not sampled


(13)   Salt water intake.   90% of  total  intake  flow.

(14)   Estimated value.
                                     324

-------
D.  Wastewater treatment system influent

    1.  Volatile organics (grab samples)

        benzene                                   110.0
        1,2-dichloroethane                          7.2
        1,1,1-trichloroethane                       7.8
        1,1-dichloroethane                          0.2
        chloroform                                  3.5
        ethyl benzene                               4.4
        methyl chloride                             3.4
        toluene                                   250.0

    2.  Semivolatile organics (24 hour composite samples)

        naphthalene                                106
        phenanthrene                                72
        2,4-dimethylphenol                         460
        phenol                                     140

    3.  Metals (24 hour composite samples)

        antimony                                   82.0
        beryllium                                   4.0
        cadmium                                     7.5
        chromium                                  2 80.0
        copper                                    125.0
        lead                                      140.0
        nickel                                     54.0
        zinc                                      290.0

    4.  Phenolics (grab sample)                    3290

    5.  Cyanide (grab sample)                      ND

    6.  Mercury (24 hour composite sample)          ND

    7.  Asbestos                              not sampled

E.  Waste treatment system effluent

    1.  Volatile organics (grab samples)

        1,2-dichloroethane                         2.6
        1,1,1-trichloroethane                      2.7
        chloroform                                 0-4
        ethyIbenzene                               0.1
        methylene chloride                         0-7

    2.  Semivolatile organics (24 hour composite samples)

        acenaphthylene                             1.4
                               325

-------
3.   Metals (24 hour composite samples)

    antimony                                   64
    beryllium                                  40i4
    cadmium                                     5
    chromium                                   35i4
    copper                                     18
    lead                                      110
    nickel                                     37
    zinc                                       38

4.   Phenolics (grab sample)                     34

5.   Cyanide (grab sample)                       ND

6.   Mercury (24 hour composite sample)          ND

7.   Asbestos                              not  sampled
                           326

-------
Refinery 132 1S

     A.  Intake water

         1.  Volatile organics  (grab samples)

             1, 2-dtchloroethane                         1.6
             1,1,1-trichloroethane                      0.8
             chloroform                                 9.4
             1,1-dlchloroethylene                       2.0
             methyl chloride                            4.7
             bromoform                                  1. i
             tetrachloroethylene                        8.1
             trichloroethylene                         19.o

         2.  Semivolatile organics (grab sample/blank)

             1,2-dichlorobenzene                        4.8/ND
             1,4-dichlorobenzene                        0.4/ND
             bis(2-ethylhexyl)phthalate                 41/38
             di-n-butyl phthalate                       2.1/4.3
             phenol                                     3.1/ND

         3.  Metals (grab sample/blank)14

             beryllium                                  NA/0.5
             chromium                                   NA/3
             lead                                       NA/9

         4.  Fhenolics (grab sample)                      20

         5.  Cyanide (grab sample)                        ND

         6.  Mercury (grab sample/blank)                NA/0.83

         7.  Asbestos                               not sampled
(15)   Fresh and municipally supplied intake waters were not sampled,
      since they contribute only ten percent of the process water
      usage.  The saltwater intake was sampled.

      Influent to the waatewater treatment system consists of the
      refinery discharge and discharges from two chemical manufacturing
      plants.   Discharges from chemical plant tl, chemical plant f2
      and influent to the wastetreatment were sampled.   The refinery
      discharge could not be sampled since it is mixed  with chemical
      plant #2 discharge prior to oil-water separation.   Priority
      pollutants that are attributable to the refinery  discharge may
      be  calculated from reported sample concentration  and flow values
      at  chemical plant #1 (1.65 MGD), chemical plant #2 (0.97 MGD) and
      the influent (6.9 MGD)  to the treatment system.
                                     327

-------
B.  Chemical manufacturing plant #1 discharge

    1.  Volatile organics (grab samples)

        benzene                                   48.C
        chloropenzene                              6.1
        1,1,1-trichloroethane                      0.9
        chloroform                                37.0
        ethylbenzene                              67.0
        methyl chloride                            3.8
        tetrachloroethylene                        1.7
        toluene                                  250.0
        trichloroethylene                          5.9

    2.  Semivolatile organics (grab samples/blank)

        1,2-dichlorobenzene                       450/ND
        1,4-dichlorobenzene                       850/ND
        naphthalene                               270/ND
        di-n-butyl phthalate                      9.7/4.3
        anthr acene                                6.9/ND

    3.  Metals (24 hour composite sample/blank)

        antimony                                  290/ND
        beryllium                                   6/0.9!"
        cadmium                                   2/0.9
        chromium                                   58/6
        copper                                     55/ND .
        lead                                      360/21
        nickel                                     74/ND
        silver                                     15/ND
        zinc                                     1500/ND

    4.  Phenolics (grab sample)                     2480

    5.  Cyanide (grab sample)                       ND

    6.  Mercury (24 hour composite sample/blank)    1.1

    7.  Asbestos                               not sampled

C.  Chemical manufacturing plant #2 discharge

    1.  Volatile organics (grab samples)

        benzene                                   36.0
        chloroform                                 1.4
        toluene                                   15.0
        trichlorethylene                           1.3

    2.  Semivolatile organics (24 hour composite sample/blank,

        isophorone                                450/ND
        bis(2-ethylhexyl)phthalate                170/38
        di-n-butyl phthalate                      5.1/4.3
        anthracene                                1.5/ND
        2,4-dimethylphenol                        215/ND
        phenol                                     10/ND
                                328

-------
    3.  Metals (24 hour composite sample/blank)
        antimony
        beryllium
        cadmium
        chromium
        copper
        lead
        nickel
        silver
        zinc
170/ND
  8/0.8

  2
     "

 95/3
260/ND
     *-
140/ND
1.8/ND
950/ND
    4.  Phenolics (grab sample)                     1000

    5.  Cyanide (grab sample)                       ND

    6.  Mercury (24 hour composite sample/blank)   1.8/ND

    7.  Asbestos                               not sampled

D.  Wastewater treatment system influent

    1.  Volatile organics (grab samples)
        benzene
        1,2-dichloroethane
        1,1,1-trichloroethane
        chloroform
        ethylbenzene
        methylene chloride
        toluene
        tri chloroethylene
 1200.0
   17.0
    4.3
   26.0
  320.0
    4.2
 2960.0
    8.2
    2.  Semivolatile organics (24 hour composite sample/blank)
        1,2,4-trichlorobenzene
        1,4-dichlorobenzene
        fluoranthene
        isophorone
        naphthalene
        bis(2-ethylhexyl)phthalate
        butyl benzyl phthalate
        anthracene
        2,4'dimethylphenol
        phenol

    3.   Metals (24 hour composite sample/blank)

        antimony
        beryllium
        chromium
        copper
        lead
        nickel
        silver
        zinc
   1.5/ND
  1230/ND
   4.5/ND
   230/ND
   240/ND
   230/38
     8/ND
    61/ND
   380/ND
  1150/ND
   130/NJ
    56/6
    67/ND
   260/20^
    55/3 14
    17/ND
   480 /ND
                              329

-------
    4.  Phenolics (grab sample)

    5.  Cyanide (grab sample)

    6.  Mercury (24 hour composite sample/blank)

    7.  Asbestos

E.  Hastewater treatment system effluent

    1.  Volatile organics (grab samples)

    n.  Semivolatile organics (24 hour composite

        isophorone
        bis(2-ethyIhexyl)phthalate
        di-n-butyl phthalate

    3.  Metals (24 hour composite sample/blank)

        antimony
        beryllium
        chromium
        copper
        lead
        nickel
        silver
        zinc

    4.  Phenolics (grab sample)

    5.  Cyanide (grab sample)

    6.  Mercury (24 hour composite sample/blank)

    7.  Asbestos
    23200

      50

   0.5/0.7

not sampled



      ND

sample/blank)

    270/ND
     75/38
    8.8/4.3
     98/ND
      7/1
         14
     40/5
     16/ND
    160/4J
     39/314
    1.9/ND
    140/ND

      27

      ND

    1.2/0.5

 not sampled
                             330

-------
Refinery 133

     A.  Intake water (all grab samples)

         1.  Volatile organics

             benzene
             1,1-dichloroethane
             1,1,2,2-tetrachloroethane
             chloroform
             1,1-dichloroethylene
             methylene chloride
             tetrachloroethylene
             toluene

         2.  Semivolatile organics

         3.  Metals14

             cadmium
             chromium
             copper
             zinc

         4.  Phenolics

         5.  Cyanide

         6.  Mercury

         7.  Asbestos

     B.  Wastewater treatment system influent

         1.  Volatile organics (grab sample/blank)

             benzene
             chloroform
             1,1-dichloroethylene
             methylene chloride
             toluene
                                               14
2.  Semivolatile organics

3.  Metals (24 hour composite samples)

    antimony
    cadmium
    chromium
    copper
    lead
    nickel
    zinc
         4.  Phenolics (24 hour composite sample)
                                              L 10
                                              L 10
                                              L 10
                                              L 10
                                              L 10
                                              L 10
                                              L 10
                                              L 10

                                               NA
                                               11
                                                5
                                                6
                                              190

                                               4.2

                                               ND

                                               0.414

                                           not sampled
                                              220/L 10
                                              L 10/ND
                                              L 10/L 10
                                              L 10/190
                                              300/L 10

                                               NA
                                                        93
                                                        90
                                                       160
                                                        21
                                                       110
                                                        38
                                                       420

                                                      1790
                                      331

-------
    5.  Cyanide (24 hour composite sample)          ND

    6.  Mercury (24 hour composite sample)          ND

    7.  Asbestos                                not sampled

C.  Wastewater treatment system effluent before chlorination

    1.  Volatile organics (grab sample/blank)
        chloroform
        1,1-dichlorethylene
        methylene chloride
        toluene
L 10/L 10
L 10/L 10
L 10/470
L 10/L 10
    2.  Semivolatile organics                  not sampled

    3.  Metals                                 not sampled

    4.  Phenolics (grab sample)                     2.1

    5.  Cyanide                                     ND

    6.  Mercury                                 not sampled

    7.  Asbestos                                not sampled

D.  Wastewater treatment system effluent after chlorination

    1.  Volatile organics

        a.  Preserved grab sample/blank

            chloroform                            L 10/L 10
            1,1-dichloroethylene                  L 10/L 10
            methylene chloride                    L 10/310
            toluene                               L 10/L 10
            chlorodibromomethane                  L 10/ND

        b.  Unpreserved grab sample/blank

            chloroform                            L 10/L 10
            1,1-dichloroethylene                  L 10/L 10
            methylene chloride                    L 10/340
            toluene                               L 10/L 10
            chlorodibromomethane                  13/ND
            bromoform                             L 10/ND
            dichlorobromomethane                  L 10/ND
            1,2-dichloroethane                    ND/L 10

    2.  Semivolatile organics                       NA
                              332

-------
                                      14
3.  Metals (24 hour composite samples)

    cadmium                                      35
    chromium                                      4
    copper                                        6
    zinc                                         200

4.  Phenolics (grab sample)                       2.1

5.  Cyanide (grab sample)                         ND

6.  Mercury (24 hour composite sample)            0.4

7.  Asbestos                                 not sampled
                           333

-------
Refinery 134

     A.  Intake Water #1 16

         1.  Volatile organics (grab samples)

             carbon tetrachloride                        0.1
             1,2-di chloroethane                          1. 2
             1,1,1-trichloroethane                       0.5
             1,1-di chloroethylene                        0.6


         2.  Semivolatile organics (grab samples)         ND

         3.  Metals (grab samples)

             cadmium                                     2
             chromium                                   7814
             copper                                    250i4
             lead                                       30*4
             nickel                                      5
             zinc                                      120

         4.  Phenolics (grab sample)                      7.4

         5.  Cyanide (grab sample)                        ND

         6.  Mercury (grab sample)                       0.4

         7.  Asbestos                                 not sampled

     B.  Intake Water #218

         1.  Volatile organics (grab samples)

             1,2-dichloroethane                          5.2
             1,1,1-trichloroethane                       2.2
             chloroform                                  0.2
             1,1-dichloroethylene                        0.5
             1,2-dichloropropane                        40.0
             methylene chloride                          1.2
             tetrachloroethylene                         1.0
             toluene                                     0.1
             trichloroethylene                           0.4

         2.  Semivolatile organics (grab samples)

             bis(2-ethylhexyl)phthalate                  635
             di-n-butyl phthalate                         23
             di-n-octyl phthalate                         74

(16)  Well water intake.

(17)  Sample blanks at Refinery 134 analyzed for all Semivolatile
      organic samples.  No parameters detected for sample blank analysis.

(18) ' Iver water intake.
                                 334

-------
              14
    3.  Metals   (grab samples)
        lead
        nickel
        zinc

    4.  Phenolics (grab sample)

    5.  Cyanide (grab sample)

    6.  Mercury (grab sample)

    7.  Asbestos

C.  Wastetreatment system influent

    1.  Volatile organics (grab sample)

        benzene
        1,2-dichloroethane
        1,1,1-trichloroethane
        chloroform
        1,2-dichloropropane
        methylene chloride
                                                       8
                                                       4
                                                      61

                                                     126

                                                      ND

                                                     0.4

                                                 not sampled
                                                      11.0
                                                       5.8
                                                     285.0
                                                       0.5
                                                       7.2
                                                      41.0
    2.  Semi volatile organics (24 hour composite sample)
        naphthalene
        anthracene
        fluorene
        pyrene

    3.  Metals (24 hour composite/blank)

        antimony
        chromium
        copper
        lead
        nickel
        zinc

    4.  Phenolics (Day 1 grab sample)

    5.  Cyanide (Day 1 grab sample)

    6.  Mercury (24 hour composite sample/blank)

    7.  Asbestos

D.  Sand filter effluent

    1.  Volatile organics (grab samples)

        1,2-dichlorethane
        1,1,1-trichlorethylene
        1,1-dichloroethylene
        ethylbenzene
        methylene chloride
        toluene
                                                     260.0
                                                      30.0
                                                      13.0
                                                       2.7
                                                   1014/NP4

                                                    310/3 14
                                                     I?/56
                                                   10^/ND
                                                      3370

                                                       ND

                                                     O.;/ND

                                                  not sampled
                                                       0.6
                                                       9.7
                                                       0.6
                                                       0.1
                                                       4.0
                                                       0.2
                            335

-------
    2.  Semivolatile organics (24 hour composite samples)
        bis(2-ethylhexyl)phthalate
        di-n-butyl phthalate

    3.  Metals (24 hour composite samples)

        chromium
        copper
        nickel
        zinc

    4.  Phenolics (grab sample)

    5.  Cyanide (grab sample)

    6.  Mercury (24 hour composite sample)

    7.  Asbestos

E.  Wastewater treatment system effluent

    1.  Volatile organics (grab samples)

        1,2-dichloroethane
        1,1,1-trichloroethane
        chloroform
        1,2-dichloropropane
        methylene chloride
        bromoform
        chlorodibromomethane

    2.  Semivolatile organics (24 hour composite

        bis(2-ethylhexyl)phthalate

    3.  Metals (24 hour composite sample/blank)

        chromium
        copper
        zinc

    4.  Phenolics (grab sample)

    5.  Cyanide (grab sample)

    6.  Mercury (24 hour composite sample/blank)

    7.  Asbestos
       43
      210
       69
       22
14
14
      27014

      11.6

       ND

       0.3

   not sampled
       0.7
       2.0
       1.3
       1.3
       7.0
       0.5
       2.4

sample/blank)

      38/ND
     9
        /514
     270/5
       7.4

        ND

      0.5/ND

   not sampled
                              336

-------
Refinery  157

     A.   Intake water

          1.  Volatile organics:                     not sampled

          2.  Semivolatile organics:                      tro19

          3.  Metals

             antimony                                  L 100
             arsenic                                       9
             beryllium                                  L 25
             cadmium                                       4
             chromium                                    L S
             copper                                       17
             lead                                          6
             nickel                                     L 25
             selenium                                    L S
             silver                                      L 5
             thallium                                  L 100
             zinc                                        237

         4.  Phenolics                                    NA

         5.  Cyanide                                      NA

         6.  Mercury                                     0.2

         7.  Asbestos                               not sampled

     B.  Bio-oxidation pond influent

         1.  Volatile organics                      not sampled

         2.  Semivolatile organics

             phenol21                                  G 100
             bis(2-ethylhexyl)phthalate                10-100
             diethyl phthalate                         10-100
             dimethyl phthalate                        10-100
(19)   Not detected at 10 ug/1 or above (some substances may  have
      somewhat higher or lower detection limits).

(20)   Other phenols or cresols (including o-cresol, p-cresol,  and  three
      dimethyl phenol or ethyl phenol isomers)  which  are  not among the
      list of 129 priority pollutants were found in this  sample.

(21)   Phenol was present in this sample at about 100  mg/1, but is
      reported as G 100 ug/1 in accordance with the analytical protocol.
                                337

-------
    3.  Metals
        antimony
        arsenic
        beryllium
        cadmium
        chromium
        copper
        lead
        nickel
        selenium
        silver
        thallium
        zinc

    4.  Phenolics

    5.  Cyanide

    6.  Mercury

    7.  Asbestos

C.   Wastetreatment system effluent

    1.  Volatile organ!cs

    2.  Semivolatile organics

    3.  Metals

        antimony
        arsenic
        beryllium
        cadmium
        chromium
        copper
        lead
        nickel
        selenium
        silver
        thallium
        zinc

    4.   Phenolics

    5.   Cyanide

    6.   Mercury

    7.   Asbestos
    150
      6
   L 25
      3
     15
    100
      8
   L 25
    950
    L 5
  L 100
    267

   230,000

     3,500

  L 0.2

 not sampled



 not sampled

    ND
 L 100
    28
  L 25
     8
    20
    12
     8
    30
    18
   L 5
   100
   242

    34

   7.5

   0.2

not sampled
                             338

-------
Refinery 181

     A.  Intake water22(sample/blank)

         1.  Volatile Organics

             a.  Preserved

                 benzene
                 chloroform
                 chlorodibromomethane
                 methylene chloride
                 dichlorobromomethane

             b.  Unpreserved

                 chloroform
                 chlorodibromomethane
                 methylene chloride

     B.  API Separator #1 effluent water

         1.  Volatile Organics (sample/blank)

             methylene chloride

     C.  API Separator #2 effluent water

         1.  Volatile Organics  (sample/blank)

             benzene
             toluene
             ethylbenzene
             methylene.chloride
                                        22
     D.  API Separator #3 effluent water

         1.  Volatile organics (sample/blank)

             benzene
             toluene
             ethylbenzene
             methylene chloride

     E.  Untreated Sour /Ammonia water

         1.  Volatile organics (sample/blank)

             benzene
             toluene
             chlorobenzene
             ehtylJbenzena
   L 1/L 1
    11/1
     8/ND
     2/39
    10/ND
    48/1
    19/ND
     5/39
    38/39
   5330/L 1
   4010/1
     25/ND
    527/39
   4650/L 1
   5560/1
    829/ND
    313/39
1060000/L 1
7580000/1
 741000/ND
 831000/KD
(22)   Semivolatiles,  metals,  phenolics,  cyanide,  mercury,  and asbestos
      not sampled.   Preserved blanks at  Site A were composited with
      other unpreserved blanks at sites  B,  C, D,  E, F,  G fi H.

(23)   m/p-xylene and o-xylene concentration reported.
                                   339.

-------
                                               ,22
F.  Wastewater treatment system influent

    1.  Volatile organics (sample/blank)

        benzene
        toluene
        ethylbenzene
        methylene chloride

G.  Wastewater treatment system effluent

    1.  Volatile organics (sample/blank)

        benzene
        toluene
        ethylbenzene
        methylene chloride

H.  Wastewater treatment system effluent #2

    1.  Volatile organics (sample/blank)

        benzene
        toluene
        chloroform
        ethylbenzene
        methylene chloride

I.  Final wastewater treatment system effluent

    1.  Volatile organics (sample/blank)

        methylene chloride

    2.  Semivolatile organics (sample/blank>

    3.  Metals
                                                22
                                                      43800/L 1
                                                        266/1
                                                        368/ND
                                                       1350/39
                                                        113/L 1
                                                         99/1
                                                         77/ND
                                                        206/39
                                                     50300/L 1
                                                      3310/1
                                                       300/1
                                                       422/ND
                                                      2660/39
                                                   24
                                                         9/26

                                                        ND/ND

                                                         NA
(24)   69.  di-n-octyl  phthalate  &  99.  endrin  aldehyde  not  reported  but
      analyzed as  not detected.   Blanks  at Site  I  analyzed  separately
      from other sites.   Phenolics,  cyanide,  mercury,  and asbestos not
      sampled.
                                  340

-------
                           APPENDIX 3






                  American Petroleum Institute



                         Sampling Results






(As extracted from "Analysis of Refinery Wastewaters for



the EPA Priority Pollutants," Interim Report, API Publica-



tion 4296, May 1978.)
                              341

-------
                                                                        CONCENTRATION OF PRIORITY LIQUID/LIQUID EXTRACTABLE ORGAN ICS AT REFINERY (
U)
^
ro

PARAMETER
NAPHTHALENE
ACENAPHTHYLEfiE
ACENA*HTKEN£
FLUOREUE
? HE NANTHflE ME /ANTHRACENE
PnENANTHHENE
ANTHRACENE
D1ETH1L PHTHALATE
FLUGaANTHENE
FYREt.E
DI-N-BU7YL PHTHALATE
CKRY£EfJE/BENZ( A) ANTHRACENE
CNRYSENE
3 IS( 2-ETHYLHEIYL )PHTHALATE
• ENZ 1 A > ANTHRACENE
DENZOf A)PYRENE
PE'J;0(O.H. DPERYlENE
PHENOL
2-4-OlttETHrLPHENOC


( 6)

(28)
(29)
(30)
(31)
(33)
(36)
(37)
OB)
(43)
(43)
(33)
(35)

DATE EPA
6
6
6
6
6
6
4
6
6
A
6
6
&
6
6
6
6
6
6
INT/
RADIAN
NDK 1
ND« 1
ND«. 1
ND«. I
MDK 1
-
-
3 a
ND«. 1
ND« 1
1 4
ND«. 1
-
16
-
NDK. 1
NDK. 3
NDK. 1
ND« 2
WE WATER
COMPANY OTHER
(6)
1 D«3 )
) B«40 )
) D«40 )
) NDK 1 )
)H -
NDK. 00)
ND« 01 )
_
) ND«. 02)
) NDK 02)
-
)H
NDK. 01)
-
NDK 01)
) 04
) NO «. 07 1
)
)
UASTEUATEH FEED TO B10TREATMCNT
EPA RADIAN COMPANY OTHER
(6)
22 3OO
NDK. 1 ) 20O
riDK. 1 ) 30
29 NDK. 1 ) C
6 4 H
2.7C
NDK. 01 > C
^60
NDK 1 ) . 3 C
1 1 C -
a a
. 3 H
- . 3
-IB
.1C
NDK. 1 ) 1 C
NO 1C a > . 2 C
13000
3000
FINAL EFFLUENT
EPA RADIAN COMPANY QTHEH
<6>
NDK. I 1 30
NDK 1 > DK10 »
NDK 1 > DK10 )
. 6 NOK 3 >C
NDK 1 )H -
NDK 2 1C
NOK. ODC
NDK 3 )
NDK. 1 ) 1C
1. 9 11C
2 -
3 M -
2 C -
2. 6
. OS C
.4 .1C
NDK. 2 > 3 C
1.9
-S3
                                D(I) - COrtPOUNO WAS DETECTED AT SOME CONCENTRATION LESS THAN X.  BUT THE CONCENTRATION COULD NOT BE QUANTIFIED.
                                ClI) - COMPOUND UAS DETECTED AT A LEVEL GREATER THAN X
                                ND(X>- COMPOUND WAS NOT DETECTEDi  X EQUALS THE LOWEST LIHIT OF SENSITIVITY OF THE METHOD FOR THAT SAMPLE
                                C    - ONE OF TWO OR MORE REPORTED VALUES FOR THIS SAMPLE
                                H    - THESE COMPOUNDS ARE INDISTINGUISHABLE IN THIS SAMPLE AS ANALYZED BY THE EPA PROTOCOL
                                t    - NAPHTHALENE.  ACENAPHTHALENE,  AND ACENAPHTHENE iY CROO CC HETHODl   OTHER SPECIES BY CC-UV METHOD.

-------
                                                                           CONCENTRATION OF PRIORITY VOLATILE OROANICB AT REFINERY I
CO
^
U)
PARAMETER
METHYLENE CHLORIDE
CHLOROFORM
1. a-DICKLOROETHANE
TRANS-1. 3-DICHLOROPROPENE
TRICHLOROETHYLENE
C13-1. 3-OICHLOROPROPENE
BENZENE
TOLUENE
ETHVLEENZENE

DATE EPA
< 6) t
2
3
6
111) 1
a
3
4
(12) 1
2
3
4
117) 1
a
3
4
118) 1
2
3
6
(20) 1
a
3
6
122) 6
126) 6
128) 6
INTAKE
RADIAN
11 Z
NDX. 3 >
NDXS >
NDX. 7 )
DX1 I
NDX. 7 )
DK! )Z
1 Z
DK1 )Z
WATER
COMPANY OTHER
DX. 9 >
6 C
NDXI )
DX. 9 )C
DX. 9 IE
NDXI 1
NDXI 1
NDXI 1
NDXI 1
NDXI )
NDXI )
DX2 )
Dxa i
DX20 )
UASTEUATER FEED TO 1IOTREATMENT
EPA RADIAN COMPANY OTHER
(2)
DX. 9 1
DX. 9 )C
-12-
9
NDXI 1C
NDX. 3 )
DX. 9 ) E
NDXI ) CE
NDXS I
NDK1 )
N&XI )
- 3 - -
NDXI 1
NDXI I
-2 -
NDXI )
NDXI
20
53 1000
93 2000
9 100
FINAL EFFLUENT
EPA RADIAN
13 Z
NDX 3 1
NDXS >
1
2
NDX. 7 1
0X1 )Z
OKI )Z
DX1 )Z
COMPANY OTHER
121
DX )
DX )
DX. )
DX 1
DX )
DX 1
DX 9 IE
NDXI IE
NDXI IE
NDXI 1
NDXI )
NOXI I
NDXI )
NDXI )
NDXI >
NDXI 1
NDXI )
NDXI I
0X10 1
DX10 1
DX4O )
                           DO)  -  COMPOUND  WAS DETECTED AT SOME CONCENTRATION LESS THAN X.  BUT THE CONCENTRATION COULD NOT DE QUANTIFIED.
                           CII)  -  COMPOUND  UAS DETECTED AT A LEVEL GREATER THAN X.
                           NDIO-  COMPOUND  UAS nOT DETECTEDi  X EQUALS THE LOUEST LIMIT OF SENSITIVITY OF THE METHOD FOR THAT SAMPLE.
                           C     -  ONE  OF TUO OH MORE REPORTED VALUES FOR THIS SAMPLE
                           E     -  MAXIMUM VALUE.  REPORTED VALUE MAY INCLUDE OTHER SPECIES UH1CH CONTRIBUTE TO THE MEASURED CONCENTRATION
                           Z     -  BLANK  DATA FOR THIS PARAMETER INDICATES CONTAMINATION
                           2     -  ORCANOHAL1DES BY BELLAR CC METHOD;   OTHER VOLATILE SPECIES BY CHOB CC METHOD

-------
                                                                               CONCENTRATION OF TRACE ELEMENTS AT REFINERY p  ue/L
U)

£>

PARAMETER
ZINC
CHftoniun
COPPER
LEAD
BERYLLIUM
ANTIMONY
THALLIUM
NICKEL
ARSENIC
SELENIUM
SILVIA
CADniun
MERCURY


< 1 >
( 2)
< 3)
f 4)
( 3)
< 6)
( 7)
( 8)
« 9)
( lOt
(11)
(12)
(13)

DATE
6
2
3
6
6
6
A
6
6
6
6
6
6
6
6
INTAKE
RADIAN
23
3 8
65
11
ND«1 >
14
NO «a >
3 3
ND«1 )
4
9
S
. 4
; UATE8
COMPANY OTHER
HAWHSLEY
10
10
32
9
ND«10 >
26
9
ND«JO )
NP«30 )
-
NDK2 )
-
-
1
ND«1 )
-
MASTEWATER FEED TO BIOTREATMENT
RADIAN COMPANY OTHER
HAWKSLEY
49 12
23
75
- 32
79 50
62 6
S 26
ND(O ) NDCC10 )
37 ND«30 )
ND«2 )
49 ND«2 )
10
9 - -
633
13 ND«1 )
3
FINAL E
RADIAN
27
94
32
3
NDK1 )
36
ND«2 )
2. I
14
74
4 2
1 1
8
:FFLUENT
COMPANY OTHER
HAWKSLEY
10
71
65
30
3
46
NDK10 )
ND«30 >
-
ND«2 )
-
-
2
NDIC1 >
-
                        DtX)  -  COMPOUND WAS  DETECTED AT SOME CONCENTRATION LESS THAN X.  BUT THE CONCENTRATION COULD NOT BE QUANTIFIED
                        CO)  -  COMPOUND UAS  DETECTED AT A LEVEL CHEATED  THAN X
                        ND(X>-  COMPOUND UAS  NOT  DETECTEDi  X EQUALS THE LOWEST LIMIT OF SENSITIVITY OF THE METHOD FOR THAT SAMPLE.

-------
                                                                                       CONCENTRATION OF TRACE ELEHENTB AT REFINERY
U)
^
Ul

PARAMETER
tlNC
CHROMIUM
COPPE*
LEAD
BERYLLIUM
ANTINOMY
THALL1UH
NICKEL
ARSENIC _
SELENIUM
B1LVER
CADMIUM
nCRCUHV


1 II
i ai
1 3)
1 41
1 91
1 41
1 7)
« B)
I 91
HOI
Ull
1121
1131
INTAKE WATER UABTCUATEM FEED TO B1OTREATHENT FINAL EFFLUENT
DATE RADIAN COMPANY OTHER RADIAN COMPANY OTHER RADIAN COMPANY OTHER
4 ... --. ...
3 - NDIC10 1 >M - 1110
4 _._ __. _._
4 .-- _-» _-,
4 __* __- _-.
4 --- _-- ---
4 -_- --- ---
4 _-- ___ __.
4 -__ .-_ ._-
4 .-- ... ---
4 ... --- -_-
4 ___ _-_ ___
4 _-- _-_ ___
| __- _-_ ...
3 .-- --- .--
                                Dill - COnFOUND HAS DETECTED AT  3ONE CONCENTRATION LESS  THAN «. BUT THE CONCENTRATION COULD NOT BE OUANTIFUD.
                                BISI - CONFOUND UAg DETECTED AT  A LEVEL CHEATER  THAN X.
                                KDI1I- CONFOUND HAS NOT  DETECTED: « EQUALS  THE LOWEST LINIT  OF  SENSITIVITY OF  THE ItETHDD FDR THAT SAMPLE
                                1    - EPA DATA ON THIS  BAHPLE POINT ALSO OBTAINED FROM  ANALYSIS BV EPA REOION V.

-------
                                                                                                    CONCENTRATION OF PRIOM1TV  VOLATILE OHOANICS AT
U)
^
CTi
PAftAnElER
HETHYLENE CK-OfllDC
1. 1-DICrt.UflOeiHkNE
CHLCftOFOftfl
l.a-DlCHLORO£lHAN£
1. 1. 1-TfllCtt^ONOETHANE
CAABON TETRACHUWIDE
inonODlCHLCAOnE THANE
1. 2-DICH-C«WHOPA«£
Tfl I CMLOSOCTHYLENE
BENZENE
1.1.2. 2-TETHACMLOBOeTHENE
TCLUENE
ETKV1.ftENZErC

ND(X>- COMPOUND W
- POSSIBLE I
- ONE OF TWO
- MAX i nun VA
- VALUE CONS
- BLANK DATA
- PUROE AND

DATE
1 6) 1
3
3
6
f V) 1
2
3
&
(11) 1
a
3
6
1 !?> 1
a
3
6
1131 1
2
3
A
U4> I
2
3
6
US) 1
a
3
*
<1A) 1
3
(IS) 1
3
3
4
<22> I
3
3
A
<24) 1
2
3
*
(24) 1
2
3
6
128> 1
a
3
6


HAD IAN COMPANY OTHER
17) SPECTRIX
33 S
40 S
BO S
A I
76
- 4
ND«I )
7
13
16
ND«1 >
3
3 S
3
NDK1 >
1
32
- 4
NDKI )
9
t
- 5
NDKI )
3 A -
ia A
ND«\
01 -:i )
i
ND ( -: i
NDKI )
NO«I I
ND«1 )
ND«I )
NDKI »
»E
ND«1 )
NDKI )
NDKI )
HO(CI »
D(Cl )
DIC1 >
0«1 »
NDKI 1
OKI )
OKI 1
OKI t
NDKI >

DENTIFICA110N
OR MORE REPORTED VALUES FOR THIS SAMPLE
FOR THIS PARAttETER
TRAP OC HETHOD UTIL
INDICATES CONTAMINATION
UNO FID AND HALL DETECTORS

RADIAN COrlPANV OTHER
(7) SPECTRIX
1O 5
li 3
10 3
29 CZ
DK1 )
OKI )
OKI )
ND«1 1C
12
IS
- I
NDKI K
OUl 1
OKI '
OKI t
NDKi )C
1
DtCl )
D(C1 I
IS C
OKI )
OKI )
OKI 1
2 Cl
OKI )
OKI )
OKI I
I-DK1 )C
OKI •
NDKI )
to
NDKI >C
NDKI )
NbKI )
NDKI )
NOK.I >C
«0
33O
iao
S40 C
ND<-:i )
NDKI }
NOK1 t
NDKI 1C
830
730
640
BO C
- 40
- 40
50
NDKI »C



RAD I AN C CMP ANY OT HER
(7 I SrECTHU
4« 3
55 9
10 5
OKI 1
D< :i i
OKI I
OKI I
OKI 1
OKI 1
OKI »
OKI I
OKI )
DC. I l
OKI t
OKI 1
OKI J
OKI )
OKI '
OKI t
OKI I
OKI 1
NDKI 1
- 5
NDKI 1
NDKI 1
NOKl )
OKI )
DtCl 1
DK1 i
NDKI >
MDKI >
NDKI 1
OKI .
OKI 1
OKI >
OKI )
OKI >
OKI )


-------
                                                                            CONCENTRATION OF  PRIORITY  LIQUID/LIQUID EXTRACTADLE ORGANIC
                                                                                                                                                      f.
                                                                                                                                        3 AT Itr1NERV £h
U)
PARAMETER
I.4-D1CHLOROOENZENE
1.2-aiCHLMoaENZEME
NAPHTHALENE
ACENAPHTHfcNE
FLUQRENE
PHENANTHRENE / ANTHR ACENE
PHENANTHRENE
ANTHRACENE
FLUOR AN THE NE
PYHENE
Dl-N-IUTVL PHTHALATE
CHRVSENE
PHENOL
2-4- D IF1E THYLFHCNOL

DATE
I 2) 6
( 41 6
( B) 1
3
A
119) 1
3
6
117) 1
3
6
(24) &
(23> 1
3
3
129} 1
3
6
<3O> 1
3
4
(31) 4
Ob) 6
193) 1
2
3
6
1991 A
INTAKE WATER
RADIAN
-
-
~
'-
-
-
-
-
~
~_
~
-
-
~
COMPANY
IB)
-
-
ND ( 1 1 >
NDKI >
NDKI )
NDKI )
NDKI )
NDKI )
-
NDK 3 )
NDK 9 »
NOK2 I
NDK2 >
NDK. 9 )
NDK S )
NDK 9 )
NDK- 9 >
-
-
NDK2O I
NDK2O )
NDK20 )
-
UASTEUATER FEED TO DIOTREATMENT
OTHER
SPECTR1X
NDKI )
NO K 1 >
\
NDKI )
N&K1 )
NDKI >H
-
-
NDKI t
NDKI )
-
-
NDKI )
NDKI >
RADIAN COMPANY
IB)
-
-
NDKI >
NDKI >
NDKI )
ND K 1 )
NDKI )
ND K 1 )
-
NDK 3 i
NDK 9 >
NDK2 >
NDK2 >
8 F
9 E
3 E
3 E
-
-
3OOO
6OOO
aoco
-
OTHER
SPECTR I R
NOK1 >
NDI'Il )
NDKI )
NDKI )
NDKI >
NDKI )H
-
-
NDKI >
\
-
-
;
NDKI )
FINAL EFFLUENT
RADIAN COMPAN> GTHER
IB> SPECTR IX
NDKI '
MDI-.l 1
NDI ') 1
NO. a
t.O ( - 1 >
NDKI I -
NDKI )
NDI-:I t
NDKI 1
ML. :j )
NDKI I H
NDK S »
NDK2 >
NDKZ >
NDK 9 1
NDK 9 1
NDKI )
NDK 3 »
NDK 3 1
NDi :i i
-
ND(-2O 1
NDK20 »
NDK2O )
-
                                     0(X> - COMPOUND WAS DETECTED AT SOME CONCENTRATION LESS THAN X. BUT THE CONCENTRATION COULD NOT  BE  QUANTIFIED
                                     G(X> - COMPOUND WAS DETECTED AT A LEVEL CHEATER THAN X
                                     ND- COMPOUND UAS NOT DETECTED.  X EQUALS THE LOWEST LIMIT OF SENSITIVITY OF THE METHOD FOR  THAT SAMPLE
                                     E    - nAiinun VALUE.  REPORTED VALUE HAY INCLUDE OTHER SPECIES WHICH CONTRIBUTE TO THE MEASURED  CONCENTRATION
                                     H    - THESE COMPOUNDS ARE INDlSTINGUISHAOLE IN THIS SAMPLE AS ANALYZED 3V THE EPA PROTOCOL.
                                     B    - PHENOLS AND POLYNUCLEAR AROMATIC HYDROCARBONS ANALYZED DV HPLC METHODS

-------
                                                                                                       CONCCOTRMION OF T««E ELEICHT9 »T
U)
4^
CD
s»
PARAMCTEM D.
ZINC t 11
CMRoniun i a>
COPPCH 1 3)
LEAD t 4)
•ERYU.1UH ( 31
ANTIMONY ( 4)
TWACLlUrt ( 71
NICKEL ( •)
ARSENIC ( 91
KLENtin (10)
SILVER 
HEftCURY U31
INTAKE MATER
klASIEUATER FEED TO DI'-".. *ENt
ATE RADIAN COnPANY OTHER RADIAN CUrtT'~n. JTHLR
lOb
106
28
37
64
47
- 47
ND«3 )
36
30
17
19
11
- e
9
29
21
- 3O
NDIO 1
NDCO )
NDK3 )
33
93
7O
NDK3 )
NDK9 )
ND«9 >
- 7
- 12
3
A
NDICS )
NDtO 1
3
- 4
3
13
OtX) - CIWOUNO UAS DETECTED AT SDnE CONCENTRATION LESS THAN X
0 - COMPOUND UAS DETECTED AT A LEVEL CHEATER THAN 1

- 60
41
- 33
106
89
NDtO >
9
- 26
- 37
- 26
20
1
- 8
19
27
27
64
e
6
- 7
- 44
67
-BO
NDtCS )
NDtO )
NbtO )
17
22
- 32
NDtO »
NDtO 1
liO
13
?
- 10
- 09
OUT THE CONCENTRATION COULD NOT DE QUANTIFIED
SENSITIVITY OF THE METHOD FOR TllAl SAMPLE

FINAL FFtt UEH1
f-lTMAN • ••1PANV OTHER
- 46
99
- 46
- 63
- 71
60
4fl
10
14
- 28
- 30
- IB
- 2
12
21
- 36
- 32
- 67
6
e
ND«3
02
69
- 66
ND(CS I
NDKS )
NKO >
19
- 12
30
174
MDK3 •
ND(-;S )
- 3
- 16
07


-------
                                                                             CONCENTRATION OF PRIORITY VOLATILE OROANICB AT REFINERY
e
                                                                     MAKEUP WATER
                                                                                                     UABTEWATER FEED TO BIOTREATHENT
                                                                                                                                                         FINAL EFFLUENT
OJ
PARAMETER

HETHYLENE CHLORIDE



1. I. I-TRICHLOROETHANE



CARBON TETRACHLOR1DE

BENZENE


TOLUENE


ETHYLBENZENE



DATE RADIAN

1 4) 1
a
3
4
(13) 1
a
3
4
(14) 2
4
(22) 1
a
4
124) 1
3
4
(26) 1
a
a
4
COMPANY OTHER
17.91
4
5
B
-
95
58
51
-
NDKI 1
-
4
S
-
13
15
-
DK. 9 )
DK. 9 )
4
~
RADIAN COMPANY OTHER
17. 9»
_
NDKI >
- - -
- - -
-
NDKI )
- - -
-
NDKI 1
_
-
NDKI >
_
_
NDKI )
-
^
NDKI 1
~ - -
- - -
RADIAN COMPANY OTHER
(7.9)
_
NDKI 1
-
_ _ -
_
NDKI 1
_
_
NDKI >
- - -
-
NDKI )
- - -
_
NDKI 1
- - -
- _ _
NDKI )

_
                             D(» - COMPOUND WAS DETECTED AT SOME CONCENTRATION LESS THAN  X. BUT THE CONCENTRATION COULD NOT BE  QUANTIFIED.
                             G«l - COMPOUND UA9 DETECTED AT A LEVEL GREATER THAN X.
                             NDUD- COMPOUND WAS NOT DETECTED! X EOUALB THE LOWEST LIMIT OF SENSITIVITY OF THE METHOD FOR THAT SAMPLE
                             Z    - BLANK DATA FOR THIS PARAMETER INDICATES CONTAMINATION
                             7    - PURSE AND TRAP OC METHOD UTILIZING FID AND HALL DETECTORS.
                             9    - EPA AND COMPANY SAMPLES WERE COLLECTED AND ANALYZED.   DATA  IB FROM COMPANY SAMPLES

-------
                                           CONCENTRATION  OF PRIORITY LIQUID/LIQUID EXTRACTABLE ORGANICS AT  REFINERY
PARAMETER
NAPHTHALENE
ACENAPHTHEME
PHENANTHfiENE/ ANTHRACENE
FLUOflANTHENE
PYRENE
SAMPLE
DATE
( B>
<19>
(24)
(29)
(3O)
6
6
6
6
b
CHRY£ENE/BENZ(A)AMTHftACENE (33) 6
B I S ( 2 -ETHYL HEX YL ) PHTHALATE
BENZO(B>/(K)FLUORANTH£NE
BENZO
(45)
(33)
OS)
(SB)
6
6
6
6
6
&
6
&
HAS DETECTED
MAS DETECTED
MAKEUP WATER

HASTEUATER FEED TO BIOTREATMENT FINAL EFFLUENT
RADIAN COMPANY OTHER RADIAN COMPANY OTHER RADIAN COMPANY OTHER
3. 6
5
146
3. 4
65
7t>
5
32
8
4
25
4
3
ND « 1 3
-
-
HC
C
C
CH
E
HC
ce
c
c
-
E
)
AT SOME CONCENTRATION LESS THAN X,
AT A LEVEL GREATER THAN X
NO«IO ) - »
NDK10) - - NDK10 )
44 HC- - 4HC-
NDtClO )C 2 C
-39C- - 5C-
16 CH - 1 4 CH -
-22E- - 1O E -
9 HC - - 2 HC
7. 8 C£ - - 9 CE -

5 C ND«10 )C
1 2 C - NDK10 )C
6 59
-HE- -BE-
ND«15 ) - 2 -
BUT THE CONCENTRATION COULD NOT BE QUANTIFIED
C    -  Oft OF TWO OR  MORE REPORTED VALUES FOR THIS SAMPLE
E    -  MAXIMUM VALUE,  REPORTED VALUE  MAY INCLUDE OTHER  SPECIES WHICH CONTRIBUTE TO THE  MEASURED CONCENTRATION
H    -  THESE COMPOUNDS ARE INDISTINGUISHABLE IN THIS SAMPLE AS ANALYZED  BY THE EPA PROTOCOL

-------
Ul
                                                                                                     CONCINTHATIIM OF IftACC CLCWITt AT
                                                                                               f-
                                                                                       MAKEUP WATER

                                                                                    RADIAN    COMPANY
                                                                     UABTEUATKR PCED TO BIOTRKATHENT

                                                                             RADIAN  COMPANY    OTHER
                                                                                                                                                                      RADIAN   COMPANY
1INC « II 1


CHROMIUM t 81

COPPEIt c 31


LEAD 1 41

BERYLLIUM I 91


ANTIMONY < 41


THALLIUM | 71

MICHCL < 11

ARCEMIC 1 »1

SELENIUM 1101

•ILVU 4111

CADMIUM 1121

MERCURY 113)


-
-


„




.


.

-
*
-
;
',
-
"
:
-
-
-
;
-
-
-
230
230
2OO
93
47
M
43
270
2*0
3
3
3
NDK
MD«
NDK
4
4
4
NOK
NDK
NDK
33
90
39
IS
10
"_
It
If
NOK
NDK
NDK
NDK
NOK
NDK
NDK
NOK
NDK










II
II
11



II
II
11






II
11
11
11
11
11
11
II
II


I
-
"
.

I
-
'
,

-
_

"
;
~
-
~
;
-
;
~.
-
-
-
'-
-
-

..
I
-
~
_

~
-
I
_

~
_

~
:
~
-
~
-
~
:
i
-
-
;
-
-
-
220
320
3*0
as
33
9S
32O
3M
440
9
4
9
NDK 1 I
NOK > I
NDK 1 I
11
4
4
a
2
NDK I 1
119
49
119
37
33
33
31
34
39
NDK II
NDK 11
NDK II
NDK II
NDK II
NDK II
NOK II
NOK II
NDK 11

_
~
-
~
_

~
-
-
_

I
_

I
-
-
;
-
-
~
:
~
;
^
:
-
-
-
»••••»••••
_
~
:
i
_

~
-
~
_

i
_

~
-
-
-
~
:
*•
;
I
;
~
;
:
-
-
170
170
"?
14
II
30
7,

120
NDK
NDK
2
HOK
NDK
NDK
11

* _
NDK
NDK
4B
4O
49
2O
19
14
II
14
NDK
NDK
NPK
NDK
NDK
NDK
NDK
NDK
NDK
" "
-
-
2
:
_

~
ii
11

ii
ii
ii
_

i
11
ii
:
-
;
I
-
I
M
II
II
11
II

II
Dill - COMPOUND 1MB DETECTED AT SOME CONCENTRATION LESS THAN I,
0(11 - COMPOUND MAS DETECTED AT A LEVEL  OREATER THAN X
NDIII- COMPOUND MAS NOT DETECTED!  X EOUM.S THE LOWEST LIMIT OF
I    - CONCENTRATION REPORTED AS 0 0
3    - EPA DATA ON THIS SAMPLE POINT ALSO OBTAINED FROM ANALYSIS BY EPA REGION V.
                                                                                                                  TIVITY OF THE hETHOD FOR THAI SAMPLE

-------
to
                               NICKEL                     < 8)  6

                               ARSENIC                    ( 9>  t>

                               SELENIUM                   (10)  1
                               SILVER                      (til  6

                               CADMlun                    (12)  6

                               MERCURY                    I13>  1
                                                                                                 CONCENTRATION OF TRACE ELEMENTS AT REFINERY jj. US/L



                                                                                  INTAKE  HATCH                   UASTEHATEH FEED TO BIOTREATMCNT                                        Ul>                                       (II >
CHROniun
COFFER
LEAD
BERYLLIUM
ANTIMONY
THALLIUM
t a>
I 3)
1 4)
t 3)
< 6)
< 7>
1 - - 940 - -
3 - - 13OO - -
6 - ND«30 ) - - -
6 ___ ___ ___
! _-_ ___ ___
2 ___ ___ .__
3 -__ ___ -___
6 - ... _
6 __- _-_ __-
1 ___ ___ _._
                                         D(X>  - COMPOUND HAS DETECTED AT SOME CONCENTRATION LESS  THAN X.  BUT THE CONCENTRATION COULD NOT OE QUANTII
                                         01X)  - COMPOUND UAS DETECTED AT A LEVEL GREATER THAN  X
                                         ND(il)- COMPOUND UAS NOT DETECTED! X EQUALS THE LOWEST LIMIT  Of SENSITIVITY OF THE METHOD F0« THAT SAMPLE
                                         4     - PHENOUICS AND CYANIDE DATA FROM RSkERL.
                                         11    - COMPOSITE OF 9 API SEPARATORS AND 010  PONO INLET

-------
                                                     (CONTINUED)  CONCENTRATION OF TRACE ELEMENTS AT REFINER Y{/»  UO/I.


                                      UA8TCUATER FEED  TO •JOTflEATMENT (A3)       UASTEHATER FEED TO B1OTREATNENT  (M4)       WASTE WATER FEED TO eiOTREATHENT  IR»)

         PARAMETER              DATE           RADIAN    COMPANY     OTHER                 AAOIAN   COMPANY     OTHER                  RADIAN   COWANY    OTHER


ZINC                       (1)1                ...                     ___                     _-„
                                 2                -__                     _..                     ___
                                 3                -          -          -                     ___                     .._
                                 4                ___                     _-_                     .         .          _

CHROMIUM                   13)1                __-                     __-                     __.
COPPER                     < 3)
LEAD                       t 4>

•ERYLLIUn                  I 3)

AMTlnONY                   I 4)

THALLIUM                   < 7)
NICKEL                     ( B>

ARSENIC                    < V>

SELENIUM                   (1O)
                                 a
SILVER                      (111  4
CAoniun                     iia>  6
HERCURY                     (13*   1
                                  2
          DID - COnPOUNO HAS  DETECTED AT  SOME CONCENTRATION LESS THAN X.  IUT THE CONCENTRATION COULD NOT DE QUANTIFIED
          OCX) - COMPOUND UAS  DETECTED AT  A LEVEL GREATER THAN X
          NO!!)- CCfVOUND UAS  NOT  DETECTED.  X  EQUALS THE LOWEST LIMIT OF SENSITIVITY OF THE METHOD FOR THAT SAMPLE

-------
U)
(«                       ANTIMONY
                                                                                 CONTINUED)   CONCENTRATION OF TRACE ELEMENTS AT REFINERY |f_ UO/L


                                                                               D TO BIOTREATHENT                    FINAL EFFLUENT
                                                          SAMPLE  	
                                   PARAMETER               DATE           RADIAN    COMPANY     OTHER                 RADIAN   COMPANY    OTHER


                          ZINC                        (I)  6                -__                      ___

                          CHROMIUM                    <  2)  I                -                                          -

                                                            3                -                                          -
                                                            6                -                                          -       ISO          -

                          COPPER                      (31  6                _-_                      _         _          _

                          LEAD                        (4)6

                          BERYLLIUM                   (5)6
                          TKALLIW1                    I  7»
                          NICKEL                      1  B>   t>

                          ARSENIC                     4  It   t>

                          SELENIUM                    (10)   1
                                                            2
                                                            3
                          SILVER                      til)   6

                          CACnIUn                     (12)   A

                          nERCuRV                     (13)   1
                                                            2
                                                            3
                                           COMPOUND  WAS DETECTED AT SOME CONCEN TRATIOM LESS  THAN  X,  BUT THE  CONCENTRATION COULD NOT BE  QUANT If-'JED
                                           COMPOUND  UAS DETECTED AT A LEVEL GREATER THAN  X
                                           COMPOUND  HAS NOT DETECTED,  X EQUALS  THE LOWEST LIMIT OF  SENSIT1V1IC OF 1 HE METHOD FOR THAT SAMPLE
                                           PHENOLICS AND CYANIDE DATA FROM RSKERL

-------
                                                                           CONCENTHAT10H Of PRIORITY VOLATILE ORQANIC* AT REFINERY ((. LJ/L
CO
C
IEN2ENE
1. 1. 3. 2-TETRACH.OROETHEIC
TOLUENE
ETHYLBENZENE
0(1) - COMPOUND h
0111 - COMPOUND II
ND(X)- CDrVOUND li
PARAMETER
NAPHTHALENE
FLUORENE
PHENANTHRENE/ANTHRACENE
DIETHYL PHTHALATE
FLUOR ANTHErE
PYRENE
DI-N-8UTYL PHTHALATE
CHRYSENE/CENZ(A>ANT>«1ACENE
SIS(2-ETHYLHEXYL)PHTKALATE
PHENOL
2-4-DlMETHYLP»«NOL
2. 4-D1CHLOROPHENOL
4. 6-D1NITRO-O-CRESOL

DATE
< 11 *
111) 4
.III) 4
 i
132) 6
(24) 6
(26) 4
1201 4
IAS DETECTED AT 3(
IAS DETECTED AT A
IAS NOT DETECTEDi
DATE
< 8) A
117) 6
124) 6
(23) 6
(29> 4
130) 4
131) 4
133) 4
137) 4
193) 4
(53) 4
<37I 4
(421 4
INTAKE WATER
RADIAN COMPANY ullltn
l»
I - -
1
1
OKI 1
1
D«l >
D«l 1
ME CONCENTRATION LESS THAN 1.
LEVEL GREATER THAN X.
I EQUALS THE LOWEST LIMIT OF !
CONCENTRATION OF PRIORI*
INTAKE UATER
RADIAN COnPANV OTHER
, ND«. 1 1
HD«. 1 ) -
ND«. 1 )H
2. 9
N0«. 1 ) -
2 - -
2. a
ND«. 1 )M
OKI )
N0«. I ) -
ND«. 2 )
D«l )
OKI )
WASTEUATER FEED TO BlOTREATnENT
RADIAN COT1PANV OTHER
4V
ND«. 3 )
18
D«l I
31000
N0« 41-
44OOO
ND(< 3 I
BUT THE CONCENTRATION COULD NOT BE QUANTIFIED.
1ENSIT1V1TV OF THE METHOD FOR THAT SAMPLE.
rt LIOUIO/LIOU10 EITRACTABLE DROAN ICS AT REFINERY !!•
UASTEUATER FEED TO BIOTREATnENT
RADIAN COMPANY OTHER
240
21
49 H
14
39
34
ND*C. 11-
1. B H
ND«. 1 )
3O - -
BO
ND«. 1 ) -
ND«. 4 >
FINAL EFFLUENT
RADIAN COnPAHV OTHER
8 - -
ND«. 3 >
NDK 3 >
D«l 1
D«l )
ND«. 41-
D«l )
ND« 3 ) -
UO/L
FINAL EFFLUENT
RADIAN COMPANY OTHER
N0« 11-
ND«. 11-
NDK- 1 IH -
43
NDK. 1 )
ND(C. 1 )
OKI )
NDK. 1 )H -
NDK. 1 )
NDK. li-
sa
NDK. 1 )
OKI 1
                           DO) - COMPOUND WAS DETECTED AT SOME CONCENTRATION LESS THAN X. BUT THE CONCENTRATION COULD NOT BE  QUANTIFIED.
                           Oil) - COMPOUND UA9 DETECTED AT A LEVEL GREATER THAN X
                           NOID- COMPOUND UAS NOT DETECTED,  X EQUALS THE LOWEST LIMIT OF SENSITIVITY OF THE METHOD FOR THAT SAMPLE.
                           H    - THESE COMPOUNDS ARE INDISTINGUISHABLE IN THIS SAMPLE AS ANALYZED BY THE EPA PROTOCOL.

-------
                                                                                             CONCENTRATION OF TRACE ELEMENTS AT HEFINERV ,
OJ
Ul

PARAMETER
ZINC
CHRoniun
COPPER
L£AD
BERYLLIUM
ANTIMONY
7KALJ-IUT1
NICKEL
AflSENlC
EEL EN run
SILVER
CADMIUM
HERCURV


( 1 )
( 2)
( 3)
( 4)
< 3)
( 6)
( 71
C B>
( 9)
(10)
<1U
(12)
(13)

DATE
6
6
6
6
&
A
6
6
&
6
6
6
6
INTAKE HATER
RADIAN COMPANY OTHER
10
- a
ND«20 >
20
NDKI >
ND«30 )
NDK10 )
- 2
- 22
N0«10 »
NDK3 >
NDKI »
3
WA3TEWATER FEED TO BIOTREATriENT
RADIAN CQMPANV OTHER
1 300
1 1 OO
ND«20 >
- 73
NDK1 )
NDt<30 >
NDK1O I
- S2
- 50
ND«10 >
ND«3 >
ND«1 )
.3
FINAL EFFLUENT
RADIAN COW ANY OTHER
- 3O
230
ND«20 t
- 10
NDKI >
ND(C3O )
NOKIO 1
9
70
NO « 10 I
ND1C3 >
NDKI )
. 3
                                    D(K) - COKPOUND  WA9 DETECTED AT SOME  CONCENTRATION LESS THAN  X.  BUT THE CONCENTRATION COULD NOT HE  QUANTIFIED
                                    gtX) - COMPOUND  WAS DETECTED AT A LEVEL  GREATER THAN X.
                                    NDIX)- COMPOUND  WAS NOT DETECTED) X EQUALS THE LOWEST  LIMIT OF SENSITIVITY OF  THE  METHOD FOR THAT SAMPLE.

-------
                                                                                                       CONCENTRATION V MlOJIIfV VOLAMLE  OMANICI  AT  HCMNMV
U)

INT AMI UATCR
PANAWCTIA DATC RADIAN COMPANY OTHER
13)
CMLCMOntTMANE 1 II
MOfOiCTMANl < 3)
ICTKTLCNC CM.CWIK 1 41
1. 1-OlCHLOMCtfMVLCNC 1 •>
CMLWOFOHM 1 1 1 1
i.a-oiw.(»ccfHA* uai
1. 1. l-TRICMLOftOCTMAfC (131
1.2-DlCrt.CMOPROPANE <141
TfllCMLQMOETHYLEM 4 !•>
DllROnOCHLOHOnCTHANC 1191
BEN2ENE iaa»
1. 1.2. a-IETRACM-OftoeTNENE <34)
1. 1.2. 2-TETRACHLOROETHANC tail
TOLUENE ta4)
ETMfLIENZCNE 12BI
iti ~ COMPOUND WAS DC
<«t - COMPOUND IMS OE
OKI- COMPOUS'D HAS NC
- POSSIBLE I DENT I
- ONE OF TUO OB nOF
- MAIlMl'M VALUE. AE
- BLANK DATA FUR It
- OACANOMAL1&E9 BY
NOKI )
NDKI >
OK 3 >
NDK 10 »
NO" 11 »
NOf-l 1
NDICI I
NDK3 1
4 CE
4 E -
4 E -
10
NOKl I
NOKI >
NDKI 1
NOKI »
NDKI )
NDKI 1
NOKI 1
NOK 31-
NDKI 1C
NOKl >E
NOKI IE
NDK3 )
HO»C* »
NDIC1 1
NDKI >
2 -
NOKI 1
WKI 1
NOKl i
NOK. 41-
NDKI )
NDKI >
NDKI J
NDK 21-
NDKI )
NDKI 1
NDKI 1
NDK 3 »
13
NOKI »
NOKI 1
NDKI »
NOK. 41-
NDK1 I
NOK1 >
NOK 3 )
43
2 " OK? ) -
TED AT SOME CONCENTRATION LEES THAN I.
TED AT A LEVEL CREATE** THAN X
£ TEC TED. * EQUALS THE LOWEST LIMIT OF
ATICN
E REPORTED VALUES FOR THIS SAMPLE
UMTEUATER FCCD TO •IDIAtAlNCMT iMl* UA*TCUATU PHP TO
RADIAN
NDKIO )
NDK10 1
ND«9 >
30
30O
NOKI )
NDKI 1
NDK 3 I
30
HDIO 1
30
NDK 3 t
1O
NDK 4 1
NDK. 4 t
NOK 4 1
NDK 2 1
3
NDK. 3 1
NDK 3 1
30
30
NDK 4 1
NDK 4 )
NDK 9 I
2
130
30
70
I GO
COMPANY OTHM
iai
NDKI »
NDKI
NOKI
NDKI 1
NOKI >
NDKI I
1 CE
1
9 CC
NOKl )
NDKI 1
NDKI >
22 C
17
ai c
14 CE
9 C
91 ce
NDKI 1
NOKI '
NDKI i
NOKI 1
NOKI 1
NDKI 1
NDKI )
NDKI 1
NDKI )
NOKl 1
NDI-'I 1
MOO C
2 C
1
4 C
NDCI 1
ND K I 1
NDKI 1
9000 C
7O C
RADIAN
NOKIO
NOKIO
HOKIO
NOKIO
NOK3
NDKS
NDK9
)A NDK9
130
19O
*0
)Z 140
NOKI >
1C
NOKI )
NDKI >
10
4
4
NOK3 1
NDKS 1
ND«» 1
NOK9 1
NDK. 3 1
10
4
NDK. 3 I
ND.K 4 I
NDK * 1
NDK 4 t
NDK 4 1
NOK 2 >
NOK a i
a
OKI 1
NDK 3 )
NDK 3 )
NDK 3 >
40
10
20
NDK 4
NDK 4
NDK. 4
NDK 3
NOK 9
2
NOK 3 1
4O
110
30
3O
10
4O
1
30
•lOTftfcATHCMT ICII
COMPANY OTHEJI
tat
I70OO
NOKI >
NDKt 1
MVKI >
OKI »
OKI 1C
3
NDKI 1
NDKI )
NDKI >
14
7 C
9
NOKI >E
NOKI IE
4 E
NDKI >
NDKI 1
NDKI 1
NDKI I
NDKI 1
NOKl 1
NDKI )
NDKI 1
NDKI t
NDKI )
NDKI )
NDKI 1
4000 C
NDKt I
NOKI t
-
NOKI I
N0K1 )
NDK1 >
70OO C
DK70 >C
BUT THE CONCENTRATION COULO NOT DE QOANT1F (CD
SENSITIVITY Of THE MCTlHJD FOR THAI SATlPLt
3ELLAB CC METHOD, OTHER VOLATILE SPECIES BY flROB OC METHOD.




-------
                                                                                           CCONT trflJEDI  CONCENTRATION OF PHIOflllV VOLATILE Ofi PANICS  *f  '
TOLUENE (24)
ETHYL BENZENE (28)
NOlll- COMPOUND UAS NOT
C - ONE OF Tuo Ofl MM
E - ruainun VALUE, ft
7 - BLANK DAI A FOR TH
NDIC1D »
NDKIO )
NDKi )
NDK3 )
D1O )
Dl "S >
1O
Did >
NDK 3 )
NOK 3 )
NOI« .
NDIO )
3
2
3
ND« 4 )
NOK 4 )
ND« 4 )
1
3
ND« 3 )
NOK 9 I
1
1
30
ND« 4 )
NDK A )
MDK. 5 )
NDK 9 1
NOK 9 )
3
3
to
1
1
SO
REPORTED VALUES FOR
COrtPANV OTHER
D»- 5 )
NO 1 •: 1 I
ND( 1 I
MD(-'.l 1
1 Ct
t. E
3 e
ND K 1 )
NOKI 1
D« S )
D«C 3 t
DC: 3 >E
OK 5 )E
NO K l 1
NOKI )
NO K 1 >
NOKI )
NDKI )
NOKI 1
NDKI >
NDKI )
NDKI )
NOKI )
3 C
NDKI I
NOKI )
NOKI >
NOKI )
NDKI )
10 C
010 >C
THIS SAMPLE
IS PARAMETER INDICATES CONTATIINAT ION

-------
                                                                                  CONCENTRATION OF FMtMITV LIOUID/L10UID EITRACTAULt WOMUCI AI DCFINCflV  ft, ua/L
Ul
PARAMETER
NAPHTHALENE
ACENAPMTHYLEHE
ACENAPHTHENE
FlUGRENE
PHENANTHRENE /ANTHRAC ENE
PHEhANTKRErC
ANTHRACENE
DIETHifL PHTHALATC
FLUOR ANTKEhE
PVRENE
DI-N-BUTVL PHTHALATC

CHRYSENE
BlS<2-ETHfLh£lVL)PHTHALATE
BENZ( A) ANTHRACENE
B£NZO< B ) / f M 1 FLUORANTHENE
BENZO ( B > FLUCRANTKENE
BENZO ( K IFLUOftANTHENE
BENZOPVHEN£
iNDEHOt I. S. 3-C. OPVRENC
D1BENZO(A. H1ANTHRACENE
BENZOIC. H, DPERVLENE
PHENOL
2-CMLOROPitENOL
2-4-DlnETHYLPM£NQL
2-NITfiOPKErrtX
3, 4-DICHLQflCPNENOL_

4-NlT«C-PH£NDL
4. 6-DIMThO-O-CRESOL
PENTACHLCfiGPnENOL
D'li - COMPOUND
Glti - COnPOuND
SAMPLE —
OATt
( a>
II4>
( 131
(17)
(34)
(23)
(26)
(28)
129)
(30)
Oil

(34)
(37)
OB)
13V)
I4Q)
(41 >
(42)
443)
(44)
149)
(33)
(94)
(33)
(36)
(97)
(3B>
(61)
(62)
(A3)
HAS DE
MAS DE
6
4
6
*
*
b
*
6
b
6
6
6
6
6
f>
6
4
&
4
6
4
4 '•
4
4
4
4
4
4
4
6
4


INTAKE
RADIAN
ND« 1 I
ND«. 1 )
ND« 1 1
NO« 1 )
3 H
-
-
20
ND«. 1 )
2
20
2
.3
B
. 1
ND« 2 >
-
-
ND«. 1 )
ND«. 2 >
N0«. 3 I
NOK 2 >
ND« 1 )
N0«. 1 )
NOK 2 >
D«l )
ND« 1 )
ND« 1 >
4
DC:I >
D«l >


WATER UA&T6MATER FEED TO DIOTHE*THFNT (R|) MA9TEUATER FEED TO BIOTHEATHCNT (Cll
CQHPANV OTHER
(6)
D«2 1
D(C2 >
D4<2 >
NOK 4 )
-
NDK 2 )
NDK O2>
-
NDIC. O4)
NDK. 03)
-
-
NDK 021
-
NDK. 01)
-
NDK O4>
NDK 1 )
07
NOK 01 >
NDK. O2 )
NDK 1 1 -
-
-
-
-
-
-
-
-
-

;R THAN x
RADIAN COHPANV OTHER
(6)
430 4OO C
NDK 1 ) D«3O )
9 200
3O 7 C -
11O H
28 C
1 C -
2 -
1 I 7 C
3 4 1 C
1O
NDK. 1 )
9 2 C -
NDK. I )
NDK 2 ) 1 4 C
NDK 21-
. 3 C
3 C
NDK. 1 ) 8 C
NOK. 2 > O2 C
NDK 3 ) . 07 C
W>«. 2 1 4 C
13OO
NOK. 1 » -
40O
NDK 21-
NDK 1 )
NDK 1 )
NDK. 3 > -
NDK 6 )
NDK. 4 )
E 00 F1ED

RAD I AN COW All V OTHEH
(6>
230 0«M 1
NOK 1 1 D(-l«0 t
NOK 1 I D: Z4O )
NDK 1 1 NDK 4 t
2 H -
NO K 0 1 1
NDK 1 t
NDK 4 1
8 04 -
DK. i ) 04
45
4 -
NDK. 1 ) NDK 02)
4 -
NDK 1 > ND(<: 04)
NDK 2 )
NDK 09i
ND« 3 1
NDK 1 ) O2
NOK 2 ) ND4-: 021
NDK 2 ) NDK 03) - ' '
NDK 2 > NDC-; S } -
13
1
a - -
NOK 3 ) -
DKI >
OKI )
ND(C 3 )
NDi< 3 ) -
OKI )

                                          ND'D- CCnPOuHD HAS NOT DETECTED.  X EQUALS  THE  LOWEST  LIMIT OF SENSITIVITY OP THE rtTHOD KW THAT SAMPLE
                                               - ONE OF TWO OR riCRE REPORTED VALUES FOR THIS SAMPLE
                                               - THESE COMPOUNDS ARE  IND1STIMCUISHAGl.E  IN THIS SAMPLE AS ANALYZED BV THE EPA PROTOCOL
                                               - NAPHTHALENE. ACfcNAPHTHALENE. AND  ACENAPHTHENE DV GflOO 5C METHOD,   01HER SPECIES 0V GC-UV METHOD

-------
                                                      ACENAPHTHYLEl*
                                                                 < /ANTHRACENE
                                                      D1CTHVL PHTHALATE


                                                      FLUORANTHEt£
                                                      PYHENE



                                                      DI-H-OUTYL PHTHALATE


                                                      ll/TYL BENZYL  PHTHALATE
                                                                                  (29)


                                                                                  (301
                                                                                  (34)


                                                                                  (34)
                                                      • I8(2-ETMYLHClYL>PHTHAi.ArE (
U)
pYftENE

BENZ016. H. 1 IPERYLENC
PHEfO-
2-Crt.OflOPKMX
a-4-D:n£THYLFHENOL
a-NITROPMENOU
2. 4-OICHLCROPHCNOL
f -C «. OH 0 -H-Cfl E SOL
4'NITRDPHENQL
4. 6-D1NITMO-0-CKE50L.
PENTACH-OHDPHENOL
O9>
(4O>
• 41,
142)
1431
(44>
(43)
I33>
(54)
(33)
(34)
(3?)
I SB)
(All
(&2>
CAD,
4
4
t,
4
4
6
6
A
6
6
4
6
A
A
6
A
NDK S t
NDK Ob)
NOK 2 I
NDK 1 ) NOK 01 )
NOK 2 > NDK O6>
NDK 3 ) NDK 02)
NDK. 2 ) NDK 1 >
HDK 1 )
NDK. 1 1
NDK 2 1
NDIC 2 (
NDK 1 )
NDK 1 )
HDK 3 (
NOK 6 1
NDK 4 )
-
-
-
-
-
-
-
-
-
-
-
-
~
-
-

                                                                        OnPOUND  MAS  DETECTED AT SOUS CONCENTRATION LESS  THAN  X.  BUT  THE CONCENTRATION COULD NOT  DE QUANTIFIED
                                                                        OffOUHO  HAS  DETECTED AT A LEVEL GREATER THAN I
                                                                     -  DS61BL6  IDENTIFICATION

                                                                     -  H£SE COMPOUNDS  AflE  INDISTINGUISHABLE ]N

                                                                     - NAPHTHAIENC.  ACENAPHTHALENE  AHU ACENAPH
                                                                                                                                                           FOR THAT  SAMPLE
             ns SAMPLE AS  ANALYZED iv THE CPA PROTOCOL
                                                                                                                                                            CC-UV METHOD

-------
                                                                                                  CONCENTRATION OF TRACE ELEMENTS AT REFINERY
                                                                                   INTAKE WATER
                                                                                                                 UASTEUATEfl FEED TO lIOTHEATrCNT  (Rl>
                                                                                                                                                           WA1TCHATEH  FEED TO UOTMEATnENT iClt
I/O
PAI
ZINC
CHjtoniun
COPPER
LEAD
KMYtxiun
ANTIMONY
THALLIUM
NICKEL
ARSENIC
SELENIUM
SILVER
CADMIUM
MERCURY
RAMETE*
< It
t at
1 3)
t 4)
1 3)
< 41
( ?>
1 •)
1 9»
I1OI
111)
413)
113)
DATE
4
1
3
3
4
4
4
4
4
4
4
4
4
4
4
1
2
3
6
RADIAN COMPANY OTHER
29
ND« )•
10
ND« )•
1300
33
4. 4
.4
.3
13
12
13
17
.1
.3
.4
RADIAN COMPANY OTHER
10OO
9OO
130
74O
7BO
39
19
3 - -
2.4
19O
31
29
17
3
41 -
4 -
RADIAN COMPANY OTHER
94OO
- 700
4OO
360
BOO
34
20
3 - -
4
34
13
21
19
31
1.7
39 - -
                                           D<1) - COnPOUND UAS DETECTED AT SOTC CONCENTRATION LESS THAN X. OUT THE CONCENTRATION COULD NOT Of QUANTIFIED
                                           Olll - COMPOUND UAS DETECTED AT A LEVEL GREATER THAN X.
                                           ND1.I- COWOwS UAS NOT DETECTED.  « EOUALS THE LOUEST LIHIT OF SENSITIVITY OF THE METHOD FOR THAI SAnPLE
                                           I    - FOSSIH.E TYPOGRAPHICAL ERROR IN ORIGINAL DATA
                                           3    - EPO DATA ON THIS SAIVLE POINT ALSO OITAINED FROn ANALYSIS SY EPA REGION u

-------
                                                                   SAMPLE   ---
                                            PARAMETER               DATE            RADIAN    COMPANY     01 HER


                                   1INC                        I It  &               33

                                   CHROMIUM                    ( 2>  i                 -       to
                                                                     3                         90
                                                                     3                         BO
                                                                     &               110

                                   COPPER                      I 3)  6               I3O

                                   LEAD                        ( 4>  A               fc i

                                   BERYL L IUH                   (3)4               - 2

                                   ANTIMONY                    1 6)  6               33
                                   --------------------------------------------------------------------------
                                   THALLIUM                    t 7)  6               48
                                                                                          (CONTINUED)   CONCENTRATION OF  TRACE ELEMENTS AT REFINERY ML UO/L


                                                                                      FINAL EFFLUENT
K,

                                   NICKEL                      ( Bt  A               34
                                   ARSENIC                     I 9)  &               22

                                   S£LENIUT1                    (10)  6               11

                                   SILVER                      ( 1 I I  6               13

                                   CADHIUH                     (12)  &               II

                                   KEDCURY                     (13)1
                                             D<1) - CDnfOUND MAS DETECTED AT  SOrlE CONCENTRATION  LESS THAN X.  OUT THE  CONCENTRATION COULD  WOT K QUANTIFIED
                                             C(X> - COnfOUND HAS DETECTED AT  A  LEVEL CHEAIER THAN  X
                                             ND(U- COrtPOUr/D HAS NOT DETECTED,  1  EQUALS THE LOWEST LIMIT OF SENSITIVITY OF THE METHOD FOB THAT SAMPLE
                                             3    - EPA  DATA ON THIS SAMPLE POINT ALSO OBTAINED  FROM ANALYSIS DY EPA  REDION U

-------
                                                                                       CONCENTRATION OF TRAC.r  ELEMENTS AT REFINER*
LA)
PARAMETER
I INC
CMtOMiun
COPPER
LEAD
BERVLLIUH
ANT1HONV
THALLIUM
NICKEL
ARSENIC
SELENIUM
SILVER
CADnlUR
MERCURY
SAMPLE
DATE
( 1)
1 21
1 3)
( 41
1 9)
I 6!
1 7)
I 81
< It
110)
!!!>
1121
113)
a
3
ft
2
3
ft
2
3
4
a
3
ft
ft
ft
ft
3
3
&
2
3
ft
2
3
ft
2
3
ft
2
3
ft
2
3
ft
INTAKE UATER
RADIAN
:
:
:
:
-
-
-
-
~
_
-
:
:
COMPANY
BO
1O
NOK10 1
N0«10 1
20
20
10
NDKIO 1
-
-
-
NDKIO )
ND«10 )
ND«10 )
NDKIO 1
NDKIO )
ND«10 )
NDKS )
NDKS >
NDICIO 1
NDKIO )
ND«1 )
NDKI )
OTHER
:
^
„
^
-
-
-
"
„
-
-
•
-
UASTEUATER FEED TO IIOT4EATNENT
RADIAN
^
-
-
^
-
-
-
:
-
~
:
_
^v
COMPANY
120
140
330
330
30
40
40
20
-
-
-
ND«10 I
NDKIO )
NDKIO >
10
NDKIO )
NDKIO <
NDK3 >
NDIO )
NDKIO 1
NDKIO >
NDK1 >
NDK1 )
OTHER
:
_
:
:
-
-
.-
:
;
_
-
~
:
PIMM. EFFLUENT
1AD1AN
~
_
-
-
-
-
-
-
:
-
-
-
-
COMPANY
40
10
130
130
1O
NDKIO 1
20
NDKIO 1
-
-
-
NDKIO >
NDKIO )
NDKIO 1
NDKIO }
NDKIO 1
NDKIO 1
NDK3 )
NDK3 )
NDKIO 1
NDKIO 1
NDKI )
NDKI )
OTHER
~
_
^
~
-
-
-
-
-
-
:
-
:
                                DfXI - COnPOUND HAS DETECTED AT SOME CONCENTRATION LESS  THAN X.  BUT THE CONCENTRATION COULD NOT B E QUANTIFIED
                                CIO - COMPOUND HAS DETECTED AT A LEVEL GREATER THAN  «.
                                NOIXI- COMPOUND UAS NOT DETECTEDi X EOUALS THE LOWEST  LIMIT  OF  SENSITIVITY OF THE METHOD FOR THAT SAMPLE.

-------
PARAMETER
NAPHTHALENE
FLL'DPENE
PHEKANTHflCNE /ANTHRACENE
PH&4ANTHRENE
ANTHNACENC

FLUOR AN THCt.'E
PYRENE

CKflVSENE/DENKAlANTHRACENE
CHHYSEN£
eiS«2-ETHYLMEXYL.PHTHALATE
BENZ, A, ANTHRACENE

D) 8ENZOI A. H) ANTHRACENE
BENZCUC. H. 1 IPESYLENE
P^NCL
2-4-D !«£ THYLPHENOL


< B> 6
(17) &
(24) 6
(=3) t
(26) 4
( 2B ) 6
429) 6
130) 6
(31) 6
(33) 6
136) 6

13S) 6
(42) 6
(44) 6
( 43) 6
(331 6
(33) 4
0(1) - COMPOUND UAS DETECTED AT
Cm - COMPOUND WAS DETECTED AT
INTAKE UATER
CXXONO)
NDK 1 ) NDKl )2
Np( < 1 I ND( Cl >
NDK 1 )H NDKl >
-
_
4 NDKl >
NDK 1 ) NDKl > NDK 03>
NDK 1 > NDKl 1 NDK. 02)
1 NDKl )
NDK I )H NDI <1 )
NDK 01)
3 NDKl )
NDK.OI)
NOK ) 1 NDKl ) 03
NDK 3 I NDKl 1
NDK- 2 ) NDKl ) NDK. 1 >
OKI ) NDKl )Z
NDK 2 ) NDKl >
SOHF CONCENTRATION LESS THAN X. BUT
A LEVEL GREATER THAN X
C - ONE OF TUG OH MORE REPORTED VALUES FOR THIS SAMPLE



V
EPA RADIAN COMPANY OTHER EPA RADIAN COMPANY OrtiFfl
MOO 1200 Cl - - NDI I 1 I NOKI  ~ " NDK 1 t NDKl »
32 C - - - NOK 2 I
- NDK OH)C - NDI . 01)
33 NDI II ) - 3 N0( 'I )
P3 NDKl ) 3 C - NDK I ) NDKl i NDI " 01)
69 NDK1)64C - 3 NDKl) 3
OKI } nD ( \ 1 ) - ' 32 NO K 1 )
13 H NDKl t - - 1 H NOKI i
-C26 - - - NDi . 02i
29 NDKl ) 13 NDKl
-14C - - - 01
44 NDK) ) 1 1 C - .4 NOKI i C<3
NDK 3 ) NDKl > 4 C - NDK 3 ) MOKI ' NDK O3I
NDK 2 ) NDKl i i C - NDK 2 1 NOKI ' MC> ? 1
1 SOOO 2&0001 - - ND ( •' 1 ) ND K 1 > i
1500 1200 - - NDK 3 f N0< :i »
THE CONCENTRATION COULD NOT OE QUANTIFIED



-------
                                                 CONCENTRATION OF PRIORITY VOLATILE ORGANIC! AT REFINERY
f,
PARAMETER
RETHYLENE CHLORIDE
TRANS-1. 2-D1CHLOROETHVLENE
CHLOROFORM
t. 1. 1-TR1CHLOROETHANC
TRANS-1. 3-D1CHLOROPROPENE
TRICHLOAO£TKYLEf«
BEN2ENE
BROnOFOim
1. 1.2. 2-TET>ACH-OflOETH£NE
TOLUENE
ETHVLBEH2ENE
•AMPLf
DATE
1 4) 1
a
3
*
1101 1
2
3
6
III) 1
2
3
6
113) 1
2
3
A
117) 1
2
3
6
(181 1
2
3
6
(221 1
2
3
6
(23) 1
2
3
(24) 1
2
3
•
(261 1
2
3
A
(28) 1
2
3

EPA
:
:
\
-
'-
-
-
-
-
"
-
INTAKE
RADIAN
4 I
* I
10 I
1
4
3
29
31
37
2
2
NDK. 3 )
NDK. 7 1
NDK. 7 >
NDK. 7 )
OKI )
1
OKI 1
D«l 1
NDK. 3 1
NDK. 3 1
NDK. 3 )
NDK. 4 1
NDK 4 )
NDK. 4 1
3
OKI 1
OKI 1
OKI 1
OKI 1
OKI 1
UATER
COMPANY
NDKI 1
NDKI 1
NDKI 1
NDKI )
NDKI 1
NDKI >
NDKI )
NDKI 1
NDKI )
NDKI 1
NDKI )

OTHER
-
j
:
;
:
:
:
:
;
:
_
UAfiT
EPA
-
;
-
:
:
;
-
j
-
-
^

RADIAN
20 I
23 I
4» I
NOK. 7 1
1
NDK. 7 1
2
7
3
NOK. 3 1
NDK. 3 I
NDK. 3 )
NDK. 7 >
2
NDK. 7 >
2
4
i
4700
IBCO
3300
NOK 3 1
OKI >
OKI I
4
3
42OO
B2O
2900
440
290
440

COMPANY OTHER
NDKI )
NDKI 1
NDKI )
NDKI I
NDKI 1
NDKI 1
0400
NDKI I
NDKI I
8300
200 C
FINAL EFFLUENT
EPA RADIAN
NOK 2 12
4 I
4 2
NDK 7 1
NDK. 7 )
NDK. 7 1
14
14
10
NDK. 3 1
NDK. 3 )
NDK. 3 1
NDK. 7 1
NDK. 7 1
OKI )
1
DKI )
OKI I
OKI 1
NDK. 3 )
NDK 3 1
NDK. 3 1
NDK. 3 1
NDK. 4 1
NDK. 4 1
NDK. 4 1
OKI 1
DKI 1
DKI 1
DKI 1
DKI 1
DKI 1
"MP.N
NDKI
NDKI
NDKI
NDKI
NDKI
NDKI
NDKI
NDKI
NDKI
NDKI
NDKI
NDKI
NOKI
NDKI
NOKI
NUK1
NDKI
NDKI
NPK1
NOKI
NDKI
NDKI
NDKI
NDKI
NDKI
NDKI
NDKI
NDKI
ND«I
NDKI
NOKI
V
1
1
1
I
1
1
1
1
1
I
1
1
)Z
)Z
1
I
>z
>z
>z
11
OTHER
:
-
:
^
-
-
:
:
-
:
:
D(K» - COr^OUND HAS DETEC1EO AT SOME CONCENTRATION LESS THAN  X, OUT THE CONCENTRATION COULD NOT OE  QUANTIFIED.
CIII - CDnPOUND UAS DETECTED AT A LEVEL CHEATER THAN I.
I.DIII- COnPCUND UAS HOT DETECTED. I EOUALS THE LOWEST LIMIT OF SENSITIVITY OF THE ME1HOD FOR  THAT SAMPLE
C    - OI1E OF IUO OR I1CRE REPORTED VALUES FOR THIS OARPLE
l    - BLAI.-H DATA FOR THIS PARAMETER INDICATES CONTAMINATION

-------
                                                                                       CONCENTRATION OF TRACE ELEMENTS AT REFINERY
en

PARAMETER
ZINC
cmoniiM
COPPER
LEAD
BERYLLIUM
ANTIMONY
THALLIUM
NICKEL
ARSENIC
SELENIUM
SILVER
CADnlUM
MERCURY


( 1)
< 2)
( 3)
< 4)
( 3)
< 6)
( 7)
( 6)
( 9)
(10)
(11)
(12)
(13)

DATE
6
6
6
6
6
6
6
t>
6
6
6
6
6
INTAKE
HADIAN
120
11
68
1 2
ND«. 1 )
4
NDK 1 )
1
18
15
1.2
. 2
3
; WATER
COMPANY OTHER
120
NEMO )
ND«1 )
ND«1 )
ND«1 )
ND«1 )
NDX1 )
ND«1 )
ND«1 )
ND«1 )
NDX1 )
NDX1 )
ND«1 )
UASTEUATER FEED
RADIAN
78
BOO
36
4
2 3
6B
33
3 6
23
15
2 3
6
a
TO BIOTREATMENT
COMPANY OTHER
7O
690
7
NDXl )
1
240
1
27
6
B
NDXl )
NDXl >
NDXl )
FINAL 1
RADIAN
82
46
16
3 3
. 7
68
9 5
3 6
16
19
8
.8
, 4
AFFLUENT
COMPANY OTHER
67 C
2B
12
7
1
190
NDXl )
16
2
NDXl )
NDXl )
NDXl >
NDXl )
                               D(X) - COMPOUND UAS DETECTED AT SOME CONCENTRATION LESS THAN  X.  BUT  THE CONCENTRATION COULD NOT BE QUANTIFIED
                               0 - COMPOUND UAS DETECTED AT A LEVEL GREATER THAN X
                               ND(x>- COMPOUND UAS NOT DETECTED,  x EQUALS THE LOWEST LIMIT OF  SENSITIVITY OF THE METHOD FOR THAT SAMPLE-
                               C    - ONE OF  TWO OR MORE REPORTED VALUES FOR THIS SAMPLE

-------