Cost Manual For The
Direct Discharge Segment
of the Petroleum Refining Industry
Prepared by:
Effluent Guidelines Division
Office of Water and Hazardous Materials
U.S. Environmental Protection Agency
Washington, D. C. 20460
John Cunningham, Project Officer
and
Burns and Roe Industrial Services Corp.
283 Rt. 17 South
Paramus, New Jersey 07652
March 1979
-------
Burns and Roe
Industrial Services Corp.
Engineers and Constructors
P.O. Box 663 • 283 Route 17 South ¦ Paramus, New Jersey 07652
Telephone N.J. (201) 265 8710 ¦ N.Y. (212) 594-9210 • Telex 134403 ¦ Cable BRISC PARAMUS, N.J.
VI.0. 4817-01
Revision of Cost Manual
Mr. David Hart, Vice President
Sobotka and Company, Inc.
83 Morgan Street
Stamford, CT 06905
Dear David:
Enclosed are two (2) copies of the following document :
Please note that there has been a change in the cost estimates for refinery
number 196 since the preliminary draft sent to you on March 19.
Although the costing procedure has not changed, some of its wording has been
slightly modified to accurately reflect the new tables just prepared.
If you have any questions regarding this document, please do not hesitate to
contact John Cunningham, Tom Fieldsend, or me at your earliest convenience.
March 27, 1979
"Cost Manual for the Direct Discharge Segment of the
Petroleum Refining Industry", March 1979.
Very truly yours,
Project Manager
BSL/ec
cc: J. Cunningham EPA w/enc.
L. DuPuis EPA w/enc.
-------
TABLE OF CONTENTS
SECTION PAGE
Introduction 1
BAT Regulatory Options 1
General Costing Methodology 3
Detailed Costing Procedure 5
Summary of Direct Discharge Refineries 6
-------
LIST OF TABLES
TABLE TITLE PAGE
1 Wastewater Discharge vs. BAT Flow 7
2 BOO Mass Discharge vs. BAT Mass Options 17
3 TSS Mass Discharge vs. BAT Mass Options 21
4 Cost Work Sheet 25
5 Refinery Crude Capacities and Throughputs 26
6 Cooling Tower Make-Up Flow Rates 28
7 Wastewater Treatment Operations 33
8 Refineries that Utilize, or Plan to Utilize ^5
Filtration Systems
9 Refineries that Utilize, or Plan to Utilize k6
Equalization Systems
10 Future Wastewater Treatment Modifications ^7
11 Planned Wastewater Flow Reductions 53
12 Refineries with Flow Reduction Costs 59
13 Plants Meeting BOD and TSS Limitations 60
14 Wastewater Flow Rate to End-of-Pipe Treatment 6l
15 Capital and Operating Costs by Refinery Number 65
16 Raw Wastewater Equalization Systems 70
Capital and Operating Costs
17 Rotating Biological Contactors (RBC's) As 71
Roughing Systems, Equipment Cost Basis
and Energy Requirements
18 Rotating Biological Contactors (RBC's) As 72
Roughing Filters, Capital and Operating
Costs
19 Powdered Activated Carbon, Equipment Cost 73
Basis and Energy Requirements Including
Costs for Sludge Disposal, 80 mg/1 Dosage
20 Powdered Activated Carbon, Capital Costs 71+
Including Costs for Sludge Disposal,
80 mg/1 Dosage
-------
LIST OF TABLES
TABLE TITLE PAGE
21 Powdered Activated Carbon, Annual Operation 75
Costs, including Credit for Sludge
Disposal, 8 mg/1 Dosage
22 Tertiary Filtration, Equipment Cost Basis 76
and Energy Requirements
23 Tertiary Filtration, Capital and Operating 77
Costs
24 Supplemental Economic Cost Information, 78
Capital and Operating Costs for 10,000
Gal/Day Treatment Systems
25 Wastewater Recycle, Capital and Operating Costs 79
26 Water Softening of Recycled Wastewater, Capital 80
Costs
27 Water Softening of Recycled Wastewater, Annual 8l
Operating Costs
-------
1
2
3
4
5
6
7
8
9
10
11
12
LIST OF FIGURES
TITLE PAGE
Pumping Capital Cost vs. Primping Distance 82
Refinery Size vs. Pumping Distance 83
Capital Cost vs. Flow for RBC's, Equaliza- g 84
tion and Filtration - 1 x 10 to 20 x 10
GPD
Capital Cost vs. Flow for RBC's, Egualiza- g 85
tion and Filtration - 0.01 x 10° to 1 x 10
GPD
Capital Cost vs. Flow for PACT Systems 86
Capital Cost vs. Flow for Water Softening 87
Annual Operating Costs for Equalization, 88
Filtration - 1 x 106 to 20 x 106 GPD
Annual Operating Costs for Equalization, 89
Filtration - 0.01 x 106 to 1.0 x 106 GPD
Annual Operating Costs for PACT, RBC - 90
1 x 106 to 20 x 106 GPD
Annual Operating Costs for PACT, RBC - 91
0.01 x 106 to 1.0 x 106 GPD
Annual Operating Costs Per Mile for 92
Wastewater Recycle
Annual Operating Costs for Water Softening 93
-------
Introduction
This report presents plant-by-plant costs for the direct discharge
segment of the petroleum refining industry to meet certain BAT technology
options presently under consideration. The cost estimates for each refinery
are presented in Table IS of this report.
The manual also describes the BAT technology model options, along with
their development. In addition, the methodology utilized in costing the BAT
options is discussed, including a detailed description of the plant-by-plant
costing procedure. Refinery data used in this effort was obtained from the
1977 EPA Petroleum Refining Industry Survey and the subsequent Supplemental
Flow Questionnaire.
It should be noted that this report is a revision of the document dated
April 1978, which should now be considered outdated and void.
BAT Regulatory Options
EPA will shortly be proposing BAT regulations for this industry. Three
options were initially considered by EPA, which will be described in detail in
the preamble to the regulations. Briefly, the three options considered are as
follows:
0
Option 1 - Set BAT regulations equal to the BPT level.
Option 2 - Base BAT regulations on BPT end-of-pipe treatment technology,
with additional reductions in total effluent flow.
Option 3 - Base BAT regulations on the same flow reduction requirements
as Option 2, with the additional requirement of granular
activated carbon adsorption.
Upon review of the three options, EPA has decided to propose regulations
using Option 2 technology.
The proposed regulations present two alternate sets of limitations based
on two different flow reduction requirements. Both alternatives are based
upon the flow model recently developed using the data collected by the 1977
industry survey. The flow model predicts wastewater generation based on
present industry practice, and takes the following form:
MF = .004C + .046K + .048 (A+L)
MF = Model Flow in units of million gallons per day.
A, C, K, L are in units of thousand barrels per day, where:
A = Sum of asphalt processes
P18 Asphalt Production
P43 Asphalt Oxidizing
P89 Asphalt Emulsifying
-1-
-------
C s Sum o£ crude processes
PI Atmospheric Crude Distillation
P2 Crude Desalting
P3 Vacuum Crude Distillation
K » Sum of cracking processes
P4 Visbreaking
P5 Thermal Cracking
P6 Fluid Catalytic Cracking
P7 Moving Bed Catalytic Cracking
P10 Hydrocracking
L b Sum of lube processes
P21 Hydrofining, Hydrofinishing, Lube Hydrofining
P22 White Oil Manufacture
P23 Propane Dewaxing, Propane Deasphalting, Propane
Fractioning, Propane Deresining
P24 Duo Sol, Solvent Treating, Solvent Extraction, Duotreating,
Solvent Dewaxing, Solvent Deasphalt
P2S Lube Vac Twr, Oil Fractionation, Batch Still (Naphtha
Strip), Bright Stock Treating
P26 Centrifuge and Chilling
P27 MEK Dewaxing, Ketone Dewaxing, MEK-Toluene Dewaxing
P28 Deoiling (wax)
P29 Naphthenic Lubes Production
P30 S02 Extraction
P34 Wax Pressing
P35 Wax Plant (with Neutral Separation)
P36 Furfural Extracting
P37 Clay Contacting - Percolation
P38 Wax Sweating
P39 Acid Treat
P40 Phenol Extraction
P506 Lube and Fuel Additives
P508 Sulfonate Plant
P522 MIBK
P529 Wax Slabbing
P531 Rust Preventives
P532 Petrolatum Oxidation
P563 Grease Mfg. V. Allied Products
P568 Misc. Blending and Packaging
The two levels of flow reduction being considered by EPA .are represented
by "Reduction Factors" (R) which are used as multipliers to the flow model.
Therefore, Level 1 and Level 2 effluent limitations are based upon discharge
flow rates represented by the following equations:
Level 1 Flow = R^(MF) Million gallons per day
Level 2 Flow = R^ (MF) Million gallons per day
where and R^ are the reduction factors for Levels 1 and 2, and are as
follows:
-2-
-------
R. = 0.73
= 0.48
The development of these reduction factors will be described in the preamble
to the regulations.
General Costing Methodology
The cost procedures used in this manual were developed so that a reason-
able amount of manhour expenditures can be utilized in developing conservative
costs. It is realized that the most accurate method would be to conduct an
engineering evaluation for each refinery. The costs and time associated with
this approach far exceed the budget allowed for this effort. Therefore, the
following general assumptions have been made:
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. If a refinery has these technologies in place, or is already planning
to install the necessary equipment, then no costs have been allocated. 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 in this
manual are expected to be conservative.
3. Although a refinery may choose to upgrade its biological treatment
system in other ways, rotating biological contactors (RBC) and powdered acti-
vated carbon can be readily priced as add-on systems. Costs for these systems
are also expected to be conservative estimates.
4. Although the costs cure 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 conservative costs within a reasonable manhour expenditure, the costs
included in this manual rely heavily on end-of-pipe treatment alternatives,
which can be directly defined. The cost procedures include reducing flow to
Level 1 requirements only. Beyond this, sophisticated end-of-pipe treatment
(biological polishing with RBC's or powdered activated carbon) are used to
represent the costs associated with meeting Level 2 requirements.
5. Effluent flow is considered to be flow to NPDES discharge. All
other forms of disposed, (i.e., evaporation, deep well, etc.), except indirect
discharge, are considered flow reduction techniques.
-3-
-------
6. Sane refineries discharge partly to POTW's and partly to surface
waters. Only those plants that directly discharge the majority of their
wastewaters sure included in this analysis. For 'these plants, the wastewater
discharged to a POTW is assumed to be included with the direct discharge flow.
General Procedure
The following control techniques are required to meet the Level 1 and
Level 2 requirements:
Level Flow Reduction End-of-Pipe Treatment
1 To Level 1 flow Equalization, filtration
2 Same Same, plus RBC's or powdered activated carbon
If any of these control technologies are already in place or planned by the
refinery, then costs will not be allocated.
Planned flow reductions used in this report do not include the elimina-
tion of once-through cooling water, as well as other "excluded wastewaters" as
described in the Supplemental Flow Question, such as stonnwater, ballast
water, etc.
Planned flow reductions have been divided into two groups: (1) reduc-
tions in flow to end-of-pipe treatment, and (2) reductions in effluent dis-
charge by end-of-pipe methods (i.e., flow recycle, evaporation, etc.). Effluent
flow is NPDES discharge minus planned flow reductions from both groups.
Refineries that have effluent flow values of 10,000 gallons per day or less
above their Level 1 flow are considered to be meeting the Level 1 flow require-
ment. Wastewater flows to end-of-pipe treatment have been reduced only by the
first type of reduction. Therefore, the costs for the treatment of recycled
effluent are considered in this analysis. Treatment costs are based on a
minimum of 10,000 gallons per day.
Capital and operating costs have been calculated for each refinery.
Plants that are not meeting either of the two levels will have two costs
calculated: costs associated with meeting Level 1 and costs associated with
meeting Level 2. The operating costs presented in Table 15 do not include
depreciation and/or interest, which need to be added prior to the economic
evaluation.
The previous cost manual included the use of BOD and TSS effluent data as
part of the analysis. Similar data are shown in Tables 2 and 3. Table 13
presents those refineries that would have no costs associated with meeting the
two options, if their effluent data were considered in this analysis.
Tables 16 through 27 present economic costs for all of the treatment
technologies discussed in this manual.
-4-
-------
Detailed Costing Procedure^
I. Costs to Meet Level 1 Requirements
A. Flow Reduction
1. Each plant that requires flow reduction is listed in Table 12.
This value is equal to the NPDES discharge, with planned flow reductions,
minus the Level 1 flow rate, as shown in Table 1.
2. If any of these refineries do not have a cooling tower (no
cooling tower makeup in Table 6), then indicate this on the work sheet.
3. Piping distance is obtained from Figure 2, based upon plant
capacity (Table 5).
4. Pumping capital cost is obtained from Figure 1 using pumping
distance and calculated flow reduction.
5. Pumping operating cost is obtained from Figure 11 times the
pumping distance.
6. Twenty-five percent of the recycled wastewater is to be sof-
tened:
a. Water softening capital cost - Figure 6
b. Water softening operating cost - Figure 12
B. End-of-Pipe Treatment
1. End-of-Pipe Treatment - Costs for equalization and filtration
are needed for plants that presently do not have or do not plan to have these
treatment operations.
2. Flow rates to be used for costing are obtained from Table 14.
a. Equalization capital costs - Figures 3, 4. Equalization
operating costs - Figures 7, 8.
b. Filtration capital costs - Figures 3, 4. Filtration operating
costs - Figures 7, 8.
II. Costs to Meet Level 2 Requirements
A. Any flow reduction or end-of-pipe treatment necessary for meeting
Level 1 are also required for Level 2. Therefore, costs calculated using the
procedures listed below must be added to the Level 1 costs already obtained.
(1) Costs for 10,000 gal/d flows are considered minimum costs.
-5-
-------
B. Flow rates to be used for costing are obtained from Table 14.
C. Plants that have, or plan to have, activated sludge, trickling
filters, or BBC systems will have powdered activated carbon added:
1. Capital costs - Figure 5 (minimum cost - $35,000)
2. Operating costs - Figures 9, 10
0. Plants that have, or plan to have, aerated lagoons or oxidation
ponds or will have BBC's added:
1. Capital costs - Figures 3, 4
2. Operating costs - Figures 9, 10
E. If a plant does not have a biological system or the type of bio
system used at a plant is unknown, assume that it has, or will install, an
activated sludge system. Therefore, cost powdered activated carbon treatment.
Summary of Direct Discharge Refineries
There are presently 175 refineries discharging all or part of their
wastewaters directly to receiving streams. However, 12 refineries were not
costed in this analysis for the following reasons:
1. Seven refineries plan to discharge to POTH's in the future.
2. Three refineries presently discharge the majority of their wastewaters-
to POTW's. These refineries are considered indirect dischargers for the
purposes of this analysis.
3. Two refineries discharge at flow rates that can be considered insignifi-
cant. In addition, these refineries would most likely meet any BAT option
considered by EPA.
Table 15 presents the capital and operating costs for direct dischargers
to meet the proposed standards.
-6-
-------
TAB LB 1
WAStBWATBH DIBCHAHQB V3. BAT FLOW OfWOB
HutmUr
Option 1 -
Calculated
Calculator
Optica
2 Flaw
Wastewater
WfOB9 ptacharRe
Ultta Flannel
Option
2 Flow
Refinery
Bo.
Oecarntod Id 1976
faal/bbl)
BTT Plow
(ftal/bbl)
1974 BAT riav
(ftal/bbl)
Level 1
(gul/bbl)
Level 2
(ael/bbl)
Qenerated
in 1976 (MOD)
In 1976
(MOD)
Flo* Beiluctiona
C«o)
Level 1
(KM)
level 2
(K3D)
1
a
/
35
10
24
16
O.190
0.190
0.190
0.733
0.462
2
3
13
7
7
It
0.05b
0.054
0.054
0.131
O.OS64
3
13
89
•»7
¦15
30
o.oiit
0.014
o.oi4
O.o$£6
0.0372
4
.04
13
7
3
2
0.000$$
0
0
0.0360
O.OriO
6
30
16
23
15
0.075
0.075
0.075
o.soe
0.314
7
l.
13
7
6
It
0.16$
0.165
0.05
0.222
0.146
e
4
39
20
26
17
0.005
0
0
0.131
0.0664
9
£3
12
18
12
0.036
0.036
0.013
0.0627
0.0412
la
lit
78
53
53
35
0.0$
0.0$
0.0$
0.316
0.203
11
35
58
39
37
24
1.5
1.499
0.779
1.73
1.14
12
13
192
31
89
40
*•7
25
6I>
30
42
20
0.691
$.0$
0.075
0
0.0736
(consUored
0 proaeot HJTW
only)
0
0.286
5.75
0.188
3.79
1>I
7
lit
8.
12
8
0.0663
0
0.145
0.0956
15
5
20
11
8
5
0.1525
0
0
0.246
0.161
16
32
17
23
15
0.324
0
0
1.11
0.731
17
7
*i7
25
31
20
0.03320
0
0
0.294
0.19J
ie
lit
V?
25
29
19
0.228
0
0
0.573
0.377
19
3
78
111
38
25
0.001)284
0.000084
0.00006U
0.0949
0.0624
20
47
26
31
20
1.91
1.91
1.9X
3.08
2.02
21
it
13
7
3
2
0.068
0
0
0.0504
0. 03124
22
13
*3
23
28
19
0.090
0
0
0.310
0.204
2)
4
13
7
6
4
0.0488
0
0
0.0934
0.0614
24
7
15
a
6
¦t .
0.3
0.3
0.3
0.325
0.214
25
10
l»3
e>t
36
24
0.484
0
0
1.95
1.2a
£6
9
16
9
19
U
0.149
0
0
0.331
0.21a
29
37
56
31
32
21
3-7*t
0
0
4.tt!
s.rft
J1*
12
U
7
3
e
o.cjyoe
0.237
0.237
0.0666
0.0433
-------
TABL8 1
MA3TBMATEB DISCHARGE VB. BAT VUM 0PTK8I3
flnety
Ho.
Wastewater
Oeoerated in 1976
(nlMl)
Option 1 -
Calculated
BPT Plow
<»al/bbl)
Calculated
1974 bat rim
(anl/ttl)
Option
2 Flow
Wastewater
Generated
to 1976 (MB»
In 1976
(MTO)
HPDEfl Discharge
With planned
Plow Reductions
(MT1D)
Ootlon
2 Flow
Level 1
(p.al/bbl)
Level 2
(eal/bbli
Level 1
(MT.Ol
Level £
tvr. a)
31
.6
22
12
17
11
0.006
0
0
0.203
0.134
32
70
51
29
29
19
5.9
3.4
3-*»
3.23
2.12
33
10
20
11
20
13
0.396
0
0
0.880
0.579
35
15
13
7
3
2
0.029^
0
0
0.0103
0.00672
36
3
4o
21
27
18
0.033
0
0
0.462
0.304
37
31
79
6o
53
35
2.36
2.36
2-36
5.49
3.61
(considered
38
37
39
22
22
15
3.065
0
0 present POTW
Mlu\
2.06
1.36
39
11
13
7
il
3
0.151
0
wujr;
0
0.111
0.0730
l|0
34
27
17
16
10
7.8
7.8
6.6
6.40
4.21
>il
36
55
42
33
22
9.38
9.38
9.3B
12.0
7.50
42
5
13
7
3
2
0.03(132
0
0
0.0£04
0.013U
(oooiidorei
•>3
62
53
30
30
20
2.869
2.1>)9
2.1^9 present W>
2.41
1.56
Ofay)
44
29
30
17
28
19
0.7
0
0
1.13
0.742
45
*¦3
*i7
26 '
37
25
3.19
0
0
4.16
2.73
U6
22
Si
55
4j
30
1.31
1.31
0.66
2.95
1.S4
4a
112
24
13
0
0
• 0.606
0
0
0
0
•(9
5
26
16
28
18
0.132
0.132
0.132
0.929
0.611
so
10
2>l
13
2B
18
0.154
0.060
0.028
0.603
0.356
51
67
<>9
31
26
17
9.9
9.9
9.9
3.«9
2.56
52
107
78
41
98
64
0.3
0.3
0.3
0.391
0.257
(considered
53
19
47
25
30
20
0.29
0.25
0.15 present DD
MJL l U ^
0.423
0.278
5*»
6
33
17
2>l
l£
0.017
0.017
OnXjf
0.017
0.0732
0.01.32
55
2
14
7
6
ii
0.14
0
0
0.352
O.eji
56
29
24
13
24
16
1.306
1.306
1.306
0.966
O.636
57
129
32
20
27
18
10.3
10.3
6.0
2.06
1.93
58
26
25
16
24
16
1.43
O
0
1.71
1.13
59
21)
33
18
24
16
1.100
1.100
0.99
1.39
0.916
6o
11
31
17
IB
12
1.9*166
1.656
1.650
3.46
2.26
-------
TABLE 1
WA3TKVATKB M3CHAB0E V8. B» MM OPTIOW3
»finery
Ho.
Wastewater
Generated Id 1976
(ft&l/bbl)
Option 1 -
Calculated
BPT Flow
(RUl/hbl)
197b BAI Flow
(nalMl)
Option 2 Flow
UuteiMter
Generated
Id 1976 (MOD)
Id 1976
(MOD)
HFDE3 MicliAne
With Manned
Plow Baductloa*
(M30)
Option 2
I'Lo'i
level 1
(gal/bbl)
level 2
(gel/bbl)
Level 1
(WO)
Level 2
61
17
38
21
23
15
2.6I»
2.6H
2.6H
«t.51
2.97
62
19
89
55
37
25
fc.B
It.8
fc.8
U.o
7.25
63
36
33
IS
30
19
2.73
2.73
2.605
2.69
1.77
61)
68
Ii3
2>t
27
18
k.&O
•i.ao
2.1*3
2.10
1.33
65
29
35
20
20
13
3.60
3.60
3-60
3.0*1
2.00
66
IMXNOUM
13
7
3
2
UNKNOWN
0
0
0.00292
0.00196
67
65
58
39
28
19
21.19
21.00
21.00
10.8
7.11
63
M
27
21
28
ia
>1.86
>>.86
t.86
3.87
2.55
70
17
13
7
6
it
0.150
0.150
0.150
O.obia
0.053d
71
13
22
12
22
15
0.2U15
0.2t»0
0.2l|0
0.ll72
0.310
72
23
51
27
28
19
0.152
0.152
0.132
0.2t|l
0.15&
(considered
73
25
23
13
23
15
0.773
0
0 present FOTV
1.026
O.67I1
only)
7"t
10
tl
23
33
22
0.200
0.19975
0.19975
0.752
O.'iS't
76
56
75
51
37
25
2.28
2.28
1.78
1.60
1.05
77
12
20
11
21
111
0.276
0.276
0.276
0.U77
0.31 It
70
26
23
13
20
13
0.68
0
0
0.595
0.391
79
UNKHOUI
I*
7
7
5
IMOKHtf
0
0
0.0219
O.OIUU
80
5
3*
19
30
20
0.23
0.08
0.08
i.n
Q.V*
01
22
28
16
19
12
1.21
1.15
1.15
1.06
0.695
6s
281
13
7
6
U
0.576
0
0
0.05fll»
o.o3ai»-
as
35
51
35
37
2>l
2.1*6
2. Ml
2.MI
3.32
2.18
84
21
21
13
19
12
1.69
l.lll
l.lll
1.51
0.992
85
25
38
A
27
18
3.29
3-29
3.29
3.68
2.1(2
.86
15
33
IB
28
19
O.3I16
0
0
0.707
O.U65
87
IB
13
7
3
2
0.0905
0.09
0.09
0.0152
0.0(»yd
83
6
13
7
5
3
0.228
0.212
0.212
0.235
0.155
89
22
3*i
23
18
12
0.0603
0.038(1
0.038t|
0.0736
o.oi»ei»
90
25
89
l»7
87
57
0.0tl5
0.032
0.030
0.191
0.126
-------
TABLE X
WASTEWATER DI8CHARQB V8. BAT FtOW OPtlCBta
ie finery
No.
Uuttntor
Generated In 1976
(gal/bbl)
Option 1 -
Calculated
BW Plow
(Kal/bbl)
CaltnJ atod
197<» BAT now
(g«i/bbl)
Option 2 Plow
Laval 1 Laval 2
(ftal/bbl) (ral/bbl)
Uutantar
Sonar* ted
In 1976 (HOD)
OTTOS Dlaohanto
With Planned
In 1976 Flow Reduction*
(MO) (H3D1
Ootloi 2 now
Laval 1 Laval 2
(two) (:•. ;d 1
91
3
13
7
3
e
0.0120
0.0120
0.0120
0.0113
0.037M)
92
Mi
89
60
36
2>»
U.16
10.69
10.1(2
9.82
6.1)5
93
15
13
7
5
3
0.0«>5
0.02»
2.3b
3.9b
2.59
99
3
20
11
19
12
0.070
0.070
0.070
0.533
0.353
100
9
13
7
6
it
0.0518
0.0518
O.OJ18
O.G&I12
O.OU22
102
32
17
IO
10
7
1.584
1.58b
1.167
0.919
0.60*.
103
2
13
7
6
0.063
0.063
0.063
0.210
0.133
i<*>
30
>il
23
27
18
7."t3
6.01
6.01
8.05
5.£5>
105
30
12
13
21
IV
2.53H
2.381
2.381
1.85
1.22
10a
18
38
21
30
so
s.ioh
1.583
1.583
4.64
3.05
107
1
0.02
0.02
0 (future POTV)
0.0350
0.0230
Ul
2tl
*3
2t
et
16
1.58
0
0
1.58
1.04
112
36
13
7
6
•»
0.203
0.203
0.203
0.0803
0.O52B
113
13
25
m
23
15
0.553
0.5
0.1)26
0.975
0.6!) 1
ii"»
12
20
11
20
13
0.250
0.250
0 (future POIW)
0.W5
0.311
115
27
56
31
28
18
2.80
2,80
2.72
3.71
2.<)l»
116
21
*¦9
27
>11
27
1.2
1.2
1.2
2.81
l.ei)
117
36
30
17
25
16
1.01
1.01
0.81
0.7h6
O.U91
llfi
9
88
1(6
*9
32
0.036
0.006
0.026
0.291
0.191
119
16
78
U
39
26
0.150
0.125
0.125
0.1)31
0.2&3
120
39
89
1)7
57
38
0.110
0.100
0.100
0.21)1
0.159
-------
TABLE 1
WAaTSWATH* PI8CHAR0E VS. BAT TUM OPTICUS
lefinery
Ho.
Uutmtftr
OoMr&tod In 1976
(««1M1)
Outlon 1 -
Calculi tot!
BPT Flaw
(nal/bbl)
Calculated
1974 BAT Flow
(.15
3.21
2.11
135
0
13
7
3
2
0
0
0
0.00730
0.00480
136
11
13
7
6
4
0.286
0
0
0.147
0.0-66
137
2
13
7
6
4
0.0104
0
0
0.0251
0.016$
138
26
17
10
15
IO
0.720
0
0
0.1.52
O.i-,1
139
2
13
7
3
2
0.014
0
0
0.0219
O.OU4
140
9
29
16
30
20
0.11
0
0
0.570
0.375
141
.09
13
7
7
5
0.0002
0
0
0.0285
O.Olid
142
26
¦(2
27
35
23
1.584
1.584
0 (future hOTV)
2.21
1.4?
143
38
1)3
24
33
22
1.2
1.2
0 (future POTW)
1.47
0.9tS
144
It
20
11
21
lb
0.654
0.199
0.U9
1.05
0.691
I«i5
5
13
7
3
2
0.00410
0
0
0.0153
0.0101
146
Sit
1*1
8
13
9
O.093
0.093
0.093
0.0653
0.0") 29
147
9
49
27
35
23
0.576
0.576
0.576
2.29
1.50
i48
10
¦>3
23
29
19
0.16
0
0
0.576
0.379
149
21f
S3
13
23
15
1.179
1.179
1.179
1.00
0.660
lso
24
22
12
22
15
1.041
1.040
0.968
1.14
0.752
-------
TAB LB 1
WASTEWATER PI8CHAHQB VS. BAT F10W 0PT10W3
Beflnarjr
No.
Wastewater
Ocucratod In 1976
(gal/bbl)
Option 1 -
Calculated
bp! rim
(gal/bbl)
C/ilmilntod
19J4 BAT Flow
(gal/bbl)
Option
Level 1
(gal/bbl)
2 Plow
"level 2
(xal/bbl)
Vutev&Ur
Generated
In 1976 (MOO)
HFDBS DlocharKO
witn runned
la 1976 Flow Reduction*
(mo) (mo)
Option 2 Flow
Level i Level 2
(KOD) I'.'.Tj)
151
25
4l
28
SO
13
3-974
3.97*
3.974
3.61
2.3*
152
83
¦(0
22
32
21
8.38
8.38
7.98
3-es
2.54
153
35
29
IB
26-
18
3.89
2.09
1.09
3.46
2.27
15"»
209
89
<17
59
39
l.ao
0.11
0.11
0.327
0.21S
155
13
35
20
32
21
0.172a
0.0936
0.0936
o.46l
0.303
156
20
29
20
24
16
1.00
0.85
0.63!)
1.30
O.C56
157
16
35
24
21
It)
2.01
2.01
2.01
2.72
1.79
158
13
26
15
22
1%
0.548
0.548
0.548
1.18
0.773
159
15
20
11
20
13
0.277
0.252
0.292
0.38J
0.252
160
a
17
10
20
13
0.175
0.175
0.175
0.468
O.30?
161
16
9
24
16
0.63
0.35
0.35
1.22
O.C04
162
30
85
58
41
27
2.45
2.IB
1.1B
3.65
2.40
163
20
£6
15
26
17
1.037
1.037
1.037
1.35
0.867
164
6
13
7
3
2
0.022
0
0
0.0146
o.oo>to
16$
5
*7
26
33
21
0.29
0.29
0.29
1.95
1.2a
166
16
69
17
67
Ml
0.11
0
0
O.S45
0.621
16?
33
31
17
16
11
5.1
4.8
4.8
3.22
2.11
l£8
19
31
17
21
13
2.88
8.70
2.70
3.49
2.29
l£9
56
31
17
21
14
8.67
6.53
6.98
3.99
2.£2
172
96
66
35
34
22
0.92
0.92
0.764
0.404
0.266
173
224
69
*17
77
51
0.626
0.626
0.448
0.270
0.177
17li
109
89
>»7
78
51
0.576
0.576
0.576
0.551
0.362
175
81
67
51
¦to
26
12.478
11.995
0 (future roiW)
6.52
4.29
176
It)
31
17
2W
16
0.4649
0.3664
0.3664
1.26
o. £26
177
134
89
47
59
39
0.765
0.765
0.765
0.446
0.293
it)
l;'
>0
W
3<1
;-4
U.14U
O.iOK
0.2U2
0.930
0.611
180
1(6
53
30
25
16
2.767
2.764
2.764
1.96
1.P9
-------
Wo.
lBl
182
lfl3
1B5
lfl6
187
168
I89
190
191
198
193
19>t
195
196
197
199
200
201
SOS
203
SOti
205
206
207
208
TABLE 1
WA3TEWATHi DISCHARGE V3. BAT MM OPTIOWa
VuUnttr
Generated la 1976
f«i/bbn
1)7
27
13
22
11
13
16
27
3
5
9
201
.2
*>3
1
£1
16
2t
2U
l"l
1
w»
3*>
2<<
3
2
IB
8
3
Option 1 -
Calculated
Calculated
ptlon 2 Mai
Vutmtu
wroea Mecbi
an now
(g«i/bbH
197*> DAT Plow
(ftal/bbl)
Level 1
(gal/bbl)
Wei 2
(f.al/bbl)
Generated
la 1976 (HOD)
In 1976
37
23
2P.
IB
16.01.
15.57
37
26
17
11
6.1.
0
16
9
12
8
o.6to
0.639
hi
26
3*i
22
1.36
1.36
th
13
19
12
0.837
0
ak
15
11
7
1.815
1.815
*>3
27
38
25
0.772
0
30
17
21
lb
2."i35
0
13
7
3
2
0.015
0.015
13
7
5
3
O.0332
0.0332
*•3
Sk
33
22
0.1.51.
0
13
7
0.11(1
0
13
7
3
a
0.00052
0
60
1)6
32
21
17.0
16.76
13
7
3
2
0.00133
0
50
38
3
2
18.5
18.5
13
7
3
2
0.008
0.008
13
7
3
2
O.Ot.92
0.01.92
36
ao
25
17
0.612
0
20
31
21
it
0.95
0.95
13
7
3
2
0.0001
0
"17
32
28
18
12.9«»
0
29
IB
29
19
3.3766
3.366
23
15
20
13
2.1)38
2.1)2*1
13
7
6
4
0.093
0
13
7
3
2
0.071
0
¦ll
31
26
17
*••99
I1.98
20
11
22
111
0.235
0
13
7
6
U
0.039
0.019
bwe
uitn Moaned
Plow Reduction*
<*"»
12.57
O
0.559
1.216
0
(considered
1.81J present DO
ooljr)
o
0
0.015
0.0332
0
0
0
13-76
o
14.5
0.000
O.OI192
o
0.95
o
0
3.366
2.U2U
0
0
<1.98
0
0.016
-------
tABLB 1
WASTEWATER DISCUASQB VS.
BAT FLOW OPTICUS
Option l .
NFDB3 Disclmnre
la finery
So,
Vhatwitsr
Generated In 1976
(KOl/bbl)
C»] tainted
Calculated
197b BAT Plow
(«al/bbl)
Option 2 Flow
Vutamtar
With Flamed
Opt l£m 2 Flow
BPS Flow
faol/bbl)
Level 1
(Kol/bbl)
Loral 2
(RBl/bbl)
Generated
In 1976 (MOD)
In 1976
(USD)
Flow Reductions
(WO)
Level 1
(KJD)
Level
f!!iD)
211
7
21
12
10
7
0.8135
0.8135
0.8135
1.26
0.831
212
13
20
13
18
12
0.703
0.703
0.703
1.05
0.691
213
4
13
7
6
0.051
0.046
0.046
0.126
0.0230
214
DATA HOT SUBMITTED.
-
-
-
-
-
0
0
-
-
215
DATA HOT SUMIRED.
-
-
-
-
-
0
0
.
.
Sl6
54
45
31)
28
18
20.1)
13.2
8.64
13.4
8.79
218
.1
13
7
3
2
0.0007
0
0
0.0175
0.0115
£19
17
28
16
25
17
1.2
1.2
1.2
2.03
1-33
220
2
as
>•5
37
25
0.023
0
0
0.374
0.246
221
29
17
13
22
15
3.312
3-312
3.312
2.e6
i.es
222
1)2
10
6
13
9
0.35
0.35
0.35
0.175
0.115
22k
12
14
8
12
a
0.17>>5
0
0
0.245
o.iei
225
35
36
20
30
20
1.19
0
0
1.22
0.799
226
8
13
17
8
5
0.036
0.036
0.036
0.0621
0.04.^3
227
37
25
lb
22
ii)
1.27
0.55
0.5068
0.971
0.638
228
16
It
a
14
9
0.208
0
0
0.352
0.231
229
3
27
15
34
22
0.0208
0
0
0.189
0.124
230
30
1)0
17
30
20
0.7
0.7
0.7
0.745
O.Uyj
231
169
13
7
3
2
0.52
0.52
0 (future POTW)
0.0315
0.0207
232
22
29
18
24
16
1.09
1.09
1.09
1.35
0.685
233
10
33
18
19
13
1.00
1.00
1.00
1.92
1.26
234
18
53
30
21
1<»
1.0
1.0
1.0
1.55
1.02
235
21
36
20
30
20
1.50
1.499
1.499
2.85
1.67
236
237
23B
28
10
27
33
89
20
17
47
U
24
52
19
16
3*)
13
0.12
0.028
1.911)
0.12
0.028
1.914
0.094
(considered
0.02B present 00
only)
1.914
0.109
0.260
1.51
0.0708
0.171
0.995
239
10
19
10
1?
10
0.126
0.126
0.126
0.340
0.224
240
130
09
1)7
61)
1)2
0.6
0.6
0.23
0.354
0.2i3
-------
TABLE 1
HASTCWAIEH DI8CHARQB V3. BAT FLOW OPTTOHS
Bofiuory
Bo.
Wastewater
Generated In 1976
(Ml/bbl)
fip"pn 1 -
Calculated
197>» BAT Flow
fft&l/bbl)
Option 2 now
Kutmatw
HPOKS
Dlacharm
With Planned
Optlcn 2 now
BP* Flow
(nil/bbl)
Level 1
(wa/bbi)
Level 2
(nal/Ubl)
Generated
In 1976 (MOO)
In 1976
fMOD>
0.432
Flow Seduction*
(MDl
Level 1
f'tio)
Level 2
/MID)
241
76
89
47
65
43
0.660
0.432
0.781
0.514
21)2
147
89
47
69
45
0.64
0.64
0.20
0.359
0.236
243
6
18
10
17
11
0.168
0.168
0.168
0.700
0.461
244
5*
28
19
24
16
1.83
0
0
1.09
0.716
21(5
26
29
16
28
19
0.600
0
0
0.689
0.453
246
53
4i
23
32
21
0.565
0
0
0.344
0.226
247
12
1^
8
12
. 8
0.2072
0
0
0.316
0.203
248
.01
13
7
3
2
0.00001
0
0
0.00292
0.iXT>2
SU9
21
16
9
22
14
0.832
0
0
1.12
0.736
250
0
13
7
3
2
0
0 ¦
0
0.00292
0.001;*
251
0
13
7
3
2
0
0
0
0.09146
O.OOO'jC
252
21
20
U
19
12
0.139
0.139
0.123
0.201
0.132
853
Dm NOT SUBKRHB.
-
-
-
-
-
0
0
.
.
25*1
.7
89
47
6
4
0.0001
0
0
0.00514
o.oo3fcu
255
u
13
7
6
4
0.129
0.125
0.125
0.185
0. 121
256
11
17
10
14
9
0.365
0.365
0.365
0.564
0.371
257
16
31
17
22
14
2.03
2.03
2.03
3.27
£.15
258
15
UO
58
29
19
1.0
1.0
1.0
2.47
1.62
259
l>
19
10
7
5
2.19 '
2.19
2.118
4.50
2.#
260
13
89
47
133
88
0.025
0.025
0.025
0.400
0.263
26l
lit
14
8
6
4
0.47
0.43
0.43
0.257
0.169
264
5
13
7
6
4
0.0150
0
0
0.148
0.0^72
265
266
278
12
25
0
25
13
13
13
7
7
11
6
3
7
4
2
1.108
0.06705
0
1.108
0.067
0
0.571
(considered
O.O67 preaent IS,
ZD coljr)
0
2.14
0.0346
O.OOU76
l.M
0.0227
0.00576
291
12
13
7
3
2
0.142
0
0
0.0444
0.0292
292
inanoMi
13
7
3
2
IMKNOVM
uoaiow
una tout
O.OOf>2
O.GOV/S*
295
129
13
7
0
0
0.2586
0.2376
0.2376
0
0
-------
Be finny
296
29fl
3ttJ
303
305
301
308
309
310
Vaatevat«r
Generated Id 1976
(«aiMi>
0
1
.dt
o
0
ia
Option 1 -
Calculated
BPT Plow
(nal/bbl)
13
13
13
13
13
13
13
IB
13
TABL8 1
WASTBWATCa DIBgiAltCg V3. BAT K1/1M nmmtt
Calculated
W» BAT Flow
(fial/bbl)
11
7
Option 2 Plow
tovel 1
(gal/bbl)
3
3
3
3
Level 2
(g-lMl)
2
2
Uuterater
Qeaer&tod
lp 1976 (WD)
0
0.013
0.00000
o
0.0"»63
0
o
0.968
0.0006
MPPES Placharge
With Planned
In 1976 Flow Reductions
(NOP) (Map)
0
o
0.582
o
o
o
0.1(32
o
Optloo 2 flow
Level 1
a.ofyz
0.013a
0.0061*2
o.ooe^e
0.0759
0.00219
0.0001I16
0
0.00876
Level 3
0.0192
o.otea
0.00ttf2
0.00192
0.0500
O.OOlUl
o.ooxi>:
o
0.00576
&
-------
TABLE 2
BOO. MASS
OZSCHABGZ VS. BAT MASS
OPTIONS
BOO. Mass OtsehAJTC* (lb/d)
300. Mass Limitations
(l£Ai)
July 1, 1977 Npoes
Oeceaber 1976
inary
Permit Limitation*
OMR Valua
Ootion 1-
Ootion 2-
DO.
DaiIv Averaoe
O&ilv Average
BPT
level 1
Level 2
X
219.9
18.3
223
196
103
2
44.9
16.4
93
28
18
3
11.96
29.0
24
12
8
4
•
•
36
3
9
«
68.0
99.2
140
108
71
7
•
•
109
47
31
•
•
42
28
18
9
16.0
6.37
17
13
9
10
•
-
100
67
44
U
402.0
1113.9
981
368
243
12
83.0
•
89
61
40
13
1726.0
HO
1640
1220
809
14
-
•
37
31
20
13
•
•
136
92
34
IS
-
•
327
236
196
17
•
-
99
63
41
ia
•
•
199
122
80
19
~
-
42
20
13
20
1000
390
1000
696
430
21
•
•
99
12
8
22
•
-
101
66
43
23
166
-
44
20
13
24
160
18
170
69
46
23
•
-
493
419
273
26
-
•
98
71
46
29
•
-
1960
899
992
30
-
-
63
14
9
31
•
•
96
43
29
32
1243
1132
1190
688
492
33
-
-
187
187
123
33
•
-
10
2
1
36
-
-
149
98
69
37
1730
240
1730
1170
769
38
•
•
733
439
290
39
•
•
72
24
16
40
-
•
2330
1360
897
41
4800
11400
4280
2960
1680
42
•
-
19
4
3
43
938
•
903
913
337
44
•
-
256
241
198
43
-
-
1110
086
981
46
1080
2719
1130
628
413
48
•
•
91
0
0
49
209
194
200
198
130
30
101
22.7
110
US
94
31
2161
4406
1970
829
949
32
•
•
66
83
59
33
•
49
140
90
39
34
16
1.9
21
16
10
33
-
-
180
79
49
36
220
189
204
206
139
37
944
1338
729
613
405
38
•
•
373
364
241
39
122
189.01
400
296
199
60
•
-
1290
737
486
61
-
•
1620
961
633
62
•
•
9990
2340
1940
63
673
196
640
973
377
64
742
-
714
447
294
63
-
-
1190
648
426
66
•
3
1
1
67
3372
9690
4700
2300
1910
68
970
609
809
824
543
70
•
11.03
36
17
11
71
71
-
98
101
66
72
24
13.3
92
91
34
73
•
" -
218
219
144
74
-
•
196
160
109
76
287.3
860.8
678
341
224
77
•
•
99
102
99
73
•
-
146
127
S3
79
-
•
9
S
3
SO
100
3
377
322
212
81
337
170
340
226
148
32
•
•
28
12
8
83
939
2169
978
707
464
84
626
116
398
322
211
83
1204
898
U20
784
919
-17-
-------
TABLE 2 (Cont'd.)
BOD. MASS DISCHARGE VS. BAT MASS OFTIOH3
¦«<«... m.Mi BOO. Mm« Limitations (lS/d)
July 1, 197V KPDESOacaaber 1976 5
tefinary
Pctmlt U»i>iHm.
CMS Valut
Option 1-
Cation 2-
Mb.
Cailv Avaraoa
D»ilv Averaaa
3PT
Laval 1
Laval ;
86
_
238
176
151
99
87
7.8
-
14
3
2
as
121
27.6
12S
SO
33
89
-
-
29
16
10
90
34.7
4.3
42
41
27
91
-
2.1
11
2
2
92
19S1
21936
5120
2090
1370
93
U
0.299
18
6
4
94
320
479
453
345
228
95
U.S
14
14
3
2
96
-
-
6070
3020
1990
97
-
-
202
193
127
98
1745
2175
1330
339
S52
99
U7
24
122
113
75
100
29
30.53
30
14
9
102
377
349
326
196
U9
103
132
35
100
45
.29
104
2285
-
2600
1710
1130
10S
552
1170
398
394
260
106
1403
198
1250
988
6S0
107
26.3
48
145
96
63
ioa
SO
4.4
262
162
106
109
160
-
10S
144
95
110
-
-
17
7
5
111
•
-
605
337
222
112
-
39.6
35
11
7
113
160
121
224
138
91
114
-
-
102
69
4S
113
584
3564
1570
527
346
116
-
-
710
399
261
117
-
-
192
106
70
113
14.6
580
112
41
27
119
24.2
23.5
133
61
40
120
14.9
14.2
BO
34
23
121
974
4S2
1700
907
'396
122
1100
2423
1070
426
280
124
-
42.1
322
178
116
US
265
92
334
179
118
126
265
92
353
305
200
127
42.61
40.4
60
56
36
US
-
-
3
4
2
U9
20
27.3
17
19
U
UO
•
-
23
23
IS
121
1470
3179
1360
731
479
132
3670
-
2620
1810
1190
133
1700
-
U30
620
•407
134
-
-
702
684
449
US
-
-
7
2
1
136
-
-
70
31
21
U7
-
-
13
S
4
138
-
-
108
96
63
U9
-
-
21
5
3
140
-
-
117
121
80
141
-
-
11
6
4
142
3800
2553
564
471
309
143
400
419
403
313
206
144
294
1.19
213
224
147
14S
-
-
15
3
2
146
-
22
14
14
9
147
686
24.6
678
488
320
148
-
-
133
U3
81
149
270
397
216
213
141
ISO
-
239
243
160
131
-
-
15S0
769
S07
152
1540
338
1020
822
541
133
670
470
772
737
484
134
-
-
104
70
46
135
-
-
108
98
65
156
-
-
340
277
182
137
-
-
971
579
381
138
-
-
302
251
165
159
-
-
81
82
34
160
161
-
-
85
100
63
•
-
174
260
171
162
1427
2449
1630
777
511
-18-
-------
TABUS 2 (Cont'd.)
BOD: MASS DISCHARGE VS. SAT MASS OPTIONS
BOD. Mais
Olscharaa (Lb/d)
300. Maaa Limitation*
(lb/d)
July 1, 1977 MSOSS
Oacaabar 1976
Rafioary
Parnit Lialtitlon-
Ma Valua
Option 1-
Option 2-
No.
Oailv Avaraan
Daily Avaraoa
bpt
Laval 1
Laval ;
163
292
326
288
288
189
164
-
-
14
]
2
169
-
-
601
415
273
166
-
. -
265
201
132
167
1331
650
1290
686
449
168
1657
1887
1120
743
488
169
1278
732
1240
850
558
172
-
-
169
86
57
173
SO
258
66
58
38
174
129
416
135
117
77
175
-
-
2360
1390
914
176
354
-
343
268
176
177
132
543
144
95
62
179
89
40
249
198
130
180
457
575
903
417
275
181
5183
4138
2860
2150
1410
182
•
18183
2560
1190
780
183
SIS
137
215
157
103
184
134
588
671
486
320
189
-
-
383
302
199
186
440
3202
946
420
277
187
-
-
513
457
300
188
-
-
639
456
100
189
-
-
14
3
2
190
12.5
12
25-
9
6
191
-
-
490
375
247
192
-
-
3
0
0
193
-
•
9
2
1
194
3405
1775
5180
275
1S10
199
-
-
3
1
1
196
-
-
3400
1910
1260
197
8.2
•
12
3
2
199
57.4
-
27
6
4
200
-
-
225
158
104
201
370
154
281
294
193
202
-
-
10
2
1
203
28200
-
3360
1990
1310
204
934
2341
636
628
413
205
450
317
506
441
290
206
-
-
101
45
30
207
•
-
127
29
19
208
1200
4884
2710
1750
1150
209
-
-
149
161
106
210
3.-34
-
50
23
15
211
217
49
559
268
177
212
496
63
256
224
147
213
25
6.77
60
27
18
214
-
-
_
215
-
.
.
.
216
-
3319
4560
2850
1870
218
-
-
17
4
2
219
530
-
481
432
283
220
-
181
80
52
221
835
445
469
609
400
222
80
43.4
29
37
24
224
-
-
60
52
34
225
-
-
310
260
170
226
-
•
21
13
9
227
262
45
240
207
136
228
-
-
75
75
49
229
-
-
32
40
26
230
154
84
213
159
104
231
-
-
28
7
4
232
406
989
340
288
189
233
800
116
703
409
268
234
410
0
847
330
217
233
660
340
721
607
398
236
-
-
32
23
15
237
-
•
95
55
36
238
4S0
600
332
322
212
239
91
16.24
92
72
48
240
-
219
104
75
30
241
158
589.5
227
166
109
242
-
208
99
76
50
243
-
53.6
161
149
98
244
-
-
265
232
153
245
-
-
149
147
96
-19-
-------
246
247
248
249
250
231
252
233
254
255
226
257
258
259
260
261
264
265
266
278
291
292
295
296
298
302
303
305
307
308
309
310
44
1
156
1
1
28
1
26
79
458
345
630
56
16
21
300
5
1
6
1
0
4
6
1
4
6
1
1
0
1
TABLE 2 (Cont'd.)
30Dj MASS OISCaABGE VS. BAT MASS OPTIOKS
BOO. Ma«« Olacharqa (lb/d)
July 1, 1977 MPOES Dacaabar 1976"
BOD. Maaa
Permit Limit*tion-
Oallv Avarnga
106
60
170
620
818
2620
344
12
DMR valua
Dail^Avaraga
22!
208
5
1530
49
208
614
16
.9
Option 1-
BFT
94
76
3
173
3
1
45
19
82
145
990
2008
2650
57
119
64
1070
16
8
42
3
10
28
41
6
3
36
2
1
211
8
Lay i 1
73
67
1
239
1
1
43
1
39
120
697
526
959
85
55
32
456
7
2
9
1
0
6
9
1
s
9
1
1
0
2
Option 2-
-20-
-------
1
2
3
4
«
7
a
9
10
11
u
13
14
13
16
17
ia
19
20
21
22
23
24
23
26
29
30
31
32
33
33
36
37
38
39
40
41
42
43
44
43
46
48
49
SO
31
32
33
34
33
36
37
38
39
60
61
62
63
64
63
66
67
68
70
71
72
73
74
76
77
78
79
30
31
82
83
84
as
DM 3
TS3 MASS OISCHABSB VS. SAT MASS OPTIONS
TS3 Maaa Discharge (Lb/d)
July 1, 1977 HPDES
7emit Limitation*
Daily Avaraqi
147.3
30.8
2.92
U
Dacambar 1976
TSS Mag a Mmicatlona (lb/d)
286
36
1129
637
134
994
1430
3200
614
772
167
87
2000
14
290
618
160
337
394
634
4330
747
47
16
203.2
130
200
822
427
789
3.3
S3
OMR Valuft
Option 1-
Ooeioti 2-
DaJ.lv Averaqo
BFT
Laval 1
Laval 2
33,2
149
104
68
6.7
37
19
12
17
16
3
3
-
24
S
4
-
93
72
47
-
70
31
21
-
28
19
12
u.a
11
9
6
-
67
43
30
1070.3
387
246
162
•
57
41
27
•
1090
817
337
-
23
21
14
•
91
33
23
•
218
138
104
-
63
42
27
-
130
81
34
-
28
13
9
570
667
437
287
•
37
8
3
•
67
44
29
-
29
13
9
66
113
46
30
-
329
277
132
-
39
47
31
-
1043
399
393
-
42
9
6
•
37
29
19
2009
793
4S9
301
-
123
123
32
-
7
1
1
-
97
66
43
778
1130
780
313
,
489
293
193
-
48
16
10
-
1330
909
398
12900
2830
1700
1120
• ¦¦
13
3
2
•
602
342
224
-
171
160
103
-
740
391
388
187
753
419
273
-
34
0
0
124
133
132
87
16.3
73
86
56
4010
1030
332
363
-
44
36
36
33
93
60
39
1.4
14
10
7
-
120
SO
33
278
136
137
90
1979
486
409
270
-
249
243
160
107.79
267
197
130
-
860
491
324
•
1080
640
422
-
3730
1360
1030
362
427
382
231
1049
476
298
196
214
767
432
284
-
2
1
1
3730
3130
1330
1010
1601
337
330
362
13.67
24
12
8
-
63
67
44
14
61
34
22
-
143
146
96
-
131
107
70
107.1
432
227
149
-
66
68
43
-
97
84
56
-
6
3
2
18.2
231
214
141
187
227
131
99
-
19
a
5
769
632
471
310
323
239
214
141
786
747
523
344
-
117
100
66
1.3
9
2
1
63.7
83
33
22
-21-
-------
39
90
91
92
91
94
95
96
97
98
99
100
102
103
104
103
106
107
108
109
110
111
112
U3
114
11S
116
117
113
119
120
121
122
124
123
126
127
128
129
130
131
132
133
134
13S
136
137
13a
139
140
141
142
143
144
145
146
147
148
149
ISO
1S1
132
133
1S4
135
136
137
138
139
160
161
162
163
164
163
166
167
168
169
172
173
174
TML8 3 (Cone.)
T33 Magi Olacharga (la/d) T3S Mass Limitation* (ib/d)
Jul; 1, 1977 HVSES Dacaobor 1376
Permit Limitation- OMR V&lua Potion 1- Potion 2-
Oallv Average Daily Avaraqa MT Laval 1 Laval 2
-
-
19
10
7
24.8
1.0
28
27
18
-
3.4
7
2
1
1600
49333
3410
1390
916
- •
-
12
4
3
420
564
302
230
132
8.3
23.9
9
2
1
4000
3976
4030
2020
1330
-
-
133
129
83
1331
1491
887
359
368
76
36
31
76
30
20
0.66
20
9
6
248
240
217
130
86
89
33
67
30
20
1830
-
1730
1140
730
362
1663
199
263
173
918
7749
831
659
433
34.7
8
97
64
42
50
4.3
173
108
71
100
-
70
96
63
- '
-
U
5
3
-
•
403
224
148
21
33.1
23
17
11
173
63
149
208
137
-
-
68
103
68
701
769
1030
790
520
-
-
473
S99
392
161.7
243
128
139
103
9.9
3.92
73
62
41
20
18.4
122
92
60
10.2
9.7
33
51
34
1871
726
1130
1360
393
883
1047
713
639
420
-
-
213
266
174
227
143
223
268
177
441
0
235
203
134
34.09
21.8
40
37
24
—
-
3
3
1
14.1
0.02
11
13
3
-
-
15
13
10
-
-
907
487
320
963
260
1730
1200
791
1400
-
833
413
271
-
-
468
436
300
-
-
3
1
1
-
-
47 '
21
14
-
-
9
4
2
-
-
72
64
42
-
-
14
3
2
-
-
78
81
53
-
-
7
4
3
380
Ril
376
314
206
813
334
269
209
138
-
-
142
149
98
-
-
10
2
1
-
-
9
9
6
S49
168.1
432
323
213
-
-
122
82
54
177
148
144
142
94
-
-
139
162
107
-
-
1030
313
338
1230
2364
680
348
361
660
493
313
491
322
-
-
69
46
31
-
-
72
63
43
-
-
227
183
122
-
647
386
234
•
-
201
168
110
-
-
34
34
36
-
-
37
66
44
-
-
116
173
114
1006
1300
1090
318
341
233
390
192
192
126
-
-
9
2
1
-
-
401
277
182
-
-
177
134
38
1063
0
360
437
300
1326
1419
747
496
32S
336
3301
327
567
372
•
-
113
57
38
10S
294
39
38
23
109
433
90
78
31
•22-
-------
175
176
177
179
180
181
182
183
184
18S
188
187
188
189
190
191
192
193
194
193
196
197
199
200
201
202
203
204
20S
206
207
208
209
210
211
212
213
214
215
216
218
219
220
221
222
224
225
228
227
228
229
230
231
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
TftBLS 3 (Cant.)
T33 Mmi Plicharga (Ih/d)
July 1, 1977 NVDIS
Dally Av«rag«
283
112
116
427
4681
560
295
520
17.1
7744
5.6
243
28200
1022
750
2300
3.34
217
327
0*caober 1976
OMR Value
Dailx_Avarage
25
38
328
3479
13011
229
662
TS3 .lata Limitation* (lb/d)
425
3500
262
429
597
4180
6.36
82
475
8.55
Potion 1-
8PT
1570
229
96
166
602
1910
1710
143
447
255
631
342
426
9
17
326
2
6
3450
2
2270
8
18
150
187
7
2240
424
337
67
84
1810
99
33
372
171
40
Option 2-
Lgvol_i
926
179
63
132
278
1430
791
104
324
202
280
305
304
2
6
250
0
1
1830
1
1230
2
4
105
196
1
1330
419
294
30
19
1160
107
15
179
149
18
Lavl 2
609
117
42
87
183
940
520
69
213
133
185
200
200
1
4
165
0
1
1200
1
839
1
3
69
129
1
972
275
193
20
13
765
71
10
118
98
12
424
835
32
209
123
325
650
330
440
400
62
57
4344
1112
92
37
112
815
196
197
180
429
18.18
310
214.6
95
40.7
47.8
13
82.2
3040
U
321
121
313
19
40
207
14
160
50
21
142
19
227
469
565
481
21
63
221
61
69
151
66
107
177
99
63
31
2
115
2
1
30
1900
3
288
53
406
25
34
173
9
138
50
27
106
4
192
273
220
405
15
37
214
48
50
111
51
99
155
98
49
45
1
159
1
1
29
1250
1
139
35
267
16
23
113
6
91
33
18
70
3
126
179
145
266
10
24
141
32
33
73
33
65
102
64
32
30
1
104
1
1
19
110
405
380
3277
167
3850
482
1735
13
55
97
660
1330'
1170
38
1
26
30
464
351
639
37
1
17
S3
305
230
420
37
-23-
-------
So
261
264
265
266
278
291
292
293
296
298
302
303
309
307
308
309
310
TABLE 3 (Coat.)
T38 Maa« Olicharqe (Ib/d)
July 1, 1977 KPCK3
?8X9iC T
Dally Averago
December 1976
OMR Value
Dally Average
Option 1-
BPT
T33 Maaa Llnitatlona (lb/d)
Level 1
Option 2-
Level 1
287
9
43
SJS
218.2
79
43
713
11
S
28
2
7
19
27
4
2
24
1
1
141
3
3
2
30
-2k'
-------
TABLE k
COST WORKSHEET
W.O. No. 4n^(0~&i Date N" Page No. '
Drawing No. Ca'g Nn Sheet of
By ChocfcnH ApprnnaH
-itto BAT Covr Pe-h^leum ffEPmina ^posT-gy
Kle.
Aw«a\>a1
Ffoto Re^o\ Covfs ^22±I__ £ovh
Cooling "f&u36<-" Md-ke-up —
f^ecudc -f-Uo nv--fe.s
RPPES dteckirttf. uirfti
-fuo r^JvjcTKTA (^t^rP) ~
- Qpkio* 2. Level | f Uui(M<5rt>)
= K<£*)wvpi*^ (»*Tte£) —
(?tc^|e. CA-piW a>vt =
Rtihclt- AK>^.f" ~
Wdttsr" soffcwi
Z'rfo rtc.j4e. (jpn) m
Cip4*-l *~£ a*WWaA «pecnj|'il^ CO*h =¦ "•
~Jnea.\>AcvJf Cotk*
Flow ¦fo Eop 4r«*: ~ R»4\>ne. Q Mo D — —
""[©M CAp»4®4 a*\*vv»«^ co^i ^enr L-t^l J *= a
^p4vyv\ 2- Ltv«.l Z i
At|ivA.W iWjf. &t$edr D R)-fvr«. CH A^60W«r- LcveJ t. ^
-------
3
4
6
7
8
9
10
11
12
13
14
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
31
32
53
34
55
56
57
38
59
60
61
62
63
64
65
66
67
68
70
71
72
73
74
76
77
78
79
80
81
82
83
34
85
beeiS-s
REFINERY CRUDE CAPACITIES AMD THROUGHPUTS
CRODE CAPACITY
30.0
20.0
1.25
13.0
22.0
38.0
3.0
3.5
6.0
47.0
4.5
193.
12.4
32.0
48.0
9.3
19.5
2.5
100.
20.
11.
16.
33.3
33.8
17.
131.1
22.8
12.
110.0
44.0
3.5
17.0
103.0
93.0
26.
405.
365.
7.
80.0
40.
111.
65.3
10.
33.3
21.5
130.
4.
14.0
3.
60.300
40.
107.0
70.0
57.0
195.0
200.0
295.0
91.0
78.0
154.0
1.0
380.0
140.0
13.0
21.0
8.50
44.5
22.5
42.452
23.159
29.9
3.
52.0
37.
10.0
90.0
80.0
138.0
THROUGHPUT IK 1976
(1000 bbl/dav)
24.7
16.9
1.1
13.0
21.3
38.0
1.4
3.378
3.6
43.4
3.6
161.5
12.3
30.7
36.05
4.873
16.2
1.5
86.6
16.
7.2
11.
41.6
49.2
13.763
100.0
20.14
10.
84.3
38.3
2.0
11.8
77.2
83.9
13.3
230.1
260.
6.3
46.1
27.842
74.2
38.5
3.425
29.274
14.93
148.
2.812
13.0
2.9
36.200
45.
79.7
33.0
46.099
173.0
159.6
252.0
76.3
70.6
124.9
0.2
328.0
118.0
3.76
18.4
6.58
31.5
19.25
40.933
22.336
25.8
3. -
47.0
54.15
2.05
70.8
78.8
132.4
REFINERY
MO-
86
87
88
89
90
91
92
93
94
95
96
97
98
99
100
102
103
104
103
106
107
108
109
110
111
112
113
114
113
116
117
118
119
120
121
122
124
123
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
135
136
157
158
159
160
161
162
163
164
163
CRUDE CAPACITY
(1000 bbl/dav)
23.0
3.2
43.0
4.0
2.2
3.873
270.
6.5
85.0
3.0
328.0
30.0
202.3
28.7
11.0
90.
36.
298.0
89.0
154.9
17.
13.8
23.5
6.
66.
12.5
42.
24.0
131.9
68.
30.
6.0
11.
4.2
295.
107.
42.
36.
46.
6.3
3.
5.
5.38
168.
300.
100.
103.0
2.5
25.147
4.523
29.93
7.5
19.0
4.020
63.0
44.0
49.9
3.25
4.836
63.0
20.00
44.
31.
177.0
120.
123.
5.5
14.5
35.
130.3
54.600
19.0
23.5
51.
90.
32.0
3.0
SO.
THROUGHPUT IS 1976
(1000 bbl/dav)
23.6
3.0
33.28
2.8
1.8
3.0
251.
3.0
81.578
3.0
472.0
26.0
202.3
22.0
5.5
71.6
34.9
247.0
85.085
119.4
8.3
2.3
11.17
3.
65.
¦ 3.7
41.
21.3
102.2
36.8
27.7
4.2
9.1
2.87
239.2
88.3
34.566
47.8
39.8
3.7
2.4
4.3
5.26
121.5
288.
92.3
82.0
1.623
25.549
4.587
27.62
6.775
12.8
2.301
61.2
31.4
46.9
0.837
3.805
62.8
13.79
44.
42.9
160.3
100.5
112.0
4.775
13 ..7
51.073
125.3
42.801
17.963
20.6
44.87
82.3
51.0
3.9
53.
-26-
-------
sx*.
166
167
168
169
172
173
174
175
176
177
179
130
181
182
183
184
18 3
186
187
188
189
190
191
192
193
194
19 S
196
197
199
200
201
202
203
204
205
206
207
208
209
210
211
212
213
214
213
216
218
219
220
221
222
224
225
226
227
228
229
230
231
232
233
234
233
236
237
238
239
240
241
242
243
244
245
246
247
248
249
250
TftBLE 5 (continued)
REFINERY CRODE CAPACITIES AMD THROUGHPUTS
CRUDE CAPACITY
THROUGHPUT IS 1976
RZFISERY
CRUDE CAPACITY
THROUGHPUT
(1000 bbl/dav)
(1000 bbl/dav)
HO.
(1000 bbl/dav)
(1000 bbl
14.
195.0
6.9
155.1
251
252
O.S
10.6
0.3
6.63
170.
132.1
253
21.0
21.0
188.
154.
254
1.
0.15
12.
9.36
2.8
S 3
255
29.3
29.173
3.5
236
40.
34.7
iss!o
154.0
257
ISO.
124.
52.
34.4
258
33.5
67.
7.6
3.7
259
653.0
523.0
26.
23.3
260
3.
2.
80.0
60.0
261
40.
34.
363.
344.6
264
23.
3.27
324.5
237.7
265
200.
140.1
63.
47.6
266
5.92
2.71
67.
.63.2
278
3.
O.S
73.0
73.0
291
13.2
11.9
185.
136.
292
1.
1.
56.0
49.6
295
3.5
2.0
100.
39.9
296
10.0
10.0
5.
3.
298
13.
9.3
9.
7.2
302
2.2
2.1
53.5
31.5
303
1.
1.0
1.0
0.7
305
13.
12.4
3.250
2.594
307
0.75
0.2
405.
392.4
308
0.05
0.05
1.0
<1.0
309
35.0
32.7
319
304.5
310
3.
3.
4.4
0.3
9.7
2.027
29.3
25.7
66.
65.9
3.5
0.1
335.
291.5
103.
98.754
103.37
101.94
36.5
27.
46.
39.
310.0
283.0
35.0
31.3
18.1
13.5
123.0
116.37
60.0
34.4
21.615
21.201
20.0
20.0
17.0
17.0
476.0
375.6
6.0
6.0
80.7
70.2
10.0
9.3
129.5
115.3
13.5
8.34
20.0
14.2
40.4
34.0
7.5
4.4
45.0
43.5
23.
13.4
5.6
6.
25.
23.1
10.0
3.080
55.0
49.6
100.
99.2
75.0
55.9
94.0
73.0
4.5
4.3
5.0
2.9
78.0
70.4
22.7
12.574
5.5
4.6
12.0
3.74
5.2
4.33
42.0
27.4
44.5
34.1
24.2
23.2
10.80
10.618
25.5
17.143
1.
1.
50.352
39.208
1.
<1.0
-27-
-------
• I ^ " ' : I
i'.-'F r^JCRr
NfiKE-'JP FLOW
DJWImLD t-:,' total
oliJ
^IIMSEP
(MOD)
EFFLUENT FLOW
IMG !':jWE!-S-
' >
0 . O'v /c"0
o. •;. i tsoo
2 • V.-S'.--.1'.''
*1 *. r1 ' *
LOO ¦ IKM'O
• >
0.0
! ' •¦'* % () 's V
4
NOT APR,
NOT APP.
0.0
/
Q
NOT APP <
MOT APP i
0.0
'7
0,107000
< 0.022455
70.1. ooo
0 .0 1.0000
<¦ o »i-;>
¦"o > o
9
0.025000
\/ * • J / t -
! o
0 ,020000
0¦> 400000
' UMI-:MO!;.!'!
¦4 4
i. X
2.90999?
1.372124
9 4.0000
12
0.500000
100.000015
UNKNOWN
J. 3
7.303997
1.476211
95.0000
L 4
0.034488
0 -5V023R
UNKNOWN
X'ci
0.OB4500
1. ¦¦ t 11042
100-0000
i. 6
0 * 30210'^
1 ..':122"*6
"2 * 00-- 0
•4 ¦**'
.L /
0 .018500
0.419121
40.0000
18
0. 108000
0.551021
UNKNOWN
.19
0.013000
3 - 250002
100.0000
20
.1.. 450000
0.7591c2
30 >0000
• *\ J
0 .298000
4.257 1. ^2
1 lxlN M'.;WN
•-\ '•>
0.094500
1 - 0 '-3P6 3
¦7 -- n n f
23
NOT AFP,
NOT APP.
0.0
24
0.350000
1*794871
15.0000
25
0.867000
2.731567
58.0000
'•> '
— U.'
0,210600
4,307499
79,0003
po
.L . 709?-98
0. 4621.62
75.0000
0.193000
0 .. SM. 5 'V.7'3
.! 00 ,00."'"
3:L
0.0
0.0
UNKNOWN
7 0
i./
4.969995
2.83999S
76.8000
35
NOT APP.
NOT APP.
0.0
0.036000
93 - 500j
•••/ "i
6.308996
2.764512
•43 ¦. 0O00
)
3 .'??°9 A
1 , 0 R'! 1 4 !
•5?
0.165000
1.099999
UNKNOWN
40
- 6.614997
1.691815
90.0000
41
6.6219?2
0.705969
4.5000
0.030000
0.239425
UNKNOWN
43
3.769996
2> 055270
99 ,9:) "'y
44
0 ,0
> o, o
95 > 0."-00
45
4.343996
1.371923
53.6000
46
1.462999
1.030281
50.0000
43
> 0.140500
> 0.962329
95.0000
4?
0.650000
4.924242
65.000';
'•;o
0.235000
1>311676
P'0.0000
"51.
r!UT APP-
MOT APP.
0 - 0
5 2
NOT APP.
NOT APP.
0.0
53
0.050000
0.223214
93.0000
54
0.030000
1»363636
100.0000
I." IV
-'•J
-GT A .-P.
N'J T iil-'i"' ¦
,?. j
•i ;/vv^r> r.
- * ¦ w "> / v ' -. «
i
3 i.. oooo
j
o f. "> o o o '?
1 : • 50652 L
j:> - \ •" . . j
it
•JO
1.314149
i r,T^o'---r
X * *J /U. US vj
66.0000
ir* r--
•; c>cr«=:/v\
J. 9 u w ,u w \/
5.00136 0,
47.8000
^ \
'7 Ar-O 1
-1 -.-C-7
AO . 000'"1
-28-
-------
' Li:
foQi Tiir rn,-;;
q j:--
.' 6 i-0:lT i
J-1 i¦'J." -1!f:. ?M i\A7*
EL'M !\!:"!v I!>: L':,! L1'J,v
"RY
r
REFINERY
NUMBER
rtAKI'-UP FLOW
(MGD>
DIVIDES BY TOTAL.
EFFLUENT FLOW
t?Y Bi"U BY
COOLING TOWERS
1
'
.Zl Sm
63
1.. 299'-99
'5 , 3 4 4 ° 9 7
1. -'33000
i i:/ t* .jj i t ^«:•
0 ,862096
0 , 490054
47,0000
i „ q, a«a
91. '• 41.00
64
65
66
4., 308998
2.484499.
0.000050
.0.874036
0.664305
UNKNOWN
66.0000
40.0000
100.0000
6 7
i 8
r,
8,8299VI
8,348999
o.o
0 >352 495
1.714373
0.0
63.6000
74.4000
UNKNOWN
"7 \
t ^
nn
75
0.359000
0.021000
0~46S000
1.495832
0.127273'
1.658162
100.0000
10.0000
* 75.0000
7 4
"7 '
' O
0.471500
1,933998
0. £>30000
2, J. 6 2 S -14
0«640397
3 7, 6 7'''3«? n
95.0000
86,5000
59 - 0000
73
79
80
0.075500
> 0.0
. 2.129998
0.243548.
UNKNOWN
.L 6. 3S459S
90.0000
"UNKNOWN
85.4000
o .1.
a*:
83
0 , 776500
0*216000
^ , o?Q9'.;o
1 ,772830
0.369863
> 0.988363
100.0000
:i 00,0000
ao , oooo
84
35
36
2.204,995 .
> .5.394799
0.440950
< 1,510271
> 1.332707
' 1.102650
75.0000
80.0000
97.0000
37
DO
s./ O
po
NOT APP.
0.735000
r», o
NOT APP.
3,325790
0 ,0
0.0
89.2000
p v Q i' W'N (\
90
•91
9°
0.017000
0.005000
A.559999
0,145299
4.999999
0.650551
60.0000
UNKNOWN
48,0000
93
9 4
O IT
¦* 1
0 - 0
0.0
0,0
:• 0,0
0 - 0
0 - 0
UNI-MOWN
86,5000
! 0 0 . 0 r- 0 0
96
97
93
19.014984
0.014040
4,989999
1-513931
0.197191
2.370166
100.0000
UNKNOWN
39 >4000
99
10 0
i.O:.'
MOT APP,
MOT APP,
0-0
NOT APP,
NOT APP.
0 - 0
0 •> 0
0 >0
0,9000
.103
104
103
0.025000
. > 6.684999
NOT APP.
0.324675
0.759659
NOT APP.
UNKNOWN
71.0000
0.0
10 6
0 7
'! ':f?
2.250000
0.045000
O .. 1 9 A f) 0 0
1-0397 42
1,499999
9 . ru^crao
10 ? .0000
L 00,0000
9 9 .. 0 0 0
109 .
110
i 1 1
0.200000
NOT APP.
9,8 49497
0.487805
NOT APP..
i ..70^0=:
7,6000
0.0
AA-OOOO
"* "J
i I. -
' -i •»
0 >302500
0 - 529300
'v " r, r. t'\ ^
. 47560°
1 . "'000
- . 9a a "
3!:" ."000
•'! 9 .. -500 f
v n . a aa
115
t 1 6
I " "7
L.933199
0.864000
1 -A-rono
0.708235
0 , 41.7593
1 ,
53,8000
40,0000
C'O, .v^oo
-29-
-------
; ••• c-
: <¦¦¦ ^oN'nN;'ed
wCOL L.'Jfi TCl-lb.
:=¦ Mr ::.v: .:r:..ci; <
3U, - 00 00
134 '
> 0.0
> 0.0
99.5000
135
0.0
UNKNOWN
UNKNOWN
136
0.378000
1.1.59509
100.0000
.137
0 . 0
> 0.0
100.0000
. 133
0.466000
1 >1767 67
1. .0000
¦* TO
0.. 07.1000
5.071.42"'
0.0
UNKNOWN
100,0000
142
0.502500
0.275554
66.5000
L 43
0.030000
0,022043
2 ¦ 0000
144
0,759500
1.130207
100.0000
•f \i~,
0,004500
1.097560
1.00 0000
146
0. .150000
1.499999
UNKNOWN
147
1.695000
1.810897
' 89.0000
148
0.126500
0,562222
100.0000
•i »> i >
, "A '/
0.740000
0 . 616667
""7 ,0000
130
NOT APP,
NOT APP,
0-0
1 '51
4-150000
1.044238
i] ,. 7000
152
3.070000
0.520339
35,0000
153
5.792998
1.418809
63.0000
154
0.063000
0,092240
UNKNOWN
155
0.391700
1 ,32331.1
L :;o - 0000
156
1.697997
2,149363
60 .0000
1 Is! 7
•U 119996
' 1.753190
89 -OOOO
159
0.570800
1.042842
71.5000
.159
0.199500
0.488971
60.0000
160
0.328000
3.065420
.LOO. 0000
161
2,1.14997
.2.812495
90.000 )
162
~2.115 499
0.836165
UNKNOWN
163
2. "?329('8
2 - 635488
88 -• 0r,00
164
0-030000
1-363636
100,0000
165
0.595400
3.335574
49.8000
156
0,050000
0.452899
67.0000
.! *.J •
3 v y/_ 4 ••37 9
0»305203
>"j' OOOU
1.-9
'!. - 240000
0.381538
20.. OOOu
.* 7*
: - 79-t'?9S
0,781737
90 . OoOO
172
0.772000
0.00166.L
91 •3000
173
0,0
0.0
UNKNOWN
1 7 A.
MHT APP,
MOT APP,
.1 A
-30-
-------
REFINERY
MAKE-UP FLOW
DIVIDED 3Y TOTAL.
I-Y G'TU ft Y
NUMBER
(MGD)
EFFLUENT FLOW
COOLING TOWERS
, u:;
L0,787498
0 ,356.L3 L
unknot
l"'o
0>086000
0»022°66
31 •• 0000
1 7 7
0 • 029.000
O.02068°
73 . ''.>000
17?
0.632700
6.025716
82.0000
180
1*870998
0.680363
98.7500
181.
> 20.376430 -
1.337379
49.0000
182
> 6.599497
0.87220?
¦ 'O.OOvO
103
2-169648
S. 488432
5*v 7000
In 4
4~675997
6.5851 AS
75 r00CO
135
1.771500
2.116487
95.0000
186
2.574697
1.555708 .
71.0000
_ 1.87
3.244994
2.561165
60.0000
,L 38
4.653300
2, 086771.
80,0000
IS 9
0.0
UNKNOWN
UNKNOWN
i. °0
0 . 085000
4. !. 66665
70,,0000
191 •
2.345500
5.606S28
100.0000
192
. 0.028000 '
UNKNOWN _ .
100.0000
193
> 0.0
• UNKNOWN
UNKNCJt-JN
>r i-
1.1 -303490
1 -1303 43
79.0000
i. \.i
0 >0
0.0
UNKNOWN
1 O i
16.445465
0-7200 30
91 .3000
197
0.002.000
0.238095
100.0000
199
0.017200
• 1.5S9648
UNKNOWN
200
1.694998
2.769604
70.0000
20'L
2.136999
2.270524
69-0000
0.009500
47.5OO000
: qa „ OOO'O
1 r, „ " a o » a ¦[
0 .76999.1
65 . :)c 0000
'*> /\ o
2 - 8 4 4998
< 0.J59 443
4 7.500'"'
°
¦0, 413500
3 .35-R-7
! '¦"¦!.J
210
0.137000
4.392356
79>9000
211
0.679049
1.226335
UNKNOWN
217
1-763000
2-507822
65 0000
213
0.038880
0.447890
. 0000
214
0 - 0
UNKNOWN
'JNKNO'/N
0 ¦ 0
UNKNOWN
l.WI ->'W nU:1-'
216
16.507477
1.261749
78.0000
218
7.800000
36.666687
100.0000
219
1.939999
< 0-786699
63.0000
220
0.022000
0,956322
100 - 0000
2 21
0,0
UNKNOWN
99.5">0O
'•tnn
0. <360000
nr , O O f\ <*. r O
1. 00 , 'to 00
224
0,0
0.0
UNKNOWN
225
1.679999
1.600000
97.9000
n a
0 .. 0
^¦?.:3000
-i j , -j.
. - ~ <:¦ w i ¦' "
!. • 1 ¦:':78'74
^0 .- OO0
'¦* *.'J
¦' rr ~ /v
6 , ..i'y t73.b
!. oo >
A ' ' . T r" A. "i
i ',0 ,,-v.'.
230
1 .150000
1.769230
83.0000
07 1
A„ %./ .i.
MOT APr'.
NOT APP-
0 - 0
\ " T
A n,
A
'! A A A (1 ri
-31-
-------
r T* '**4 »1"
the
.. "fv it n'1 "1
:::: '.•¦> r:' r1 , 1 r ¦; r t
)
'• V
REFINERY
MAKE-UP FLOW
DIVIDED BY TOTAL
BY STIJ G'Y
DUMBER
(MGD)
EFFLUENT FLOW
cor.
LINO TOWERS
>
2 o450000
2. *r::oooo
iv'O , 0000.
z:-4
f\
UMKNijlJM
i INNfj WN
~4JOOOO
1. . 4131.1?
S3 ¦ 0000
236
0.016000
0.164948
UNKNOWN
237
0*016000
0.571428
9010000
233
1.999999
1 - 039500
34.5000
239
c.casooo
0.329341
-5 7. 000O
2 ¦* 0
0,130000
0 ,15 0 311
UNKNOWN
*•% j
."u. • ~ ».
0 >324000
L ,3728:71
1.00 • 00 00'
242
0.450000
0.702023
95,000,0
243
0.524000
4.563433
69.0000
244
0 - 612000
0.304024
99.0000
2 43
0... 707000
•;. 001.410
?9 : .$000
') A L
0,182500
0 - 40 L0'-?9
UNKNOUN
*"> A,
0 ,'=v58?:00
3 • 6 32 0
00.. oooo
249
0.0
UNKNOWN
100,0000
249
0.330000
0.684635
50,0000
250
0.0
UNKNOWN
UNKNOWN
'.;'J!.
NOT APR ,
NOT APR,
0 V
/•j r- —,
0 >009000
0.03910?
90¦>0000
2~; ~
0 >0
UNKNOWN
UNKNOT M
254
0,0
0,0
UNKNOWN
255
0.0
0.0
UNKNOWN
256
0.040000
0.100025
100,0000
257
NOT APR.
NOT APR >
0,0
253
0 , 792000
0 • ? 0 4 '¦> 4 "
40,0000
NOT APR .
NOT ^P,:'.
0,0
260
NOT APR,
NOT APP,
0>0
261
0.640000
.1.36 L 701
90.0000
264
0 >0
0.0
UNKNOWN
n
L.296000
i/;n97'-39
UNK.-K.:1.'-.1!
o ,r. .v'.
.«•. • i -¦
NOT APR.
NOT APR.
0 .0
¦'""3
0.0
! INK NOUN
SJNKNfiyf-1
2?i
0 - 506000 .
3,373335
90.0000
295
0.610600
1,327391
90.0000
298
> 0,0
0.0
100,0000
301
0 »144000
/\ ' 1 C l:~ **> -1
\/ * C5 v. ~ \ t
?4.S=" 00
/: ."i p
MOT AF'F.
NOT rlP° -
0,0
7 0'
0-0
UNKNOWN
¦: iNKNC'i.:!."'
305
0,0
0,0
UNKNOWN
307
0.0
UNKNOWN
UNKNOWN
303
> 0,0
UNKNOWN
UNKNOWN
3f,o
0 - 720000
2 >3571 4 L
1. j1, ¦> .....'..'. .*
- DUE
TO UNKNOWN MAKE-UP
FLOWS FOR SOME COOLING
TOWERS :>
THE
NUMBER IS GREATER
THAN SHOWN
- DUE
TO UNKNOWN EFFLUEN
T FLOWS* THE NUMBER
IS
LESS THAN SHOWN
¦ i '**1 l" •" .
- : j-j f :-V-i'f'M E
v.;hp
!'¦ D.M... ::*'G •
-32-
-------
Ref .
No.
001
TABLE 7
Wastewater Treatment Operations
Treatment Ooerations
Corr. Plate Sep.
DAF
Act. Sludge
002 Chemical Floe.
Rof.
NO.
015
Treatment Ooerations
Chemical Floe.
OAF
016 I None
003
RBC
017 | Chemical Floe.
Evap. or perc. Pond
004 | none
018 None
006
DAF
Aerated Lag.
019 I None
007
008
DAF
Aerated La?.
020 | chemical Floe.
DAF
Act. Sludge
Pol. Pond
021 I None
009 I Aerated Lag.
Pol. Pood
022 DAF
010 I Stab. Pond
023 I Filtration
Evap. or Perc. Pond
011
024 | DAF
Aerated Lag.
Other Org. Rem.
012 | Pre-Filtration
Stab. Pond
02S | DAF
Other Org. Rem.
013 | Chemical Floe.
DAF
026 Other Org. Rea.
014
027
-33-
-------
TABLE 7
Wastewater Treatment Operations
Ref.
No. Treatment Operations
Ref.
No. Treatment Operation
OAF
Evap. or Perc. Pond
DAF
DAF
Aerated Lag.
Stab.. Pond
None
Evap. or Perc. Pond
OAF
Aerated Lag.
Pol. Pond
Corr Plate Sep.
DAF
Chemical Floe.
DAF
Act. Sludge
Others Org. Rem.
-34-
041
042
043
044
045
046
047
048
049
050
051
052
053
Corr. Plate Sep.
Aerated Lag.
Stab. Pond
Pol. Pond
Chemical Floe.
Aeratod Lag.
Evap. or Perc. pond
DAF
Stab. Pond
Filtration
Evap. or Perc. Pond
Chemical Floe.
DAF
OAF
Chemical Floe.
DAF
Evap. or Perc. Pond
Aerated Lag,.
Pol. Pond
DAF
Aerated Lag.
Stab. Pond
Filtration
Chemical Floe.
DAF
&ct. Sludge
Pol. Pond
Stab. Pond
Pol. Pond
Filtration
-------
TABLE 7
Wastewater Treatment Operations
Treatment Operations
Ref.
No.
Corr. Plate Sep.
Stab. Fond
Pol. Pond
Evap. or Perc. Pond
DAF
Aerated Lag.
PolV Pond
Step, or Perc. Fond
Aerated Lag.
Pol. Pond
OAF
dar
Act. Sludge
Chemical Floe.
DAF
Act. Sludge
Filtration
Chemical Floe.
OAF
Act. Sludge
Pol. Pond
Trick. Filter
Aerated Lag.
Pol. Pond
Aerated Lag.
Pol. Pond
OAF
Act. Sludge
Act. Sludge
Pol. Pond
067
068
070
071
072
073
074
075
076
077
078
079
080
Treatment Operations
Chemical Floe.
DAF
Aerated Lag.
Act. Sludge
None
Chemical Floe.
DAF
Aerated Lag.
Pol. Pond
Chemical Floe.
Aerated Lag.
Pol. Pond
Chemical Floe.
Aerated Lag.
Pol. Pond
Aerated Lag.
Pol. Pond
Chemical Floe.
Aerated Lag.
Pol. Pond
Act. Sludge
Pol. Pood
Evap. or Perc. Pond
Chemical Floe.
Stab. Pond
Evap. or Perc. Pond
-35-
-------
TABLE 7
Wastewater Treatment Operations
Treatment Operations
Aerated Lag.
Pol. Pond
Evap. or Perc. Pood
OAF
DAF
Act. Sludge
Pol. Pond
ChemicaJL.Floc.
OAF
Act. Sludge
Chemical Floe.
DAF
Evap. or Perc. Pond
Stab. Pond
Evap. or Perc. Pond
Aerated Lag.
None
. DAF
Act. Sludge
Aerated Lag.
Pol. Pond
None
Ref.
No.
094
095
096
097
098
099
100
101
102
103
104
105
106
Treatment Operations
Corr. Plate Sep.
DAF
Act. Sludge
Pel. Pond
Stab. Pond
Pol. Pond
Corr Plate Sep.
Chemical Floe.
DAF
Act. Sludge
Hone
OAF
DAF
Aerated Lag.
Stab Pond
OAF
Aerated Lag.
Pol. Fond
Filtration
Aerated Lag.
Aerated Lag.
Corr. Plate Sep.
Aerated Lag.
Stab. Pond
Chemical Floe.
OAF
Aerated Lag.
Aerated Lag.
Pol. Pond
-------
TABLE 7
Wastewater Treatment Operations
Reg.
No.
107
108
109
110
Treatment Operations
Filtration
OAF
Chemical Floe.
OAF
Act. Sludge
Trick. Filter
Pol. Fond.
Chemical Floe,
i OAF
Aerated Lag.
Aerated Lag.
Pol. Fond
Aerated Lag.
Pol. Fond
Pre-Filtration
Act. Sludge
Pol: Pond
Stab. Pond
OAF
Aerated Lag.
Pol. Pond
Aerated Lag.
Filtration
Aerated Lag.
Filtration
Aerated Lag.
Filtration
Ref.
No.
121
122
124
125
126
127
128
129
130
131
132
133
134
Treatment On^r.^i- i»„«:
Corr. Plato Sep.
OAF
Aerated Lag.
Other Org. Rem
Pol. Pond
Aerated Lag.
Chemical Floe.
DAF
Stab. Pond
Aerated Lag.
Other Org. Rem.
Pol. Pond
Aerated Lag.
Pol. Pond
Chemical Floe.
DAF
Aerated Lag;
Pol. Pond
Evap. or Pere Pond
Aerated Lag.
Evap. or Perc. Pond
Pol. Pond
None
OAF
RBC
OAF
Activated Sludge
DAF
Act. Sludge
Trick. Filter
Filtration
Act. Sludge
Filtration
-37-
-------
TABLE 7
Wastewater Treatment Operations
Ret.
Ref.
No.
135
136
I Treatment Operations
137 Hone
138
139
Corr. Plate Sep.
140
141
142
143
144
145
146
147
Evap. or Perc. Pond
Evap. or Perc. pond
Evap. or Perc. Pond
Evap. or Perc. Pond
Chemical Floe.
DAF
Chemical Floe.
DAF
Aerated Lag.
Pol. Pond
Hone
Stab. Pond
Chemical Floe.
DAF
Act. Sludge
NO.
148
149
150
151
152
153
154
155
156
157
158
159
160
Treatment Operations
DAF
Corr. Plate Sep.
Aerated Lag.
Corr. Plate Sep.
Act. Sludge
Chemical Floe.
DAF
Aerated Lag.
Pol. Pond
DAF
Act. Sludge
Other Organics Rem.
Filtration
Stab. Pond
Pol. Pond
Stab. Pond
Pol. Pond
Chemical Floe.
DAF
Aerated Lag.
Pol. Pond
Act. Sludge
Aerated Lag.
Other Organics Rem.
Act. Sludge
Pol. Pond
Stab, pond
Pol. Pond
Checical Floe.
OAF
Act. Sludge
Stab. Pond
Pol. Pond
Evap. or Perc. Pond
-38-
-------
TABLE 7
Ref.
No.
Wastewater Treatment Operations
Ref.
Treatment Operations
Aerated Lag.
Other Organics Rem.
Pol. Pond
DAF
Act. Sludge
Aerated Lag.
Pol. Pond
Evap. or Perc. Pond
Chemical Floe.
DAF
Stab. Pond
Pol. Pond
Hone
Chemical Floe.
OAF
Act. Sludge
Pre-Flltra.tloa
Act. Carbon
Act. Sludge
Trick. Filter
Hone
None
Aerated Lag.
-39-
iN'O.
175
176
177
178
179
180
181
182
183
184
185
186
187.
Treatment Operations
Corr. Plate Sep.
Aerated Lag.
None
Chemical Floe.
Aerated Lag.
Stab. Pond
Pol. Pond
DAF
Act. Sludge
Pre-ET titration
Act. Sludge
Filtration
Act. Sludge
Chemical Floe.
DAF
Aerated Lag.
PoL-Pond
Chemical Floe.
Act. Sludge
Evap. or Perc. Pond
DAF
Act. Sludge
Stab.. Pond
Filtration
Evap. or Perc. Pond
-------
TABLE 7
Wastewater Treatment Operations
Roff.
188
189
190
191
192
193
194
195
196
197
198
199
200
Treatment Operations
Corr. Plate Sep.
Aerated Lag.
Pol. Pond
Aerated Lag.
Pol:. Pond
Evap. or Perc. Pond
Hone.
Aerated Lag.
Pol. Pond
None
Corr. Plated Sep.
Chemical Floe.
OAF
Act. Sludge
Stab. Pond
Aerated Lag.
Pol. Pond
Pre-Filtration
Aerated Lag.
Filtration
None
-ifO-
Ref.
No.
201
202
203
204
205
206
207
208
209
210
211
212
213
Treatment Operations
Chemical Floe.
DAF
Act. Sludge
Filtration
Chemical Floe.
DAF
Chemical Floe.
DAF
Act. Sludge
Pol. Pond
DAF
Aerated Lag.
Pol. Pond
None
Corr. Plate Sep.
Act. Sludge
Trick. Filter
Stab. Pond
DAF
Stab. Pond
Pol. Pond
Evap. or Perc. Pond
None
Chemical Floe.
DAF
Act. Sludge
Aerated Lag.
Filtration
OAF
Act. Sludge
OAF
Aerated Lag.
Stab. Pond
Pol. Pood
-------
TABLE 7
Wastewater Treatment Operations
Ref.
No.
214
215
216
218
219
220
221
222
223
224
225
226
Treatment Operations
Evap. or Fere. Pond
Evap. or Perc. Pond
Chemical Floe.
Act. Sludge
Aerated Lag.
Aerated Lag.
Pol. Pond
Filtration
Other Organics Rem.
Aerated Lag.
Pol. Pond
Hons
Chemical Floe.
OAF
OAF
Filtration
Stab. Pond
Pol. Pond
Ref.
No.
227
228
229
230
231
232
233
234
235
236
237
238
239
Treatment Operations
OAF
Aerated Lag.
RBC
Pol. Pond
Filtration
Stab. Pond
Pol. Pond
Evap. or Perc. Pond
Stab. Pond
-Al-
chemical Floe.
Filtration
Act. Sludge
Trick, Filter
Pol. Pond
OAF
Act. Sludge
iTrick. Filter
. Pol. Pond
I
1
Act. Sludge
Ttick. Filter
Pol. Pond
Corz. Plate Sep.
OAF
Act. carbon
Act. Sludge
Trick. Filter
Aerated Lag.
Stab. Pond
Pol. Pond
Corr Plate Sep.
RBC
Pol. Pond
-------
TABLE 7
Wastewater Treatment Operations
Treatment Operations
Act. Sludge
Pol.. Fond
None
Aerated Lag.
Pol. Fond
Evap. or Perc. Pond
Corr, Plate Sep.
Aerated tag.
Pol. Pond
Evap, or Perc. Fond
Aerated Lag.
Evap. or Perc. Pond
Pol.'Pond
Evap. or Perc. Pond
Evap. or Perc. Pond
OAF
Evap. or Perc Pond
Stab. Pond
Re£.
No.
2S3
254
255
256
257
258
259
260
261
264
265
266
Treatment Operations
Evap. or Perc. Pond
None
Pre-Filtration
Aerated Lag.
Pol. Pond
Corr. Plate Sep.
Stab. Pond
Stab. Pond
DAF
Act. Sludge
Pol. Pond
OAF
Act. Sludge
Aerated Lag.
DAF
Trick. Filter
RBC
Evap. or Perc. -pond
Corr. Plate Sep.
DAF
Act. Sludge
Stab. Pond
Pol. Pond
None
-------
TABLE 7
Wastewater Treatment Operations
Ref.
NO.
275
278
282
283
284
287
288
289
290
291
292
293
29U
Treatment Oneratioris
None
-^3-
Ref.
295
295
297
298
299
300
301
302
303
30U
305
306
307
Treatment Operations
Evap. or Perc. Pond
-------
TABLE 7
Wastewater Treatment Operations
Treatment Operations
Evap. or Perc. Pond
Cheaical Floe.
Act. Sludge
Aerated Lag.
Evap. or Perc. Pond
-hk-
-------
TABLE 8
Refineries that Utilize, or Plan
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
-J+5-
-------
TABLE 9
REFINERIES THAT UTILIZE, OR PLAN TO UTILIZE
EQUALIZATION SYSTEMS*
PRESENTLY INSTALLED
009 102 187
020 105 188
024 106 190
038 110 196
040 113 197
041 114 200
043 115 204
044 126 208
051 130 210
060 131 211
062 147 212
063 153 216
064 156 219
065 160 227
072 161 230
074 162 232
081 175 243
085 180 256
088 181 258
094 182 301
096 183
099 184
FUTURE INSTALLATIONS
76 163 221
77 168 222
83 172 242
104 173
132 174
*Note - Minimum Detention 3.0 hours
-U6-
-------
fi;
No
3
10
11
15
16
25
32
37
38
39
40
42
44
46
50
51
57
62
TABLE 10
FUTURE WASTEWATER TREATMENT MODIFICATIONS
Modifications
Steam stripper to be added
DAF unit to be installed
Sour waters to be stripped; Separator effluent to equal-
ization, pH adjustment, flocculation, DAF, bio-reactors,
clarification and filtering
API effluent to CPI and then to detention pond
DAF unit to be.installed
API sludge handling system to be installed
Replace stabilization with bio-disc, and effluent to pass
through clarifier carbon and filtration
DAF sludge thickener to be installed
Chemical floculation and DAF unit to be added
Final effluent to be used as boiler feed water
DAF effluent to equalization, activated sludge, and clari-
fication
Detention pond effluent to oxidation pond, then percolation
ponds;Clarifier effluent to filter before recycle to cool-
ing tower
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
Segregated streams to trickling filter where effluent
to combine with DAF effluent to activated sludge and
clarifier
Separate stabilization pond for sludge recirculation
Additional foul water stripping; IAF for ballast water
Activated sludge unit with pre-and pust-filtration to
be added along with surge pond
DAF units being added
-U7-
-------
fi:
No,
67
70
71
72
74
76
77
78
83
86
87
88
90
92
95
97
98
TABLE 10 Cont'd.
FUTURE WASTEWATER TREATMENT MODIFICATIONS
Modifications
Activated sludge plant to be added
Segregate process and non-process wastewater and add
oil to skimmer and filter
Segregate storm water; New API units and equalization
pond; Increase lagoon aeration
Total renovation of barometric recycle water system
Possible addition of pH adjustment, chemical flocu-
lation, and DAF
Equalization after API; Two new DAF units; Activated
sludge unit; Final clarifier
Adding DAF, equalization, pH adjustment, activated sludge
unit, and clarification
Add sour water stripper effluent and coker effluent
to desalter
New equalization, bio-discs, and clarifiers after DAF,
and sludge to be treated and digested
Storm water surge basin
All sour water to be evaporated
Adding two additional oil separators, and by-passing off-
property water
Segregation of storm sewers and boiler blowdowns, and
installation of bio-discs
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
Adding API separator
Adding activated sludge plant
Storm water segregation and overall plant modifications
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
-k&-
-------
fine
No.
104
105
106
107
110
114
115
120
121
122
124
12 5
127
132
142
143
150
TABLE ¦10 Cont'd.
FUTURE WASTEWATER TREATMENT MODIFICATIONS
Modifications
New impounding basin before aerated lagoon
Areated lagoon to be converted to activated sludge basins
and to be followed by sand filters
Storm water segregation
Tie in to POTW
Boiler blowdown, sour water, desalter condensate, water
treatment system blowdown, and spent caustic to be routed
to new separator and into.POTW
Tie in to POTW
Storm water segregation; Separator effluent to pH adjustment,
equalization, chemical floculation, DAF unit, activated
sludge and clarification
Additional API separators and enlargement of aeration ponds;
Activated carbon to be added if necessary
Plant source control programs
Stormwater segregation; Extra aerators to aeration basins;
Mixed media filter for final effluent; Some recycle of
final effluent to cooling water
Storm water retention pond
DAF unit to be installed
Baffles added to final polishing pond
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
Tie in to POTW
Tie in to POTW
Bio-discs to be added
Additional ammonia removal facilities; Bio-discs studies
on aerated lagoon effluent
-1+9-
-------
TABLE 10 Cont'd.
FUTURE WASTEWATER TREATMENT MODIFICATIONS
Refinery
No.
152
154 .
163
165
168
172
173
175
177
181
182
184
185
187
190
194
199
204
Modifications
Downflow sand filter to be added prior to final discharge
API separator to be added with new holding pond
API effluent to equalization pond with skimmer, four stage
bio-disc unit, two parallel clarifiers, and final pond-
ing with skimmers
Storm water runoff retention basin
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
Adding IAF, equalization, bio-discs, and clarification
API effluent to equalization, chemical addition, DAF,
activated sludge,and clarification
To join regional POTW
Installation, of bio-discs and clarifiers
API effluent to primary clarifiers before equalization
Expanded reuse of stripped sour water; Increased rainfall
collection and retention facilities
Addition of chemical flocculation, DAF units, and cooling
towers, and modification of aeration basin and clarifier
Add secondary treatment, effluent reuse, and, in 1981,
solar evaporation
Larger API separator
Increase lagoon size
Improve API and polishing pond
Additional API separator
Modify DAF for recycle pressurization; Aerators in equali
zation pond; Dual media filters for bio-treator effluent;
Improve chlorination; Better storm water segregation
-50-
-------
fin'
No.
205
208
212
216
219
221
222
230
231
232
236
240
241
242
246
TABLE 10 Cont'd.
FUTURE WASTEWATER TREATMENT MODIFICATION
Modifications
Sour water stripping systems; Larger API separator; Pond-
ing or biological systems
Existing two parallel plate interceptors and three API
separators to be replaced by five CPI units
Sand filtration for plant effluent
Aerated lagoon to be converted to activated sludge; New
contaminated runoff impoundment facilities; Sour water
oxidizer to be replaced by .single stage stripper
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
Equalization before aeration, and storm water segregation
Increase surge pond size; Chemical Floculation and
clarification to be added; Effluent recycle facilities
installed
IAF provided for API separator and equalization basin
enlarged for grit removal
Tie in to POTW
Storm water retention, activated sludge, aid filtration
uader construction
New system to irclude API separator, holding tank,CPI,
aerated equalization basin, four stage bio-disc unit, and
final clarifier
New oil-water separator and existing pond to be sub-
divided into primary settling, aeration, and final settling
New parallel separator to combine with old separator and
go to two parallel DAF units, activated sludge pond,
clarifier, and final chlorination
Adding equalization basin after API separators, then
chemical floculation, DAF, activated sludge, and final
clarification
Total impoundment for all but once-thru cooling water
New API separator additional treatment pond, DAF, new
aeration basin, and phenolic treatment
-51-
-------
TABLE 10 Cont'd.
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
-52-
-------
TABLE 11
PLANNED WASTEWATER FLOW REDUCTIONS
Refinery Expected Flow Effective
No. Reduction (MGD) Date
7
9
11
12
13
18
22
31
35
39
40
42
44
45
46
50
53
0.115
0.023
0.72
0.0014
0.0462
0.021
0.00189
1.2
0.005
0.230
0.13
0.450
0.052
0.100
Reduction Technique
1978 Upgrade piping and installing air
coolers.
1977 Stripping steam to crude unit.
In plant modifications.
1977 Better cooling tower controls and
wastewater supervision.
1977 Recycle.
Cascading of sour water.
1977 Sour water stripper effluent to
desalter and cooling towers.
1978 Recycle.
Wastewater to cooling tower.
1977 Replace once-thru condensers with
recycled water.
- Reuse; final effluent to be used for
boiler feedwater.
1978 Discontinue selected quench
streams.
Recycle treated effluent to cooling
tower.
1979 Recycle cooling tower water and
boiler blowdown.
1977 Stripped sour water to desalter.
1977 Stripped sour water to cooling
towers and recycle cooling water
and desalter water.
1977 Sour water used for desalting.
1978 Reuse and increase cooling water
cycles
-53-
-------
TABLE 11 (continued)
PLANNED WASTEWATER FLOW REDUCTIONS
Refinery Expected Flow Effective
No. Reduction (MGD) Date
57
59
63
64
67
72
74
76
77
78
82
87
90
92
96
102
113
4.3
0.11
0.125
2.37
0.020
0.5
0.063
0.002
0.270
2.1
0.417
0.072
Reduction Technique
1977 Recycle cooling water and control
blowdowns.
1980 Water management within refinery.
1977 Reroute cooling tower blowdown
out of end-of-pipe treatment
system.
1983 Closed system for pump cooling;
once-thru cooling eliminated;
cooling cycles increased via acid
injection.
Recycle and make-up for firewater.
1977 Larger cooling capacity for lower
blowdown rates; total rennovation
of barometric recycle water systems.
1977 Improved condensate recovery.
1978 Fin fan air condensing.
1977 Stripped sour water used as de-
salt er make-up.
Treated sour water to desalter.
1982 Switch to fin fan cooling.
1977 Reuse of wastewater in gas hand-
ling system; all sour water to be
evaporated.
1978 Closed cooling system and some
recycle.
1978 Cooling towers replacing once-
thru cooling.
1977 Treated wastewater for firewater
system.
Recycle treated wastewater.
1977 Reduce once-thru cooling and tower
blowdown.
-5b-
-------
TABLE 11 (continued)
PLANNED WASTEWATER FLOW REDUCTIONS
Refinery
No.
115
117
122
132
138
144
150
152
153
156
162
169
172
173
Expected Plow Effective
Reduction (MGD) Date
0.08
0.200
0.700
0.7
0.538
0.08
0.072
0.4
1.0
0.216
1.0
1.55
0.156
0.180
1978
1977
1977
1978
1977
1978
1978
1977
1977
1977
1977
1977
1977
Reduction Technique
Recycle process wastewater to
coker cooling.
Pump gland cooling to cooling
towers.
Coker recycle water system; some
recycle of final effluent to
cooling system.
Process wastewater reductions to
end-of-pipe treatment; reuse of
stripper sour water.
Recycle to cooling towers.
Two series desalter.
Segregated once-thru pump
gland cooling and plant waste-
water conservation program.
Firewater use reduction and
mechanical pump seal replacement.
Recycle treated wastewater to
cooling towers.
Increase cooling tower cycle, de-
creasing blowdown.
Recycle wastewater to process
units.
Reuse of process water
Replace barometric condenser
with surface condensers and
recycle treated sour water to
desalter.
Replace barometric condenser
with non-contact condensing
system.
-55-
-------
TABLE 11 (continued)
PLANNED WASTEWATER FLOW REDUCTIONS
Refinery Expected Flow Effective
No. Reduction (MGD) Date
181 3.0 1978
Reduction Technique
Reduce boiler blowdown via
better control; increase cooling
tower cycles; cascade boiler
blowdown from high pressure
boilers to low pressure boilers;
use boiler blowdown as desalter
water; use clarifier overflow
and regeneration water from
condensate polisher as cooling
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 firewater system.
182 0.94 1977
183 0.080 1977
184 0.144 1978
Treated wastewater used as
utility water and greater reuse
of stripper bottoms.
Recycle desalter effluent.
Steam condensate collection and
reuse.
185 0.837 1981
187 0.72 1977
191 0.140 1979
194 3.0 1977
196 4. 1983
200 0.022 1977
202 0.0001 1977
207 0.0005 1977
Effluent reuse and evaporation.
Recycle effluent to cooling towers.
Sour water stripper.
Replace barometric condenser; use
recycled fire water in wet gas
scrubbers on cat cracker;
automate cooling tower blowdown.
Recycle treated effluent to cool-
ing tower.
Stripped sour water to desalter.
Total recycle.
Increase heat recovery at re-
former to reduce cooling require-
ments .
-56-
-------
TABLE 11 (continued)
PLANNED WASTEWATER FLOW REDUCTIONS
Refinery
No.
208
Expected Flow
Reduction (MGD)
210
216
220
222
227
229
236
240
242
247
249
252
259
265
0.003
4.56
0.001
0.0432
0.0125
0.026
0.37
0.36
0.000652
0.0144
0.016
0.072
0.537
Effective
Date
1980
1977
1977
1978
1978
1977
1977
1977
1977
1977
1977
Reduction Technique
Increase cooling tower cycles;
reuse boiler blowdown; recover con-
densate; recycle demineralizing
regenerants to fire system; re-
use appropriate water for cool-
ing.
Boiler blowdown and stripped sour
water to be used in desalter.
Reuse treated effluent and sludge
blowdown decant as intake water
sources.
Condensate from tower overheads
to desalter feed.
Recycle some treated effluent.
Sour water treatment to reduce
volume requiring stripping.
Strip ammonia from cat cracking
condensate to release water for
desalter.
Contact cooling to non-contact
cooling.
Contact cooling to non-contact
cooling.
Non-contact cooling water
segregation.
Find market for spent phenolic
caustic.
Reroute cooling tower blowdown to
spray pond.
Additional wastewater evaporation.
Recycle boiler blowdown.
Desalter water and zealite
regeneration brine to disposal
well.
-57-
-------
TABLE 11 (continued)
PLANNED WASTEWATER FLOW REDUCTIONS
Refinery Expected Flow Effective
No. Reduction (MGD) Date
298
309 0.15 1978
Reduction Technique
Install water softeners to reduce
cooling tower blowdown.
Replace two vacuum jet ejecters
on solfolane unit with vacuum
pump.
-58-
-------
TABLE 12
REFINERIES WITH FLOW REDUCTION COSTS
30 105 173
40 112 174
51 137 177
56 122 180
57 126 18]
64 129 194
65 132 196
67 133 199
68 134 204
70 146 205
76 149 221
81 151 222
87 152 238
92 167 261
94 169 266
102 172 309
-59-
-------
TABLE 13
PLANTS MEETING BOD AND TSS LIMITATIONS
Total: 32
PLANTS MEETING BOTH BOD AND TSS FOR LEVEL 1
REFINERY NO.
1 119
2 120
37 121
49 125
50 126
53 127
54 147
59 167
63 179
72 211
80 213
90 227
99 233
107 235
108 239
113 243
PLANTS MEETING BOTH BOD AND TSS FOR LEVELS 1 AND 2
REFINERY NO.
1 120
2 121
50 125
53 126
54 147
59 179
72 211
80 213
90 235
99 239
119 243
Total: 22
-60-
-------
1
2
3
6
7
9
10
11
12
13
19
20
24
30
32
37
38
40
41
43
TABLE 14
WASTEWATER FLOW RATE
TO
END-OF-PIPE TREATMENT
FLOW RATE REFINERY FLOW RATE
(MGD) NO. (MGD)
0.19 49 0.132
0.054 50 0.768
0.014 51 9.9
0.075 52 0.3
0.05 53 0.15
0.013 54 0.017
0.05 56 1.306
0.779 57 6.0
0.59 ,59 0.99
* 60 1.944
INSIGNIFICANT 61 2.64
1.91 62 4.80
0.30 63 2.605
0.237 64 2.43
5.9 65 3.60
2.36 67 21.0
* 68 4.86
6.6 70 0.150
9.38 71 0.240
2.869 72 0.132
0.86 73 *
-61-
-------
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
TABLE 14 (continued)
FLOW RATE
(MGD)
0.19975
1.78
0.276
0.08
1.21
2.44
1.69
3.29
0.09
0.212
0.0576
0.03
0.012
10.42
0.024
1.836
11.82
0.0712
2.34
0.07
0.0518
1.584
0.063
6.01
2.381
FLOW RATE
(MGD)
1.583
**
0.044
0.24
**
0.203
0.428
**
2.72
1.2
0.81
0.026
0.125
O.'lOO
4.5
6.4
0.475
0.444
6.48
0.173
0.10
2.88
10.13
7.93
4.15
REFINERY
NO.
106
107
108
109
110
112
113
114
115
116
1] 7
118
119.
120
121
122
124
125
126
127
129
131
132
133
134
-62-
-------
142
143
144
146
147
149
150
151
152
153
154
155
156
157
158
159
160
161
162
163
165
167
168
169
172
TABLE 14 (continued)
FLOW RATE
(MGD)
REFINERY
NO.
FLOW RATE
(MGD)
**
173
0.472
**
174
0.576
0.119
175
*~
0.093
176
0.3684
0.576
177
0.765
1.179
179
0.282
0.968
180
2.764
3.974
181
12.57
7.98
183
0.559
3.89
184
1.216
1.0
186
1.815
0.0936
189
0.015
0.634
190
0.0332
2.01
194
13.76
0.548
196
18.5
0.277
197
0.008
0.175
199
0.0492
0.35
201
0.95
2.45
204
3.366
1.037
205
2.424
0.29
208
4.98
5.1
210
0.016
2.88
211
0.8135
8.67
212
0.703
0.764
213
0.051
-63-
-------
216
219
221
222
226
227
230
231
232
233
234
235
236
237
238
239
240
241
242
243
252
255
256
257
258
TABLE 14 (continued)
FLOW RATE
(MGD)
20.5
1.2
3.312
0.35
0.036
1.2268
0.7
**
1.09
1.00
1.0
1.499
0.094
0.028
1.914
0.126
0.23
0.432
0.28
0.168
0.123
0.125
0.365
2.03
1.0
REFINERY FLOW RATE
NO. (MGD)
259 2.127
260 0.025
261 0.43
265 0.571
266 0.067
292 INSIGNIFICANT
295 0.2376
309 0.432
* Consider present indirect
discharge only.
** Will be discharging to POTW
in future.
¦Sh-
-------
1
2
3
6
7
9
10
11
12
13
19
20
24
30
32
37
38
40
41
43
46
49
30
31
32
33
'34
36
37
39
60
61
62
63
64
63
PVBLE 15
CAPITAL AMD OPSBATTHG COSTS BY REFINERY HPMBER
ECONOMIC COSTS. DOLLARS
OPTION 2 LEVEL 1 OPTIOH 2 LEVEL 2
CAPITAL ANNUAL OPERATING CAPITAL ANNUAL OPERATING
COSTS COSTS COSTS COSTS
131.000
3.600
181.000
30.100
76,000
3.900
126.000
14.900
30.000
4.700
33,000
9,700
36.000
6,700
171,000
14,700
70,000
3,600
140,000
12,600
13.000
3.200
67,000
9.400
70,000
3,600
140,000
12.600
178,000
6,300
238,000
73.300
143.000
3.200
386,000
32.200
No cost -
considered presently Indirect discharger only.
He eost -
insignificant flow.
200.000
13,000
273,000
163.000
73.000
6,900
313,000
22.900
323.000
19,800
375,000
43,800
730,000
29,300
4,730,000
122,000
610,000
32,300
2.210,000
117,000
He coat - considered presently indirect discharger only
933.000
47.300
1.060.000
338,000
330.000
37.300
6.930,000
328.000
300,000
17,300
2,400,000
120.000
338,000
17,300
398.000
90,300
110,000
7,800
230,000
17.800
180,000
6,600
745,000
40.600
1,420,000
606,000
3,690,000
942.000
166,000
10,100
406,000
26.100
63,000
2.200
100,000
20.200
33,000
4.000
88,000
15.000
645,000
33,800
1,330,000
83.800
1.280,000
121.000
1,380,000
683.000
383,000
19.100
460,000
104,000
0
0
73,000
143.000
630,000
33.800
730,000
238.000
400,000
24.300
300,000
397,000
230,000
18.000
2,130,000
108.000
483,000
32.300
360,000
223,000
720,000
47,600
320,000
330,000
4,310,000
360,000
7,760.000
720,000
1,383.000
38.000
1,490.000
464.000
190,000
10,700
223.000
28,700
-65-
-------
TABLE 13 {continued)
CAPITAL AND OPgRftTINQ COSTS BY RETINERY SPMBER
ECONOMIC COSTS. DOLLARS
OPTICS 2 LEVEL I OPTICS 2 LEVEL 2
CAPITAL ANNUAL OPERATING CAPITAL ANNUAL OPERATING
COSTS COSTS COSTS COSTS
71
143.000
9.300
34S.000
24,300
72
30,000
5.700
85,000
22,700
73
Ho cost -
considered presently indirect discharger only.
74
72.000
2.300
242.000
13,500
76
380,000
26,400
1.630.000
92.400
77
70,000
6.700
110,000
34.700
80
91.000
6.800
181.000
15,800
81
270.000
21,100
1.150.000
69,100
33
210.000
17,000
293.000
209,000
34
520,000
25,400
595,000
164,000
83
300,000
22.000
395,000
286.000
87
220,000
13.400
315,000
24,400
38
60.000
6.200
235,000
19,200
89
79,000
6,100
156.000
15,100
90
S8.000
4.700
118.000
11.700
91
45.000
3.400
80,000
7,400
92
1.680.000
73.100
4.010.000
413,000
93
31,000
4,000
86,000
10.000
94
428,000
27,400
503,000
172,000
96
600,000
44,300
3,080.000
387.000
97
85,000.
6.500
120,000
17,500
98
650.000
30,800
2.250.000
111.000
99
43,000
3,000
128,000
13.000
100
30,000
1,100
63,000
10,600
102
230,000
13,600
303,000
32,600
103
48,000
6,100
137,000
14,100
104
500.000
28.000
4,600,000
208,000
10 S
305,000
22.200
330,000
203,000
106
200,000
13.000
1,300,000
73,000
107
No cost -
will discharge
to POT* in
fa tare.
108
70,000
3.400
105,000
13,400
109
143,000
9.300
185,000
118,000
110
No cost -
will discharge
to POTW in
future.
112
295.000
184,000
465,000
31.400
113
90.000
7.800
420,000
28,300
114
So cost -
will discharge to POTW in
futare.
US
0
0
90,000
216.000
116
400.000
21.000
1,300.000
69.000
117
677,000
25,300
1.270,000
59.300
-66-
-------
TOBLB 15 (continued)
REFINERY
SOMBER
CAPITAL AND OPERATING COSTS BY RETCTERY NUMBER
ECONOMIC COST" nijr.riB^
OPTION 2 LEVEL 1
OPTION 2 LEVEL 2
CAPITAL
COSTS
ANNUAL OPERATING
COSTS
CAPITAL
COSTS
ANNUAL OPERATING
COSTS
118
20,000
900
75,000
7,400
119
60.000
2,000
17S.000
12.000
120
33,000
l.aoo
135,000
10,800
121
1,000,000
47,300
4,100,000
197.500
122
1,320,000
113,000
5,720,000
319,000
124
220,000
12,400
583,000
33,400
123
210,000
12,000
530,000
33,500
126
760,000
54,300
5,160.000
265,000
127
126,000
8.400
276,000
20,400
129
221,000
13,600
521,000
24.600
131
300,000
17,500
390,000
234,000
132
740,000
108,000
3,070,000
434,000
133
1.360,000
172,000
1,690,000
772.000
134
940,000
56,500
1,040,000
381.000
142
So coat -
will discharge to POTW in
future.
143
No coat -
will discharge to POTW in
future.
144
110.000
7,700
223,000
17,700
146
220,000
13,300
313,000
24,300
147
109,000
8,700
149,000
39,700
149
* 370,000
31,700
1,370,000
73,700
150
372,000
18,900
424,000
99,900
131
1,230,000
62.000
3,930,000
.94,000
132
1,330,000
135,000
1,650,000
'67,000
133
0
0
100,000
100,000
1S4
310,000
19,400
1,010,000
39,400
1SS
93.000
7.000
190.000
16,000
136
113,000
9,000
590,000
37.300
137
380,000
28,300
655,000
189,000
136
243,000
13,400
283,000
62,400
139
138,000
10,200
383,000
25.700
160
36,000
6,300
91,000
27,000
161
80,000
7,200
355,000
25,200
162
220,000
17,000
293,000
215.000
163
163.000
11,400
365.000
53.A00
163
162.000
10,000
396,000
26,000
167
1,680,000
111,000
1.780.000
507,000
168
0
0
80.000
228.000
169
2,220,000
172,000
2.340.000
340,000
172
320,000
24,000
370,000
39,000
173
233,000
17.700
293,000
60,700
-67-
-------
173
176
177
179
180
181
183
184
186
189
190
194
196
197
199
201
204
20S
208
210
211
21?
213
216
219
221
222
226
227
230
231
232
233
234
235
TABLE 13 (continued)
CAPH3VL AMD OPERATING COSTS 3Y REFIHERY NUMBER
ECONOMIC COSTS. DOLLARS
OPTICS 2 LEVEL 1 OPTIOB 2 LEVEL 2
CAPITAL ANNUAL OPERATING CAPITAL ANNUAL OPERATORS
COSTS COSTS COSTS COSTS
244,000 16.900 674.000 42,900
No cost - will discharge to POTW in future.
18S.000
11.000
470,000
30,000
483,000
28.300
.333.000
93,300
138,000
9,800
383,000
23.600
363,000
46,100
640,000
263,000
980,000
106,000
3,340,000
448,000
106,000
8,300
326,000
33,400
130,000
12,000
225,000
112.000
380,000
26,300
633,000
171.300
30,000
3,700
103.000
9,900
38,000
3,800
60.000
6,400
2,870,000
134,000
12.200.000
650,000
2,230,000
233,000
5,330,000
611,000
33,000
3,000
83,000
9,000
133.000
9,300
227,000
16,300
209.000
7,700
269,000
87,700
268,000
18,700
358,000
283,000
890,000
48,400
2,390,000
133,000
420.000
23,000
320,000
413,000
33,000
3,200
70,000
8,200
0
0
60,000
69,000
0
0
30,000
61,000
71,000
3,700
144,000
12,700
1,000,000
66,800
4,230,000
424,000
0
0
830,000
48,000
600,000
423,000
690,000
301.000
233,000
17.000
310.000
33,000
63.000
3,000
128,000
12.000
0
0
60,000
96.000
123.000
9,400
643,000
40,400
No cost -
will discharge to POTW in Suture.
0
0
60,000
90,000
383,000
19.400
443,000
103,400
383,000
19.400
443,000
103.400
400,000
24,000
475,000
144,000
100,000
7,100
133,000
20,100
55.000
4,300
90,000
10,300
793,000
43,100
366,000
196,000
-68-
-------
239
240
241
242
243
252
233
236
237
238
239
260
261
263
266
292
293
309
TABI£_^3 (continued)
CAPITAL AMD OPERATING COSTS BY RETISTBtY NUMBER
ECONOMIC COSTS- nnr.raBg
OPTICS 2 LEVEL 1 OPTIQB 2 LEVEL 2
CAPITAL ANNUAL OPERATING CAPITAL AHHUAL OPERATING
COSTS
COSTS
COSTS
COSTS
110.000
7,700
143,000
24,200
143,000
9,100
183,000
33,600
203,000
11,300
230,000
31.S00
70,000
6,700
110,000
34,700
33,000
6,000
200,000
17,300
110,000
7,700
225,000
17,700
60,000
2,000
173,000
12.000
so.ooo
7,300
363,000
26,300
390,000
29,000
990,000
101.000
165,000
11,400
225.000
95,400
390,000
29,300
665.000
198,000
38,000
4,400
116.000
10,700
383,000
22,100
433,000
261,000
248,000
13.700
296,000
64,700
410,000
23,200
470;000
31.200
o coat - insignificant
flow.
315,000
20.100
353,000
43,100
423,000
39.100
470,000
99.100
-69-
-------
TABLE 16
RAW WASTEWATER EQUALIZATION SYSTEMS
CAPITAL AND OPERATING COSTS
Capital Cost, Dollars
Description 380 M^/day 3800 M^/day 19,000 M^/day 38,000 M^/day 76,000 M^/day
(0.1 x 10 ) (1.0 x 10 ) (5 x 10) (10 x 10) (20 x 10)
gal/day gal/day gal/day gal/day gal/day
Detention tank, 12 hours detention, $ 30,000 $ 116,000 $ 346,000 $ 595,000 $1,020,000
steel shell on concrete pad
Pumps, and associated controls,
installed
8,000
30,000
87,000
149,000
255,000
Subtotal
$
38,000
$
146,000
$
433,000
$ 744,000
$1,275,000
Piping, installed (15%)
5,700
22,000
65,000
117,000
192,000
Total Installed Cost
$
43,700
$
168,000
$
498,000
$ 861,000
$1,467,000
Engineering
6,650
26,000
75,000
129,500
221,500
Contingency
6,650
26,000
75,000
129,500
221,500
Total Capital Cost
$
57,000
$
220,000
$
648,000
$1,120,000
$1,910,000
2
Land Requirements, Ft
585
§,780 ,
28,200
57,600
113,000
Annual Operating Costs
, Dollars
Pumping
$
140
$
1,400
$
7,000
$ 14,000
$ 28,000
Maintenance (3% of Capital Cost)
1,700
6,600
19,500
33,600
57,300
Total Annual Cost
$
1,840
$
8,000
$
26,500
$ 47,600
$ 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.
-------
TABLE 17
ROTATING BIOLOGICAL CONTACTORS (RBC's)
AS ROUGHING SYSTEMS
EQUIPMENT COST BASIS
AND ENERGY REQUIREMENTS
Equipment Size
Description
380 M /da^ 3800 M /dgy 19,000 M^day 38,000 M /gay
76,000 M /gay
Design Percent Removal
of BOD
Number of Units
Shaft Lengths, each
Total Square Feet of Surface Area
(0.1 x 10")
gal/day
50
1
15
75,000
(1.0 x 10")
gal/day
50
6
20
630,000
(5 x 10")
gal/day
50
24
25
3,200,000
(10 x 10 )
gal/day
50
48
25
6,400,000
(20 x 10 )
gal/day
50
96
25
12,800,000
Manpower Requirements, hours
Power Requirements, kwh/year
500
33,000
Annual Operating and Energy Requirements
750
294,000
1,000
1,180,000
1,500
2,360,000
2,000
4,720,000
-------
TABLE 18
ROTATING BIOLOGICAL CONTACTORS (RBC's)
AS ROUGHING FILTERS
CAPITAL AND OPERATING COSTS
Capital Cost, Dollars
Description
380 M /dag 3800 M/dgy 19.000 M^day
38,000 M /^ay
76,000 M/gay
(0.1 x 10 )
gal/day
(1.0 x 10 )
gal/day
(5 x 10 )
gal/day
(10 x 10 )
gal/day
(20 x 10 )
gal/day
RBC Units, Steel Shell,
Fiberglass Cover
$ 46,000
$340,000
$1,590,000
$3,170,000
$6,340,000
Piping
5,000
35,000
160,000
317,000
634,000
Total Equipment Cost
51,000
375,000
1,750,000
3,487,000
6,974,000
Installation (50%)
25,500
187,500
875,000
1,744,000
3,487,000
Total Constructed Cost
76,500
562,500
2,625,000
5,231,000
10,461,000
Engineering
11,750
84,750
397,500
784,500
1,569,500
Contingency
11,750
84,750
397,500
784,500
1,569,500
Total Capital Cost
$100,000
$732,000
$3,420,000
$6,800,000
$13,600,000
2
Land Required, Ft
420
2,800
13,500
27,000
54,000
Annual Operating Costs*
Power
$
1,500
$ 12,000
$ 48,000
$ 95,000
$ 190,000
Labor
5,000
7,500
10,000
15,000
20,000
Maintenance (3% of Total Capital Cost)
3,000
22,000
103,000
204,000
408,000
Total Annual Cost
$
9,500
$ 41,500
$ 161,000
$ 314,000
$ 798,000
Note: The depreciation factor has been omitted from
in the Economic Impact Analysis Supplement.
this analysis
due to the fact
that it will be
included sepai
-------
TABLE 19
POWDERED ACTIVATED CARBON
EQUIPMENT COST BASIS
AND ENERGY REQUIREMENTS
INCLUDING COSTS FOR SLUDGE DISPOSAL
80 mg/1 DOSAGE RATE
Equipment Size
Description
380
M /da%
3800
M /dgy 19,000 M ^day 38,000 M /jiay 76,000 M /{iay
Powdered Carbon Feed Tanks (2 each)
Capacity, gallons (Based on feed
concentration of one pound
carbon/gallon water)
Feed Rate pounds/day
Sludge handling and/or regeneration
system, lbs/day dry solids
(0.1 x ioT
gal/day
700
67
290
(1.0 x 10")
gal/day
7,000
670
2,900
(5 x 10 )
gal/day
35,000
3,350
14,600
(10 x 10*
gal/day
70,000
6,700
29,000
(20 x 10 )
gal/day
140,000
,13,400
58,000
Annual Operating and Energy Requirements
Carbon make-up lbs/day
67
670
3,350
2,000
4,000
Furnace power requirements
Fuel, BTU/hr
Connected hp
N.A.
N.A.
N.A.
N.A.
N.A.
N.A.
2,500,000
100
4,500,000
140
Manpower requirement, hours
400
540
940
10,000
10,700
-------
TABLE 20
POWDERED ACTIVATED CARBON
CAPITAL COSTS
INCLUDING COSTS FOR SLUDGE DISPOSAL
Description
Capital Costs, Dollars
380 M /da^ 3800 M /dgy 19,000 M ^day 38,000 M /fjay
76,000 M /fiay
Powdered Carbon Feed System
Solids Dewatering System
(0.1 x 10 )
gal/day
$10,000
(1.0 x 10 )
gal/day
$30,000
(5 x 10 )
gal/day
$45,000
(10 x 10 )
gal/day
$60,000
397,000
(20 x 10 )
gal/day
$100,000
585,000
Subtotal
10,000
30,000
45,000
, vww
497,000
f
745,000
Piping (10%)
1.000
3.000
4.500
49,700
74,500
Total Equipment Cost
11,000
33,000
49,500
546,700
819,500
Installation (50%)
6.000
16.500
24.800
273,400
410,000
Total Constructed Cost
Engineering
17,000
9,000
49,500
7,750
74,300
11,350
820,100
119,950
119,950
1,229,500
185,250
Subtotal
35,000
65,000
97,000
1,060,000
1,600,000
Activated Carbon Regeneration
900,000
1,200,000
System (installed)
Contingency (For utility hook-up etc.)
190,000
250,000
Engineering for Carbon Regeneration
System
150,000
200,000
Total Capital Cost
$35,000
$65,000
$97,000
$2,300,000
$3,250,000
2
Land Requirements, Ft.
100
200
900
3,000
4,500
-------
TABLE 21
POWDERED ACTIVATED CARBON
ANNUAL OPERATING COSTS
INCLUDING CREDIT FOR SLUDGE DISPOSAL
80 mg/1 DOSAGE RATE
Annual Cost, Dollars
Description
380 M
3800 M
38,000 M
76,000 M"
(0.1 x 10 )
gal/day
(1.0 x 10 )
gal/day
(5 x 10 )
gal/day
(10 x 10 )
gal/day
(20 x 10 )
gal/day
Carbon Make-Up
$7,400
$74,000
$370,000
$220,000
$440,000
Furnace Power
76,000
132,000
Miscellaneous Power Requirements
1,000
2,000
5,000
8,000
15,000
Labor ($10/manhour)
4,000
5,400
9,400
100,000
108,000
Sludge Disposal Credit
{->400,000
(->800,000
Maintenance
1,000
2,000
3,000
332,000
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 22
Description
TERTIARY FILTRATION
EQUIPMENT COST BASIS AND ENERGY REQUIREMENTS
Equipment Cost Basis
(all units are
automatic and
air scoured)
Bed depth, ft.
Operation type
Media type
380 M3/ day
3800 M3/day
19,000 M3/day
38,000 M3/day
76,000 M3/day
(0.1 X 106gal/day)
(1 X 106gal/day)
(5 X 10^gal/day)
(10 X 106gal/day
(20 X 106gal/day)
2 units
2 units
1 unit, 4-35'square
1 unit,4-47'square
2 units, 47' square
5' diam.,steel
11' diam.,steel
cells, concrete
cells, concrete
cells, concrete
4
4
4
4
4
Gravity
Gravity
Gravity
Gravity
Gravity
Dual media
Dual media
Dual media
Dual media
Dual media
Annual Operating and Energy Requirements
Pumping, 3,440 34,400 172,000 344,000 688,000
KWH/year
Labor, 400 500 600 700 800
Manhours/year
-------
TABLE 23
TERTIARY FILTRATION
CAPITAL AND OPERATING COSTS
Capital Cost, Dollars
Description
380 H^/dav
3800 M^/day
19,000 M /day
38,000 M3/
-------
TABLE 24
SUPPLEMENTAL ECONOMIC COST INFORMATION
CAPITAL AND OPERATING COSTS
FOR 10,000 GALLON PER DAY TREATMENT SYSTEMS
Capital Cost, Annual Operating Cost
Treatment System Dollars Dollars*
Equalization $ 12,000 $ 400
Rotating Biological 50,000 6,100
Contactors
Filtration 35,000 3,000
Powdered Activated 35,000 4,300
Carbon
Granular Carbon 60,000 10,000
-78-
-------
TABLE 25
Wastewater Recycle - Capital and Operating Costs
Capital
Costs, Dollars - Per Mile
Description^
2.3 m^/hr 16 m^/hr
(10 gpm) (70 gpm)
80 rivfyhr 160 m^/hr
(350 gpm) (700 gpm)
320 m3/hr 800 m3/hr
(1400 gpm) (3500 gpm)
Piping:
Piping,Installed,per mile
M1sc. Costs (15%)
$32,000
5,000
$53,000
8.000
$100,000
15,000
$135,000
20,000
$175,000
26,000
$243,000
36,000
Total Constructed cost,
per mile
Engineering (15%)
Contingency
37,000
6,000
7,000
61,000
9,000
10,000
115,000
18,000
17,000
155,000
23,000
22,000
201,000
30,000
29,000
279,000
42,000
42,000
Piping-total capital costs
per mile
$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,
per year
Maintenance (V.5% of capital
costs) per mile,per year
$100
800
$ 700
1300
$2600
2500
$4500
3300
$ 9200
4300
$24,300
6,000
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.
-79-
-------
TABLE 26
Water Softening of Recycled Wastewater
Canital Hosts
Capital Costs, Dollars
Description 2.3 m^/hr 16 m-fyhr 80 m-fyhr 160 m^/hr 320 m^/hr 800 m^/hr
(10 qpm) (70 qpm) (350 qpm) (700 qpm) (1400 qpm) (3500 qpm)
Solids Contact Clarifier
$ 25,000
$ 30,000
$ 45,000
$ 65,000
$ 80,000
$125,000
(Diameter, ft)
(8)
(11)
(23)
(32)
(45)
(72)
Chemical Feed System(s)
5,000
7,000
10,000
15,000
25,000
50,000
Filter Unit
15,000
25,000
30,000
40,000
80,000
150,000
(Diameter, ft)
(3)
(8)
(11)
(15)
(two-15'
(three-20'
units)
unitsj^
Subtotal
45,000
62,000
85,000
120,000
185,000
325,000
Auxiliary Equipment
5,000
8,000
10,000
15,000
20,000
35,000
Total Capital Cost
50,000
70,000
95,000
135,000
205,000
360,000
Installation(50%)
25,000
35,000
50,000
70,000
100,000
180,000
Total Constructed Cost
75,000
105,000
145,000
205,000
305,000
540,000
Engineering
15,000
20,000
25,000
30,000
45,000
80,000
Continqencv
15,000
20,000
25,000
30,000
45,000
80,000
Total Capital Costs $105,000 $145,000 $195,000 $265,000 $395,000 $700,000
-8o-
-------
TABLE 27
Description
Lime and Caustic Feed
(Based on 500 mg/1
Hardness)
Misc. Power
Labor ($10/Manhour)
Maintenance (3% of
Total Capital Cost)
TOTAL ANNUAL COST
WATER SOFTENING OF RECYCLE D WASTEWATER
ANNUAL OPERATING COSTS. DOLLARS
2.3 m 3/hr
(10 gpm)
$1,000
16 m ?/hr
(70 crom)
$ 7,000
80 m 3/hr
(350 gpm)
$35,000
160 m 3/hr
(700 crom)
$70,000
320 m 3/hr
(1400 crom)
$140,000
800 m 3/hr
(3500 gpm)
$350,000
100
4,000
3,200
700
5,000
4,400
3,500
6,000
5,900
7,000
7,000
8,000
14,000
8,000
12,000
35,000
9,000
21,000
$8,300
$17,100
$50,400
$92,000
$174,000
$415,000
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