CE
oEPA
Department
of the Army
United States
Environmental Protection
Agency
Corps of
Engineers
Office of Water
Program Operations (WH-595)
Washington DC 20460
May 1979
430/9-79-01
Water
Computer-Assisted
Procedure for the Design
and Evaluation
of Wastewater Treatment
System
Users Guide
-------
EPA/CE REV I EM NOTICE
This report has been reviewed by the U.S. Environmental Protection
Agency (EPA) and by the U.S. Army Corps of Engineers (CE) and approved
for publication.
Approval does not signify that the contents necessarily reflect the views
and policies of EPA or CE, nor does mention of trade names or commercial
products constitute endorsement or recommendation for use.
The three reports listed below were prepared in conjunction with
the EPA/CE interagency agreement in 1976 to expand and upgrade the
CAPDET model. These reports are:
Part I. Design of Major Systems Wastewater Treatment
Facilities
Part II. Design of Small Systems Wastewater Treatment
Facilities
Part III. Computer Assisted Procedure for the Design and
Evaluation of Wastewater Treatment Systems
(CAPDET) -- User's Guide
-------
ACKNOWLEDGEMENTS
CAPDET was originally developed by the U.S. Army Corps of
Engineers Waterways Experiment Station (WES) in Vicksburg, Mississippi
in 1974. The Environmental Protection Agency (EPA) and Corps of
Engineers (CE) entered into an interagency agreement in 1976 to expand
and upgrade the CAPDET to the needs of both the EPA Construction
Grants Program and the urban area comprehensive planning program
in which CE was involved.
This user's guide was produced by Mississippi State University.
The members of the workgroup are listed as follows:
INTERAGENCY WORKGROUP
Corps of Engineers: Andrew J. Green
x, Norman R. Francineues
John Cull inane
^
>• EPA: James A. Chamblee
0 Wen H. Huang
A Richard Kezer
~)
,M Contractors and Consultants
Mississippi State Univ.: Marion Corey
James W. Epps
Sage Murphy & Assoc.: R. Sage Murphy
Joseph Fulton
Patricia A. Spaine
Clark, Dietz & Assoc.: Roy Harris
Paul T. Sun
Dames & Moore: William Moore, Jr.
Michael Dominica
-------
ENGINEERING AND DESIGN
Design of Wastewater Treatment Facilities
Part I. Design of Major Systems Wastewater Treatment Facilities
Part II. Design of Small Systems Wastewater Treatment Facilities
Part III. Computer Assisted Procedure for the Design and Evaluation of
Wastewater Treatment Systems (CAPDET) — User's Guide
Table of Contents
Subject
Paragraph Page
CHAPTER 1. INTRODUCTION
Purpose 1-1 1-1
Applicability 1-2 1-1
References 1-3 1-1
Scope 1-4 1-1
CHAPTER 2. MODEL DESCRIPTION
Definitions 2-1 2-1
Program Organization 2-2 2-1
Input Data 2-3 2-4
Unit Process Specification 2-4 2-4
Title Card 2-5 2-8
Scheme Description 2-6 2-8
Waste Influent Characteristics 2-7 2-13
Des.ired Effluent Characteristics 2-8 2-16
Unit Cost Data 2-9 2-16
Program Control Cards 2-10 2-19
Cost Analysis in the Computerized
Design Process 2-11 2-22
CHAPTER 3. UNIT PROCESS SPECIFICATIONS
General 3-1 3-1
Aerated Lagoon 3-2 3-4
Aerobic Digestion 3-3 3-6
Anaerobic Digestion 3-4 3-8
Anion Exchange ^ 3-5 3-10
Carbon Adsorption 3-6 3-12
Cascade Aeration 3-7 3-14
Cation Exchange 3-8 3-16
Centrifugation 3-9 3-18
Chlorination 3-10 3-20
Coagulation ,3-11 3-22
Comminution 3-12 3-24
Complete Mix Activated Sludge 3-13 3-26
-------
Subj cc t Paragraph Page
Contact Stabilization Activated
Sludge 3-14 3-28
Costs Override 3-15 3-30
Counter Current Amronia Stripping 3-16 3-34
Cross Current Ammonia Stripping 3-17 3-36
Denitrification 3-18 3-38
Drying Beds 3-19 3-42
Dummy Process 3-20 3-44
Equalization 3-21 3-48
Extended Aeration Activated Sludge 3-22 3-50
Facultative Aerated Lagoon 3-23 3-52
Filter Press 3-24 3-54
Filtration 3-25 3-56
Flocculation 3-26 3-62
Flotation 3-27 3-64
Fluidized Bed Incineration 3-28 3-66
Gravity Thickening 3-29 3-68
Grit Removal 3-30 3-70
High Rate Activated Sludge 3-31 3-72
Lagoons 3-32 3-74
Microscreening • 3-33 3-76
Multiple Hearth Incineration 3-34 3-78
Neutralization 3-35 3-80
Nitrification— 3-36 3-82
Overland Flow Land Treatment 3-37 3-86
Oxidation Ditch Activated Sludge 3-38 3-88
Plug Flow Activated Sludge 3-39 3-90
Post Aeration . 3-40 3-92
Pressure Filtration 3-41 3-94
Primary Clarification 3-42 3-96
Primary Clarification (Coagulation) 3-43 3-100
Primary Clarification (Two Stage
Lime Treatment) 3-44 3-104
Pure Oxygen Activated Sludge 3-45 3-108
Rapid Infiltration Land Treatment 3-46 3-110
Recarbonation 3-47 3-112
First Stage Recarbonation 3-48 3-114
Second Stage Recarbonation 3-49 3-116
Screening 3-50 3-118
Secondary Clarification (activated
Sludge) 3-51 3-120
Secondary Clarification (Nitrification/
Denitrification) 3-52 3-122
Secondary Clarification (Trickling
Filter) 3-53 3-124
Slow Infiltration Land Treatment 3-54 3-126
Sludge Flotation 3-55 3-128
Sludge Hauling and Land Filling 3-56 3-130
Step Aeration Activated Sludge 3-57 3-132
Trickling Filtration 3-58 3-134
Vacuum Filtration 3-59 3-136
Wet Oxidation 3-60 3-138
-------
APPENDIX A. BASIC PROCEDURE FOR USING CAPDET
APPENDIX B. EXAMPLE PROBLEM OUTPUT
-------
CHAPTER I
INTRODUCTION
1-1. Purpose. This manual provides guidance for the selection of
wastewater treatment processes and systems, and criteria for the design
of wastewater treatment facilities using^ the Computer Assisted Procedure
for the Design and Evaluation of Wastewater Treatment Systems (CAPDET).
1-2. Applicability. The provisions of this manual are applicable to
Corps of Engineers Districts and Divisions, the U.S. Environmental
Protection Agency, other Federal and State agencies, and private firms
concerned with the design and cost effective analysis of new and upgraded
wastewater treatment facilities for civil and public works and military
construction projects.
1-3. References.
a. EM 1110-2-501, Part 1, Design of Wastewater Treatment Facilities.
b. EM 1110-2-501, Part 2 (Draft), Design of Small Systems Wastewater
Treatment Facilities.
c. EPA-430/9-75-003, Cost of Wastewater Treatment by Land
Application.
d. EPA 430/9-77-013, MCD-37, Construction Costs for Municipal
Wastewater Treatment Plants: 1973-1977.
e. EPA 430/9-77-014, MCD-38, Construction Costs for Municipal
Wastewater Conveyance Systems: 1973-1977.
f. EPA 430/9-77-015, MCD-39, Analysis of Operations & Maintenance
Costs for Municipal Wastewater Treatment Systems.
1-4. Scope.
a. The user's guide contains detailed instruction for coding data
for the CAPDET model. This computer-based design procedure can be used
to select viable process trains to meet a given effluent criteria and will
rank the selected trains according to least annual cost. Cost and design
data are included for 0.3 to 500 million gallons per day (mgd) systems.
b. Available characterization data do not always include all of
the input parameters required for certain processes. Therefore, typical
default data have been included in the program to be used in the absence
of user specified values. The default data provided for each unit process
are average values and may need adjustment to accurately reflect site-
specific or waste-specific conditions.
1-1
-------
c. The program contains a library of unit processes that may be
used to treat a waste stream. Individual unit processes comprising a
waste treatment scheme may be supplied with the appropriate design
parameters pertinent to each process or the default values included in
the program may be used. The program is sufficient in size and flexi-
bility to allow for the processing of up to four general types of
treatment schemes (e.g. physical-chemical, biological, land treatment,
etc.)
d. When a treatment scheme is analyzed, the influent waste stream
is processed in turn by each unit process on the liquid line. The
treatment processes use the effluent of the previous process for their
influent. Those processes producing sludge automatically output the
sludge into one of two sludge lines (primary or secondary). These
sludges may be processed separately or they may be mixed together.
Figure 1-1 presents the organization chart for a treatment scheme.
e. The sequence of analysis for the processes of a waste stream
involves analyzing all of the liquid line processes first, then processing
the secondary sludge line, and finally processing the primary sludge line.
Once the sequence is finished for a given process train, the effluent may
be checked against a preset effluent criteria. Those trains not meeting
the desired effluent specifications are immediately discarded, while
those meeting the desired effluent specifications are ranked in order by
least annual cost. The costs are determined by a separate cost routine
which estimates the capital and operating and maintenance (O&M) costs
for each unit process and performs an average annual cost analysis on
each train over the design life as the basis for economic comparison.
1-2
-------
LIQUID LINE
Liquid
influent
Liquid
Treatment
Process
Liquid
Treatment
Process
Liquid
Treatment
Process
Liquid
Treatment
Process
Liquid
Treatment
SECONDARY SLUDGE LINE
/Sludge
Treatment
Treatment
Treatment
PRIMARY SLUDGE LINE
Treatment
Treatment
Treatment
Liquid
effluent
Figure 1-1. Organization of a Typical Treatment Scheme
-------
CHAPTER 2
MODEL DESCRIPTION
2-1. Definitions.
a. Unit Process. A unit process is a single unique unit or
group of parallel units of the same type. Examples of unit processes
are bar screens, comminutors, grit chambers, contact stabilization
processes, and secondary clarifiers.
b. Treatment Process. A treatment process is a sequence or one
or more unit processes which are automatically linked together by CAPDET.
For example, the preliminary treatment process consists of the unit
processes bar screens, grit chambers, and comminutors linked in sequence.
The contact stabilization treatment process consists of the contact stabi-
lization unit process and a secondary clarifier. The filtration treat-
ment process consist of merely the filtration unit process.
c. Block. A block is a treatment process location. The user of
CAPDET may specify several alternative treatment processes for each treat-
ment process location or block.
d. Scheme. A treatment scheme consists of the blocks on the
liquid line, the secondary sludge line, and the primary sludge line.
e. Train. A train is similar to a scheme except that each block
contains only one treatment process. A scheme may define several possible
trains. CAPDET will automatically produce all trains specified in the
treatment scheme by selecting all combinations of the alternatives in the
blocks.
2-2. Program Organization.
a. This program allows the user to specify various types of unit
processes for the treatment of wastewaters. A treatment process consists
of one or more of these unit processes. The combination of unit processes
into treatment processes is accomplished automatically by the CAPDET
program. Treatment processes may then be assembled in sequence to form
a treatment scheme. A scheme organization chart is shown in Figure 2-1
and a typical scheme is shown in Figure 2-2. A maximum of four treat-
ment schemes may be specified. Each scheme contains a liquid line, a
secondary sludge line, and a primary sludge line. A total of 20 blocks
may be specified in each scheme. Each block may contain up to 10 alterna-
tive treatment processes.
2-1
-------
N3
I
Liquid
Line
Influent
A MIX
LOCATION
Secondary Sludge
PRIMARY SLUDGE ?
B MIX
LOCATION
Secondary Sludge Collection Line
Primary Sludge Collection Line
Sludge Mixing Line
C MIX
LOCATION
Liquid
*- Effluent
Figure 2-1. Scheme organization chart
-------
LI QUID LINE
to
CO
WASTE
INFIULNT
^| PRELWNARY
j TRE*,,IJn
I!'
'I*
FLOTATION
COAGULATION
i i '
( pj ryvViY -J TRICKLING
\ \ \ RLTER
Lf- •
^! NITRIrlCATIOri-
^ DENITR1FICATION
**
CARBON I ^! POST
AOSOSFT10N i " j AERATION
SECONDARY SLUDGE LINE
«*- EFFLUENT
SECOKDARY
5LUDGE FROM,
LIQUID PROCESSES
1. SLUDGE FLOTATION
"L A MIX
1. ANAEROBIC DIGESTION
2. & MIX
3. NULL
PRIMARV SLUDGE LINE
PRIMARY
SLUDGE FROM
LIQUID PROCESSES
1. GRAVITY THICKENING
2. HULL
^J 1. AEROSi: DIGESTION
"^n 2. A,NAERCB:C DIGESTION
2. ORYIXG 8FCS
3. VACUUM FILTRATION
-o- DISPOSAL
Figure 2-2. A typical scheme. This represents one scheme and 576 trains (or
variations) of that scheme. The program will evaluate all 576 trains but will
save only the 100 most cost-effective.
-------
b. A train consists of one treatment process from each block
connected together in the sequence of the blocks. The program examines
all combinations of treatment processes in the series of blocks and de-
termines the cost for each train. The trains are saved in the computer
and ranked according to least equivalent annual cost. If desired, the
user may have the effluent checked against desired effluent characteris-
tics. Those trains not meeting the desired effluent characteristics
will b'e discarded. A maximum of 100 trains will be saved.
c. Two types of output may be obtained. The first output lists
the cost data for up to the 100 most cost-effective trains. The user
may also specify which of these trains (or all if he chooses) he desires
to investigate further. The second output gives detailed unit process
design information for all chosen trains. Optionally, this output may
include the quantities of materials required for construction.
2-3. Input data.
Data for this program consist of seven major divisions.
a. Unit process specifications.
b. Title card.
c. Scheme descriptions.
d. Waste influent characteristics.
e. Desired effluent characteristics.
f. Unit cost data.
g. Program control.
For an outline of program input, the user may refer to the "Basic
Procedure for Using CAPDET" in Appendix A. The following sections out-
line the complete procedure required to describe a proposed treatment
scheme and obtain the desired output from CAPDET.
2~4• Unit Process Specification.
a. The data cards used in the specification of a unit process con-
sist of a key word in the first six columns of the card followed by the
required numeric data in columns 7-80. The numeric data may be placed in
any of the allowed columns but must be in the order shown for that
particular card. No other numeric characters may be placed in columns 7-80.
2-4
-------
For purposes of this description, numeric characters are taken as the
numerals 0-9, the minus sign (-), the plus sign (+), and the decimal
point or period (.)• Any other characters may be used in these columns
to allow the user to identify the data items. Note, however, that the
computer ignores these alpha descriptions and requires a specific order
for the data on a card. The key word (columns 1-6) must appear exactly
as shown on the card description^
b. The specification of a unit process begins with the process
header card which names the process and terminates with an END card.
c. Data may be supplied for three separate modifications of each
unit process. The three modifications are numbered 0, 1, and 2. If the
modificrtion number is omitted on the unit process header card, modifica-
tion 0 will be assumed. Default data have been included in the program
for modification zero. These data may be changed by the user by specify-
ing a unit process header card, data cards for the items the user wishes
to change, and an END card. If the user desires the use of modification 1
or 2 of a unit process, complete data for that modification of the unit
process must be specified. Default data or user specified data must be
available for each of the unit processes which will be used by the
treatment processes specified on the BLOCK cards.
d. The following unit processes may be specified:
Header
Card
Key Word Unit Processes
A SECO Secondary clarification (activated sludge)
AERATE Aerated lagoon
AEROBI Aerobic digestion
ANAERO Anaerobic digestion
ANION Anion exchange
C PRIM Primary clarification (coagulation)
CARBON Carbon adsorption
Q
The input may be in the form of cards or teletype lines. Since a
line is equivalent to a card, the format described also applies to
lines of input.
2-5
-------
Header
Card
Key Word
CASCAD
CATION
CENTRI
CHLORI
COAGUL
COMMIN
COMPLE
CONTAC
COSTS
COUNTE
CROSS
DENITR
DRYING
DUMMY
EQUALI
EXTEND
FACULT
FILTRA
FIRST
FLOCCU
FLOTAT
FLTR P
FLUIDI
Unit Processes
Cascade aeration
Cation exchange
Centrifugation
Chlorination
Coagulation
Comminution
Complete mix activated sludge
Contact stabilization activated sludge
User specified costs for processes
Counter current ammonia stripping
Cross current ammonia stripping
Denitrification
Drying beds
User specified process
Equalization
Extended aeration activated sludge
Facultative aerated lagoon
Filtration
First stage recarbonation (lime treatment)
Flocculation
Flotation
Filter press
Fluidized bed incineration
2-6
-------
Header
Card
Key Word
GRAVIT
GRIT R
HAULIN
HIGH R
L SECO
LAGOON
MICROS
MULTIP
N SECO
NEUTRA
NITRIF
OVERLA
OXIDAT
PLUG F
POST A
PRESSU
PRIMAR
PURE 0
RAPID
RECARB
SCREEN
SECOND
SLOW I
Unit Processes
Gravity thickening
Grit removal
Sludge hauling and land filling
High-rate activated sludge
Secondary clarification (two-step lime clarification)
Lagoons (stabilization ponds)
Microscreening
Multiple hearth incineration
Secondary clarification (nitrification-denitrification)
Neutralization
Nitrification
Overland flow land treatment
Oxidation ditch
Plug flow activated sludge
Post aeration
Pressure filtration
Primary clarification
Pure oxygen activated sludge
Rapid infiltration land treatment
Recarbonation
Screening
Second stage recarbonation (lime treatment)
Slow infiltration land treatment
2-7
-------
Header
Card
Key Word Unit Processes
SLUDGE Sludge flotation
STEP A Step aeration activated sludge
T SECO Secondary clarification (trickling filters)
TRICKL Trickling filtration
VACUUM Vacuum filtration
WET OX Wet oxidation
e. The data cards for each of the unit processes are described in
Chapter 3. An xx.x shown on these cards indicates that a numeric value
must be supplied. The last card for each unit process is an END card.
2-5. Title Card.
a. A title card should be placed after the END card of the last
unit process specification and prior to the LIQUID LINE card of the first
scheme description. This title card allows an identification to be given
at the top of each sheet of output. The card has the word TITLE in the
first five columns followed by the desired description.
b. If the user wishes to completely rely on the default data, he
should begin the data input with a TITLE card, and should not specify
modification numbers on the BLOCK cards.
2-6. Scheme Description.
a. The third major division of input is the desired scheme de-
scriptions. This input begins with the liquid line of the first scheme.
b. Each scheme description must begin with a LIQUID LINE card
and may contain a SECONDARY SLUDGE LINE card and a PRIMARY SLUDGE LINE
card. Inputs immediately following each of these line cardo are
BLOCK cards describing the treatment proc -.ses to be consider- • :'•
that block. As many as 10 treatment procest , - --. v be tried in
block. A total of 20 blocks may be used in ea, \. treatment schemt..
2-8
-------
c. To eliminate the need for the user to continually link
together unit processes that are often used in combination, treat-
ment processes of one or more unit processes have been defined
(e.g. secondary clarification following activated sludge).
d. Treatment processes consist of one or more unit processes
(including the pseudo unit processes such as A MIX, B MIX, C MIX, and
NULL). Only treatment process key words are used on the BLOCK cards.
e. Sludge treatment processes can only be used in conjunction
with the secondary or primary sludge lines. Liquid processes can
be used on the liquid line only. The NULL process can be used on any
line. MIX processes can be used on the secondary sludge line only.
Treatment processes are designated at a particular block by placing
the six-character key word and one-character modification number
describing that process in a position on the block card. The block
card starts with the six-character key word "BLOCK " in columns 1-6,
followed by the first treatment process key word and modification
number in the seven column position beginning in column 11. Sub-
sequent treatment process key words and modification numbers are placed
in succeeding seven character fields.
f. Listed below are the various treatment processes and the
associated key words describing the unit processes which comprise
the treatment process. The first thirteen are sludge treatment pro-
cesses, the last four are pseudo processes, and the others are liquid
treatment processes.
Sludge
Treatment
Process
Key Words
AEROBI
ANAERO
CENTRI
DRYING
FLTR P
FLUIDI
GRAVIT
HAULIN
Treatment Process
Aerobic digestion
Anaerobic digestion
Centrifugation
Drying beds
Filter press
Fluidized bed incineration
Gravity thickening
Hauling and land filling
Key Words
for Associated
Unit Processes
AEROBI
ANAERO
CENTRI
DRYING
FLTR P
FLUIDI
GRAVIT
HAULIN
2-9
-------
Treatment
Process
Key Words
01 , MULTIP
Sludge
PRESSU
SLUDGE
VACUUM
WET OX
Liquid
AERATE
ANION
CARBON
CASCAD
CATION
CHLORI
COAGUL
COMB IN
COMPLE
CONTAC
COUNTE
CROSS
DITCH
DUMMY
EQUALI
EXTDEN
Treatment Process
Multiple hearth incineration
Pressure filtration
Sludge flotation
Vacuum filtration
Wet oxidation
Aerated lagoon
Anion exchange
Carbon adsorption
Cascade aeration
Cation exchange
Chlorination
Coagulation
Combined nitrification-
deuitr if ication
Complete mix activated sludge
Contact stabilization
activated sludge
Counter current ammonia
stripping
Cross current ammonia stripping
Ditch irrigation land treatment
User specified process
Equalization
Extended aeration with
Key Words
for Associated
Unit Processes
MULTIP
PRESSU
SLUDGE
VACUUM
WET OX
AERATE
ANION
CARBON
CASCAD
CATION
CHLORI
COAGUL, C PRIM
NITRIF, N SECO,
DENITR, N SECO
COMPLE, A SECO
CONTAC, A SECO
COUNTE
CROSS
DITCH
DUMMY
EQUALI
EXTDEN, A SECO,
DENITRIFICATION
DENITR, N SECO
2-10
-------
Liquid
Treatment
Process
Key Words
EXTEND
FACULT
FILTRA
FLOOD
FLOTAT
HIGH R
LAGOON
MICROS
NEUTRA
NITRIF
OVERLA
OXIDAT
PLUG F
POST A
PRELIM
PRIMAR
PURE 0
RAPID
RECARB
SPRAY
STEP A
TRANSM
TRICKL
Treatment Process
Extended aeration activated sludge
Facultative aerated lagoon
Filtration
Flood irrigation land treatment
Flotation
High-rate activated sludge
Lagoon
Microscreening
Neutralization
Nitrification
Overland flow land treatment
Oxidation ditch
Plug flow activated sludge
Post aeration
Preliminary treatment
Primary clarification
Pure oxygen activated sludge
Rapid infiltration land treatment
Recarbonation
Spray irrigation land treatment
Step aeration activated sludge
Transmission and pumping
Trickling filtration
2-11
Key Words
for Associated
Unit Processes
EXTEND, A SECO
FACULT
FILTRA
FLOOD
FLOTAT
HIGH R, A SECO
LAGOON
MICROS
NEUTRA
NITRIF, N SECO
OVERLA
OXIDAT, A SECO
PLUG F, A SECO
POST A
GRIT R, SCREEN,
COMMIN
PRIMAR
PURE 0, A SECO
RAPID
RECARB
SPRAY
STEP A, A SECO
TRANSM
TRICKL, T SECO
-------
Treatment
Process
Key Words
Treatment Process
Key Words
for Associated
Unit Processes
Liquid TWO ST Two-stage lime treatment
Pseudo
A MIX Secondary and primary sludge
mixing
B MIX Secondary and primary sludge
mixing
C MIX Secondary and primary sludge
mixing
NULL No process
FLOCCU, L SECO,
FIRST, SECOND
NONE
NONE
NONE
NONE
g. A treatment process of a given modification number consists
of one or more unit processes with the same modification number. For
example, if the user wishes to specify modification 1 of the treatment
process Extended Aeration, he must have supplied data for the associated
unit processes Extended Aeration (EXTEND) and Secondary Clarification
(A SECO).
h. The mixing process, A MIX, B MIX, or C MIX, is used to mix
the secondary sludge line into the primary sludge line before the first,
second, or third block on the primary sludge line, respectively
(fig. 2-1). The presence of a MIX block in a process train will cause
processing of the secondary line to be terminated at that point. The
NULL block is used to allow the option of a "no process" in a block
of the train.
i. A typical treatment scheme was shown in figure 2-2. The data
cards describing that scheme are shown in figure 2-3. Up to four treat-
ment schemes may be described.
2-12
-------
COLUMN 1
LIQUID
BLOCK
BLOCK
BLOCK
BLOCK
BLOCK
BLOCK
BLOCK
BLOCK
BLOCK
o o
S5 53
-O TJ
)g £
11 18 25
LINE
PRELIM
PRIMAR FLOTAT COAGUL
DUMMY
TRICKL
COMBIN
FILTRA
CARBON
POST A
CHLORI
S
•o
2
32
NULL
SECONDARY SLUDGE LINE
BLOCK
BLOCK
BLOCK
PRIMARY
BLOCK
BLOCK
BLOCK
SLUDGE A MIX
ANAERO B MIX NULL
C MIX NULL
SLUDGE LINE
GRAVIT NULL
AEROBI ANAERO
CENTRI DRYING VACUUM
Figure 2-3. Scheme description format
2-7. Waste Influent Characteristics.
a. The fourth major division of input is the waste influent
characteristics. The statement of waste influent characteristics begins
with a header card containing the key word WASTE in the first five
columns. The individual characteristic cards are in the same format as
the Unit Process Specification cards. Numeric data cannot begin before
column 7. The characteristic cards listed below may be used. The better
the characterizations of the waste, the better will be the results of
the model. However, all 20 waste influent specification cards need not
be included in order for the program to operate. NOTE: the waste
characterization data must be given in the units indicated.
2-13
-------
Waste Influent Characteristic Cards
WASTE INFLUENT CHARACTERISTICS
MINIMUM FLOW
AVERAGE FLOW
MAXIMUM FLOW
TEMPERATURE
SUSPENDED SOLIDS
VOLATILE SOLIDS
SETTLEABLE SOLIDS
BOD5
SBOD5 (SOLUBLE)
COD
SCOD (SOLUBLE)
PH
CATIONS
ANIONS
P04 (as P)
TKN (as N)
NH3 (as N)
N02 (as N)
N03 (as N)
OIL AND GREASE
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
MGD
MGD
MGD
DEG CENT
MG/L
% OF SUSPENDED
MG/L
MG/L
MG/L
MG/L
MG/L
MG/L
MG/L
MG/L
MG/L
MG/L
MG/L
MG/L
MG/L
2-14
-------
b. The order of the waste characteristic cards is not important.
c. Default data describing a typical municipal waste have been
included in the program. Waste influent characteristics not specified by
the user will be taken from these default data. The user must specify
the average flow, as no default value is supplied for this data item.
If minimum or maximum flows are not specified, they will be set equal to
the average flow automatically.
d. The data included in the program are shown below:
I^!^™R^, ™ I? DFG CENT
SETTAHLF SOLIDS 15 MG/l
R005 psn MG/I
SHOD SOLUBLE 75 MG/l
COO coo MG/t
SCOD SOLUBLE °00 MG/L
CATIONS Ten MG/l
gN'ONS }gg Kg^t
T^S ^ MG/L
M.J-X •*-• MG/r
wn? 25 MG/'-
N03 °'n MG/L
OIL AND GRFASE fi6°MG/LL
2-15
-------
2-8. Desired Effluent Characteristics.
a. The fifth major division of input data is the statement of
the desired effluent characteristics. Only those characteristics the
user wishes to have checked need be specified in the input. If the
user does not wish to have any effluent characteristics checked, he need
only list the header card.
b. The specification of the individual effluent characteristics
is the same as for .the waste influent and will not be repeated here. The
header card must contain the key word DESIRE in the first six columns and
may be specified as follows:
DESIRED EFFLUENT CHARACTERISTICS
c. The input of desired effluent characteristics is terminated
with the unit cost header card "UNIT COST." This header card must con-
tain the key word UNIT C in the first six columns.
d. There are no default data for the Desired Effluent characteris-
tics included in the program.
2-9. Unit Cost Data.
a. The sixth major division of input data is the unit cost data.
This section begins with the header card "UNIT COST DATA" and ends with
an "END" card. The unit cost data cards which may be specified are
listed below with their associated units.
Unit Cost Data Cards
UNIT COST DATA
BUILDING COST xx.x $/SQ FT
WALL CONCRETE xx.x $/CU YD
SLAB CONCRETE xx.x $/CU YD
EXCAVATION COST xx.x $/CU YD
MARSHALL AND SWIFT INDEX3 xx.x
CRANE RENTAL xx.x $/HR
CANOPY ROOF COST xx.x $/SQ FT
LABOR RATE xx.x $/HR
(Continued)
2-16
-------
Unit Cost Data Cards (Continued)
OPERATOR II LABOR RATE xx.x $/HR
ELECTRICITY COST xx.x $/KWHR
CHEMICALS LIME = xx.x ALUM = xx.x IRON = xx.x
POLYMER = xx.x $/LB
ENGINEERING NEWS RECORD INDEX xx.x
HANDRAIL COST xx.x $/FT
PIPE COST INDEX xx.x INSTALLATION LABOR RATE xx.x $/HR
EIGHT INCH PIPE COSTS PIPE = xx.x $/FT
BEND = xx.x $/UNIT Tee = xx.x $/UNIT VALVE = xx.x $AJNIT
LARGE CITY EPA INDEX
SMALL CITY EPA INDEXb
BLOWERS COSTBS = xx.x
LAND COST
MISCELLANEOUS COST
ADMINISTRATIVE/LEGAL COST
201 PLANNING COST
INSPECTION COST
CONTINGENCY COST
PROFIT AND OVERHEAD COST
TECHNICAL COST
SPECIAL FOUNDATIONS*1
PUMPING (INFLUENT)d
OUTFALL PUMPINGd
xx.x
xx.x
COSTSBM = xx.x COSTSBL = xx.x
xx.x $/ACRE
xx.x PERCENT
xx.x PERCENT
xx.x PERCENT
xx.x PERCENT
xx.x PERCENT
xx.x PERCENT
xx.x PERCENT
(continued)
2-17
-------
Unit Cost Data Cards (Continued)
DIFFUSED OUTFALLd
END
Available from Chemical Engineering magazine.
Use large city or small city index, but not both - default is
First Quarter 1977 Small City EPA Index.
°COSTSBS = Cost of standard 3000 scfm @ 8 psig capacity rotary
positive displacement blower - default value = $16,000.
COSTSBM = Cost of Standard 12,000 scfm @ 8 psig capacity vertically-
split multistage centrifugal blower - default value = $45,000.
COSTSBL = Cost of standard 50,000 scfm @ 8 psig capacity pedestal-
type single-stage centrifugal blower - default value = $300,000.
Optional cards which should be used only when the indicated
facilities are required.
2-18
-------
b. Default data for the unit cost items included in the program
are listed below:
10.1) $/SOFT
LABOR RATE
10
ft. 00
6.00
O.OU
$/LR
ninci COSTS un.o
FXCAi/ATION 1.15
WALL CONCKFTF 300.00
SLAM CONCrvFTF POO. 00
MARSHALL ANil) SWIFT JNOFX <4fH.f>
CIJAMt-1 MENTAL U0.no
CAuOI'Y ROOf
LAiKJK t?ATF
OPFRATOW IT
Fl KCTlUriTY
CHKMICAL COST I IMF 0.0? T/IB Al UM 0
FUMHKFHlrjr, IJM.S PFCORn COST IMHFX
HA/jf) KAIL PS.20 ^/FT
P1PF COST TfJDf-X 241. 0 PIPF INSTALLATION
ridllT INCH PIPF COST PIf'F 7. '41 RFMO 70. 88 TFF
LAKGH CITY KPA IMDFX 13?. 0
'•'ISCFl L/UJf-OS r.ON'COWSTRU COSTS S.O *
ADMIM/LFGAI i.U y
?01 Pl.AU.-JlMG J.5 *
iMSPKCriON 2.0 !«;
COUTIUGMICIFS fl.OO %
PROFIT AMD OVFRMFAO ?2.0 *
TFCumCAL COSTS 2.0 «
LAND COSTS 1000.00 S/ACRF
•s/sn
•5/CII
•S/CII
S/CII
S/HR
IRON o.i a wt.n
FT
YD
YO
Yn
S/HR
t /HR
•»;/KHR
POLYMFR
1.0
PATF 10.0 U/HR
104.
-------
b. Program control cards use the same format as the Unit Process
Specification cards. The following control cards may be used:
CONTROL CARDS
ANALYZE
LIST TOTAL OF XXX TRAINS
OUTPUT QUANTITIES '
PRINT DESIGNS FOR TRAIN NO X, X, X, ... X.
SUMMARY ONLY
GO I = xx.x NY = xx.x
c. The GO card should be the last card included in the data. The
"GO" card is required as it causes the program to begin its execution
phase. The letters GO must appear in columns 1 and 2 of the card with all
other data beginning no sooner than column 7. The sequence of the two
numeric data values must be specified as shown. Both the interest rate
and amortization period must be specified as no default data are provided
for these two values. The data required on the GO card consist of:
I - annual interest rate, percent
NY - amortization period, years
d. All other output control cards are optional. Under the "LIST T"
option, a specified number of trains are listed with capital, O&M, and
equivalent annual costs. The "PRINT" option will provide detailed design
and cost data for each treatment process within each specified train.
Either or both options may be included for each run. The ANALYZE card
causes unit process design data to be printed on the first pass through the
computer in the order in which they are initially processed, i.e., prior
to economic ranking or checking for desired effluent quality. The OUTPUT
QUANTITIES will cause the quantities computed for estimate costing to
be printed. These quantities include such items as volume of excavation,
quantity of reinforced concrete and the annual energy requirement. The
SUMMARY ONLY card will defeat the printing of design data and quantity
output and will allow only the cost summary sheet for each train to be
printed. The cost summaries will be printed only for those trains which
would have had design data printed if this card was not present.
e. Figure 2-4 shows the total input needed to make the program run.
The user should refer to the detailed procedure for data input in
Appendix A.
2-20
-------
-------
2-11. Cost Analysis in the Computerized Design Process.
a. The user through the use of the "GO" control card inputs
the interest rate and design life into the program. These parameters
are described in 2-10c.
b. The annual interest rate is used to amortize the capital cost
and compute the equivalent annual cost to determine the most cost-
effective process train. The design life pertains to the period over
which the design is evaluated for cost-effectiveness.
c. Cost data for the unit processes used in the process train are
stored in the program. These cost data form the basis for an analysis of
the capital, O&M, and equivalent annual costs of the process trains.
d. To allow for unique site-specific problems, the user may elect
to input locally generated costs for some or all unit processes.
These cost data will then override the cost equations or cost estimate
formulations used in the model. The format for the user specified costs
for each process is shown in Chapter 3.
e. The output of the program is generally a listing of the process
trains that meet the desired effluent criteria in order of increasing
average annual cost. The capital, O&M, and equivalent annual costs are
listed for each process train. A more detailed cost analysis of individual
processes in a particular train is available through the "PRINT" control
card.
2-22
-------
CHAPTER 3
UNIT PROCESS SPECIFICATIONS
3-1. a) General. This chapter contains the specific input data for
each unit process. Each line of data that may be included for a partic-
ular unit process is listed along with the proper units. Each line of
data under each unit process in this chapter corresponds to one card or
line of input to the model. It is permissible to interchange whole
lines of data; however, within each line the data must be typed in the
order shown. The unit process name (header card) and the END card must
be the first and last lines or cards for each unit process.
b) Estimate Costing. This is a new approach to planning level
costing. For each process a typical configuration and method of con-
struction has been assumed. Using these assumptions, quantities are
calculated and costs extended by multiplying by unit costs supplied by
the user. This allows the user to update the cost base to his specific
location and to the current year by inputting the current unit prices.
The user requests the use of this costing technique by including an
ESTIMATE card in the input data for each unit process.
c) ESTIMATE Card. The ESTIMATE card which may optionally be
included in the unit process input data specifies that estimate type
costing is to be used for the particular process. In general, the data
on this card will include the cost of one or more 'standard size' items
of equipment. Costs of the required sizes of these items of equipment
will be generated within the program. If the user elects to specify
the costs of these items, he should use the current cost of the standard
size unit. If these costs are omitted from the ESTIMATE card or are
specified as zero, the program will use the-€ss»di quarter 1977 cost
updated by the Marshall and Swift equipment cost index specified in the
unit cost input.
d) Parametric Costing. If Estimate costing is not specified
costs will be computed using parametric equations obtained from various
sources. Where applicable the Dames and Moore equations will be used.
These costs will be updated to the current year using the EPA construc-
tion cost index. Parametric cost equations are not available for all
processes thus some costs will be indicated as zero. For this reason,
extreme care should be used in evaluating costs generated using the
parametric equations.
3-1
-------
(This page left blank intentionally.)
3-2
-------
e) Default Data. Default data have been included within the
program for modification zero of all unit processes included within
CAPDET. Thus, for modification zero of these processes it is necessary
to include data only for those data items the user wishes to change.
To change one or more data items the user should specify a unit process
header card for modification zero of the process followed by data cards
for those items the user wishes to change. An END card will conclude
input of data for that process. The user will have to include an
ESTIMATE card in the input for any process which he changes if he
wishes to retain estimate type costing, as changing any item of data
will revert that process to parametric costing unless otherwise
specified. Estimate costing is the default option if no data are
entered for the process. This default may be defeated and the process
reverted to parametric costing by including a header card and an END
card for the particular process.
NOTE: No data have been included in the program for modifications
one or two of the unit processes. Complete data must be supplied by
the user if he uses either of these modifications.
3-3
-------
3-2. Aerated Lagoon (See page 7-205 of Design Manual).
a. Design Parameters
Eckenfelder's Approach
Reaction rate constant, 0.0007-0.002 £/mg-hr.
Fraction of BOD synthesized, -0.73-
Fraction of BOD oxidized for energy, - 0.52.
K
A
AV
B
B
THETA
ALPHA
BETA
HP
STE
Endogenous respiration rate (oxygen
basis) w 0.075/day.
Endogenous respiration rate (sludge
basis) ~ 0.15/day-
Temperature Coefficient ~ 1.035.
0- transfer in waste/0,, transfer in water,
0- saturation in waste/0™ saturation in
water, -0.9.
Horsepower per 1000 gallons. Horsepower
required to keep solids in suspension
> 0.06 hp/1000 gal.
,0.9.
Standard transfer efficiency.
Mechanical Aerators ~ 2.0-3.5
High Speed =s 2.0
Slow Speed * 3.5
Diffused Aerator « 6.0-11.0%
Coarse bubble x 6.0
Fine bubble -11.0
Ib 02/hp-hr
b. Default Data
ESTIMATE
LINFR 1.00 PFR SO FT
SUMMER TEMPERATURE
CENT
30
fOfJr,TAMTS K = 0.001 A-O.Sn APnn.53 n=0.06 RP=0.1fi
MFCHANICAL Ah K AT I ON ALPHA = 0.9 HETA=0.9 HP=0.01«t HP/TO
=.^.S in 0/HP
3-4
-------
c. Aerated Lagoon Unit Process Data Cards.
AERATED LAGOON MOD xx
SUMMER WATER TEMPERATURE xx.x DEC CENT
WINTER WATER TEMPERATURE xx.x DEC CENT
EFFLUENT SOLUBLE BOD xx.x MG/L
V V
CONSTANTS K=xx.x A=xx.x A =xx.x B =xx.x THETA=xx.x
MECHANICAL AERATION ALPHAa=xx.x BETA=xx.x HP=xx.x HP/TG
STE = xx.x LB 0/HP-HR
DIFFUSED AERATION ALPHA3=xx.x BETA=xx.x AFb=xx.x CFM/TG
STE = xx.x PERCENT
ESTIMATE0 COSTSA=xx.x $
LINER UPILL=xx.x $/SQ FT
END
o
Use mechanical or diffused; not both
AF (minimum air flow) specifies a lower limit on airflow.
Model will calculate actual airflow and compare it with
input value. Higher value will be output. Input zero
for AF to obtain calculated value only.
CCOSTSA = Cost of standard 5-hp aerator - default value = $13,960.
3-5
-------
3-3. Aerobic Digestion (See page 7-277 of Design Manual)
a. Design Parameters
Detention time, days at 20°C
Activated sludge only ~ 12-16 days
Activated sludge from plant without primary
settling x 16-18 days
Primary sludge plus activated or trickling
filter sludge ~ 18-22 days
Detention time should be increased for
temperatures below 20°C
Volatile solids destroyed: 40 percent is common
but it increases with temperature and retention
time from approximately 33 to 70 percent
Mixed Liquor solids ~ 12000 mg/£
Solids in digested sludge x 2.5 percent
ALPHA 0- transfer in waste/00 transfer in water ~ 0.9
«. 2.
BETA 02 saturation in waste/0- saturation in water =0.9
Standard Transfer Efficiency £ 6.0-11.0%
Coarse bubbled. 0
Fine bubble-11.0
b. Default Data
FSTIMATF
DIFFUSED
DFTFHTION TIME
VOLAT1LF SOLIDS HFSTROYFD
TFMPEKATURF
=n.9
15
SO
i?B°°
12.0
20
HAYS
PERCFNT
PFRCFMT
CENT
3-6
-------
c. Aerobic Digestion Unit Process Data Cards
AEROBIC DIGESTION MOD xx
DETENTION TIME
VOLATILE SOLIDS DESTROYED
MIXED LIQUOR SOLIDS
SOLIDS IN DIGESTED SLUDGE
DIFFUSED AERATION3
MECHANICAL AERATION3
CONSTANT ALPHA = xx.x BETA = xx.x
STANDARD TRANSFER EFFICIENCY xx.x
TEMPERATURE xx.x
ESTIMATE*5 SSXSA=xx.x COSTPD=xx.x
END
XX. X
XX. X
XX. X
XX. X
DAYS
PERCENT
MG/L
PERCENT
PERCENT
DEC CENT
COSTPH=ss.s
Use mechanical or diffused; not both.
SSXSA = Cost of standard slow-speed pier-mounted 20-hp
aerator default value = $16,300.
COSTPD = Cost of standard 12.0 scfm coarse-bubble diffuser
default value = $6.50.
COSTPH = Cost of standard 550 scfm swing arm diffuser -
default value = $5,000.
3-7
-------
3-4. Anaerobic Digestion (see page 7-291 of Design Manual)
a. Design Parameters.
Specific gravity ~ 1.05
Percent volatile solids destroyed (See Figure 3-1 provided
below) ~ 40-60 percent
Concentration of solids in digester ~ 3-7 percent
Detention time ~ 15-70 days
U Heat Loss Coefficient ~ 0.18 BTU/hr/ft /°F
b.
10 20 30 40 50 60 70
DETENTION. DAYS. BASED ON RAW SLUDGE FEED
Figure 3-1. Reduction in volatile solids in raw
sludge, for detentions from 15 to 70 days, T=85 to 95°F.
Default Data
SOUTHERN U S
FSTIMATf-
SPFC1F- 1C GRAVITY
PFUCRlT VS DKSTROYFn
CONCENTRATION IN 1HGESTFR
TFMPKRATUKF
OFTFM1ION TIME
OFPTH
COfJSTANT
1.05
50
STF.R=100
PFRCFNT
PFRCFMT
DFG F
DAYS
FT
fUU HP/^OFT/F
3-8
-------
c. Anaerobic Digestion Unit Process Data Cards
ANAEROBIC DIGESTION MOD xx
SPECIFIC GRAVITY xx.x
PERCENT VS DESTROYED xx.x PERCENT
CONCENTRATION IN DIGESTER xx.x PERCENT
TEMPERATURE RAW = xx.x = xx.x Air= XX.X DEC F
DETENTION TIME xx.x DAYS
DEPTH3 xx.x FT
CONSTANT U = xx.x BTU/HR/
SQFT/DEG F
AREAS WALLa = xx.x FLOOR = xx.x Cover xx.x SQFT
SOUTHERN UNITED STATESb
MIDDLE UNITED STATESb
NORTHERN UNITED STATESb
ESTIMATE0 SFLOCO = xx.x CGCUS = xx.x HRHXS = xx.x CGSES = xx.x
CSPUMP = xx.x
END
a
List areas or depths, not both.
Use only one of Southern, Middle, or Northern cards - default
is Southern United States.
SFLOCO = Cost of standard 70-foot diameter floating cover -
default value = $71,000.
CGCUS = Cost of standard 60-foot diameter gas circulation unit -
default value = $32,000.
HRHXS = Cost of standard 1 million Btu/hour heating unit - default
value = $49,000.
CGSES = Cost of standard 2-inch diameter gas safety equipment -
default value = $7,100
CSPUMP = Cost of standard size sludge pump (8- gpm @ 70 feet
of head) - default value = $2,500.
3-9
-------
3-5. Anlon Exchange (see page 6-43 of Design Manual)
a. Design Parameters
Treatment flow rate, 2-5 gpm/ft3
Regenerant flow rate, 1-2 gpm/ft3
Rinsing flow rate, 0.5-1.5 gpm/ft3
Amount of rinse water, 30-120 gal/ft3
Column depth, 24-30 inches minimum
Amount of backwash water, z 100 gal/ft3
Backwash water rate,.:: 15 gpm/ft3
Resin exchange capacity, lb/ft3 (consult manufacturer
specifications)
Regenerant dose, level, concentration, and specific
gravity (consult resin manufacturer specifications)
b. Default Data
FTFUJf-NT f.ONCFMTnATTON ?
WFSIN FXCH/UJbh CAPACITY <4 LH/CFT
HFGFrjf-'iMTL ijnSFzl,? Ln/CFT LFVFI-?.1^ I H/CF-T fOMr = 7.5 PFR
FlOW (-(ATt'S Ti
-------
c. Anion Exchange Unit Process Data Cards
ANION EXCHANGE MOD xx
EFFLUENT CONCENTRATION xx.x
RESIN EXCHANGE CAPACITY xx.x
MG/L
LB/CFT
REGENERANT DOSE = xx.x LB/CFT LEVEL = xx.x LB/CUFT
CONC = xx. x% SG = xx.x
FLOW RATES TREAT = xx.x REGEN = xx.x RINSE = xx.x GPM/CFT
HOURS PER DAY
AMOUNT OF RINSE WATER
COLUMN DEPTH
BACKWASH AMOUNT = xx.x G/CFT
END
xx.x
xx.x
xx.x
RATE = xx.x
HOURS
G/CFT
INCHES
GPM/CFT
3-11
-------
3-6. Carbon Adsorption (see page 6-3 of Design Manual)
a. Design Parameters
Carbon Requirements
Tertiary treatment = 250-350 16/million gal
Secondary treatment ~ 500-1800 16/ciillion gal
2
Hydraulic loading, 4-8 gpm/ft
Contact time, 30-60 min.
2
Backwash rate, 10-15 gpm/ft
Backwash time, ~ 15 min.
Adsorption capacity (from laboratory study)
Rate Constant (from laboratory study)
b. Default Data
300
HYDRAULIC IOAHING f> GPM/SOFT
COMTACT TH'f £*'5 MINtlTFS
BACKWASH RATF= IS fiPM/SOFT TIf/,E= 10 MIN
ADSORPTlOfJ CAPACITY H I R/r
RRFAKHOINF CO^.Ct:NTUATIOM 5 VG/l
PATF COUS1ANT 12
3-12
-------
c. Carbon Adsorption Unit Process Data Cards
CARBON ADSORPTION MOD xx
CARBON REQUIREMENTS xx.x
HYDRAULIC LOADING xx.x
CONTACT TIME xx.x
BACKWASH RATE = xx.x GPM/SQFT TIME = xx.x
ADSORPTION CAPACITY xx.x
BREAKPOINT CONCENTRATION xx.x
RATE CONSTANT xx.x
END
LB/MG
GPM/SQFT
MIN
MIN
LB/CFT
MG/L
3-13
-------
3-7. Cascade Aeration (see page 5-165 of Design Manual)
a. Design Parameters
Free weir indicates a free fall aeration process.
Step weir is a series of free falls. A step weir
reduces the required head as it increases the
oxygen transfer efficiency.
b. Default Data
DISSOLVFD OXYGFN INITIAL. = ?.0 FINAL= S.O M(VL
TFMPEKATUKF 18 OEG CFMT
3-14
-------
c. Cascade Aeration Unit Process Data Cards
CASCADE AERATION MOD xx
DISSOLVED OXYGEN INITIAL = xx.x FINAL = xx.x MG/L
FREE WEIRS3
STEP WEIRS3
TEMPERATURE xx.x DEC CENT
END
3.
Use free or step; not both.
3-15
-------
3-8. Cation Exchange (see page 6-43 of Design Manual)
a. Design Parameters
3
Treatment flow rate, 2-5 gpm/ft
3
Regerierant flow rate, 1-2 gpm/ft
3
Rinsing flow rate, 0.5-1.5 gpm/ft
3
Amount of rinse water, 30-120 gal/ft
Column depth, 24-30 inches minimum
3
Amount of backwash water, « 100 gal/ft
3
Backwash water rate, ~ 15 gpm/ft
Resin exchange capacity, lb/ft (consult manufacturer
specifications)
Regenerant dose, level, concentration, and specific
gravity (consult resin manufacturer
specifications)
b. Default Data
FFFLUFNT CnMCf-MIRATION 2 Mfi/l
RFSlrJ f-'XCMANr-F CAPACITY U LH/fFT
RFbFXERr, if. OOSC = 1?. LB/CFT iFVFL = 7.ri LH/CFT C.Ci'iC-7.^ PFP
FIOW f •
fiV,OU:>il OF RIM.SF WATFR SO G/CFT
COI UMIi nhPTH ?4 INCHFS
BACKWASH AMOUNT-lOO.n G/CFT RATK=10 GPM/CFT
3-16
-------
c. Cation Exchange Unit Process Data Cards
CATION EXCHANGE MOD xx
EFFLUENT CONCENTRATION xx.x MG/L
RESIN EXCHANGE CAPACITY xx.x LB/CFT
REGENERANT DOSE = xx.x LB/CFT Level = xx.x LB/CUFT
CONG = xx.x % SG = xx.x
FLOW RATES TREAT = xx.x REGEN = xx.x
RINSE = xx.x GPM/CFT
HOURS PER DAY xx.x HOURS
AMOUNT OF RINSE WATER xx.x G/CFT
COLUMN DEPTH xx.x INCHES
BACKWASH AMOUNT = xx.x GAL/CUFT RATE= xx.x GPM/CFT
END
3-17
-------
3-9. Centrifugation (see page 5-131 of Design Manual)
a. Design Parameters
Power requirement for centrifuge* 0.5-2.0 hp/gpm
Excess capacity factors^ 1.25
Chemical dosages 10.0% of dry weight of solids
b. Default Data
r&TIMATF
POWER Rf-QUTRFfFNT
HOURS PFR PAY
DAYS PER M'EK
NUMRF.K OF IJMIT5
FXCF^ CAPACITY FACTOR
CHEMICAL OOSt-
1.0
fl
5
2.0
Ifi*'
HP/fiPM
HOURS
HAYS
UfJITS
PERCENT DRY
3-18
-------
c. Centrifugation Unit Process Data Cards
CENTRIFUGATION MOD xx
POWER REQUIREMENT xx.x
HOURS PER DAY xx.x
DAYS PER WEEK xx.x
NUMBER OF UNITS xx.x
EXCESS CAPACITY FACTOR
CHEMICAL DOSE
ESTIMATE3
END
xx.x
xx.x
COSTSC = xx.x
HP/GPM
HOURS
DAYS
UNITS
PERCENT
PERCENT DRY WT
COSTSC = Cost of standard 50-hp centrifuge - default value
$165,000
3-19
-------
3-10. Chlorination (see page 6-35 of Design Manual)
a. Design Parameters
Contact time should not be less than 15 minutes at peak
flow.
Typical chlorine dosages for disinfection and odor con-
trol are shown in Table 3-1.
Table 3-1. Typical Chlorine Dosages for
Disinfection and Odor Control
Dosage Range
Effluent from ,»
Untreated wastewater (prechlorination) 6 to 25
Primary sedimentation 5 to 20
Chemical precipitation plant 2 to 6
Trickling filter plant 3 to 15
Activated sludge plant 2 to 8
Multimedia filter following activated sludge plant 1 to 5
b. Default Data
FCTTMATF 1°° I/TON
tb I 1 ™" I r £ n M TM
CONTACT TIME ?0 WIN
CHLORINE UOSF 10 MS/I
3-20
-------
c. Chlorination Unit Process Data Cards
CHLORINATION MOD xx
CONTACT TIME xx.x MIN
CHLORINE DOSE xx.x MG/L
NUMBER OF TANKS xx
ESTIMATE3 CHLCOST = xx.x $/TON COSTCLE xx.x
END
aCHLCOST = Cost of chlorine - no default value.
COSTCLE = Cost of standard 2000 Ib/day chlorinator default
value = $2,700.
3-21
-------
3-11. Coagulation (see page 6-17 of Design -Manual)
a. Design Parameters
Detention time in rapid mix basin- 1.0-3.0 minutes
Detention time in flocculator~ 15-60 minutes
Coagulant Coagulant Dose (mg/£) Optimum Ph
Lime 200.0 - 500.0 10.0 - 11.0
Alum 50.0 - 100.0 5.0 - 6.5
Iron Salts 100.0 - 250.0 5.0 - 6.5
b. Design Parameters
FSTTMATF
DETENTION TIME RAPID MIX=?.0 FLOCCULATOR=H5 MTN
COAGULANT nOSE 100 MG/I
LIME
3-22
-------
c. Coagulation Unit Process Data Cards
COAGULATION
DETENTION TIME
OPTIMUM PH
COAGULANT DOSE
LIMEb
ALUMb
IRON SALTSb
ESTIMATE0
END
MOD xx
RAPID MIX = xx.x FLOCCULATOR = xx.x MIN
XX. X
XX.X
MG/L
COSTCL - xx.x
User must also specify primary clarification (coagulation).
Use only one of lime, alum, or iron salts cards - default
is lime.
•>
"If estimate costing is requested, pricing will be based on
a combined flocculator and clarifier and separate prices for
the clarifier will not be calculated. With parametric
costing, the costs of both units will be calculated separately.
COSTCL =* Cost of standard 60-foot diameter upflow clarifier -
default value = $110,000.
3-23
-------
3-12. Comminution (see page 5-29 of Design Manual)
a. Default Data
NUMBER OF UNITS 2
3-24
-------
b. Comminution Unit Process Data Cards
COMMINUTION3 MOD xx
NUMBER OF UNITS xx
END
a
This process used with preliminary treatment.
3-25
-------
3~13. £omplete Mix Activated Sludge (see page 7-37 of Design Manual)
a. Design Parameters
Eckenfelder's Approach
Reaction rate constants
k, BOD removal rate constant- 0.0007-0.002 £/mg/hr
a, fraction of BOD synthesized -0.73
V
a , fraction of BOD oxidized for energy - 0.52
b, endogenous rate (oxygen basis) - 0.075/day
b , endogenous rate (sludge basis) x 0.15/day
f, nonbiodegradable fraction of VSS in influent - 0.40
f , degradable fraction of the MLVSS - 0.53
.F/M ratio = 0.3 - 0.6
Mixed liquor suspended solids^ 3000 - 6000 mg/£
Mixed liquor volatile solids^ 2100 - 4200 mg/&
Temperature correction coefficient- 1.0 - 1.04
Effluent BOD soluble ~ 10 mg/i
ALPHA 0_ transfer in waste/0 in water- 0.90
BETA 0« saturation in waste/0- saturation in water- 0.90
>
HP Horsepower per 1000 gallons - 0.10 hp/1000 gal
STE Standard transfer efficiency
Mechanical Aerators^ 2.0-3.5 16 02/hp-hr
High Speed- 2.0
Slow Speeds 3.5
Diffused Aerator- 6.0 - 11.0%
Coarse bubble- 6.0
Fine bubble x 11.0
b. Default Data
CONSTANTS K=0. 00135 A=0.73 AP=0.52 R=0.075 RP=n. J S P=O.U
F/M RATIO 0«5 LR ROH/I R VSS
MIXFt) LIQUOR SS=U500 VS=3150 MG/I
TFMPFKA1URF COFFF I C. IFINT 1.035
AP=0.0
3-26
-------
c. Complete Mix Activated Sludge Unit Process Data Cards
COMPLETE MIX ACTIVATED SLUDGE3 MOD xx
V V
CONSTANTS K = xx.x A = xx.x A = xx.x B = xx.x F = xx.x
V
F = xx.x
F/M RATIO xx.x LB BOD/LB VSS
MIXED LIQUOR SS = xx.x VS = xx.x MG/L
TEMPERATURE COEFFICIENT xx.x
EFFLUENT BOD SOLUBLE xx.x MG/L
MECHANICAL AERATION ALPHAb = xx.x BETA = xx.x HP = xx.x
HP/TG STE = xx.x LB 0/HP-HR
DERATION ALPHAb = xx.x
CFM/TG STE = xx.x PER
DIFFUSED AERATION ALPHAb = xx.x BETA = xx.x AF° = xx.x
ESTIMATE*1 SSXSA = xx.x COSTPD = xx.x COSTPH = xx.x
COSTPS = xx.x
END
Q
User must also specify secondary clarification (activated
sludge).
Use mechanical or diffused, not both.
Q
AF (minimum airflow) specifies a lower limit on airflow.
Model will calculate actual airflow and compare it with
input value. Higher value will be output. Input zero for
AF to obtain calculated value only.
SSXSA = Cost of standard slow-speed pier-mounted 20-hp aerator
default value = $16,300.
COSTPD = Cost of standard 12.0 scfm coarse-bubble diffuser -
default value = $6.50.
COSTPH = Cost of standard 550 scfm swing arm diffuser -
default value = $5,000.
COSTPS = Cost of standard 3000 gpm pump and driver unit -
default value = $17,250.
3-27
-------
a. Design Parameters
Contact Tank Stabilization Tank
Contact time, hrs 0.5 - 1.0 2.0-4.0
Mixed liquor SS, mg/i 2500-3500 4000-8000
Percent volatile ~ 70 percent
Oxygen Required, 1.25 - 1.50 lb 0,,/lb BOD removed/day
Sludge Productions 0.2 - 0.4 lb solids/lb BOD removed/
f , nonbiodegradable fraction of VSS z 0.53
Effluent BOD soluble ~ 10 mg/fc
ALPHA 02 transfer in waste/02 transfer in water ~ 0.90
BETA 02 saturation in waste/0'2 saturation in water ^0.90
HP Horsepower per 1000 gallons > 0.10 hp/1000 gal
STE Standard transfer efficiency
Mechanical Aerators -2.0-3.5 16 0 /hp-hr
High Speeds 2.0 2
Slow Speed- 3.5
Diffused Aerator ~ 6.0 - 11.0%
Coarse bubble^ 6.0
Fine bubble- 11.0
b. Default Data
AFHATION TTMF CONTACT i.o STABILISATION 3 HOURS
MIXFI) LIQUOR SS COUTACT=3UnO STAR IL I7AT I OM=fSnnO MG/I
PFHCt'NT VOI ATILF 70 PFPTFNT
OXYGfl-J KKGIlIKfc'n 1.^5 Lfi O/L » nOn/HAY
SLUDGh P'^OnUClIOM 0.3 LH/I n MOO/DAY
COfJSTANTS FP=0.5
FFFLUHi
-------
c. Contact Stabilization Activated Sludge Unit Process
Cards
CONTACT STABILIZATION ACTIVATED SLUDGE3 MOD xx
AERATION TIME CONTACT = xx.x STAB BASIN = xx.x
MIXED LIQUOR SS CONTACT = xx.x STAB BASIN = xx. x
PERCENT VOLATILE xx.x
OXYGEN REQUIRED xx.x
SLUDGE PRODUCTION xx.x
CONSTANT F = xx.x
EFFLUENT BOD SOLUBLE xx.x
Data
HOURS
MG/L
PERCENT
LB 0/LB
BOD/DAY
LB SOLID/LB
BOD/DAY
FRACTION
MG/L
MECHANICAL AERATION ALPHA = xx.x BETA = xx.x
HP = xx.x HP/TG STE = xx.x LB 0/HP-HR
DIFFUSED AERATION ALPHAb = xx.x BETA = xx.x
AF° = xx.x CFM/TG STE = xx.x PER
ESTIMATEd SSXSA = xx.x COSTPD = xx.x COSTPH = xx.x
COSTPS = xx.x
END
User must also specify secondary clarification (activated
sludge).
Use mechanical or diffused, not both.
Q
AF (minimum airflow) specifies a lower limit on airflow.
Model will calculate actual airflow and compare it with
input value. Higher value will be output. Input zero for
AF to obtain calculated value only.
SSXSA = Cost of standard slow-speed pier-mounted 20-hp
aerator - default value = $16,300.
COSTPD = Cost of standard 12.0 scfm coarse-bubble diffuser
default value = $6.50.
COSTPH = Cost of standard 550 scfm swing arm diffuser -
default value = $5,000.
COSTPS = Cost of standard 3000 gpm pump and driver unit -
default value = $17,250.
3-29
-------
3-15. Costs Overrides
a. To allow for unique site-specific problems, the user may
elect to input locally generated costs for some or all unit processes.
Within the Unit Specification Section, the user has the option to
insert, under the COSTS header card, costs of unit processes for which
the user has more accurate data than that generated by the CAPDET model.
There are four values required for each process. The first item of
data is present day capital cost in dollars, the second item is the
number of operational man-hours per year associated with the process,
the third item is the number of maintenance man-hours per year required,
and the fourth item is the supply cost in present day dollars per year.
b. The COSTS section is loaded with the value -1 in all four
data items. These values are simply space fillers which represent no
cost override options. To override CAPDET cost estimates the user
would substitute the four items for the -1's.
EXAMPLE:
COSTS
AERATED LAGOON -1 -1 -1 1200
AEROBIC DIGESTION 86870 700 400 0
PRIMARY CLARIFICATION 0 000
END
This example shows three unit processes which will use the cost override
option. Only the supply cost is overridden for the lagoon. This might
be done in the cases where electric rates are extremely high. All aerobic
digestion CAPDET values are overridden with actual figures for cost and
man-hours required. In the last process, primary clarification, all
costs are overridden with zeroes. This may be used when studying treat-
ment plant expansion, where it is necessary to evaluate the characteris-
tics of the waste stream through the existing facility but it is
unnecessary to include the existing processes in the system cost evalua-
tion.
3-30
-------
C. Cost Override Data Cards
MAINT
MAN-
COSTS
A SECONDARY CLARIFICATION
(ACTIVATED SLUDGE)
AERATED LAGOON
AEROBIC DIGESTION
ANAEROBIC DIGESTION
ANION EXCHANGE
C PRIMARY CLARIFICATION
(COAGULATION)
CARBON ADSORPTION
CASCADE AERATION
CATION EXCHANGE
CENTRIFUGATION
CHLORINATION
COAGULATION
COMMINUTORS
COMPLETE MIX ACTIVATED SLUDGE
CONTACT STABILIZATION
COUNTER CURRENT AMMONIA
STRIPPING
CROSS CURRENT AMMONIA
STRIPPING
CAPITAL
COST $
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
OPERATION HOURS SUPPLY
MAN-HOURS HR/ COST
HR/YEAR YEAR $/YEAR
XX . X XX . X XX . X
XX . X XX . X XX . X
XX. X XX. X XX. X
XX . X XX . X XX . X
XX . X XX . X XX . X
XX . X XX . X XX . X
XX . X XX . X XX . X
XX . X XX . X XX . X
XX . X XX . X XX . X
XX . X XX . X XX . X
XX . X XX . X XX . X
XX . X XX . X XX . X
XX . X XX . X XX . X
XX . X XX . X XX . X
XX . X XX . X XX . X
XX . X XX . X XX . X
XX . X XX . X XX . X
List only those lines describing the unit process whose cost func-
tions are to be replaced.
If any value is changed in a line all other values must be reset to
-1.0.
3-31
-------
c. Cost Override Data Cards (Continued)
MAINT
MAN-
DENITRIFICATION
DIFFUSED AERATION
DRYING BEDS
DUMMY PROCESS
EQUALIZATION
EXTENDED AERATION ACTIVATED SLUDGE
FACULTATIVE LAGOON
FILTRATION
FIRST-STAGE RECARBONATION
FLOCCULATOR
FLUIDIZED BED INCINERATION
FLOTATION
FLTR PRESS
GRAVITY THICKENING
GRIT REMOVAL & SCREENS & FLOW
MEASUREMENT
HAULING AND LAND FILLING
HIGH RATE ACTIVATED SLUDGE
L CLARIFICATION (LIME TREATMENT)
LAGOONS
MECHANICAL AERATION
MICROSGREENING
MULTIPLE HEARTH INCINERATION
N SECONDARY CLARIFICATION
(NITRIFY-DENITRIFY)
NEUTRALIZATION
NITRIFICATION
OVERLAND FLOW LAND TREATMENT
CAPITAL
COST $
XX. X
XX. X
XX. X
XX. X
xx. x
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
OPERATION
MAN-HOURS
HR/YEAR
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
HOURS
HR/
YEAR
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
SUPPLY
COST
$/YEAR
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
f
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
3-32
-------
c. Cost Override Data Cards (Continued)
MAINT
MAN-
OXIDATION DITCH
PLUG FLOW ACTIVATED SLUDGE
POST AERATION
PRESSURE FILTRATION
PRIMARY CLARIFICATION
PURE OXYGEN ACTIVATED SLUDGE
RAPID INFILTRATION LAND TREATMENT
RECARBONATION
RECYCLE PUMPING (ACTIVATED SLUDGE)
SCREENS
SECOND STAGE RECARBONATION
SLUDGE FLOTATION
SLOW IRRIGATION LAND TREATMENT
STEP AERATION ACTIVATED SLUDGE
T SECONDARY CLARIFICATION
(TRICKLING FILTER)
TRICKLING FILTRATION
VACUUM FILTRATION
WET OXIDATION
CAPITAL
COST $
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
OPERATION
MAN-HOURS
HR/YEAR
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
HOURS
HR/
YEAR
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
SUPPLY
COST
$/YEAR
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
3-33
-------
3-16. Counter Current Ammonia Stripping (see page 6-25 of Design
Manual)
a. Design Parameters
2
Liquid loading rate s 500-1000 Ib water/hr/ft
Gas loading rate = 2-4 times liquid loading rate
(consult manufacturer for packing characteristics)
Lime Dosage ~ 200-500 mg/i
Height of transfer unit (consult manufacturer
specifications)
Ammonia concentration in air at top of tower ~ 0.02-0.05
Desired effluent quality -2.0-8.0 mg/H
b. Default Data
OFSIKKO EFFLUFNT OUALITY
LIQUID LOADlNb KATF
GAS LpAnI.NR RATh.
- TRANSFER
2.0
MG/I
iano
?oo
15
ATR LFAVING TOWFR
MG/L
FEFT
0.03
MG/L
3-34
-------
c. Counter Current Ammonia Stripping Unit Process Data Cards
COUNTER CURRENT AMMONIA STRIPPING MOD xx
DESIRED EFFLUENT QUALITY xx.x HG/L
LIQUID LOADING RATE xx.x LB/HR/SQFT
GAS LOADING RATE xx.x LB/HR/SQFT
LIME DOSE xx.x MG/L
HEIGHT OF TRANSFER UNIT xx.x FT
AMMONIA CONCENTRATION IN AIR TOP OF TOWER xx.x MG/L
END
3-35
-------
3-17. Cross Current Ammonia Stripping (see page-6-25 of Design Manual)
a. Design Parameters
2
Liquid loading rate -500-1000 Ib water/hr/ft
Gas loading rate ~2-4 times liquid loading rate
(consult manufacturer for packing characteristics)
Lime dosage =200-500 mg/£
Height of transfer unit (consult manufacturer
specifications)
Ammonia concentration in air at the top of tower ~
0.02-0.05 mg/£
Desired effluent quality ~ 2.0-8.0 mg/£
b. Default Data
EFrLuruT QUALITY
I OAnlNf, KATF
GAS LOAP.ING PATF
LIMF DO^L
HFIGHT OF TRANSffcR UNIT
f>00
IflOO
200
15
MG/I
I H/MR/c;oFT
MG/I
FT
3-36
-------
c. Cross Current Ammonia Stripping Unit Process Data Cards
CROSS CURRENT AMMONIA STRIPPING
DESIRED EFFLUENT QUALITY
LIQUID LOADING RATE
GAS LOADING RATE
LIME DOSE
HEIGHT OF TRANSFER UNIT
AMMONIA CONCENTRATION IN AIR TOP
OF TOWER
END
MOD xx
XX. X
XX. X
XX.X
XX.X
XX. X
XX.X
MG/L
LB/HR/SQFT
LB/HR/SQFT
MG/L
FT
MG/L
3-37
-------
3-18. Denitrification (see page 7-253) of Design Manual)
a. Design Parameters
Mixed liquor volatile solids ^1200-2000 mg/£
Dissolved oxygen~ 2.0 mg/£
Nitrate loading rate (see Figures 3-2 and 3-3
based on winter temperature and MLVSS)
Efficiency (removal based on pH; see Table 3-2)
Table 3-2. Effect of pK on Denitrification
Condition
Optimum
90% of optimum
50% of optimum
At "6.5 < pH < 7.5
At 6.3 < pH < 6.5
At 7.5 < pH < 7.7
At 5.6 < pH < 6.3
At 7.7 < pH < 8.6
b. Default Data
MIXED LIQUOR VS
WINTER TEMPFRATURF
FFFIC1ENCY
2000
10
90
MG/I
PEG CFNT
,n/TCFT/r>AY
PERCFNT
3-38
-------
c. Denitrification (Biological) Unit Process Data Cards
DENTRIF1CATION3 MOD xx
MIXED LIQUOR VS = xx.x MG/L
WINTER TEMPERATURE xx.x DEC CENT
NITRATE LOADING xx.x LB/TCFT/D
DISSOLVED OXYGEN xx.x MG/L
EFFICIENCY xx.x PERCENT
END
Q
This process used with combined nitrification-denitrification
and can not be used independently.
3-39
-------
180 r—
160 —
3000
2500
MLVSS
10 15 20
TEMPERATURE ; °C
Zb
30
From Mulbarger
Figure 3-2. Permissible denitrification tank loadings.
3-40
-------
TEMPERATURE , C
20 25
From Mulbarger
Figure 3-3. Effect of temperature upon rate of denitrification.
3-41
-------
3-19. Drying Beds (see page 5-149 of Design Manual)
a. Design Parameters
Depth of sludge applied ~8-12 inches
Time to drain~ 1-8 days
Drained solids content after T days- 15-25%
Final solids content =30%
Evaporation rate (available from U.S. Weather Bureau)
Rainfall during wet month (available from U.S. Weather
Bureau)
Correction for evaporation rate for sludge ~0.75
Fraction of rainfall absorbed by sludge ~0.57
b. Default Data
FSTIX.AIF
OFPTH
TIMF TO DRAIN
FINAL SOLInS
DRAIU SOLIDS
FVAPORATION RATE
RAINFALL
CORRECTION FOR EVAPORATION
FRACTION ADSORBED
NUMOEH OF SECTIONS
3
0.75
0.50
12
2 DAYS
50 y,
20 V,
5 IN/MO
IN/MO
3-42
-------
c. Drying Beds Unit Process Data Cards
DRYING BEDS MOD xx
DEPTH APPLIED xx.x INCHES
TIME TO DRAIN xx.x DAYS
DRAINED SOLIDS xx.x PERCENT
FINAL SOLIDS xx.x PERCENT
EVAPORATION RATE xx.x IN/MO.
RAINFALL xx.x IN/MO.
CORRECTION FOR EVAPORATION xx.x
FRACTION ABSORBED xx.x
NUMBER OF SECTIONS xx.x
ESTIMATE3 PIPE COSTS « xx.x xx.x xx.x COSAND = xx.x
COGRVL = xx.x
END
aPipe costs for 4-, 6-, 8-inch perforated clay pipe in place, $/FT
default values are $2.15, $2.75, and $4.25 per foot respectively.
COSAND = Cost of sand in place, $/Cu Yd - default value = $5.90.
COGRVL = Cost of gravel in place, $/Cu YD - default value = $4.30.
3-43
-------
3-20. Dummy Process
a. In certain situations, the user may wish to adjust the waste
characteristics at some point within the train (to simulate
side flows, new processes, etc.). For these cases, the DUMMY
process is available. The DUMMY process is a liquid line
process and is listed on the BLOCK card with the key word
DUMMY. The data cards for the DUMMY process are shown on
the following page. The parameters of flow, temperature,
and pH are set to describe the waste stream at that point
in the train. All other waste characteristic parameters are
modified as percent reductions of that particular parameter
from the value it possessed as influent to the DUMMY process.
The cost data are user input and the data card is of the same
format as the cost override card. The sludge lines can be
modified to indicate sludge production at that point in the
train, by inputting values for volume of sludge, percent
solids of sludge, and volatile portion of the sludge. If the
sludge cards are included, all three values must be present
and in the proper order.
b. The schematic description of a process in CAPDET is shown in
Figure 3-4. Q., C., T., and pH. are waste descriptors which
are either input by the user, it it is at the head of the
plant, or are effluent characteristics generated by the flow
through previous processes. Since for the DUMMY process
there is no standard design and cost formulation within CAPDET,
the user must simulate the effect of the process on the waste
stream. This is done by setting Q., T., pH., sludge volumes,
costs, and describing the C 's as percent reductions of the
3-44
-------
c. Dummy Process Data Cards
DUMMY PROCESS
MINIMUM FLOW
AVERAGE FLOW
MAXIMUM FLOW
TEMPERATURE
SUSPENDED SOLIDS
VOLATILE SOLIDS
BODS
BODS SOLUBLE
COD
COD SOLUBLE
PH
CATIONS
ANIONS
TKN
P04
NH3
SETTLEABLE SOLIDS
OIL AND GREASE
N02
N03
PRIMARY SLUDGE xx.x GAL/DAY xx.x PER SOLIDS xx.x
PER VOLATILE
SECONDARY SLUDGE xx.x GAL/DAY xx.x PER SOLIDS xx.x
PER VOLATILE
COSTS xx.x CAPITAL xx.x OPER MAN HRS xx.x MAINT MAN HRS xx.x
SUPPLY COST
END
3-45
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
MGD
MGD
MGD
DEG
PER RED
PER RED
PER RED
PER RED
PER RED
PER RED
UNITS
PER RED
PER RED
PER RED
PER RED
PER RED
PER RED
PER RED
PER RED
PER RED
-------
(This page left blank intentionally.)
3-46
-------
Q = FLOW
C = CONCENTRATION OF VARIOUS WASTE DESCRIPTORS
T= TEMPERATURE
PH:
DESIGN FACTORS
SIZE
REMOVALS OR CONVERSIONS
SLUDGE PRODUCTION
COSTS
Qe
PH
COSTS
CAPITAL
0 8 M
AVERAGE ANNUAL
SLUDGE, Ib/dcy
Qe
Figure 3-4. A schematic description of a CAPDET unit process
3-47
-------
3-21. Equalization (see page 5-33 of Design Manual)
a. Design Parameters
Detention time (dependent on the fluctuation cycle) -
0.1-0.7 days
Mixing requirements z 0.02-0.04 hp/1000 gal
Air requirements - 5-20 cfm/cubic foot
Oxygen concentration (minimum) in tank - 2.0 mg/£
ALPHA 0 transfer in waste/0 transfer in water- 0.90
BETA 0_ saturation in waste/0_ saturation in water -0.90
STE Standard transfer efficiency
Mechanical Aerators- 2.0-3.5 Ib 0~/hp-hr
High Speed- 2.0
Slow Speeds 3.5
Diffused Aerators 6.0-11.0%
Coarse bubble~6.0
Fine bubble*11.0
b. Default Data
nFTFNTlON TIMF O.S
MIXING (
-------
c. Equalization Unit Process Data Cards
EQUALIZATION MOD xx
DETENTION TIME xx.x
MIXING REQUIREMENTS xx.x
AIR REQUIREMENTS xx.x
ALPHA xx.x
BETA xx.x
STANDARD TRANSFER
EFFICIENCY xx.x
OXYGEN CONCENTRATION
IN TANK xx.x
END
DAYS
HP/TG
CFM/CFT
LB 0/HP-HR
MG/L
3-49
-------
3-22. Extended Aeration Activated Sludge (see page 7-95 of Design
Manual)
a. Design Parameters
Eckenfelder's Approach
Reaction rate constants
k, BOD removal rate constant~0.0007-0.002 £/mg/hr
a, fraction of BOD synthesized~0.73
V
a , fraction of BOD oxidized for energy~0.52
b, endogenous rate (oxygen basis)~0.075/day
y
b , endogenous rate (sludge basis)~0.15/day
f, nonbiodegradable fraction of VSS in influent~0.40
V
f , degradable fraction of the MLVSS-0.53
a , fraction of BODS synthesized to degradable solids^
. ° 0.77a~0.56
F/M ratio^O.05-0.15
Mixed liquor suspended solidss:3000-6000 mg/Jl
Mixed liquor volatile solids=2100-4200 mg/£
Temperature correction coefficients;!.0-1.04
Effluent BOD solublealO mg/£
ALPHA 0- transfer in waste/0_ transfer in water~0.90
BETA 0_ saturation in waste/0_ saturation in water^0.90
HP Horsepower per 1000 gallons >0.10 hp/1000 gal
STE Standard transfer efficiency
Mechanical Aerators~2.0-3.5 Ib 02/hp-hr
High Speeds2..0
Slow Speeds:3.5
Diffused Aerators;6.0-11.0%
Coarse bubble~6.0
Fine bubblesll.O
b. Default Data
„ ,
»P=0..1
3-50
-------
c. Extended Aeration Activated Sludge Unit Process Data Cards
EXTENDED AERATION ACTIVATED SLUDGE3 MOD xx
V V
CONSTANTS K>xx.x A=xx.x A =xx.x B=xx.x B =xx.x F=xx.x
V
F =xx.x A0=xx.x
F/M RATIO xx.x LB BOD/LB VSS
MIXED LIQUOR SS = xx.x VS =xx.x MG/L
TEMPERATURE COEFFICIENT xx.x
EFFLUENT BOD SOLUBLE xx.x MG/L
MECHANICAL AERATION ALPHAb=xx.x BETA=xx.x HP=xx.x HP/TG
STE=xx.x LB 0/HP-HR
JSED AERATION ALPH/
STE=xx.x PERCENT
!ATEd SSXSA =
COSTPS = xx.x
DIFFUSED AERATION ALPHAb=xx.x BETA=xx.x AFC=xx.x CFM
E=s
ESTIMATE01 SSXSA = xx.x COSTPD = xx.x COSTPH = xx.x
END
Q
User must also specify secondary clarification (activated
sludge).
Use mechanical or diffused, not both.
f*
AF (minimum airflow) specifies a lower limit on airflow.
Model will calculate actual airflow and compare it with
input value. Higher value will be output. Input zero
for AF to obtain calculated value only.
SSXSA -• Cost of standard slow-speed pier-mounted 20-hp aerator-
default value = $16,300.
COSTPD = Cost of standard 12.0 scfm coarse-bubble diffuser-
default value = $6.50.
COSTPH = Cost of standard 550 scfm swing arm diffuser-default
value. = $5,000.
COSTPS = Cost of standard 3000 gpm pump and driver unit -
default value = $17,250.
3-51
-------
3-23. Faculative Aerated Lagoon (see page 7-223 of Design Manual)
a. Design Parameters
K, reaction rate constant~0.5-1.0 per day (avg 0.75)
V
a , fraction of BOD oxidized for energy^O.90-1.40
THETA, temperature correction coefficients!.075
Effluent soluble BOD~10 rng/£
Suspended solids in effluent^50-150 mg/£
ALPHA 02 transfer in waste/0, in water=0.90
BETA 0- saturation in waste/0 saturation in watersO.90
HP Horsepower per 1000 gallons>0.10 hp/1000 gal
STE Standard transfer efficiency
Mechanical Aerators=2.0-3.5 Ib 02/hp-hr
High speeds2.0
Slow speed~3.5
Diffused Aerator~6.0-11.0%
Coarse bubble~6.0
Fine bubble-11.0
b. Default Data
SUM^FR ThVPfRATURF 3Q TFMT
V.'I.-JTKK TEMPM?ATURF 10 rFMT
FFFH»:NT SOLOHLE nnn .TO MG/I
CO.-JSTAMTS K = '),S AP=1.? THFrA = l.,T7S
^U^PF.hDFO SOI.IDS IN FFFI UFMT t^O MG/I
VFCHANICAL AKKATIOW ALHHA=n.g flFTA=0.9 HP=n.01 MP/TR STFr.^.5 LR O/HP HR
3-52
-------
c. Facultative Aerated Lagoon Unit Process Data Cards
FACULTATIVE AERATED LAGOON MOD xx
SUMMER TEMPERATURE xx.x DEC CENT
WINTER TEMPERATURE xx.x DEC CENT
EFFLUENT SOLUBLE BOD xx.x MC/L
CONSTANTS K = xx.x A = xx.x THETA = xx.x
SUSPENDED SOLIDS IN EFFLUENT xx.x MG/L
SCHANICAL AERATION ALI
STE=xx.x LB 0/HP-HR
MECHANICAL AERATION ALPHAa=xx.x BETA=xx.x HP=xx.x KP/TG
DIFFUSED AERATION ALPHA3=xx.x BETA=xx.x AFb=xx.x CFM/TC
STE=xx.x PERCENT
END
o
Use mechanical or diffused, not both.
AF (minimum airflow) specifies a lower limit on airflow.
Model will calculate actual airflow and compare it with
input value. Higher value will be output. Input zero for
AF to obtain calculated value only.
3-53
-------
3-24. Filter Press
a. Design Parameters
Cake solids contents35-50%
Density of cake (see Table 3-3 for typical specific
gravities)
Chamber volume (see manufacturer specifications) ~
1.0-2.0 ft3
Hours operation per day~8-16 hours
Cycle time of filter~2.0 hours
Table 3-3. Normal Quantities of Sludge Produced by
Treatment Processes
Different
Wastewater Treatment Process
Primary sedimentation
Undigested
Digested in separate tanks
Trickling filter
Chemical precipitation
Primary sedimentation and
activated sludge
Undigested
Digested in separate tanks
Activated sludge
Waste sludge
Septic tanks, digested
Imhoff tanks, digested
Gallons
Sludge/
mg
Treated
2,950
1,450
745
5,120
6,900
2,700
19,400
900
500
Solids
Percent
5.0
6.0
7.5
7.5
4.0
6.0
1.5
10.0
15.0
Sludge
Specific
Gravity
1.02
1.03
1.025
1.03
1.02
1.03
1.005
1.04
1.04
b. Default Data
CAKF SOLirK CONTENT
DFNSITY OF CAKE
CHAMBf-.R VOI UUH
HOURS OF OPERATION
CYCLE TIME
U5.0 PFRCFNT
65.0 LK/CIIFT
2.0 CUFT
8.0 HOURS
2.0 HOURS
3-54
-------
c. Filter Press Unit Process Data Cards
FLTR PRESSa MOD XX
CAKE SOLIDS CONTENT xx.x
DENSITY OF CAKE xx.x
CHAMBER VOLUME xx.x
HOURS OPERATION PER DAY xx.x
CYCLE TIME xx.x
END
PERCENT
LB/CUFT
CUFT
HRS
HRS
The user must spell the process name 'FLTR' agSsg^ftS as
shown to insure the proper input for the Filter Press process.
3-55
-------
3-25. Filtration (see page 5-93 of Design Manual)
Design Parameters (for general design characteristics
see Table 3-4)
Filter media characteristics (see Table 3-5)
Loading rate, dual mediae-ID gpm/ft^; multi mediae 2-12
gpm/ft2
K, coefficient of permeability- 6
FOR, porosity~0.50 for anthracite and= 0.40 for sand
DIA, particle diameter or effective size (Table 3-5)
SF, shape factor=6.0 for spherical or 8.5 for crushed
granules
SG, specific gravity =1.67 for anthracite or 2.65 for sand
Sixty percent finer size of ^he sand- 0.75 mm
Density of water =62.4 Ib/ft
Viscosity of water =1.009 centipoises
Porosity of unexpanded beds; 0.40
b. Default Data
(FOlLOW WITH
01 A = 0.00?0
DJ A-n.ooio
ESTIMATE
LOADING RATE
APPROACH Vri OCITY
LAYFRS NUN'RFR = 4
n=i.ou x=6 poi<=o.sn
n=i.oo K=5 POR=O.HO
1)1! K-H POR = (J,U7
1 . (JO K~(i POt'^0 . 60
XTY Pr'RCTNT FINER SI7F
SPEC 11- ic 'Aric.Hr OF SAND
nruSITY OF IvATFR
KT^f-'-iAS'IC VISCOSITY (PGM WILL
POROSITY OP RED
FXPA;-Ji;F(> DEPTH
KkJMRl-Rj Of TI^OUGHS
s
?_ G/M/SnFT
0.005 FT/SFC
OfJE CARD r>ER I AYFR TOP TO "uT
:7.0 SG=1,UO (ANTHRACITES)
:n.S SG-P.GS (SAMO)
:.H.O SG^'^.fi^ (GARUFT '
:fi.O SG-6.00 (GRAVEL)
(1.75 MM
16ci.<4 t B/CFT
L'lM/CUFT
UNLESS V;M UF SPECIFIED)
COMPUTE
0.4
5
50
WIDTH OF TROUGHS i
UNDFRORAli1] OFPTH 1
HFAD LOSS IN uwnt'pnRAiN i
OPFRATIN3 OFPril OF WATFR AROVF. SAND
HFIGHT OF TROUGH FROM UNDF.RORAIN (S.5
RAGK.VAStl TTMF. 10
FHFFHOARD I
ARSOLUTE VISCOSITY OF WATER 1.00B7
FEFT
THOUGH*;
FEET
FEET
FEET
3 FEET
FEET
MINUTED
FEET
CENTtPOTSES
3-56
-------
c. Filtration Unit Process Data Cards
FILTRATION MOD xx
LOADING RATE xx.x
APPROACH VELOCITY xx.x
LAYERS3 NUMBER = xx.x (follow with one
bottom) D=xx.x FT K=xx.x POR=xx.x
FT SF=xx.x SG=xx.x
SIXTY PERCENT FINER SIZE xx.x
SPECIFIC WEIGHT OF SAND xx.x
DENSITY OF WATER xx.x
KINEMATIC VISCOSITY (may
be specified or will
be calculated if left
blank) xx.x
POROSITY OF BED xx.x
EXPANDED DEPTH xx.x
NUMBER OF TROUGHS xx.x
WIDTH OF TROUGHS xx.x
UNDERDRAIN DEPTH xx.x
HEAD LOSS IN UNDERDRAIN xx.x
OPERATING DEPTH OF WATER
ABOVE SAND xx.x
HEIGHT OF TROUGH FROM
UNDERDRAIN xx.x
BACKWASH TIME xx.x
FREEBOARD xx.x
ABSOLUTE VISCOSITY OF WATER xx.x
ESTIMATE13 COSF = xx.x COSTPS = xx.x
END
G/MSQFT
FT/SEC
card/layer top to
DIA=xx.x
MM
LB/CFT
LBS/CFT
SQFT/SEC
FT
FT
FT
FT
FT
FT
MIN
FT
CENTIPOISES
The "LAYERS" card must be followed immediately with one card
per layer in the order of top to bottom. These cards have no
key word. They must contain the depth (ft), permeability,
porosity, mean diameter (ft), shape factor, and specific gravity
for the layers in the order shown.
3COSF=Cost of standard 784 square ft filter unit-default value=
$165,000.
COSTPS=Cost of standard 3000 gpm pump and driver unit-default
value=$17,250.
3-57
-------
Table 3-4. General Features of Construction and Operation of
Conventional Slow and Rapid Sand Filters
Feature
Slow Sand Filters
Rate of filtration 1 to 3 to 10 mgad
Size of bed
Large, half acre
Depth of bed
12 in. of gravel; 42 in.
of sand, usually reduced
to no less than 24 in. by
scraping
Rapid Sand Filters
100 to 125 cc 300 mgad
"SmallTT/lOOto 1/10 acre"
18 in. of gravel; 30 in.
of sand or less; not re-
duced by washing
Size of sand
Effective size 0.25 to
0.3 to 0.35 mm; co-
efficient of nonuniform-
ity 2 to 2.5 to 3
0.45 mm and higher; co-
efficient of nonuniformity
1.5 and lower, depending
on uriderdrainage system
Grain size distri- Unstratified
bution of sand in
filter
Stratified with smallest
or lightest grains at top
and coursest or heaviest
at bottom
Underdrainage
system
Split tile laterals laid
in coarse stone and dis-
charging into tile or
concrete main drains
(1) Perforated pipe lat-
erals discharging into
pipe mains; (2) porous plates
above inlet box; (3) porous
blocks with included
channels
Loss of head
0.2 ft initial to 4
final
ft 1 ft initial to 8 or 9 ft
final
Length of run be-
tween cleanings
20 to 30 to 60 days
12 to 24 hr
Penetration of sus- Superficial
pended matter
Deep
Method of cleaning
(1) Scraping off surface
layer of sand and washing
and storing cleaned sand
for periodic resanding of
bed; (2) washing surface
sand and sand in place by
washer traveling over
sand bed
Dislodging and removing sus-
pended matter by upward flow
or back-washing, which
fluidizes the bed. Possible
use of water or air jets, or
mechanical rakes to improve
scour
0.2 to 0.6 percent of
water filtered
Amount of wash
water used in
cleaning sand
1 to 4 to 6 percent of water
'filtered
(Continued)
3-58
-------
Table 3-4. General Features of Construction and Operation of
Conventional Slow and Rapid Sand Filters (Concluded)
Feature
Slow Sand Filters
Preparatory treatment Generally none
of water
Rapid Sand Filters
Coagulation, floccula-
tion, and sedimentation
Supplementary treat- Chlorination
ment of water
Chlorination
Cost of construction, Relatively high
U.S.
Relatively low
Cost of operation
Relatively low where sand Relatively high
is cleaned in place
Depreciation cost
Relatively low
Relatively high
From Fair, Geyer, and Okun, 1958
3-59
-------
(This page left blank intentionally.)
3-60
-------
Table 3-5. Typical Design Data for Dual-Media and Multimedia
Filters
Value
Characteristic
Anthracite
Depth, in.
Effective size, mm
Uniformity coefficient
Sand
Depth, in.
Effective size, mm
Uniformity coefficient
2
Filtration rate, gpm/ft
Dual-Media
Range
8 to 24
0.8 to 2.0
1.4 to 1.8
10 to 24
0.3 to 0.8
1.2 to 1.6
2 to 10
Typical
18.0
1.2
1.5
12.0
0.5
1.4
6.0
Multimedia
Anthracite
Depth, in.
Effective size, mm
Uniformity coefficient
Sand
Depth, in.
Effective size, mm
Uniformity coefficient
*a
Garnet
Depth, in.
Effective size, mm
Uniformity coefficient
2
Filtration rate, gpm/ft
8 to 20
1.0 to 2.0
1.4 to 1.8
8 to 16
0.4 to 0.8
1.2 to 1.6
2 to 4
0.2 to 0.6
2 to 12
15.0
1.4
1.5
12.0
0.6
1.4
3.0
0.3
1.0
6.0
Garnet becomes intermixed with sand and anthracite.
From Metcalf and Eddy, 1972
3-61
-------
3-26. Flocculation (see page 6-17 of Design Manual)
a. Design Parameters
Lime dosage (determine from jar test)=200-500 mg/£
Optimum Ph (determine from jar test)~10-ll
Detention time for flash mix .basin~ 1.0 - 3.0 minutes
Detention time for flocculator basin^ 15.0 - 60.0 minutes
b. Default Data
L IMF nor>F.-ioo MG/L
OFTENTION TIMF FLASH MIX=3 FLOCCULATOR-U5 MTN
OPTIMUM PH 10.5
3-62
-------
c. Flocculation Unit Process Data Cards
FLOCCULATION MOD xx
LIME DOSE xxx MG/L
DETENTION TIME FLASH MIX xxx FLOCCULATOR xxx MIN
OPTIMUM PH xxx
END
3-63
-------
3-27. Flotation (see page 5-41 of Design Manual)
a. Design Parameters
Air pressure- 40-70 psig
Detention time in float tank- 0.25-0.5 hrs
Solid loading (determine from laboratory tests)
Hydraulic loading- 1.0-4.0 gal/min/ft
Recycle time in pressure tanks: 1.0-3.0 min
Percent removal of solids (determine from bench test)- 80.0
Air/solids ratio (determine from laboratory test)
Float concentration (determine from bench test)- 5.0%
Removal of BOD (determine from bench test)
Removal of COD (determine from bench test)
Removal of TKN (determine from bench test)
b. Default Data
ESTIMATE
AIR PRESSURE 40
DETENTION TIME IN FLOAT TANK 0.5
SOLID LOADING 15
HYDRAULIC I OAOING 3.5
RECYCLE TlMf- IN PRFSS TANK 3.0
PERCENT REf.'OVAL OF SOLIDS fl5
AIK/bULlQS RATIO 0.02
FLOAT CONCENTRATION 3
REMOVAL
R00=30 C00=30 TKN=10
PS it;
MRS
Lli/SOFT/DAY
GPM/SOFT
MIN
PERCENT
PERCENT
PERCENT
3-64
-------
c. Flotation Unit Process Data Cards
FLOTATION MOD xx
AIR PRESSURE3 xx.x
DETENTION TIME IN
FLOAT TANK xx.x
SOLID LOADING xx.x
HYDRAULIC LOADING xx.x
RECYCLE TIME IN PRESS
TANKa xx.x
PERCENT REMOVAL OF
SOLIDS xx.x
AIR/SOLIDS RATIO xx.x
FLOAT CONCENTRATION xx.x
REMOVAL BOD = xx.x COD = xx.x TKN = xx.x
b
PSIG
HRS
LB/SQFT/DAY
GPM/SQFT
MIN
PERCENT
PERCENT
PERCENT
Estimate
END
COSTFS
xx.x
Use with recycle only.
"*COSTFS = Cost of standard 350 square foot air flotation
unit - default value = $44,200
3-65
-------
3-28, Fluiclised _Bed Incineration (see page 5rl89 of Design Manual)
a. Design Parameters
Sludge analysis (determine from bench tests)
Carbon content ~ 43.6%
Hydrogen content x 6.4%
Oxygen content x 33.4%
Sulfur content x 0.3%
Fuel analysis (use reported values for desired fuel;
typical values for fuel oil are provided)
Carbon content * 87.3%
Hydrogen content x 12.6%
Oxygen content x 0.0%
Sulfur content x 1.0%
Heat value of fuel (use reported value for desired fuel),
for fuel oil =18,000 BTU/lb
Operating temperature of preheater unit -1000-1200 F
Sand to sludge ratio x 3.0-8.0
Detention time ~ 10.0-60.0 sec
Default Data
HOI IMS PFK HAY B HOURS
SA . . . .
ri,K ANMYsIS CrR7.3 H-12.6 0-0.0 5-1.0
MFAr V.M UF OF FUFI lfin9S-,nT^?rrc r
Oi^RATlMG TE--VPFHAT1IRE 1000 nFMFFS F
AV.Hhrn TCf-'!'FHATU«F JS nt Wjp ', F
SAr-n TO SLUiJGi" FJATIO 6 ; l?nLP,
-------
c. Fluid ^ze,. L'-H! T-icineration Unit Process Data Cards
FLUID; mi BED INCINERATION
C: P?.R j)A'7
MOD
xx. X
=xx . x
jj, .-1 f< ' *V"Y "V
f I A,».SJ.I.\. .AA • A.
,.\:-!>.' C=x>:,x H-xx.x 0-xx.x S=xx.x
,Y">':•'." C-xx,x IJ-'xx.x 0=xx.x
HE.AT -'\LI:E OF FUEL xx.x
s^i:, ';'•'•. .,;u£.oi. RATIO
spi-<;u'c wEi'-'ir OP SAND
DECLNTIOJ I IMF
ELECTRi'C POWER COST
E'-rrj.vTF,' cosiri - xx.x
iTN'D
XX. X
XX. X
XX. X
"C "-•- Carbon content.
L - L;'c::r£cn content
0 -- '"xypB'i content
'j S-i.l fur concent
PERCENT
PERCENT
BTU/LB
DEC F
DiTG F
l.B/CUFT
SECONDS
D07.LARS/KWHR
OJS'''"T. -- COK*. if standard 15-foot diameter incinerator
dffc.u'c ',-ilue - ^>1,100,000.
3-67
-------
3-29. Gravity Thickening (see page 5-57 of Design Manual)
a. Design Parameters
Underflow concentration (determine from bench test)
Mass loading rate (See Table 3-6.)
Settling velocity (determine from lab test with results
similar to Figure 3.5)
Initial height (determine from lab test with results
similar to Figure 3.5)
Intercept (determine from lab test with results similar
to Figure 3.5)
Table 3-6. Concentrations of Unthickened anrl Thickened
Sludges and Solids Loading for Mechanical Thickeners
Type of Sludgy
SJudgo, Solid, Percent.
Unthickenrd 'Jli icl.ened
Solid*
Loading for
Mechanical
Thickeners
Separate sludges
Primary
Trickling fil Lei-
Modi Tied aeration
Act ivated
Combined Kludges
1'riniary and trick] in;; filter
Primary and modified aeration
Primary and activated
2.5 to 5.5
4.0 to 7.0
2.0 to 4.0
0.5 to 1.2
8.0 to 10.0
7.0 to 9.0
A. 3 to 7.9
2.5 to 3.3
20 to 30
8 to 10
7 to 18
4 to 18
3.0 to f,.0
3.0 to 4.0
2.6 to 4.8
7.0to 9.0
8.3 to 11. f>
4.6 to 9.0
12 to 20
12 to 20
8 to 16
Figure 3-5. Typical settling curve from laboratory test.
b. Default Data
UUnFiifl-Od CONCENTRATION
MASS LUADlNjG
NinnLr« OF TAMKS
Jo
9
PF.KCFNT
I H/s-QFT/OAY
FFFT
3-68
-------
c. Gravity Thickening Unit Process Data Cards
GRAVITY THICKENING MOD xx
UNDERFLOW CONCENTRATION xx.x PERCENT
MASS LOADING3 xx.x LB/SQFT/DAY
DEPTH xx.x FT
NUMBER OF TANKS xx
SETTLING VELOCITY3 xx.x FT/DAY
INITIAL HEIGHT3 xx.x FT
INTERCEPT3 xx.x FT
ESTIMATED3 COSTTS = xx.x
END
o
List either mass loading or the three parameters: settling,
velocity, initial height, and intercept; not both.
COSTTS = Cost of standard 90-foot diameter thickener-default
value = $82,500.
3-69
-------
3-30. Grit Removal (see page 5-3 of Design Manual)
a. Design Parameters
Specific gravity of particles -2.65
Particle size (see Table 3-7)
Table 3-7. Grit Settling Velocities
Particle Size
Settling Velocity
Area Required
Mesh
18
20
35
48, ,
65 (a>
100
150
mm
0.833
0.595
0.417
0.295
1 0.208
0.147
0.105
ft/min
14.7
10.5
7.4
5.2
3.7
2.6
1.8
gpd/ft^
160,000
114,500
80,100
56,700
40,000
28,200
20,200
mgd/ft/
0.1600
0.1145
0.0801
0.0567
0.0400
0.0282
0.0202
ft^/million gal
6.3
8.7
12.5
17.7
25.0
35.5
49.5
(a)
From Metcalf and Eddy, 1972
Minimum particle size desirable for removal.
Depth- 1.0 foot
Current allowance -1.70
Manning coefficient ^0.03
Aerated grit chamber design parameters
Air supply - 3 cfm/ft of tank length
Air diffusers - located 2 to 3 ft above tank bottom on
one side of tank
Surface velocity - 1.5 to 2 fps
Tank floor velocity - 1 to 1.5 fps
Grit collectors - air lift pumps to decanting channels,
grit conveyors or grit pumps
Detention time - 2 to 3 min
Efficiency - 100% removal of 65-mesh grit
From Metcalf and Eddy, 1972
b. Default Data
FSTIMATF
PAHT1CLF r-T7F
SPFCIFIC GRAVITY
HORIZONTAL FLOW
Of-" UNITS
DFPTH
"
VOl UMf-
AU O-JANCF:
COFf-'F ICIP.NT
OF C,RIT
0.2
VAVF.-i.nn
I FT
1.7
0.035
H CFT/VG
3-70
-------
Grit Removal Unit Process Data Cards
GRIT REMOVALa MOD xx
PARTICLE SIZE xx.x MM
SPECIFIC GRAVITY xx.x
HORIZONTAL FLOWb VMAX=xx.x VAVG=xx.x FPS
AERATEDb VMAX=xx.x VAVG=xx.x FPX
NUMBER OF UNITS xx.x
DEPTH0 xx.x FT
WIDTH0 xx.x FT
CURRENT ALLOWANCE xx.x
MANNING COEFFICIENT xx.x
VOLUME OF GRIT xx.x CFT/MG
DETENTION TIMEd xx.x MIN
AIR SUPPLYd xx.x CFM/FT
ESTIMATE6
END
a
This process is part of preliminary treatment.
Use horizontal flow or aerated, not both.
CUse depth or width card, not both.
Use with aerated flow only.
eThe ESTIMATE card in Grit Removal specifies estimate pricing
for Preliminary Treatment which includes Grit Removal,
Comminutors, and Bar Screens.
3-71
-------
3-31. High-rate Activated Sludge (see page 7-129 of Design Manual)
a. Design Parameters
Eckenf elder ' s Approach
Reaction rate constants
a, fraction of BOD synthesized -0.73
V
a , fraction of BOD oxidized for energy =0.52
b, endogenous rate (oxygen basis) ~0.075/day
V
b , endogenous rate (sludge basis) ~0.15/day
f, nonbiodegradable fraction of VSS in influent -0.40
V
f , degradable fraction of the MLVSS -0.53
F/M ratio =1.5 - 5.0
Mixed liquor suspended solids -200 - 1000 mg/£
Mixed liquor volatile solids -140 - 700 mg/£
Temperature correction coefficient -1.0 - 1.04
Effluent BOD soluble =10
ALPHA 0^ transfer in waste/0? transfer in water =0.90
BETA 09 saturation in waste/0,, saturation in water =0.90
HP Horsepower per 1000 gallons >0.10 hp/1000 gal
STE Standard transfer efficiency
Mechanical Aerators =2.0-3.5 Ib 0 /hp-hr
High speed =2.0
Slow speed s;3.5
DIFFUSED AERATOR =6.0 - 11.0%
Coarse bubble -6.0
Fine bubble =11.0
b. Default Data
A=0.7 AP=0.53 n=0.07nOn VS=4SOO MG/L
TFMPLKATUHF COKF;" 1C (ENT I,',035 wr /i
G «;TE=12 PFRCFMT
3-72
-------
c. High Rate Activated Sludge Unit Process Data Cards
HIGH RATE ACTIVATED SLUDGEa MOD xx
V V V
CONSTANTS A=xx.x A =xx.x B=xx.x B =xx.x F=xx.x F =xx.x
F/M RATIO xx.x LB BOD/LB VSS
MIXED LIQUOR SS=xx.x VS=xx.x MG/L
TEMPERATURE COEFFICIENT xx.x
EFFLUENT BOD SOLUBLE xx.x MG/L
MECHANICAL AERATION ALPHAb=xx.x BETA=xx.x HP=xx.x HP/TG
STE=xx.x LB 0/HP-HR
DIFFUSED AERATION ALPHAb=xx.x BETA=xx.x AFC=xx.x CFN/TG
STE=xx.x PER
ESTIMATEd SSXSA=xx.x COSTPD-xx.x COSTPH=xx.x COSTPS=ss.s
END
User must also specify secondary clarification (activated sludge),
Use mechanical or diffused, not both.
£
AF (minimum airflow) specifies a lower limit on airflow. Model
will calculate actual airflow and compare it with input value.
Higher value will be output. Input zero for AF to obtain
calculated value only.
SSXSA - Cost of standard slow-speed pier-mounted 20-hp aerator -
default value = $16,300.
COSTPD = Cost of standard 12.0 scfm coarse-bubble diffuser -
default value = $6.50.
COSTPH = Cost of standard 550 scfm swing arm diffuser - default
value = $5,000.
COSTPS = Cost of standard 3000 gpm pump and driver unit - default
value = $17,250.
3-73
-------
3-32. _Lagoons_(sec page 7-307 of Design Manual)
a. Design Parameters (see Table 3-8)
Table 3-8. Design Parameters for Stabilization ;v..ds.
Parameter
2Mov regime
Fond size, acres
Operation
Detention time, days
Depth, ft
?H
Temperature range, °C
Optlnwn temperature, °C
BOlij. loadings Ib/acre/day
BOD,- conversion
2
Principal conversion products
Algal concentration, mg/t
Effluent suspended solids,
Aerobic '
Intermittently mixed
<10 Multiples
Series or parallf-1
10 to 1)0
3 to h
6.5 to 10.5
0 to ItC
20
CO to lCo'd)
60 to 70
Algae, CO?, bacterial
cell tis-.-ue
80 tu 200
lUo to 3:>0
Type of Pom!
Facult at i vc Ftx~ 'il t at i ve
MixeJ r.urfa-.'e layer
2 to 10 multiples 2 to 10 nnltiy-les
Series or parallel Cc-rj t-s cr ^tirtil^ei
7 to 30 Y to f.
3 to 6 3 to 6
6.5 to 9.0 6,!i to 8.1)
0 to 50 0 to i..C
20 "0
15 to 50 20 :c< ,-',0
60 t,o 70 6r; t ;» "','
Algae, COg, CH^, CO,.,.. -:K;, , -. -'',•. -I .:
bactet'ial cell r^'M i. : •• v '
tissue
kQ to 160 '.10 t . ' '
160 to 1'CO 110 U: IvIO
.toao
0.5 to 2.
Series
20
8
6.8
6
200
50
cell ti
80
roMc
__
0 mult
to 50
to 15
to f.i
to 50
30
to 50C
to 70
bactt
7. sue
_„
to i6c
*a' Conventional aerobic potido designed in maxiinlze the anoant of oxygen prLiducuJ raider thn-i the miiouut ol' i
produced.
f *» \
ll} Depends on climatic conditions,
Typical values (much hipb.cr values have lieen applied at various loadinps), Lc-tlln.j vi/'nea are often spec
by state cc/itrol agencies,
'td' Some states limit this fic'are to 50 or >ss.
'e/ Includes algae, nioroor^anic^r-. , and residual influent suspended soli^a. Valves -i.-e cacpd on f.n influent
ble FOD5 of ?00 mg/t and, uitli the exe'.'yUon of the aerobic poi :ln , tin influcr.t su.!oer.dt.".i-i:oliJ'3 conccntrut
of 200 mg/t. From Metcclf and EdJ,
b. Default Data
,
ROi) LOAniNG ^fl
Ef-TLUFNT Sn hO
3-74
-------
c. Lagoons Unit Process Data Cards
LAGOONS MOD xx
DEPTH xx.x FT
BOD LOADING xx.x LB/A
EFFLUENT SS xx.x MG/L
END
3-75
-------
3-33. Microscreening (see page 5-139 of Design Manual)
a. Design Parameters
Initial resistance of clean filter fabric (see manufacturer
specifications)- 0.25-0.50 feet
Filterability index of influent (determine from bench test)
= 1.50-2.50
Number of Units ~2
Speed of strainer »4.0-7.0 rev/min
Table 3-9. Suggested Removals from Secondary
Effluents by Microscreens
Fabric Aperture
microns
23
35
Anticipated Removal, %
Suspended Solids
70 to 80
50 to 60
BOD
60 to 70
40 to 50
Flow, gpm/ft""
of Submerged Area
6.7
10.0
From Gulp and Gulp, 1971
Table 3-10. Microscreen Sizes Available from
Glenfield and Kennedy
Drum Sizes, ft
Diameter Width
Motors, bhp Approximate
Wash Ranges of
Drive Pump Capacity, mgd
Recommended Maximum
Flow for Tertiary
Sewage Applications, mgd
23 microns 35 microns
5
5
7-1/2
10
1
3
5
10
1/2
3/4
2
4
1
3
5
7-1/2
0
0
0
.05
.3
.8
3
to
to
to
to
0.5
1.5
4
10
0.
0.
0.
2.
075
20
70
00
0.
0.
1.
3.
11
30
00
00
Table 3-11.
From Gulp and Gulp, 1971
Microscreen-Sizes (Zurn Industries)
Drum
Diameter
4
4
6
6
6
10
Sizes, ft
Width
2
4
4
6
8
10
Screen Area
J.U
24
48
72
108
144
3.5
From Gulp and Gulp, 1971
b. Default Data
INITIAL RE?,IST/\NCF
SPFF.D OP STRAINER
3-76
i.n
i.o
FT
REV/MTN
-------
c. Microscreening Unit Process Data Cards
MICROSCREENING MOD xx
NUMBER OF UNITS3 xx.x UNITS
INITIAL RESISTANCE xx.x FT
FILTERABILITY INDEX3 xx.x
SPEED OF STRAINER xx.x REV/MIN
END
Value will be calculated if input is left blank.
3-77
-------
3-34. Multiple Hearth Incineration (see page 5-177 of Design Manual)
a. Design Parameters
2
Wet sludge loading rate =7.0-12.0 Ib/hr/ft @ 20-25% total solid;
b. Default Data
WFT si unGF LOADING RATF 10.0
nAfs PER YFAR OPERATION 260.o DAYS
FSTIMATF
3-78
-------
c. Multiple Hearth Incineration Unit Process Data Cards
MULTIPLE HEARTH INCINERATION MOD xx
WET SLUDGE LOADING RATE xx.x LB/HR/SQFT
DAYS PER YEAR OPERATION xx.x DAYS
ESTIMATE3 COSTIS « xx.x
END
aCOSTIS = Cost of standard 1580-square foot incinerator -
default value - $1,190,000.
3-79
-------
3-35. Neutralization (see page 6-55 of Design Manual)
a. Design Parameters
Buffer capacity (determine from titration curves) ~
pound of reagent per gallon of waste required to
neutralize the waste to the desired pH.
Degree of mixing (see manufacturer specifications) ~
0.2-0.4 hp/1000 gallons
Mixing time (see manufacturer specifications) ~5.0-10.0 min
b. Default Data
niJFFKK CAPACITY 0.1 LR/GAL
OFGREF OF MIXING n.3 HP/TO
MIXING TIMF 5 MIN
3-80
-------
c. Neutralization Unit Process Data Cards
NEUTRALIZATION MOD xx
BUFFER CAPACITY xx.x LB/GAL
DEGREE OF MIXING xx.x HP/TG
MIXING TIME xx.x MIN
END
3-81
-------
3-36. Nitrification (see page 7-253 of the Design Manual)
a. Design Parameters
Effluent ammonia
Mixed liquor volatile SS =1200-2000 mg/£
Ammonia loading (see Figure 3-6)
Correction for pH= 60-70% (see Figure 3-7 DM)
ALPHA 09 transfer in waste/0,, transfer in water^O.90
BETA 0» saturation in waste/0,, saturation in water~0.90
HP Horsepower per 1000 gallons >0.10 hp/1000 gal
STE Standard transfer efficiency
Mechanical Aerators -2.0-3.5 Ib 0 /hp-hr
High speed -2.0
Slow speed -3.5
Diffused Aerator -6.0-11.0%
Coarse bubble- 6.0
Fine bubble -11.0
b. Default Data
WINTKH TEMPERATURE
FFFt UENT AN'MONIA
MIXFIJ LIOUOU
AMMONIA LOAOING
OIFFUSFn AHiATION ai f
FACTOR FOR PH
10 OFG CFMT
?.n MG/I
VS=2000 MG/I
10 LH/TCFT/DAY
nfTA=o.y AF=o.n CFM/TG STF=12
n.a
PFP
3-82
-------
c. Nitrification Unit Process Data Card?
NITRIFICATION3
WINTER TEMPERATURE xx.x DEC CENT
EFFLUENT AMMONIA xx.x MG/L
MIXED LIQUOR VS=xx.x MG/L
AMMONIA LOADING xx.x LB/TCFT/DAY
MECHANICAL AERATION ALPHAb=xx.x BETA=xx.x HP=xx.x
HP/TG STE=xx.x LB/HP-HR
DIFFUSED AERATION ALPHAb=xx.x BETA=xx.x AF°=xx.x
CFM/TG STE=xx.x PER
CORRECTION FOR PH xx.x
END
Q
User must also specify secondary clarification (nitrify-
dentrify).
Use mechanical or diffused, not both.
Q
AF (minimum airflow) specifies a lower limit on airflow.
Model will calculate actual airflow and compare it with input
value. Higher value will be output. Input zero for AF to
obtain calculated value only.
3-83
-------
25
r>
I-
g 20
I
z
«• 15
rt
I
Z
(D
10
8.4
10'
,00,
10 15
TEMPERATURE , °C
20
25
Figure 3-6. Permissible nitrification tank loadings.
3-84
-------
100
eo
tc
I 60
x
H 40
U
ec
AT 20"C
I I L
a
pH
10
Figure 3-7. Percent of maximum rate of nitrification at
constant temperature versus pH.
3-85
-------
3-37. Overland Flow Land Treatment
a. Design Parameters
Application ratez2.5-6.0 in/wk (screened wastewater)
Application rater6.0-16.0 in/wk (lagoon or secondary effluent)
Runoff (site dependent):0.0 in/wk
Spray evaporation (percent of application rate)-2.0-8.0%
Percolate of soil (percent of application rate);8.0%
Buffer zone (site dependent)=0.0-500.0 ft
Slope-2.0-8.0% (over 8.0% requires finished slopes)
Fraction of nitrogen loading denitrified=75.0-90.0%
Ammonia volatilization^ 0.0
Removal of phosphorus-50.0%
NW Number of recovery wells
WDIA Diameter of recovery wells
DW Depth of recovery wells
PS Cost of standard 3000 gpm pump and driver unit -
default value » $17,250.00
SP Cost of 12-inch welded steel pipe in-place -
default value = $12.80 per feet
SV Cost of 12-inch butterfly value - default value = $952.10
CS Cost of 6-15 gpm impact type rotor pop-up full circle
sprinkler - default value * $61.65
CG Cost of clearing and grubbing - default value = $3000.00
per acre
MW Cost of 4-inch water well - default value = $8.00 per foot
SC Cost of 24-inch reinforced concrete drain pipe -
default value = $10.20 per foot
b. Default Data
APPLICATION RATF 5.0 TN/WFFK
PWCIPITATTOfj RATr O.fl TN/wFFK
FVAPOTRAUbPlRAFlCN RATF 0. «4 IM/rtFfK
RUNOFF- 0.0 IM/.VFFK
WASTrisAFLR GFNiFR ATT f>N' PFRI01) 361.0 DAYS/YR
FIFl.1) At1|JLTCAlIUN PFRIOQ 52.0 WFFKS/YR
SPRAY LV/APoRAI J0fj RATr 5.0 PfrRCFMT
PFRCOI ATL RATE. uF SOIL fl.O PFRCf NT
NO STOUrtGF
GRAVITY PIPK KFCOVF:?Y SYSTTM
nllFFFt* /'OIJF 0.0 FFFT
CUiJUrijT GiiOUN'h COVFR FORFS.T PO.O % RRUC>M 30.0 * I"\STURF S
SI OPf ?..n PFRCFMT
MONITORING V.n.LS 9 WFI I S AT 10 FT/wFI.I
FFNf.IHG ^.7b T./FT
FRACTION l.'FtaiRTFIFD 90.0 PFRCFf'T OF APPLirn N
AMMOU1A VOI AT ILI/ATIOU 0.0 PFf'CFNT OF APPITFR N
RFMOVAL or PHOSPHORUS no.o pFRcrNT OF APPLTFD P
DAYS" PFR WFF'K (^'('RATION 7.0 nAYS/l-.FFK
HOURb PFU nAY OPFRATION ft.O HOURS/HAY
FSTIMATF 3 _ g6
-------
c. Overland Flow Land Treatment Unit Process Data Cards
OVERLAND FLOW LAND TREATMENT
APPLICATION RATE
PRECIPITATION RATE
EVAPOTRANSPIRATION RATE
RUNOFF
WASTEWATER GENERATION PERIOD
FIELD APPLICATION PERIOD
SPRAY EVAPORATION
PERCOLATE OF SOIL
NO STORAGEa
STORAGE3'b (MINIMUM)
LINER REQUIRED
EMBANKMENT PROTECTION1*
GRAVITY PIPE RECOVERY SYSTEM0
OPEN CHANNEL RECOVERY SYSTEM0
BUFFER ZONE WIDTH
MOD xx
XX. X
XX. X
XX. X
xx. x
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
XX. X
IN/WK
IN/WK
IN/WK
IN/WK
DAYS/YR
DAYS/YR
PERCENT
PERCENT
DAYS/YR
$/SQ FT
$/CU YD
XX.X
FT
CURRENT GROUND COVER
SLOPE OF LAND
MONITORING WELLS NO.-xx.x
FENCING
FRACTION DENITRIFIED
AMMONIA VOLATILIZATION
REMOVAL OF PHOSPHORUS
HOURS PER DAY OPERATION
DAYS PER WEEK OPERATION
FOREST xx.x% BRUSH xx.x% PASTURE xx.x%
XX.X
DEPTH/WELL xx.x
XX. X
xx.x
xx.x
xx.x
xx.x
xx.x
PERCENT
FT
$/FT
PERCENT
PERCENT
PERCENT
HOURS
DAYS
ESTIMATE
END
PS xx.x SP xx.x SV xx.x CS xx.x CG xx.x MW xx.x SC xx.x
a
Use no storage or storage, not both.
Liner or embankment protection should only be used with storage.
c
Use gravity pipe or open channel, not both.
3-87
-------
3-38. Oxidation Ditch Activated Sludge (see page 7-235 of Design Manual)
a. Design Parameters
Reaction rate constants
k, BOD removal rate constant~0.0007-0.002 5,/mg/hr
a, fraction of BOD synthesized~0.73
V
a , fraction of BOD oxidized for energy=0.52
b, endogenous rate (oxygen basis)~0.075/day
V
b , endogenous rate (sludge basis)~0.15/day
f, nonbiodegradable fraction of VSS in influent~0.40
V
f , degradable fraction of the MLVSS-0.53
a , fraction of BOD synthesized to degradable solids~0.56
F/M ratio~0.03-0.10
Mixed liquor suspended solids~4000-8000 mg/£
Mixed liquor volatile solids^2800-5600 mg/A
Temperature correction coefficient~1.0-l.03
Effluent BOD soluble-ID mg/£
ALPHA 0 transfer in waste/0_ transfer in water~0.90
BETA 09 saturation in waste/0- saturation in water~0.90
HP Horsepower per 1000 gallons >0.10 hp/1000 gal
STE Standard transfer efficiency
Mechanical Aerators~2.0-3.5 Ib 0_/hp-hr
High speed-2.0
Slow speed~3.5
Diffused Aerator^.0-11.0%
Coarse bubble~6.0
Fine bubble -11.0
b. Default Data
UT<; K=O.OOI? A=O.V AP=O.S ^-^ =l}r °'5 An::n'7ft
^ >\ T T 1 0«L)r>5
MlxrB L OUOR SS=^Onn VS=3750
TFMlVKATUf'.F COrFFTCIENT J-OJ5
0/MP HR
3-88
-------
c. Oxidation Ditch Activated Sludge Unit Process Data Cards
OXIDATION DITCH ACTIVATED SLUDGE
V V
CONSTANTS K=xx.x A=xx.x A =xx.x B=xx.x B =xx.x F=xx.x
V
F =xx.x A0=xx.x
F/M RATIO xx.x LB BOD/LB VSS
MIXED LIQUOR SS=xx.x MG/L
TEMPERATURE COEFFICIENT xx.x
EFFLUENT BOD SOLUBLE xx.x MG/L
MECHANICAL AERATION ALPHAb=xx.x BETA=xx.x HP=xx.x HP/TG
STE=xx.x LB 0/HP-HR
DIFFUSED AERATION ALPHAb=xx.x BETA=xx.x AFC=xx.x CFM/TG
STE=xx.x PER
ESTIMATEd COSTDS = xx.x COSTPS = xx.x
END
a
User must also specify secondary clarification (activated
sludge).
Use mechanical or diffused, not both.
Q
AD (minimum airflow) specifies a lower limit on airflow. Model
will calculate actual airflow and compare it with input value.
Higher value will be output. Input zero for AF to obtain
calculated value only.
COSTDS = Cost of standard 42-inch diameter by 20-foot rotor -
default value = $15,340.
COSTPS = Cost of standard 3000 gpm pump and driver unit -
default value = $17,250.
3-89
-------
3-39. Plug Flow Activated Sludge (see page 7-13 of Design Manual)
a. Design Parameters
Eckenfelder's Approach
Reaction rate constants
k, BOD removal rate constant~0.0007-0.002 £/mg/hr
a, fraction of BOD synthesized~0.73
V
a , fraction'of BOD oxidized for energy~0.52
b, endogenous rate (oxygen basis)~0.075/day
V
b , endogenous rate (sludge basis)x0.15/day
f, nonbiodegradable fraction of VSS in influent«0.40
V
f , degradable fraction of the MLVSS-0.53
F/M ratio=0.2-0,4
Mixed liquor suspended solids=1500-3000 mg/£
Mixed liquor volatile solids-1050-2100 mg/JJ,
Temperature correction coefficient~1.0-1.03
Effluent BOD soluble-10 mg/£
ALPHA 0 transfer in waste/0 transfer in water~0.90
BETA 0? saturation in waste/0» saturation in water~0.90
HP Horsepower per 1000 gallons>0.10 hp/1000 gal
STE Standard transfer efficiency
Mechanical Aerators=2.0-3.5 Ib 0?/hp-hr
High speed^2.0
Slow speed~3.5
Diffused Aerators6.0-ll. 0%
Coarse bubble~6.0
Fine bubble-11.0
b. Default Data
CONSTANTS K = 0.0013r. A-0.73 AP=n.52 0-0.075 RP = 0.1B F^O.U
F/M HAFIO 0,.} l.t\ KOn/l H VSS
.
TFMPHMlUKF CDf-FFICieMT 1.03
rmn SOLUFUJ: 5 vo/i
AFRATIOfJ ALPMA = 0.9 HF.TA = 0.9 AP=0.n CPM/TR ^tF = 12 PFRCFNT
3-90
-------
c. Plug Flow Activated Sludge Unit Process Data Cards
PLUG FLOW ACTIVATED SLUDGE3 MOD xx
V V
CONSTANTS K=xx.x A=xx.x A =xx.x B=xx.x B =xx.x F=xx.x
V
F =xx.x
F/M RATIO xx.x LB BOD/LB VSS
MIXED LIQUOR SS=xx.x VS=xx.x MG/L
TEMPERATURE COEFFICIENT xx.x
EFFLUENT BOD SOLUBLE xx.x MG/L
MECHANICAL AERATION ALPHAb=xx.x BETA=xx.x HP=xx.x HP/TG
STE=xx.x LB 0/HP-HR
DIFFUSED AERATION ALPHAb=xx.x BETA=xx.x AFC=xx.x CFM/TG
STE=xx.x PER
ESTIMATEd SSXSA = xx.x COSTPD = xx.x COSTPH = xx.x
COSTPS = xx.x
END
*a
User must also specify secondary clarification (activated
sludge).
Use mechanical or diffused, not both.
£
AF (minimum airflow) specifies a lower limit on airflow.
Model will calculate actual airflow and compare it with
input value. Higher value will be output. Input zero for
AF to obtain calculated value only.
SSXSA = Cost of standard slow-speed pier-mounted 20-hp aerator-
default value = $16,300.
COSTPD = Cost of standard 12.0 scfm coarse-bubble diffuser -
default value = $6.50.
COSTPH = Cost of standard 550 scfm swing arm diffuser -
default value = $5,000.
COSTPS = Cost of standard 3000 gpm pump and driver unit -
default value = $17,250.
3-91
-------
3-40. Post Aeration (see page 5-159 of Design Manual)
a. Design Parameters
Detention time~5.0-10.0 min
Air flow*20.0-30.0 cfm/1000 gal
Dissolved oxygen (determine initial DO from standard
tables based on summer temperature)
Final dissolved oxygens:2.0 mg/£
ALPHA 0- transfer in waste/0_ transfer in water~0.90
BETA 0_ saturation in waste/09 saturation in water~0.90
HP Horsepower per 1000 gallons>0.10 hp/1000 gal
STE Standard transfer efficiency
Mechanical Aerators~2.0-3.5 Ib 02/hp-hr
High speed=2.0
Slow speed~3.5
Diffused Aerator~6.0-11.0%
Coarse bubble~6.0
Fine bubble-11.0
b. Default Data
f/FCHANICAL AFRATION ALPH-Q.9 RFTA^O.9 HP^Q.l HP/Tr, ^TF = 6.f) LF? O/MP Hf
ION TIMF ?50 MIN!
OXYGFN IWITIAL=2.0 riNAL^S.O MR/L
3-92
-------
c. Post Aeration Unit Process Data Cards
POST AERATION MOD xx
MECHANICAL AERATION ALPHAa=xx.x BETA=xx.x HP=xx.x
HP/TG STE=xx.x LB 0/HP-HR
DIFFUSED AERATION ALPHA3=xx.x BETA=xx.x AFb=xx.x
CFM/TG STE=xx.x PER
DETENTION TIME xx.x MIN
DISSOLVED OXYGEN INITIAL = xx.x FINAL = xx.x MG/L
END
o
Use mechanical or diffused, not both.
AF (minimum airflow) specifies a lower limit on airflow.
Model will calculate actual airflow and compare it with
input value. Higher value will be output. Input zero
for AF to obtain calculated value only.
3-93
-------
3-41. Pressure Filtration
a. Design Parameters
3
Density of cake~70.0-80.0 Ib/ft
Solids loading rate (determine from lab tests)«5.0-8.0
Ib/ft2/hr
Operating schedulers.0-16.0 hours/day
Cake solids content (see Table 3-12)
Table 3-12. Normal Quantities of Sludge Produced by
Different Treatment Processes
Wastewater
Treatment Process
Primary sedimentation
Undigested
Digested in separate
tanks
Trickling filter
Chemical precipitation
Primary sedimentation &
activated sludge
Undigested
Digested in
separate tanks
Activated Sludge
Waste sludge
Septic tanks, digested
Imhoff tanks, digested
Gallons Sludge
MG Treated
2950
1450
745
5120
6900
2700
19400
900
500
Solids
Z
5.0
6.0
7.5
7.5
4
6
1.5
10
15
Sludge
Specific Gravity
1.02
1.03
1.025
1.03
1.02
1.03
1.005
1.04
1.04
From Metcalf & Eddy, Inc., 19"
b. Default Data
CAKF; soi IDS CONTENT
nr.NjSUY or- CAKF
OPFRATJNG SCHfnULF
O'o LOADING RATF
5.0 PFRCFMT
75.0 PFRCFNT
8.0 HOURS/DAY
6.0 LR/SOFT/HR
3-94
-------
c. Pressure Filtration Unit Process Data Cards
PRESSURE FILTRATION
CAKE SOLIDS CONTENT
DENSITY OF CAKE
OPERATING SCHEDULE
SOLIDS LOADING RATE
END
MOD xx
XX. X
XX.X
XX.X
XX. X
PERCENT
LB/CUFT
HOURS/DAY
LBS/SQFT/HR
3-95
-------
3-42. Primary Clarification (see page 5-67 of Design Manual)
a. Design Parameters
Sidewater depth 7.0-12.0 ft
Underflow concentration of solids~4.0-6.0%
Weir overflow rate~10,000-15,000 gal/day/ft
Surface overflow rate (see Table 3-13)
Table 3-13. Recommended Surface-Loading Rates for
Various Suspensions
2
Loading Rate, gpd/ft
Suspension Range Peak Flow
Untreated wastewater 600 to 1200 1200
Alum floe3 360 to 600 600
Iron floca 540 to '800 800
Lime floe3 540 to 1200 1200
aMixed with the settleable suspended solids in the untreated wastewater
and colloidal or other suspended solids swept out by the floe.
From Metcalf and Eddy, Inc., 1971
Specific gravity of sludge (see Table 3-14)
Table 3-14. Specific Gravity of Raw Sludge Produced
From Various Types of Sewage
Type of
Sewerage System
Sanitary
Sanitary
Combined
Comb i ned
Strength
of Sewage
Weak
Medium
Medium
Strong
Specific
Gravity
1.02
1.03
1.05
1.07
From Metcalf and Eddy, Inc., 1971
Suspended solids removal (see figure 3-8)
BOD removal (see Figure 3-9)
b. Default Data
C IlfCOLAR C| /VHIFIER
f
-------
c. Primary Clarification Unit Process Data Cards
PRIMARY CLARIFICATION
SURFACE OVERFLOW RATE xx.x G/D/SQFT
SIDEWATER DEPTH xx.x FT
SPECIFIC GRAVITY xx.x
UNDERFLOW CONCENTRATION xx.x PERCENT
REMOVAL SOLIDS=xx.x BOD=xx.x COD=xx.x TKN=xx.x
P0=xx.x PERCENT
WEIR OVERFLOW RATE xx.x G/D/FT
RECTANGULAR CLARIFIER3
CIRCULAR CLARIFIER3
ESTIMATE13 STANDARD MECHANISM COST=xx.x
END
Use rectangular or circular clarifier, not both-default is
circular clarifier.
Rectangular clarifier-cost of standard 20-foot by 120-foot
clarifier mechanism-default value = $42,000.
Circular clarifier - cost of standard 90-foot diameter
clarifier mechanism-default value = $75,000.
3-97
-------
Co
I
oo
c
n
fD
CO
00
"O (/>
H C
(D
3
n a-
i— i
ID 01
^ O
H- M
t-h H-
H- CL
f!) cn
i-j
cn c(
O
0)
C
cn
o
r
> >
2 33
n"
-------
60 .
40
»-
J
q
in
cc
o
O
m
20
o
3000
1000 5OO
SETTLING RATE. GPD'SQ FT TANK AREA (DESIGN FLOW)
400
Figure 3-9. BOD removal rate in primary clarifier.
3-99
-------
3-43. Primary Clarification (coagulation;see page 5-67 of Design
Manual)
a. Design Parameters
Sidewater depth«7.0-12.0 ft
Underflow concentration of solids~4.0-6.0%
Weir overflow rate«10,000-15,000 gal/day/ft
Surface overflow rate (see Table 3-15)
Table 3-15. Recommended Surface-Loading Rates
for Various Suspensions
Suspension
Untreated wastewater
•a
Alum floe
Iron floe
Lime floe
Loading Rate,
Range
600 to 1200
360 to 600
540 to 800
540 to 1200
gpd/ft2
Peak Flow
1200
600
800
1200
Mixed with the settleable suspended solids in the untreated wastewater
and colloidal or other suspended solids swept, out by the floe.
From Metcalf and Eddy, Inc., 1971
Specific gravity of sludge (see Table 3-16)
Table 3-16. Specific Gravity of Raw Sludge Produced
from Various Types of Sewage
Type of
Sewerage System
Sanitary
Sanitary
Combined
Combined
Strength
of Sewage
Weak
Med ium
Med ium
Strong
Specific
Gravity
1.02
1.03
1.05
1.07
From Metcalf and Eddy, Inc., 1971
Suspended solids removal (see Figure 3-10)
BOD removal (see Figure 3-11)
b. Default Data
f.r OVFRR r>4 ivar£
V/AItR Drf-TH
^PKCiriC GRAVITY
UMDFl^l OW rOt'Q NTMTTOM
REMOVAL r,s=^o nnn=Go
WF1K OVFKFl OvJ KATF
f)00
9
1.05
4
15
FEFT
Pl-'RfFNT
P0=50 PFNCFNT
G/D/FT
3-100
-------
c. Primary Clarification (Coagulation) Unit Process Data Cards
C PRIMARY CLARIFICATION (COAGULATION)3 MOD xx
SURFACE OVERFLOW RATE xx.x G/SQFT/DAY
SIDEWATER DEPTH xx.x FT
SPECIFIC GRAVITY xx.x
UNDERFLOW CONCENTRATION xx.x PERCENT'
REMOVAL SS=xx.x BODd=xx.x COD=xx.x TKN=xx.x PERCENT
WEIR OVERFLOW RATE xx.x G/FT/DAY
RECTANGULAR CLARIFIERb
CIRCULAR CLARIFIERb
ESTIMATE0 STANDARD MECHANISM COST = xx.x
END
a
This process is used as part of the coagulation/process.
Use rectangular or circular clarifier, not both. Defaxilt is
circular clarifier.
c
Rectangular clarifier - cost of standard 20-foot by 120-foot
clarifier mechanism - default value = $42,000.
Circular clarifier - cost of standard 90-foot diameter
clarifier mechanism - default value = $75,000.
BOD removal rate is rate of removal of non-soluble BOD5.
3-101
-------
o
NJ
TO
H
ro
to
•o en
>-! C
H- (n
3 T3
O (D
11 a
^ a.
(t>
o a,
Hi H-
H. CL
CD W
(D
a
o
(B
i-t
cn
c
cn
o
(B
(U
(T
(D
8
o
m
2
' O
O o
H
m
o
o
H
SUSPENDED SOLIDE REMOVAL. %
8
A
O
in
O
•f-l
00
0 *
°
o
O
o
I
o «
O 3)
^ II
o n
?! o
•° c
-i r
> >
Z 71
5 -i
>
2
-------
60
O
z
tu
1C
O
O
CD
20
3000
1000 500
SETTLING RATE. GPD'SQ FT TANK AREA (DESIGN FLOW)
400
Figure 3-11. BOD removal rate in primary clarifier.
3-103
-------
3-44. Primary clarification (Two Stage Lime Treatment; see
page 5-67 of Design Manual)
a. Design Parameters
Sidewater depth 7.0-12.0 ft
Underflow concentration of solids 4.0-6.0%
Weir overflow rate 10,000-15,000 gal/day/ft
Surface overflow rate (see Table 3-17)
Table 3-17. Recommended Surface-Loading Rates for
_ Various Suspensions
Loading Rate, gpd/ft
Suspension
Untreated wastewater
Alum floca
Iron floe3
Lime floca
Range
600 to 1200
360 to 600
540 to 800
540 to 1200
Peak Flow
1200
600
800
1200
nixed with the settleable suspended solids in the untreated wastewater
and colloidal or other suspended solids swept out by the floe.
From Metcalf and Eddy, Inc., 1971
Specific gravity of sludge (see Table 3-18)
Table 3-18.
Specific Gravity of Raw Sludge Produced
from Various Types of Sewage
Type of
Sewerage System
Sanitary
Sanitary
Combined
Combined
Strength
of Sewage
Weak
Medium
Medium
Strong
Specific
Gravity
1.02
1.03
1.05
1.07
From Metcalf and Eddy, Inc., 1971
Suspended solids removal (see Figure 3-12)
BOD removal (see Figure 3-13)
b. Default Data
FSTTMAIF
SUHFACF OVrRFLCM HATE
SlOf WATER OFPTH
spFCihic GPAVITY
UNDF.KFLOW rOMCFUTRATIOM
Kf-MOVAL SS=ttU R0n=fib
WFIK OVFHFl OW RATF
1000
9
1.03
1. 00
TKN=30
15000
G/SfiFT/nAY
FEF.T
PFRTFNT
0 PFRCFNT
G/FT/DAY
3-104
-------
c. Primary Clarification (Two-Stage Lime Treatment) Unit Process
Data Cards
L PRIMARY CLARIFICATION (TWO-STAGE LIME TREATMENT) MOD xx
SURFACE OVERFLOW RATE xx.x G/SQFT/DAY
SIDEWATER DEPTH xx.x FT
SPECIFIC GRAVITY xx.x
UNDERFLOW CONCENTRATION xx.x PERCENT
REMOVAL SOLIDS = xx.x BOD = xx.x COD = xx.x
TKN = xx.x PO = xx.x PERCENT
WEIR OVERFLOW RATE xx.x G/FT/DAY
RECTANGULAR CLARIFIER3
CIRCULAR CLARIFIER3
ESTIMATE13 STANDARD MECHANISM COST = xx.x
END
»3
Use rectangular or circular clarifier, not both - default is
circular clarifier.
Rectangular clarifier - cost of standard 20-foot by 120-foot
clarifier mechanism - default value = $42,000.
Circular clarifier - cost of standard 90-foot diameter clarifier
mechanism - default value = $75,000.
3-105
-------
eo
70
60
o
2 50
o
\
\
• \
REMOVALS'] /
RFLOW y"
"D/SO FT j
O
0
LEG
END
• RtCTANGULAR TANKS
o CIRCULAR TANKS
Xs
•\
\
» ^^
500
100o 1500
OVERFLOW RATE. GPD/SQ FT
2500
Figure 3-12.
Suspended solids removal versus overflow rate for
primary clarifiers.
3-106
-------
3000
1000 500
SETTLING RATE. GPD'SQ FT TANK AREA (DESIGN FLOW5
400
Figure 3-13. BOD removal rate In primary clarifier.
3-107
-------
3-45. Pure Oxygen Activated Sludge (see page 7-171 of Design Manual)
a. Design Parameters
Eckenf elder ' s Approach
Reaction rate constants
k, BOD removal rate constant- 0.0007-0. 002 £/mg/hr
a, fraction of BOD synthesized* 0.73
V
a , fraction of BOD oxidized for energys;0.52
b, endogenous rate (oxygen basis)~0.075/day
y
b , endogenous rate (sludge basis)^0. 15/day
f, nonbiodegradable fraction of VSS in inf luent~0.40
V
f , degradable fraction of the MLVSS-0.53
F/M ratios 0.25-1.0
Mixed liquor suspended solidss4000-7000 mg/£
Mixed liquor volatile solidsx3200-5600 mg/£
Temperature correction coefficients 1.0-1. 03
Effluent BOD soluble^lO mg/£
ALPHA 0- transfer in waste/0_ transfer in waters;0.90
BETA 0» saturation in waste/0? saturation in water^0.70
HP Horsepower per 1000 gallons>0.10 hp/1000 gal
STE Standard transfer efficiency
Mechanical Aerator s^2. 0-3. 5 Ib 0 /hp-hr
High speed -2.0
Slow speed =3.5
Diffused Aerator 6.0-11.0%
Coarse bubble^G.O
Fine bubble~11.0
b. Default Data
s K=o.ooi35 *=
Mi'xVSAL OUOR ..r
TF.-lf'EUATUKF CO! t-lC.IF
HP=0,ri HP/T. STF^.S LH 0/HP MR
3-108
-------
c. Pure Oxygen Activated Sludge Unit Process Data Cards
PURE OXYGEN ACTIVATED SLUDGEa MOD xx
CONSTANTS K=xx.x A=xx.x A =xx.x B=xx.x B =xx.x F=xx.x
FV=xx.x
F/M RATIO xx.x LB BOD/LB VSS
MIXED LIQUOR SS=xx.x VS=xx.x MG/L
TEMPERATURE COEFFICIENT xx.x
EFFLUENT BOD SOLUBLE xx.x MG/L
MECHANICAL AERATION ALPHAb=xx.x BETA=xx.x HP=xx.x HP/TG
STE=xx.x LB 0/HP-HR
DIFFUSED AERATION ALPHA =xx.x BETA=xx.x AF°=xx.x CFM/TG
STE=xx.x PER
ESTIMATEd SSXSA = xx.x COSTSP = xx.x COSTSCR = xx.x
COSTPS = xx.x
END
User must also specify secondary clarification (activated sludge),
Use mechanical or diffused, not both.
p
AF (minimum airflow) specifies a lower limit on airflow. Model
will calculate actual airflow and compare it with input value.
Higher value will be output. Input zero for AF to obtain
calculated value only.
SSXSA = Cost of standard slow-speed pier-mounted 20-hp aerator -
default value = $16,300.
COSTSP = Cost of standard 10-ton PSA oxygen generation unit -
default value = $800,000.
COSTSCR = Cost of standard 50-ton cryogenic oxygen generation
unit - default value = $1,900,000.
COSTPS = Cost of standard 3000 gpm pump and driver unit - default
value = $17,250.
3-109
-------
3-46. Rapid Infiltration Land Treatment
a. Design Parameters
Application rates:4.0-150.0 in/wk
Runoff (site dependent)-0.0
Buffer zone (site dependent)=0.0-500.0 ft
Slope is not critical but values over 8.0% require
excessive earthwork
Fraction of nitrogen loading denitrif ieds:30.0-60. 0%
Ammonia volatilization~0.0%
Removal of phosphorus-90.0%
NW Number of recovery wells
WDIA Diameter of recovery wells
DW Depth of recovery wells
SP Cost of 12-inch welded steel pipe in-place -
default value = $12.80 per foot
BV Cost of 12-inch butterfly valve -
default value = $952.10
PP Cost of 6-inch perforated PVC pipe
default value = $6.94 per foot
CP Cost of 24-inch concrete Class III pipe -
default value = $10.20 per foot
WW Cost of 4-inch water well -
default value = $8.00 per foot
RW Cost of 4-inch recovery well -
default value = $8.00 per foot
PS Cost of standard 3000 gpm pump and driver unit -
default value = $17,250.
b. Default Data
APPLICATION HATE 3«- 0 IN/WFFK
PRFCIMITATION hATr 0 A TN/WFFK
FVAPCHRANSPIKAriON RATF O.S UJ/WFFK
RUIJOFF 0.0 TM/WFFK
WASTFir.ATfJ< GF.\jFi BtCOVFRY SYSTEM
KUFFFK /Ol.F 0.0 FFFT
MONITORING U'FLLS 9 WF'.LI S AT 10 FT/WFI L
FFIJCIi-IG ?.7S f/FT
F«ACTiorj nr-Ni iinfiFn
-------
c. Rapid Infiltration Land Treatment Unit Process Data Cards
RAPID INFILTRATION LAND TREATMENT MOD xx
APPLICATION RATE xx.x
PRECIPITATION RATE xx.x
EVAPOTRANSPIRATION RATE xx.x
RUNOFF xx.x
WASTEWATER GENERATION PERIOD xx.x
FIELD APPLICATION PERIOD xx.x
NO RECOVERY SYSTEM3
UNDERDRAIN RECOVERY SYSTEM3
RECOVERY WELLS SYSTEM3 NW xx.x WDIA xx.x
BUFFER WIDTH xx.x
MONITORING WELLS NO = xx.x DEPTH/WELL = xx.x
FENCING xx.x
FRACTION DENITRIFIED xx.x
AMMONIA VOLATILIZATION xx.x
REMOVAL OF PHOSPHORUS xx.x
ESTIMATE SP xx.x BV xx.x PP xx.x CP xx.x WW xx.x
END
IN/WK
IN/WK
IN/WK
IN/WK
DAYS/YR
WKS/YR
IN DW xx.x FT
FT
FT
$/FT
PERCENT
PERCENT
PERCENT
RW xx.x PS xx.x
Use recovery wells, underdrains, or no recovery system, but no
more than one.
3-111
-------
3-47. Recarbonation (see page 6-61 of Design -Manual)
a. Design Parameters
Detention time~15. 0-30.0 min
Alkalinity of hydroxide (determine from waste characteriza-
tion study) «50.0 mg/£
Alkalinity of carbonate (determine from waste characteriza-
tion study)~150.0 mg/£
b. Default Data
HYD«OXinr=50 CARriONATE=lRO Mfi/L
3-112
-------
c. Recarbonation Unit Process Data Cards
RECARBONATION MOD xx
DETENTION TIME xx.x MIN
ALKALINITY HYDROXIDE=xx.x CARBONATE=xx.x MG/L
END
3-113
-------
3-48. First Stage Recarbonation (see page 6-61 of Design Manual)
a. Design Parameters
Detention time-15.0-30.0 min
Alkalinity of hydroxide (determine from waste characteriza-
tion study)~50.0 mg/£
Alkalinity of carbonate (determine from waste characteriza-
tion study~150.0 mg/£
b. Default Data
DFTFNTION TIME 15 MIN
ALKALINITY HYnHOXln£=50 CARBONATE::! 50 MR/L
3-114
-------
c. First Stage Recarbonation Unit Process Data Cards
FIRST STAGE RECARBONATION MOD xx
DETENTION TIME xx.x MIN
ALKALINITY HYDROXIDE=xx.x CARBONATE=xx.x MG/L
END
3-115
-------
3-49. Second Stage Recarbonation (see page 6-61 of Design Manual)
a. Design Parameters
Detention time~15.0-30.0 min
Alkalinity of hydroxide (determine from waste characteriza-
tion study)~50.0 mg/£
Alkalinity of carbonate (determine from waste characteriza-
tion study)~150.0 mg/£
b. Default Data
DETENTION TIME 15 MIN
ALKALH4ITY HYOROXinE=50 CARBONATE=150 MR/L
3-116
-------
c. Second Stage Recarbonation Unit Process Data Cards
SECOND STAGE RECARBONATION MOD xx
DETENTION TIME xx.x MIN
ALKALINITY HYDROXIDE=xx.x CARBONATE=xx.x MG/L
END
3-117
-------
3-50. Screening (see page 5-19 of Design Manual)
a. Design Parameters
Bar shape factor
Sharp-edged rectangular bars:»2.42
Rectangular bars with semi-circular upstream
face*1.83
Circular bars~1.79
Rectangular bars with both ends semi-circular~1.67
Rectangular bars with semi-circular upstream face
and tapered symmetrical circular downstream
face~0.76
Bar screen width (see Table 3-19)
Bar screen spacing (see Table 3-19)
Bar screen slope (see Table 3-19)
Approach velocities (see Table 3-19)
Table 3-19. General Characteristics of
Bar Screens
Item
Bar screen size
Width, in.
Depth, in.
Spacing, in.
Slope from vertical, deg
Approach velocity, fps
Allowable head loss, in.
Hand Cleaned
1/4
1
1
30
1
to
to
to
to
to
6
5/8
3
2
45
2
Mechanically
Cleaned
1/4
1
5/8
0
2
to
to
to
to
to
6
5/8
3
3
30
3
b. Default Data
SPRCE=1.5 IN
APPUOACH=2.5 MAX=1.0
OEG
3-118
-------
c. Screening Unit Process Data Cards
SCREENING3 MOD xx
MECHANICALLY CLEANED** WIDTH=xx.x FT
MANUALLY CLEANEDb WIDTH=xx/x FT
BARS WIDTH=xx.x IN SPACE=xx.x IN SLOPE=xx.x DEC
SHAPE FACTOR=xx.x
VELOCITIES APPROACH=xx.x MAX=xx.x AVG=xx.x FT/SEC
END
Q
This process is part of preliminary treatment.
Use mechanically cleaned or manually cleaned, not both.
3-119
-------
3-51. Secondary clarification (Activated Sludge; see page 5-83 of
Design Manual)
a. Design Parameters
2
Solids loading rates!2.0-30.0 Ib/ft /day
2
Surface overflow rate (small plants< 1.0 mgd)s <600 gal/ft /day
> 2
Surface overflow rate (large plants;* 1.0 mgd)~ <800 gal/ft /day
Underflow concentration~0.8-1.2%
Weir overflow rate~10,000-15,000 gal/ft/day
Sidewater depth-7.0-12.0 ft
Specific gravity of sludge (see Table 3-20)
Table 3-20. Specific Gravity of Raw Sludge
Produced from Various Types of Sewage
Type of
Sewerage System
Sanitary
Sanitary
Combined
Combined
Strength
of Sewage
Weak
Medium
Medium
Strong
Specific
Gravity
1.02
1.03
1.05
1.07
From Metcalf and Eddy, Inc., 197
b. Default Data
FSTIMATF
RFCTANGULAW
SOIIU LOADING TIMR
SUKFACF CVrRFl OVi RATF (MAXIMUM)
SPFCIFIC GRAVITY OF SLUDGE
UtJHFKFLOW fiOUCFNTHATION
WFtR 0
-------
c. Secondary Clarification (Activated Sludge) Unit Process Data Cards
A SECONDARY CLARIFICATION (ACTIVATED SLUDGE)
SOLID LOADING RATE xx.x
SURFACE OVERFLOW RATE xx.x
SPECIFIC GRAVITY OF SLUDGE xx.x
UNDERFLOW CONCENTRATION xx.x
WEIR OVERFLOW RATE xx.x
SIDEWATER DEPTH xx.x
EFFLUENT SUSPENDED SOLIDS xx.x
RECTANGULAR CLARIFIERb
CIRCULAR CLARIFIERb
c
ESTIMATE
END
STANDARD MECHANISM COST = xx.x
MOD xx
LB/SQFT/DAY
G/SQFT/DAY
PERCENT
G/FT/DAY
FT
MG/L
This process is used with all activated sludge processes. It need
be specified only once.
Use rectangular or circular clarifier, not both - default is
circular clarifier.
•*
'Rectangular clarifier - cost of standard 20-foot by 120-foot
clarifier mechanism - default value = $42,000.
Circular clarifier - cost of standard 90-foot diameter clarifier
mechanism - default value = $75,000.
3-121
-------
3-52. Secondary Clarification (Nitrify-Denitr.ify; see page 5-83 of
Design Manual)
a. Design Parameters
Solids loading rates!2.0-30.0 Ib/ft2/day
2
Surface overflow rate=;<600 gal/ft /day
Underflow concentration~0.8-1.2%
Weir overflow rateslO,000-15,000 gal/ft/day
Sidewater depths?.0-12.0 ft
V
f , degradable fraction of the MLVSS«0.53
Specific gravity of sludge (see Table 3-21)
Table 3-21. Specific Gravity of Raw Sludge
Produced from Various Types of Sewage
Type of
Sewerage System
Sanitary
Sanitary
Combined
Combined
Strength
of Sewage
Weak
Medium
Medium
Strong
Specific
Gravity
1.02
1.03
1.05
1.07
From Metcalf and Eddy, Inc., 1971
b. Default Data
.MAXIMUM)
. GRAVITY OF SLUPfiF.
uunFHf-'Low roNcnmJATioti
WKK? OVhRFlO'.-.1 !^ATF (MAXIMYM)
StDF *ATER Oi-'HTH
FFFLUKUT SllSPt'MEO SOLIDS
15
1000
1 .03
1 .0
15000
1
20
L.H/ iQr~ I / * / A
G/SOKT/nAY
PFRCFtJT
G/n/FT
FFFT
KG/I
3-122
-------
c. Secondary Clarification (Nitrify/Denitrify) Unit Process Data
Cards
N SECONDARY CLARIFICATION (NITRIFY/DENITRIFY)
SOLID OVERFLOW RATE (MAXIMUM)
SURFACE LOADING RATE
CONSTANT FV= xx.x
SPECIFIC GRAVITY OF SLUDGE
UNDERFLOW CONCENTRATION
WEIR OVERFLOW RATE (MAXIMUM)
SIDEWATER DEPTH
EFFLUENT SUSPENDED SOLIDS
RECTANGULAR CLARIFIERb
CIRCULAR CLARIFIERb
,c
.TKIFY; i
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
10D xx
LB/SQFT/DAY
G/SQFT/DAY
FRACTION
PERCENT
G/FT/DAY
FT
MG/L
ESTIMATE
END
STANDARD MECHANISM COST = xx.x
This process is used with the nitrification process and with the
combined nitrivication/denitrification process. It need be
specified only once.
Use rectangular or circular clarifier, not both - default is
circular clarifier.
"Rectangular clarifier - cost of standard 20-foot by 120-foot
clarifier mechanism - default value = $42,000.
Circular clarifier - cost of standard 90-foot diameter clarifier
mechanism - default value = $75,000.
3-123
-------
3-53. Secondary Clarification (Trickling Filters; see page 5-83 of
Design Manual)
a. Design Parameters
Solids loading rate~12.0-30.0 Ib/ft2/day
2
Surface overflow rate (small plants< 1.0 mgd)= <600 gal/ft /day
2
Surface overflow rate (large plants> 1.0 mgd)~ <800 gal/ft /day
Underflow concentration-2.0-4.0%
Weir overflow rateslO,000-15,000 gal/ft/day
Sidewater depths?.0-12.0 ft
Mixed liquor volatile solids-1000-2500 mg/£
Specific gravity of sludge (see Table 3-22)
Table 3-22. Specific Gravity of Raw Sludge
Produced from Various Types of Sewage
Type of
Sewerage System
Sanitary
Sanitary
Combined
Combined
Strength
of Sewage
Weak
Medium
Medium
Strong
Specific
Gravity
1.02
1.03
1.05
1.07
From Metcalf and Eddy, Inc., 1971
b. Default Data
SOI 1!) LOADING RATF 15 LH/^OFT/DAY
SURFACF OVfRFLO.V RATF (MAXIMUM) 1000 G/SOFT/nAY
SPFCICIC GRAVITY OF SLUDGE 1.03
UNOFRFLO.-/ rONCF.-JTKATIOM 1.0 PFRCFMT
WFFR OVFRFl OW RATF (MAXIMUM) 15000 G/O/FT
SIDF WATER DKPTM 9 FEFT
EFFLUFNT SliSPFtlOEO SOLIDS 20 MG/I
' vss aoo MG/I.
3-124
-------
c. Secondary Clarification (Trickling Filters) Unit Process Data
Cards
T SECONDARY CLARIFICATION (TRICKLING FILTERS) MOD xx
SOLID LOADING RATE
SURFACE OVERFLOW RATE (MAXIMUM)
SPECIFIC GRAVITY OF SLUDGE
UNDERFLOW CONCENTRATION
WEIR OVERFLOW RATE (MAXIMUM)
SIDEWATER DEPTH
EFFLUENT SUSPENDED SOLIDS
MIXED LIQUOR VS
RECTANGULAR CLARIFIERb
CIRCULAR CLARIFIERb
ESTIMATE0 STANDARD MECHANISM COST = xx.x
END
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
xx.x
LB/SQFT/
G/SQFT/D,
PERCENT
G/FT/DAY
FT
MG/L
MG/L
This process is part of the trickling filtration process.
Use rectangular or circular clarifier, not both - default is
circular clarifier.
"Rectangular clarifier - cost of standard 20-foot by 120-foot
clarifier mechanism - default value = $42,000.
Circular clarifier - cost of standard 90-foot diameter clarifier
mechanism - default value = $75,000.
3-125
-------
3-54. Slow Infiltration Land Treatment
a. Design Parameters
Average Application rate~0. 5-4.0 in/wk
Maximum Application rate~0. 10-0.50 in/hr
Runoff (site depend ent)~0.0
Buffer zone (site dependent)~0. 0-500.0 ft
Fraction of nitrogen loading denitrif ied~15. 0-25.0%
Ammonia volatilization~0.0%
Removal of phosphorus-80.0%
Slope on cultivated land~20.0%
Slope on noncultivated land~40.0%
NW Number of recovery wells
WDIA Diameter of recovery wells
DW Depth of recovery wells
PS Cost of standard 3000 gpm pump and driver unit -
default value = $17,250.0
SP Cost of 12-inch welded steel pipe in-place -
default value = $12.80 per foot
SV Cost of 12-inch butterfly valve -
default value = $952.10
EN Cost of 6-15 gpm impact type rotor pop-up full circle
sprinkler - default value = $61.65
CG Cost of clearing and grubbing - default value =
$3000.00 per acre
MW Cost of 4-inch water well - default value = $8.00 per foot
PC Cost of center pivot 100 acre sprinkler system -
default value = $27,690.00
b. Default Data
FORAGF
APPLICATION KATF AVFKAGF ?.0 TKI/V.TFK MAX T Ml IV O.?(l IN/HR
PRKCIPI1 A] TOM f'ATF O.R TN/WFFK
n.n IM/WFFK
WASTFt.ATt-K GFI.r^ATlOf! PFRlon 364.0 OAYS/YR
FIFLI) APPi.ICATIOfi PF'?I:)0 52.0 WFFKS/YW
SOLID bFT PIPING Ann Puvpifjf,
NO STuK/iGF
NO r< 70MS-- 0.0 FFFT
r.u.w-;t,T GKouni, CCVFR FORFST ?o.o ^ HPUSH ^o.n * PASTURF sn.n*.
SI.OPK p ri prr?rFiMT
MONlTOfnNf, WfLLS 9 WFI.LS AT 10JFT/WFLI
2.7S 1./FT
HOURS Ph» HAY OPH.ATJOtJ ftlo HODRS/nAY
FSTIMATK
3 - 126
-------
Slow Infiltration Land Treatment Unit Process Data Cards
SLOW INFILTRATION LAND TREATMENT MOD xx
FORAGE GRASSESa
CORN3
APPLICATION RATE AVERAGE xx.x IN/WEEK MAXIMUM xx.x IN/HOUR
PRECIPITATION RATE xx.x IN/WK
EVAPOTRANSPIRATION RATE xx.x IN/WK
RUNOFF xx.x IN/WK
WASTEWATER GENERATION PERIOD xx.x DAYS/YR
FIELD APPLICATION PERIOD xx.x WKS/YR
SOLID SET PIPING3
CENTER PIVOT PIPING3
NO STORAGEb
STORAGEb'C (MINIMUM) xx.x DAYS/YEAR
LINER REQUIRED0 xx.x $/SQFT
EMBANKMENT PROTECTION0 xx.x $/CUFT
NO RECOVERY SYSTEMd
UNDERDRAIN RECOVERY SYSTEM*1
BUFFER WIDTH xx.x FT
CURRENT GROUND COVER FOREST xx.x% BRUSH xx.x% PASTURE xx.x%
SLOPE xx.x PERCENT
MONITORING WELLS NO = xx.x DEPTH/WELL = xx.x FT
FENCING xx.x $/FT
FRACTION DENITRIFIED xx.x PERCENT
AMMONIA VOLITILIZATION xx.x PERCENT
SOIL RETENTION xx.x PERCENT
HOURS PER DAY OPERATION xx.x HOURS
DAYS PER WEEK OPERATION xx.x DAYS
ESTIMATE PS xx.x SP xx.x SV xx.x EN xx.x CG xx.x MW xx.x PC xx.x
END
Use solid set or center pivot, not both.
Use storage or no storage, not both.
Liner or embankment protection should only be used with storage.
not
3-127
Use underdrain or no recovery, not both.
-------
3-55. Sludge Flotation (see page 5-41 of Design Manual)
a. Design Parameters
Air pressure~40-70 psig
Detention time in float tank~0.25-0.5 hrs
Solid loading (determine from laboratory tests)
2
Hydraulic loadings;!.0-4.0 gal/min/ft
Recycle time in pressure tank«l.0-3.0 rain
Percent removal of solids (determine from bench test)«80.0
Air/solids ratio (determine from laboratory test)
Float concentration (determine from bench test)«5.0%
Removal of BOD (determine from bench test)
Removal of COD (determine from bench test)
Removal of TKN (determine from bench test)
Polymer dosage required~10.0 Ib/ton dry solids
IN FLOAT TANK
b. Default Data
FSTIMATF
DFTFNl ION Tl
SOI. ID LOADING
HYORAULIC I OAfilNG
PFCYCLF TJVF. IN PMFSS TANK
PFUCL'NT R[>OVAL OF SOLIDS
AIR/SOLIDS RATIO
FLOAT CONCFNTRMION
POI YMf-R RL'OUIKF.n
60
3
0
?.
2
fl5
0
02
LM/TON
PS If,
HRS
LH/SCFT/OAf
RPf-VSOFT
VIM
PERCFMT
PERCFNT
3-128
-------
c. Sludge Flotation Unit Process Data Cards
SLUDGE FLOTATION MOD xx
AIR PRESSURE xx.x
DETENTION TIME IN FLOAT TANK xx.x
SOLID LOADING xx.x
HYDRAULIC LOADING xx.x
RECYCLE TIME IN PRESS TANK xx.x
PERCENT REMOVAL OF SOLIDS xx.x
AIR/SOLIDS RATIO xx.x
FLOAT CONCENTRATION xx.x
POLYMER REQUIRED xx.x
ESTIMATE3 COSTFS = xx.x
END
PSIG
HRS
LB/SQFT/DAY
GPM/SQFT
MIN
PERCENT
PERCENT
LB/TON
COSTFS = Cost of standard 350-square foot air flotation unit -
default value = $44,200.
3-129
-------
3-56. Sludge Hauling and Landfilling (see page 5-169 of Design
Manual)
a. Design Parameters
Distance to disposal site (based on local conditions)
Hours per day working schedule~6.0-8.0 hours
Loading time per vehicle~0.2-2.0 hrs
Hauling time (based on local conditions)
b. Default Data
DISTAhCF To DISPOSAL '->TTF 10 .
HOUR::> PF'K HAY 8 HOURS
I OAOIUG TIvF K-T< VFHICLF 0.75
HAiJl I,\0 TiMF' PF^ TrMP l.(l HOUR
FSTI'^ATF 0.0 MOOD 1>/YR
3-130
-------
c. Sludge Hauling and Landfilling Unit Process Data Cards
HAULING AND LAND FILLING MOD xx
DISTANCE TO DISPOSAL SITE xx.x MILES
HOURS PER DAY xx.x HOURS
LOADING TIME PER VEHICLE xx.x HOURS
HAULING TIME PER TRIP xx.x HOURS
ESTIMATE3 COSTSSV=xx.x CYC=xx.xb CPCY=xx.xb CPT=xx.xb
END
aCOSTSSV = Cost of standard 22 cubic yard vehicle - default
value = $51,700.
CYC = Constant annual charge for landfill, $/year.
CPCY = Cost of sludge disposal per cubic yard, $/Cu Yd.
CPT = Cost of sludge disposal per ton, $/ton.
One of the three land fill charges must be specified; the other
must be specified as 0.0.
3-131
-------
3-57. Step Aeration Activated Sludge (see page 7-69 of Design
Manual)
a. Design Parameters
Eckenfelder's Approach
Reaction rate constants
k, BOD removal rate constant~0.0007-0.002 5,/mg/hr
a, fraction of BOD synthesized~0.73
V
a , fraction of BOD oxidized for energy=0.52
b, endogenous rate (oxygen basis)«0.075/day
V
b , endogenous rate (sludge basis)*0.15/day
f, nonbiogradable fraction of VSS in influent~0.40
7
£ , degradable fraction of the MLVSS-0.53
F/M ratio~0.2-0.4
Mixed liquor suspended solids~2000-3500 mg/&
Mixed liquor volatile solids~1400-2450 mg/5,
Temperature correction coefficientsl.0-1.04
Effluent BOD soluble~10 mg/£
ALPHA 0- transfer in waste/02 transfer in water«0.90
BETA 0- saturation in waste/02 saturation in water~0.90
HP Horsepower per 1000 gallons^ 0.10 hp/1000 gal
STE Standard transfer efficiency
Mechanical Aerators~2.0-3.5 Ib 0-/hp-hr
High speed=2.0
Slow speed=3.5
Diffused Aerator=6.0-11.0%
Coarse bubble~6.0
Fine bubble^ll.O
b. Default Data
K=0.001P. A=0.73 AP=O.S2 R=0.07h HP.O ,,^^0.^=0.5,
SSr^OD VS=17SO ' M6/I
COFFFICIENT 1'03S MG/|
o.9 HP=0.0 W/Tfi STE=3., LH 0/HP
3-132
-------
c. Step Aeration Activated Sludge Unit Process Data Cards
STEP AERATION ACTIVATED SLUDGEa MOD xx
V V V
CONSTANTS K=xx.x A=xx.x A =xx.x B=xx.x B =xx.x F=xx.x F =xx.x
F/M RATIO xx.x LB BOD/LB VSS
MIXED LIQUOR SS=xx.x VS=xx.x MG/L
TEMPERATURE COEFFICIENT xx.x
EFFLUENT BOD SOLUBLE xx.x MG/L
CHANICAL AERATION AI
STE=xx.x LB 0/HP-HR
MECHANICAL AERATION ALPHAb=xx.x BETA=xx.x HP=xx.x HP/TG
DIFFUSED AERATION ALPHAb=xx.x BETA=xx.x AFC=xx.x CFM/TG
STE=xx.x PER
ESTIMATE*1 SSXSA = xx.x COSTPH = xx.x COSTPS = xx.x
END
User must also specify secondary clarification (activated sludge).
Use mechanical or diffused, not both.
p
AF (minimum airflow) specifies a lower limit on airflow. Model will
calculate actual airflow and compare it with input value. Higher
value will be output. Input zero for AF to obtain calculated value
only.
SSXSA = Cost of standard slow-speed pier-mounted 20-hp aerator -
default value. = $16,300.
COSTPH = Cost of standard 550 scfm swing arm diffuser - default
value = $5,000.
COSTPS = Cost of standard 3000 gpm pump and driver unit - default
value = $17,250.
3-133
-------
3-58. c (se
a. Design Parameters
Desired effluent-BOD 15.0-30.0 mg/£
Recirculation ratio*!. 00-1. 20
Default Data
ESTIMATF FILTFR MFHIA COST 3.0 -5/CUFT
OFSIRFO ETFLUFflT 3n.O Mfi/L
RFCIKCULATION RATIO 1.?
3-134
-------
c. Trickling Filtration Unit Process Data Cards
TRICKLING FILTRATION3 MOD xx
DESIRED EFFLUENT BOD- xx.x MG/L
RECIRCULATION RATIO xx.x
ESTIMATE13 UPFM=xx.x $/CUFT CODAS=xx.x COSTPS=xx.x
END
o
User should also specify secondary clarification (trickling
filters).
UPFM = Cost of selected plastic media per cubic foot, installed
default value = $2.50 per cubic foot.
CODAS = Cost of standard 50-£oot diameter distributor arm -
default value = $39,000.
COSTPS = Cost of standard 3000 gpm pump and driver unit -
default value = $17,250.
3-135
-------
3-59. Vacuum Filtration (see page 5-119 of Design Manual)
a. Design Parameters
Chemical dosage 1.0%
Hours per day 8.0-16.0 hrs
Loading rate (see Table 3-23)
Table 3-23. Expected Performance of Vacuum
Filters Handling Properly Conditioned Sludge
Type of Sludge Yield. Ib/ft2/hr
Fresh solids
Primary 4 to 12
Primary plus trickling filter 4 to 8
Primary plus activated 4 to 5
Activated (alone) 2.5 to 3.5
Digested solids (with or without elutriation)
Primary 4 to 8
Primary plus trickling filter 4 to 5
Primary plus activated 4 to 5
From Simpson, 1964
b. Default Data
FSTIMATE
DRY WT
HOURS PFR DAY fl HOURS
LOADING RATE 3.5 LB/SQFT/HR
3-136
-------
c. Vacuum Filtration Unit Process Data Cards
VACUUM FILTRATION MOD xx
CHEMICAL DOSE xx.x
DAYS PER WEEK xx.x
HOURS PER DAY xx.x
LOADING RATE xx.x
ESTIMATE3 COSTSF=xx.x
END
PERCENT DRY WT
DAYS
HOURS
LB/SQFT/HR
COSTSF = Cost of standard 300-square foot vacuum filter -
default value = $150,000.
3-137
-------
3-60. Wet Oxidation
a. Design Parameters
Sludge COD=20.0-40.0 mg/£
Saturated stream pressure (determine from standard steam
tables; see Figure 3-14 below)=600.0-3000.0 psia
Specific volume of saturate steam (determine from standard
steam tables; see Figure 3-14 below)=1.446 ft3/lb @ 450°F
COD removed=60.0-90.0%
Temperature of reactor 250.0-700.0°F
Retention time (from Figure 3-14)
Temperature Pressure
5?2F 1300.0
600.0
220.0
Specific
Volume
0.33
0.77
2.00
67.00
14.697
6.50
26.80
1 2
Time, hours
Figure 3-14. Material Oxidized Versus Time
at Various Temperatures.
b. Default Data
SLUOGF COD
SATURATI-D mFAM PflFSSUKF
SPFCK-IC VOLUNit-: CF STEAM
COD RFMOVFn
.
RFTENTION TIMF
30.0
f.00.0
0.77
75.0
ilo
Mfi/L
CUFT/I n
PFRCFMT
DFGHFFS F
HOURS
3-138
-------
c. Wet Oxidation Unit Process Data Cards
WET OXIDATION MOD xx
SLUDGE COD xx.x
SATURATED STEAM PRESSURE xx.x
SPECIFIC VOLUME OF SATURATE STEAM xx.x
RETENTION TIME xx.x
COD REMOVED xx.x
TEMPERATURE OF REACTOR xx.x
END
GM/L
PSIA
CUFT/LB
HOURS
GM/L
DEC F
3-139
-------
APPENDIX A
BASIC PROCEDURE FOR USING CAPDET
A-l. This section provides the user with a comprehensive outline of a
recommended procedure for using the CAPDET program. The ten recommended
steps are intended to illustrate to the user the logical sequence of
events which will allow the user to accurately describe a proposed treat-
ment scheme to the CAPDET program.
A-l
-------
BASIC PROCEDURE FOR USING CAPDET
1. From the list on page 2-9 select those treatment processes which are
to be investigated. Make a sketch showing the treatment scheme in-
cluding in each treatment process block those options or alternatives
to be used.
EXAMPLE:
LIQUID LINE
INFLUENT
PRELIMINARY
TRE3THEST
J PR1HP.RY
| CLfirtlFICRuGN
1
1
STEP RERRHGN
GR
TRKKLING
FILTER
. rmnRlNRTTflN EFFLUENT
I
SECBNORflY SLUDGE LINE
mx SECC:;DSRY
SLUDGE RT THE
cEGI.'.-'.'lliG Cr
TF.c PRItlSRY
SLUDGE LINE
PR1KSRY SLUDGE LINE
R5RG3IC
CiGESTiSN
Cfl
F.NSr?.:3!C
CIGESTI::I
CRYIt.'G
BEGS
HS'JLING
RKD
LfiKO
FILLING
A-2
-------
2. For each treatment process selected, list the unit process key words
associated with the treatment processes and identify the unit process
involved by referring to the list on page 2-3.
EXAMPLE:
Treatment
Process
Key Word
PRELIM
Associated
Unit Process
Key Words
GRIT R
SCREEN
COMM1N
Unit Process
Name
Grit Removal
Bar Screens
Communition
PRIMAR
STEP A
TRICKL
CHLORI
A MIX
AEROBI
ANAERO
DRYING
HAULIN
PRIMAR
STEP A
A SECE
TRICKL
T SECO
CHLORI
None
AEROBI
ANAERO
DRYING
HAULIN
Primary Clarifica-
tion
Step Aeration
Secondary Clarifica-
tion (Activated
Sludge)
Trickling Filter
Secondary Clarifica-
tion (Trickling
Filter)
Chlorination
None
Aerobic digestion
Anaerobic digestion
Drying beds
Sludge hauling and
land filling
A-3
-------
3. In Chapter 3 review the default data supplied for modification zero for
each of the unit processes you have listed in 2 above. For each process
in which you wish to change data code a unit process header card for
the process and data for those items you wish to change. Close the in-
put for each process with an END card. Be sure to include an ESTIMATE
card if you wish to retain estimate type costing.
EXAMPLE: After examining the default data you wish to change the
sidewater depth of the primary clarifier and the rainfall
for drying beds, code the following data.
PRIMARY CLARIFICATION
SIDEWATER DEPTH 10.0 FEET
ESTIMATE
END
DRYING BEDS
RAINFALL 6 IN/MO
ESTIMATE
END
4. Code a TITLE card.
EXAMPLE:
TITLE EXAMPLE PROBLEM
5. Refer to the sketch in 1 above and code the scheme description as
outlined in section 2-5.
EXAMPLE:
LIQUID LINE
BLOCK PRELIM
BLOCK PRIMAR
BLOCK STEP A TRICKL
BLOCK CHLORI
SECONDARY SLUDGE LINE
BLOCK A MIX
PRIMARY SLUDGE LINE
BLOCK AEROBI ANAERO
BLOCK DRYING
BLOCK HAULIN
A-4
-------
6. Examine the default data for the waste influent (page 2-15) and
select those items you wish to change. Code a waste influent
header card and data cards for those items you wish to change.
EXAMPLE: After examining the waste influent default data you wish
to change the BODS to 300 mg/1 and the oil and grease to
zero. You wish an average flow of 10 mgd. You should
code the following:
WASTE INFLUENT
AVERAGE FLOW 10.0 MGD
BODS 300 MG/L
OIL AND GREASE 0 MG/L
Code a desired effluent header card and data for those items you wish
checked. Those trains that do not meet the specified effluent values
will be discarded. If you have specified only a few trains you should
use this option with care as over-rigid specifications may cause all of
the alternative trains to be discarded.
EXAMPLE: As only four trains have been specifit in this sample
problem, no desired characteristics wilj. be specified.
This will allow all four trains to be retained. You may
examine them for effectiveness after they are printed.
In this case we will only have to code the desired
effluent header card as follows:
DESIRED EFFLUENT CHARACTERISTICS
A-5
-------
8. Review the unit cost default data (page 2-19) and select those
items you wish to change. Code these data items following a unit
cost header card and terminate this input with an END card.
EXAMPLE: You wish to change the building costs, excavation costs,
concrete costs, and the Marshall and Swift and EPA
indices. You should code the following:
UNIT COSTS
BUILDING 42.0 $/SQFT
EXCAVATION 1.75 $/CUYD
WALL CONCRETE 275.0 $/CUYD
SLAB CONCRETE 230.0 $/CUYD
MARSHALL AND SWIFT 490.0
SMALL CITY EPA INDEX 140.0
END
9. Refer to section 2-7 arid select the type of output you desire. Code
the appropriate output control cards followed by the GO card.
EXAMPLE: You desire the cost information for all four trains and
complete design information including construction quantities
for the most cost effective train. You should code the
following:
CONTROL CARDS
LIST 4 TRAINS
PRINT TRAIN NO 1
OUTPUT QUANTITIES
GO I = 6.625 30 YEARS
A-6
-------
10. Assemble all data in the order coded above and submit to the CAPDET
program.
EXAMPLE: The complete data list for the example coded above would
be:
PRIMARY CLARIFICATION
SIDEWATER DEPTH
ESTIMATE
END
DRYING BEDS
RAINFALL
ESTIMATE
END
TITLE EXAMPLE PROBLEM
LIQUID LINE
BLOCK PRELIM
BLOCK PRIMAR
BLOCK STEP A TRICKL
BLOCK CHLORI
SECONDARY SLUDGE LINE
10.0
BLOCK
A MIX
PRIMARY SLUDGE LINE
BLOCK AEP.OBI ANAERO
BLOCK DRYING
BLOCK HAULIN
WASTE INFLUENT
AVERAGE FLOW
BOD5
OIL AND
DESIRED EFFL
UNIT COSTS
BUILDING
EXCAVATION
WALL CONCRETE
SLAB CONCRETE
MARSHALL AM) SWIFT
SMALL CITY EPA INDEX
END
CONTROL CARDS
LIST
PRINT TRAIN NO 1
OUTPUT QUANTITIES
GO 1=6,625
10.0
300
0
CHARACTERISTICS
42.0
1.75
275.0
230.0
490.0
140.0
FEET
IN/MO
MGD
MG/L
MG/L
$/SQFT
$/CUYD
$/CUYD
$/CUYD
TRAINS
30 YEARS
A-7
-------
APPENDIX B
CAPDET EXAMPLE PROBLEM OUTPUT
B-I. This section provides the user with the output of the example
problem outlined in Appendix A.
B-l
-------
COST ANALYSIS INPUT PARAMFTFRS
IHTFKEST RATE 6.f>? X
Pi ANNING PERIOD 3ft YRS
KAGf RATE 6.00 S/HR
UNIT PRICFS AND COSTS INOICFS
nuuniNG
EXCAVATION
WAI. I. CGHrRFTE
SLAP. CGMfRFTF
MARSHALL AND SWIFT
INDEX
.EPA COnSTPUCTION COST
CANOf'Y RrOF
INDEX
i AHPR KAIF
OPf-RATOR CLASS
TLKCTR1CTTY
CHEMICAL COSTS
ALUM
IKON SAI TS
POI YMhH
FfJGIfjFt -RING
HANHRAIL
PIPF COST INDEX
PIPF Il.bTAI L.ATI
FIGHT I UfH PIPE
FIGHT INCH PIPF
F IGHT irJCM PIPF
FIGHT INCH PIPl
II
RK.rORfj COST IMDFX
N LABOR RATF
REND
TEE
VALVE
>?.00 */SQ FT
1 .75 'B/CU YD
TO t/CU YD
230.00 t./CU YD
FT
40.00 $/HR
140.00
10. Of) ^/SO
h.OO -B/HR
f,.00 S/HR
.04 t/KWHR
.02 "S/LR
.10 -S/LP.
.18 S/LR
1 .00 "5/LR
?47f). 00
?5.20 -5./FT
241.00
10.00 ti/HR
7.41 "S/FT
7(1.Hfl 'B/DNIT
lOU.90 1,/UNIT
1099.00 't/UNIT
B-2
-------
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-------
EXAMPLE PKORLEM TRAIN MO
INFLUENT
LIQUID CHARACTERISTICS
FLOW (MGn) SOLIDS (MG/L) (Mfi/L) (WG/l )
MAXIMUK 10.0000 SUSPRJDFD 200.00 RODS .100.00 TKN US. 00
AVERAGE 10.0000 VOLATILF 60. nO % ROD5S 75.00 NH3 ?5.00
MiiJiMUK in. oooo SFTTLFABLF is.oo con soo.oo NO? .00
CODS 400.00 M03 ,00
TFMP Ifl.O C OIL R GREASE .00 P04 18.00
PH 7.60 CATIOrJS 160.00
AM IONS 160.00
SLUOGE
PRIMARY SECONDARY
V/OI IJMt (GAL/0) .00 .00
* SOLIDS .00 .00
* VOLATILF .00 ,00
B-4
-------
EXAN.PLE PROflLEM TRAIN NO
*********************.*****************
MECHAMCALl Y CLEANED RAR SCREEN
0 BAR SIZE .2504-00 IN
[) HAH SPACING .150 + 01 IN
D SLOFF- OF RARS FROM HORIZONTAL .300 + 02 DFG
HeAn LuSS THROUGH SCREEN .206-01 FT
i) APf-hOACH VELOCITY .250 + 01 FPS
L) AVf RAGL FLO.'J TnROUGH VELOCITY .250 + 01 FPS
[) f'-«Xir-,U:V, FL Oiv1 THROUGH VELOCITY .300+01 FPS
SChTt-N O.AtJNiFL WIDTH .616+01 FT
0 fiVFKAGt THANrJEL DEPTH .100+01 FT
B-5
-------
EXAMPLE PRORLEM
TRAIN NO
********************
HORIZONTAL FLOW GRIT CHAMBER
MAXIMUM FLOW
AVFKAGF. FLOW
MINIMUM FLOrt
TEMPFFATURE
0 VAXH'.Uf-i PLOd THROUGH VELOCITY
D AVFRAGF. FLOW THROUGH VELOCITY
u SI^F SMAIL. PART, loox REMOVED
0 SPFCIFIC GRAVITY OF PARTICLF
U hUMFU R OF UNITS
MAATMJM FLOjf/UNIT
D 1*II)TH OF CMANNFL
D DEPTH OF CHANNEL
LENGTH OF CHANNEL
SETTLING. VELOCITY OF PARTICLE
SLOPT Of- CMANIJI.L OOTTOM
0 ALLO/.ANCF FOR CURRENTS
[) fjETFMTlOM TIME
0 MANMNb COFFFICIENT
VOLUME OF GI?IT
***.***************
CFS
CFS
CFS
DE3
FPS
FPS
MM
,154+02
.1RO+02
,100+01
,200+00
20U+01
770+01
400+01
Kifl + 03
7RS-01
9'»7-t!3
170+01
867+0?
350-01
400+02
CFS
FT
FT
FT
FPS
SEC
CUFT/DA
*****
****************
B-6
-------
EXAMPLE PROHLEM
*********************
COMMINUTION
D NUMRER OF UNITS
DRUM DIAMETER
DRUM RPM
AV/tRAGt SLOT 'JIDTH
HOKSEPU'A'FR/UNIT
STANDARD HEIGHT
STANDARD NET WtlfiHT
*****
TRAIN NO
!• * * * *
.POO+01 UNITS
.?bO+02 INCHES
.?bO+02 REV/MIN
.Sum 00 INCHES
.lbO+01 HP
.S79+01 FEET
.P10+04 POUNDS
* *
******************************
LIQUID CHARACTERISTICS
FLOW
MAXIMUM
AVFRAf.F
MINIMUM
TEMP
PH
(MGf))
1 n . n D o o
in . o o o o
in.uooo
18.0 C
7.bO
SOLIf)S (MG/l )
bUSPf. rjHED 200.00
VOLATILE 60.00 %
SFTTLFIABLF 15.00
OIL (, GREASE .00
CATIONS ifio.oo
Ah IONS 160.00
ROP5
ROCSS
cnc
CODS
P04
(MG/L)
300.00
75.00
soo.on
400.00
18.00
(MG/L)
TKN U5.00
NHS P5.00
N02 .00
ri03 .00
VOIUMt (GAL/D)
* SOLIDS
* VOLATILE
SLUDGE CHARACTERISTICS
PRIMARY SECONDARY
.00 .00
.no .00
.00 .00
B-7
-------
EXAMPLE PROBLEM TRAIN NO
**************************************
PRIMARY CLARIFIER
CIRCULAR CLARIFIER
0 OVFRFLOlv RATE .100+Ot GO/SOFT
SURFACE ARFA .100+05 SOFT
I Slf)F V;ATFR DEPTH .lOu+02 FT
hLTKhTlOn TIME .180*01 HOURS
SOL 10 LOADING .167+01 PSF/D
0 '..tIR LOADING .150+05 GD/FT
ir,ElR LLNf.TH .667+03 FEET
VOt IJI..F OF SI UDuE PRODUCFO .??>Hf05 GAL/HAY
u subPFNi/en s<)Liijs RLVOVAL .500+02 %
0 HOfi KF.MOVAL .360 + 02 «
NUl/.MtR Ot- TANKS .100 + 01 UNITS
Q CUf; KFMOVAL .500+02 »
U TKN RCN.OVAL .500 + 01 X
i) POit REMOVAL .500 + 01 «
**************************************
B-8
-------
EXAMPLE PROBLEM
QUANTITIES FOR SEDIMENTATION
CIRCULAR ClAFUFIER
PRIMARY CLARIFIER
EXCESS CAPACITY FACTOR
CALCUlATtU SURFACE ARFA
ADJUSTED SURFACE AREA
AVERAGE DAILY V.ASTF.VATER FLOW
.gUf'-rti-R OF riFJCULAR CLARIFIERS
rJUMUR OF MATTER iES
SUf^FACL ARFA PER UNIT
UTAMi-ThP OF UNIT
EARTHWORK REQUIRED
SIOL*ATEK DEPTH
TulCKM SS OF THE SLAB
.vAL L THICKNESS
TOTAL QUANTITY OF R.C. WALL REQUIRED
TOTAl UUAN1ITY OF H.C. SLAM RF1UIRFD
MA TNTrtiA^Cl-- MANPO^F« RE
OHFRnTIOij N.AUPO.-.'FR REOUIHED
ELFCTPJCAL FNFRoY RtGUIRE.D
TRAIN NO
.192+01
.100+05
.192+05
.100+02
2
1
.960+04
.111+03
,2(V)+06
.100+02
.lO'H-02
.1PO+02
.fl2U+OU
. iay+os
,8.V)+03
.1SP+01
.119+05
SOFT
SOFT
wen
SOFT
FT
CUFT
FT
INCHES
INCHES
CUFT
CUFT
MAN-HDUHS/YR
MAN-HOURS/YR
KWHR/YR
FLOW (N'GD)
MAXlMINi in.0000
AVFUAGF: Id. 1)000
MINIMUM in. DO00
TEMP
PH
1H.O C
7.(SO
LIOUID CHARACTFRISTICS
SOLIDS (WG/L)
SIISPI.MDFO 10(1.00
VOLATILE 60.00
SFTTLEAHLF .00
OIL « GRFASE
CATIONS
.00
ifto.no
160.00
RODS
•A 00 55
coo
CODS
P04
(MG/L)
219,
75,
400,
17,
on
oo
oo
oo
10
(MG/L)
TKN 44.00
WHS P5.00
MO? .00
(J03 .00
VOl.Uf/E (GAL/D)
1* SOLIDS
*• VOLATILE
SLUDGF CHAPACTFRISTICS
PRIMARY SFCOMHARY
P3809.52 .00
4.00 .00
oO.OO ,00
B-9
-------
EXAMPLE PRORLEM TRAIN NO
************************.*
TRICKLING FILTRATION
REMOVAL EFFICIENCY .R63+02 %
TOTAL VOI UMF .109+06 CUFT
TOTAL SURFACE ARFA .18U+Q5 SOFT
DEPTH .llfl+02 FT
O RECJRCULATION KATIO .120+01
nlAMKTtiR/UUIT ,10flf03 FT
UUMHER OF UNITS .200+01 UfJITS
B-10
-------
EXAMPLE PRORLEM
TRAIN NO
QUANTITIES FOR TRICKLING FILTER
TOWFR
OF TOWERS
V/OI.UN.F PER FILTER
DEPTH OF Tf/A/EH
DlAMFTtR OF FILTER TOWER
TOT At MllwUFR OF POSTS
LENGTH OF
K.C. WALL
K.C. SLAB
TOTAL LENGTH OF PRECAST REAMS
TOTAL K.C. WALL IN PLACE
TOTAL K.C. SLAB I!J PLACE
TOTAL tAKTuwoRK REQUIRED
AVn
-------
EXAMPLE PRORLEM
QUANTITIES FOR INTERMEDIATE PUMPING
AVERAGE UATLY WASTFWATER FLOW
DESIGN CAPACITY PEH PUMP
NUMBER OF PUMPS
IJUiVHFR OF RATTERIES
AHFA OF PUfP HUILDING
V/OLUNF OF FARTH.VORK (iFQUIRED
FIM^I PUVPlKifi CAPACITY
OPfUATINb f. AUPOi-.fR REQUIKED
MATMTf-UAIN.CF MANPOdFR PEOUIREO
ELFCTR1CAL FNFRjY HEGUIRfcD
TRAIN NO
.100 + 02 MGT)
.H17+QH RPM
3
.877+03 SO FT
.701+04 CU FT
.l?n+02 MfiO
.677+03 MAN-HOURS/YR
.572+03 MAI1-HOURS/YR
.666+06 KWHR/YR
B-12
-------
EXAMPLE PROBLEM
SECONDARY CLARIFIER
CIRCULAR CLARIFIER
D SOLIDS LOADING RATE
SURFACt OVFRFLOW RATE
Di-ITFNTlON, TIME
H i-.EIR OVFPFLOW RATE
3 TANK SIDF'AAIEU DFPTH
l.EIR LtiNGTH
VJLt.ME OF WASTFI) SLUDGF
U iJNDFKFLO'.v CONCI- i-JTRATION
TOTAL bUi'FACE ARKA
BUMPER OF TANKS
.ISO+n? LR/SOFT/n
fi/SOFT/0
HOURS
G/FT/0
.900+01 FEET
. 1U7 + 04 FEET
. HdO + O't G/DAY
.10U+nl X
,2?l) + n5 SOFT
.ino + ni UNITS
* * *
* *
4 * * ******************
* * * *
B-13
-------
EXAMPLE PROBLEM
QUANTITIES FOR SEDIMENTATION
TRAIN NO
CIRCULAR CLARIFIER
SECONDARY CLARIFIER
EXCESS CAPACITY (-ACTOR
CALCUl ATLD SURFACE AKFA
AUJUSTt-n Sl'RFACE AREA
AVfKAttt- DATL Y riASTFfl/ATER FLOW
NUMLiKFv OF CIRCULAR CLARIFIERS
iMU?.'BH> OF RATTFR1ES
SURFACE ARFA PF R UNIT
UIAMtTl.R OF UNIT
EAKTH'AURK RFfjUIRfcO
blDEi'.ATEK DEPTH
ruiCKf.tSb OF THE SLAtJ
WALL ThlCKUFSS
TOTAL. QUANTITY OF
TOTAl (.UAiJTITY 01-
MrtIinpl.Ai-.Cr r/
UPI-RATIOU ^AfJPO.a
ELFC1K1CAL FUFRGY
R.C
.<.C
RFOUIhTD
WALL
f,LAn
RFOUlRFD
RFOUIRFD
.193+01
.220+05
.425+05
.100+02
2
1
.212+05
.165+03
.697+06
.900+01
.101+02
.115+02
.I0h+05
.399+05
.136+04
.244+04
.189+05
SOFT
SOFT
MfiO
SOFT
FT
CUFT
FT
INCHES
INCHES
CUFT
CUFT
MAM-HOURS/YR
MAN-HOURS/YR
KWHR/YR
FLOW (
MAXIMUM 1(1.0000
AVFUAGt 10.0000
MifJlMUl IP,. OOOO
PH
MP
18. U C
7.60
LIQUID CHARACTFRISTTCS
SOLIUS (MG/L.)
SUSPI Nutn 20.00
VOLATILE RO.OO *
SFTU.EAPLF .00
OIL ft GREASE .00
(MG/L)
ROD5 30.00
ROD5S 15.00
con 45.00
CODS 22.50
P04 11.97
CATIONS 160.00
AMOKS 160.00
TKM .^O.fiO
NH3 30.80
r:0? .00
N03 .00
(GAL/0)
SuLTQS
VULAT
ILK
SLUDGE CHARACTERISTICS
PRIMARY SECONDARY
2 ^000.00
4.00 1.00
uO.QO 80.00
B-14
-------
EXAMPLE PROBLEM TRAIN NO
***************************************
CHLOHINATION
MAXIMUM FLOW .lOn+02 MGD
AVFRAGt H.OW .t00+02 MGD
0 COhTACT TIME .300+02 MIN
TOTAL VOI UVF .?08t06 GAL
AVFPAGt CHLORIfjE RERUIHKMENT .P34 + 03 LIVOAY
PLAK CHLC.RIUF REOUIREMFNT .H.i4+o3 LR/DAY
COLIt-OHM REOUCTION .996 + 02 %
B-15
-------
EXAMPLE PRORLEM
QUANTITIES FOR DISINFECTION
NUMFJFR OF CHLORINATORS AND EVAPORATORS
CHI OhTNATlON BUILDING AREA
[JUt/BHR OF CHLORINE CYl INUERS
ARFA OF CHI OKINE STORAGE BUILDING
AVFRAGE DAI.Y WASTFVuATER FLOW MGO
VOlUiVF OF FARTh,',(;RK RFQU1RED
VOtU,4r OF R.C. FOR WALLS
VCI UNiF CF R.C. FOR Si AH
ChLOKTf.E RFGUIREMEUT PER YEAR
OPFUATIOIviAl LABOR
MAIMTFUANCF MANPo'wFR REQUIRED
ELECTRICAL FUFRviTr KEQUlRtn
CHI OKIfjE HFOUIRc'MEfJT
0 fi M MATERIAL AixiO SUPPLY COSTS
TRAIN NO
1
.220+03
13
.182+04
.100+02
.144+05
,56fS+04
.307+04
.15?+03
.14b+04
.363+03
.131+06
.834+03
.313+01
SOFT
SOFT
MGD
CUFT
CHFT
CUFT
TONS/Y9
MAN-HOURS/YR
MAN-HOURS/YR
KWH/YR
LR/DAY
PERCENT
FLOW
MAXlViliM 10.0000
AVERAGE 10.01)00
MINIMUM If!. 0000
LIQUID CHARACTFRISTTCS
TEH'P
PH
lfl.0 C
7.63
SOLIOS (MG/L)
suspFNiiF.n 2n.no
VOLATILF fio.oo %
SFTTLEAHLF .00
OIL e. &PEASE .00
CATIONS i^o.oo
AMOI^S 160.00
(MG/L)
Rons 30.00
ROD5S 15.00
COD 45.00
COPS 22.50
P04 11.97
(MG/L)
TKM 30.flO
MH3 30.RO
i^n? .00
N03 .00
VOLUVE (GAL/D)
*. SULIDS
*. VOLATILE
SLUOGF CHARACTFRTSTICS
PRIMARY SFCONDARY
23009.52 ^000.00
4.00 1.00
60.00 80.00
B-16
-------
EXAMPLE PRORLEM TRAIN NO
**************************************
**** SECONDARY SLUOGE LINE MIXED INTO PRIMARY SLUDGE LINE ****
TEMP
PH
FLOW
MAXIMUM in. 0000
AVFRAGE io.noon
MiMK-iUf-' 10.0000
in.o c
7.60
INFLUENT
LIQUID CHARACTFRISTICS
SOLlbS (MG/L)
SUSPKIOFD 20.00
VOLATILF 80.00 *
SFTTLEARLF .00
OIL « (iRFASE .00
CATIuMb 160.00
ANIONS 160.00
(MG/L)
ROD5 30.00
nnnss 15.00
COD U5.00
cons 22.50
P0<4 11.97
(MR/I )
TKN .^0.00
MH3 ,^O.flO
MO? .00
NOS .00
VOI UME (GAL/0)
a suLins
* VOLATILE
SLUDGE CHARACTFUTSTICS
PKIMAWY SFCONDAPfY
31809.52 .00
3.?5 .00
f>l.55 .00
B-17
-------
EXAMPLE PRORLEM
TRAIN NO
* *
***************************
AEROFUC DIGESTION
RAW SLUDGE SPECIFIC GRAVITY
D DETENTION TIME
0 VOLATILE SOLIDS [lESTROYED
0 MIXFU LIOUOR SOLIDS
i) SOLIDS ir, DIGESTED SLUDGE
Q ALPHA
D F1ETA
I) STANDARD TRANSFER EFFICIENCY
LOAOING
SOLILS ACCUMULATFO PER GAY
nlGFSTLR CAPACITY
VOU IMF UP V.ASTKO SLUDGE
C.OLH-S RFTruTIOU TU'E
OX>fiLN R
AIR SUPPI Y
.105+01
.150+02 DAYS
.500+02 %
.120+05 MG/L
.250+01 %
.900+00
.900+00
.120+02 %
H/DA
M
.21R+06 GAL
.763+01 DAYS
.556+04 tt/DAY
.6U2+02 CFM/TCFT
B-18
-------
EXAMPLE PROBLEM
QUANTITIES FOR ACTIVATED SLUDGE PROCESSFS:
COMPLETELY MIXED FLOW
AVFUAGF UATl Y FLOW
TOTAL NUI-.HFR OF TANKS
riUf.'HFP Oh AFKATOHS PER TANK
NUV.i-ihR OF BATTERIES OF UNITS
CAPACITY OF FACH INDIVIDUAL AFRATOR
.JATdK UEHTH OF ThE ALRATIOU TANKS
..IHTH OF AFRATION TANK
Ucr.GTh Of- /TKATIOM TANK
PIPING GALI FRY .VIDIM
UurtillTY OK EARTHWORK REQUIRED
if. li.Th OF THF PLATFORM
Tc/TAL QUANTITY OF l<. C . SLAn
TOTAL QUANTITY OF K.C. WALL
HAMIJKAIL LFDGTH
T(;TAL CAPACITY OF AERATION FOUIPMFNT
JI-FixATICfJAl MANt->u.vKR REOdlKtO
!Ali>IIFI,AiviCh MAfjiJuri(-l< RLOblRED
"LFCTP1CAL FliFRGt FOR OPERATION
J AN(; K NiATFR. IAL AUL) SUPf'LY COST
TRAIN NO
MECHANICAL AFRATION SYSTEMS
.310-01
2
1
.100+02
.12U+02
.589+02
.589+0?
.200+02
.673+05
.812+01
.113+05
.llfl+05
.105+03
.800+02
. 121+01
.622+03
.536+06
.237+01
MGD
HP
FT
FT
ft
CUFT
FT
CHFT
CUFT
FT
HP
MAN-HOURS/YR
MAN-HOURS/YR
KWHR/YR
PERCENT
LlOUin CHARACTERISTICS
rLOW (N'GD) SOLIfiS (MG/I )
^lAXIMJfi 10.0000 SUSPI NOED 20.00
(WFrtAGt 10.0000 VOLATILE 80.00 *
•11MMUM in. oooo SFTTLEABLF .00
TkN'.P 18.0 C OIL H GREASE .00
JH 7.60 CATIONS 160.00
ANIONS 160.00
(MG/L)
ROD5 30.00
ROD5S 15.00
COD 15.00
COOS
P01
11.97
(MR/I.)
TKN 30.flO
MH3 ..TO.flO
M02 .00
h:03 .00
V(H UVK (GAL/D)
*. SuLins
% VOLATILE
CHAPACTFRI«;TICS
PRIMARY SFCONOARY
?H5Bb.f>7 .00
2.50 .00
11.16 .00
B-19
-------
EXAMPLE PROBLEM TRAIN NO
ft************************.************
5LUDGF DKYING REDS
TOTAL. SURFACE ARFA REOUIHED .193+06 SO FT
0 INITIAL PFPTH OF SLUDGE .1PO+02 INCHES
0 FINAL HrT,CFr4T SOLIDS .500 + 02
RED HOLDING TIME .3HO+02 DAYS
+ ^** +
-------
EXAMPLE PROBLEM
TRAIN NO
QUANTITIES FOR DRYING BED
TOTAL DRYING BED SURFACE AREA .193+06
NU'.'HH* BLDS 33
SUrFACF. AREA OF FACH INDIVIDUAL BFD .5«5+04
LFI.G1H OF- FACH liFD .293+03
VOLUME OF EAUTHrtOHK RFQUIRED .957+06
voi UMF R.C. ;N-PLACE FOR niviniNG WALL .570+05
Vut UMF OF K.C. IN-PLACF. FOR TRUCK TRACKS .290+05
v/CI UMF OF SAND .145 + 06
VOI. Ur-F OK f.RAVFL .193 + 06
CLAY PIPF. DIAMETER .000 + 01
TOTAL LENGTH CLAY PIPF .193+05
SLUDGE SOL ins PEU DAY .290+01
>KiH 7.60
VOlU^t (GAL/0)
•V SOLIDS
9 VOLATILE
LIQUID CHARACTERISTICS
SOLIfJS CMG/I )
SUSPK\DF"D 20.00
VOLATILE 61). 00 9
SFTTLEARLF .00
OIL b. GREASE .00
CATIONS 160.00
ANIOUS 160.00
(MG/L)
RODS 30.00
RODfjS IB. 00
COD
CODS
P04
45.00
22.50
11.97
(MG/L)
TKN 30.00
MH3 30.80
N02 .00
N03 .00
SLUDGE CHARACTERISTICS
PRIMARY SECONDARY
3783.53 .00
17.00 .00
44.46 .00
B-21
-------
EXAMPLE PROBLEM TRAIN NO
**************************************
SLUDGE HAU1 ING AND LAND FILLING
VOLUME OF SLUDGE HAULED . 1P7+02 CUYD/OAY
TRUCK CAPACITY .190+02 CUYO
D ROUND 1HTP Tlvir-- TO DISPOSAL SITE .1004-01 MRS
L) THUCK LOADT'JG TIN'E .7RO-fOO MRS
0 hOuKS uF OP(-RATION PER DAY .600*01 MRS
TOhS OF SLUDGE riAULFH PER HAY .166+02 TONS
i) HISTANCE TO LHSPOSAI SITE .100 + 02 MILES
**************************************
B-22
-------
EXAMPLE PROBLEM
QUANTITIES FOR SLUDGE HAULING AND LANDFILL
TOTAL SI Unr.F VOLUMF HAULED
MAXIMUM ANTICIPATED LANDFILL DOWNTIME
ANTICIPATE!', M UDbE STORAGE HEIGHT
SLUDGE STORAGE SHED AREA
jlDFH OF Si UDGE STORAGE SHFQ SLAR
LENGTH OF '-.LUNGE STORAGE SHED SLAR
VUl UMF OF f AR IHl-.ORK
VO! UMF OF r,LAH CONCRETE
SUFiFACf ART A OF CANOPY ROOF
DISTANCE Tf; DISPOSAL SITF.
ROUND TRIP HAUL DISTANCE
Fo:;S OF SLUDGF HAULED PFR DAY
OPERATION rANPOuf H RFOUIRFD
ROUfJD TRIPS PFR DAY f-'FR TRUCK
DISTANCE TRAVFLFD PER YEAR PER TRUCK
MAINTENANCE AND MATERIAL SUPPLY COST
TRAIN NO
.lR7-f-0?
.300+02
.000+01
.190+04
.30U+02
.616+02
,5."5'f + 04
.232+04
.190+04
.100+02
.200+02
. 166+02
.293+03
.100+01
.500+04
.650+01
CU YD/DAY
DAYS
FT
SO FT
FT
FT.
CU FT
CD FT
SO FT
MILES
MTLES
TONS/DAY
MAN-HOURS/YR
MTLFS/YR
PFRCFNT
LIOUID CHARACTERISTICS
FLOW
MAXIMUM
AVERAGE
MINIMUM
TEMP
PH
(^•GD)
in. onoo
Ki.nooo
in. oooo
ia.0 c
7.60
SOLIDS CMG/D
SUSPENDED 20.00
VOLATILE en.oo
SETTLEABLF .00
OIL K GREASE
CATIOfJS
AM IONS
.00
I60.no
160.00
ROD5
ROD5S
COD
cons
P04
(MG/L)
30.00
15.00
45.00
22.50
11.97
(Mfi/L)
TKN 30.BO
nH3 .io.no
M02 .00
.00
VOIUME (GAL/D)
% SOLIDS
% VOLATILE
SLUDGF CHARACTERISTICS
PRIMARY SFCONDARY
.no .00
.00 .00
.00 .00
B-23
-------
T'xAMf t :-' >^>i~;" f :*.
AVf .';AC,: -/:;., /!'<:;; ruOW 10.00 MGD
LK,'ii<:. • , i "I«'JM 0 TRIC 0 CHLO
Pur-iMs'. ; ! • '• • >":••; YI o HAUL o
0
COST SUMMARY
OPFR MAIMT
UflJT .OS'i
PRTL! i"! f: : "'; -(-t,
PRJ^ f i .* •';';s-q-i
TKI'O/ ii ' "';•';•
r i '''i i f * ' ' i*
A! i-'O ,' « ' ' ''.",•*
MA-'i!. i" r ' - '
10"' '"-! '' •• ;'
i ) I : i ' > f i ' .
»yi 'v f - } ; " " " > ;
c 7 f f
f-. ; " i •' ! •" ' i ' " —
(""(" ',! I . " ' ' ' !' ':" ' J
Y.\M'. f' ' " •'
UA -•. • , ' • • ' I. »
I ,M i ft . : ' ' - ' i
>''ii.j\ : ; ; c ... .
IN!;' :•:'"• . , ',
v,v- ' ' • • '••'.I'.
'?(' - !'l '.
^;.-i,^';lf ;; .'
•) r -...I;; . ' .•< .">/ r '
i'^>".
Lf'ND f'.... '
A!)'.'IL- :-.',••.' ' ' '
LAir.it-.'- r'-'.<
AN" WORT I AF10R
COST COST
1/YH WYR
31018 1 11 32
3 :'jt 9 2 8R21
t'iil'18 3026
!i).k;:"-4 3939
^fi'jSfl 72 3S
o "^ 1 1 ''} 1 1 1R (( 9 6
•i'ldOR 1705
>» 171*58 76996
t j "^ 0 D 0 G i
991290 t
1^89798 S
f > 3 2 o i ! ( i S
] u 1 ? 1 U 5 't
1 M J , J AX O T>
1638576 "6
108887 -fc
2 V o 3 S 7 7 1
10649/03 5
/f^oMi t
3 Oh SOb •£
:2?M?i 1
J";06505 $
4329121 $
19,,2 , (
22731 9./YR
22919 $/YR
L AROR
COST
S/YR
4701
4129
6700
2004
2815
1780
3061
7R17
0
33018
POWER MATFRIAI fHFMTCAl.
COST
$/YR
1R59
476
756
767R
26652
5250
p 1 <4 14.14.
0
0
64118
TOTAL CONSTRUCTION
20. ACRES)
COST COST
5,/YP 5/YR
5566
9286
BM3
128R
20610
137R
7590
10746
68764
COST 15325292
n
0
n
n
n
n
n
n
0
0
5
PHjiSnH "5,/YR
if
------- |