EPA 400/9-73/001
  OCTOBER 1973

           A COMPUTER MODEL FOR EVALUATING
    COMMUNITY PHOSPHORUS  REMOVAL STRATEGIES
                         ^ PRO^°
            UNITED STATES ENVIRONMENTAL PROTECTION AGENCY
                  Office of Air and Water Programs
                     Washington, D.C. 20460

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     A COMPUTER MODEL FOR EVALUATING
COMMUNITY PHOSPHORUS REMOVAL STRATEGIES
                        By
                 Donald S.  Yeaple
                 David A.  Barnes
                Francis A. DiGiano
             JBF Scientific Corporation
                   2 Ray Avenue
          Burlington, Massachusetts 01803
              Contract No. 68-01-0758
                   Prepared for
     OFFICE OF AIR AND WATER PROGRAMS
  U. S. ENVIRONMENTAL PROTECTION AGENCY
            WASHINGTON, D. C.  20460

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                 EPA REVIEW NOTICE

 This report has been reviewed by the Environmental Protection
 Agency and approved for publication.  Approval does not signify
 that the contents necessarily reflect the views  and policies of the
 Environmental Protection Agency, ncr does mention of trade
 names or commercial products constitute endorsement or re-
 commendation for use.

 The Environmental Protection Agency has not verified this
 computer model by using it to calculate the phosphorus removal
 costs of many existing  sewage treatment plants,  and comparing
 these calculated costs with the known costs of these operating
 plants.  The Office of Air and Water Programs would appreciate
 receiving results of any such comparisons.   Users of the model
 may borrow a copy of Sensitivity Analysis__of a^Phosphorus Removal
 Strategy Computer Model from the Office of Air  and Water Programs,
 ThTs~unp~ublis"hed report analyzes the sensitivity  of the model's
 parameters.

 The Soap  and  Detergent Association has made the following comment
 on this model.

     "The phosphorus substitutes available at this time have costs
 associated with their use which may partially offset or totally
 outweight the  savings in phosphorus  removal costs which would
 ensue from a  ban on phosphorus in detergents.  Examples are
higher raw material costs, shorter garment life,  increased fre-
quency of washing machine service calls,  loss  of flame retardancy
of finishes on children's sleepwear,  increased  ingestion hazard,
potentially increased cost for treating the phosphate replacement
at the waste treatment plant.   The  costs do not lend themselves to
inclusion  in a computer program.  Every user  of this program is
advised to evaluate magnitude  of these off-setting  costs in the
community of concern before drawing any conclusions. "

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                          ABSTRACT

A computer model for evaluating a number of strategies for removing
phosphorus in wastewater has been developed.  The influence on
total treatment cost of several non-treatment strategies such as the
elimination of phosphates in detergents can be evaluated in terms of
the treatment cost at local waste treatment plants.

A review of phosphorus removal technology was conducted in order
to  determine what methods  should be included as available techniques
in  a treatment strategy.  Chemical precipitation techniques were
selected as being both available and most  effective at the present time
and in the immediate future.

The model reports to the user the total cost of  a selected strategy
for removing  phosphorus.   Over 21 treatment schemes with several
sludge handling  schemes can be selected and evaluated depending
on local conditions.  The computer guides the user through a series
of  questions and answers to develop a local profile and prediction
of  future conditions.
                              ill

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                        CONTENTS
Section
   I      Conclusions
  II      Purpose  of Model
  III      Introduction                                     7
              Scope and Purpose                          7
  IV       Phosphorus Control Strategies                   9
              Legislation to Limit Detergent Phosphorus  10
              Upgrading of Treatment Facilities
              to Include Phosphorus Removal             10
              Effluent Diversion                         11
  V       Treatment Alternatives for Removing
          Phosphorus From Wastewater                  15
              Chemical Precipitation Systems             16
              Biological Phosphorus Uptake               29
              Activated Alumina                         30
              Ion Exchange                               31
              Selection of Phosphorus Removal Scheme    33
                  Process Options                        34
                     Input Data  Required
                     for Process Options                 35
 VI       Phosphorus Removal Strategy and Cost Model    41
              Use of Model                               41
              Model Description                          41
              Modeling Considerations                    43
              Subroutines                                 4g
              Assumptions and Limitations                50
              Subroutine Descriptions and Flow Charts     55
              Common Block  Descriptions                 95
VII      Case Studies                                   111
              Case 1  - 5 MGD Trickling Filter  Plant      112
              Case 2-20 MGD Activated Sludge Plant    112
              Case 3-50 MGD Primary Plant            122

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VIII       Operating Manual for the Phosphorus
          Removal Cost Model (REMOVE)               151
              Questioning Procedure                    151
              Printout                                  152
              Keywords                                154
              Variables                                155
              Errors                                   165
              Scheme                                  166
              Errata Sheet for Program                 171
              Program Listing                          172
 IX       Acknowledgements                            285
  X       References                                   287
              Section IV                                287
              Section V                                287
              Section VI                                290
 XI       Appendices                                   293
              A - Liquid-Phase Treatment System
                  Options for Phosphorus Removal       293
              B - Sludge  Handling System Options        298
              C - Design Parameters                   301

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                         FIGURES






Figure                                                 Page




   1      System Diagram                               55




   2      REMOVE Flow Chart                           59




   3      SYSTEM Flow Chart                            61




   4      STRTGY Flow Chart                            64




   5      INTIME Flow Chart                            65




   6      SPOPFNC Flow Chart                          66




   7      DTGLIM Flow Chart                            72




   8      EFFLIM Flow Chart                            74




   9      INDLIM Flow Chart                            75




  10      LCHOSE Flow Chart                            77




  11      TRTMNT Flow Chart                           81




  12      SCHOSE Flow Chart                            83




  13      SIZE Flow Chart                               85




  14      TSCHME Flow Chart                           86




  15       BUILD Flow Chart                             87




  16       LSKCST Flow Chart                            91




  17      SSKCST Flow Chart                            93




  18       5 MGD Trickling Filter Plant                   114




  19       5 MGD Trickling Filter Plant                   118




  20       20 MGD Activated Sludge Plant                  124




  21       20 MGD Activated Sludge Plant                  128




  22       20 MGD Activated Sludge Plant                  132
                             VI

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23      50 MGD Primary Plant                        138




24      50 MGD Primary Plant                        142




25      50 MGD Primary Plant                        146
                          VII

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                          TABLES

Table                                                    Page

   1      Effect of Chemical Additions for
          Phosphorus Removal on Digestion                24

   2      Effect of Chemical Additions for Phosphorus
          Removal on Vacuum Filtration                   25

   3      Achievable Effluent Phosphorus Concentrations   36

   4      Cation/Influent Phosphorus Weight Ratios         36

   5      Lime Dosages                                   37

   6      Sludge Production                               38

   7      Per Cent Solids of Chemical Sludges              39

   8      Sludge Handling Options                          40

   9      Cost Function Locator                           47

  10      Construction Cost - Valid Ranges  for
          Sizing Parameters                               52

  11      5 MGD Trickling Filter Plant                   113

  12      20 MGD Activated Sludge Plant                  123

  13      50 MGD Primary Plant                         137

  14      Treatment Schemes                             150
                            Vlll

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                       SECTION I

                     CONCLUSIONS

1.  This model is for evaluating strategies available to communi-
ties for the control of phosphorus in municipal wastewater.  The
model will report to the user the cost of various strategies which
include  the alternatives of controlling phosphorus concentration
in the raw sewage, limiting industrial discharge of phosphorus
and treating by various methods at the wastewater treatment plant.
The costs are computed from amortized capital costs,  operation
and maintenance expenses, and materials cost for a predetermined
time period.

2.  The costs of phosphorus  removal strategies will vary depend-
ing on type of local treatment, the quantity of phosphorus in the
treatment plant influent and the final effluent concentration require-
ment.   For a hypothetical community of 50, 000 population served
by a 5 MGD trickling filter plant, it has been found that alum treat-
ment after the trickling filter to achieve an effluent of Z.O mg/1
total phosphorus results in a cost of 7.7 cents/I 000 gallons.  The
corresponding cost to achieve an effluent of 0.5 mg/1 is 13.7 cents/
1000 gallons  and involves the addition of multi-media filtration to
the treatment scheme.  These cost estimates are for a stable popu-
lation.  The model will also  predict costs based on various growth
rates.  In contrast to the above, a hypothetical 200,000 population
city served by a 20 MGD  activated sludge  plant can achieve 2.0 mg/1
phosphorus effluents at a cost of 6.2 cents/I 000 gallons using a
scheme of ferric chloride added to  the aeration basins.  If an
effluent limit of 0.5 mg/1 phosphorus is required,  a tertiary
single-stage  lime treatment scheme is the least-cost scheme at
a cost to the  community of 9.4 cents/1000 gallons.

Cost to  the community may be substantially reduced if  State and/
or Federal grant funds  are available to  assist with financing.
Costs may also be reduced by controlling the phosphorus load to
the treat nent plant through imposition of  legislative limits on  sale
and use of detergent products  containing a high percentage of
phosphorus.  Restriction of  significant phosphorus discharges to
the sewerage system from industrial and  commercial sources
may also be  enforced to reduce treatment costs to  the community.

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The model provides for cost computations using these alternatives
on financing and control of phosphorus discharged to the sewerage
system.  The  model requires as an input a description of present
treatment facilities and a prediction of the  community growth rate.
The most cost-effective treatment scheme  can then be determined.

3. In addition to being  a valuable tool for planning local strategies,
the model can be used to evaluate and optimize  various  treatment
processes.  Changes in design parameters, costs of chemicals,
transportation rates, power costs,  and the introduction of automa-
tion to reduce manpower requirements can all be evaluated  as to
their effect on overall treatment costs.

4. Several inconsistencies have been noted in the generally
accepted assumption that  approximately 50 percent of the phosphorus
in domestic wastewater is due to the use of phosphate detergent
products.  In  several reports this assumption appears to be justi-
fied on the  basis  of an annual per capita use of  27 pounds of deter-
gent.  This assumption may be erroneous for use in the model by
all communities.  If legislative controls will be imposed on per-
cent phosphorus in detergents  and industrial or commercial sources
of phosphorus controlled it is important that the community or user
of the model know the specific ratio of detergent phosphorus in the
sewage and the industrial-commercial contribution in order to
arrive at a valid  best strategy for phosphorus removal.

5. After reviewing the current technology  for phosphorus removal,
chemical precipitation was  selected as being the  most widely
accepted and effective means of removing phosphorus from  waste-
water.

6.  Four levels of effluent phosphorus concentration (total unfil-
tered phosphorus) were assumed to be achievable depending upon
the type  of treatment provided. These are:

                   2. Q  mg/1    (Option 1)*  Chemical addition  to
                              the primary clarifier
*See p. 34-35 and Table 14,  p. 150, for description of process
 options.

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                              (Option 2)  Chemical addition to a
                              flocculation basin prior to the primary
                               clarifier

                              (Option 3)  Chemical addition to the
                              aeration basin

                              (Option 4)  Chemical addition after
                              the trickling filter.

                   0. 5 mg/1  (Option 5)  Chemical addition to the
                              aeration basin plus multi-media
                              filtration
                                            or
                              Chemical addition after the  trickling
                              filter plus  multi-media filtration

                              (Option 6)  Addition of lime  to a
                              flocculation basin following  conven-
                              tional  secondary treatment

                   0. 3 mg/1  (Option 7)  Addition of alum, or ferric
                              chloride to a  flocculation basin  follow-
                              ing conventional secondary treatment--
                              one stage.

                   0. 1 mg/1  (Option 6)  Addition of lime  to a
                              flocculation basin following  conven-
                              tional  secondary treatment--two
                              stages

7.  Chemical precipitation provided seven alternative process
schemes:  (1) addition to the primary clarifier; (2)  addition to
a flocculation basin prior to a primary clarifier; (3)  addition  to
the aeration basin; (4)  addition to the secondary clarifier  of a
trickling filter; (5)  scheme (3)  or (4) plus a multi-media filter;
(6) addition of lime to a tertiary treatment  process; and (7)
addition of alum or ferric chloride in a tertiary process.

8.  With chemical precipitation, sludge production is increased.
Although stoichiometric equations can be used to predict the total
additional  sludge, variations to those estimates have been noted

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in many sources.  In the future, there may be a trend toward using
oxygen in activated sludge and aerobic digestion schemes.  This
will lead to decreased sludge production and improved sludge de-
watering and will probably have a beneficial effect on the  costs of
sludge handling particularly for larger treatment plants.

9.  Estimates of design parameters for  gravity thickening,  vacuum
filtration,  sludge drying beds, anaerobic digestion, flotation thicken-
ing and multiple-hearth incineration have been presented.

A number of effects on the sludge handling capacity of a treatment
plant  are a direct  result of chemical addition.  The following have
been noted:

       a.   Vacuum filter yields have been noted to decrease
            with alum sludges and increase with lime and ferric
            chloride sludges.

       b.   Lime sludges have an adverse effect on anaerobic
            digestion unless carefully controlled.  Iron and
            aluminum sludge will not noticeably affect anaerobic
            digestion.

       c.   Some release of phosphorus from the sludge may occur
            in anaerobic digestion of iron sludges.

10. In regard to chemical addition  schemes  the following conclu-
sions apply:

       a.   Chemical addition to the primary clarifier may en-
            hance the removal of  BOD and suspended solids in ad-
            dition to phosphorus removal.  However, because the
            hydrolysis of complex organic and inorganic phosphorus
            compounds is incomplete prior to biological treatment,
            the expected final effluent phosphorus concentration is
            quite variable and significantly higher than that achiev-
            able by tertiary phosphorus  removal.  Filtration of the
            primary effluent must be practiced if low values are
            to be achieved.

       b.    Lime dosing cannot be based upon influent phosphorus
           concentration.  The dosage of lime  is related to the

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    alkalinity of the influent.  Higher alkalinities require
    higher dosing.  As a practical limit, wastewaters hav-
    ing alkalinity less than 150 mg/1  as  CaCC>3  are  not
    amenable to lime treatment because pH will increase
    to levels greater  than 10. 0 before effective phosphorus
    removal occurs.  This will be unacceptable if biological
    treatment  follows.  For alkalinities between 150 and
    300  an addition of 150 mg/1 of CaCC is required while
    200  mg/1 of CaO  is  required for  alkalinities greater
    than 300.  Estimates  of dosage are  also a function of
    application point — primary versus tertiary.

c.   Lime  addition in  tertiary  treatment offers  two  alterna-
    tives-- single and two stage.   The choice of process
    depends on alkalinity.  Single stage can be  used when
    alkalinity is greater than 200 mg/1, while  two  stage is
    required for low  alkalinity wastewater.

d.   Alum  addition in  tertiary  treatment is also feasible.
    While lime addition requires that rccarbonation be
    practiced,  alum does not  because pH is depressed to
    a manageable  extent rather than  increased. Alterna-
    tively, lime can be  recovered  from tertiary sludge
    while  alum, thus  far, cannot.

e.   Data thus far reported indicate that the  dosage of
    iron or  aluminum is dependent upon influent phosphorus
    concentration  but the  exact ratio of  cation/phosphorus
    is not well  established.  In the computer model an
    Al/P ratio  of 2/1  and  an Fe/P  ratio of 3. 1/1 were
    assumed when the chemicals were added to the primary
    clarifier and I. 5/1 and 4/1 respectively  when added
    to the aeration basin.

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                      SECTION II

                   PURPOSE OF MODEL

The computer model developed in this program can be used by
local communities or their consulting engineers to plan the
expansion of present wastewater treatment facilities or provide
for new ones in order  to meet requirements for phosphorus removal.

The model as it is presently conceived is based on best available
data. In order to insure its usefulness,  EPA plans to periodically
update the model as additional performance data on phosphorus
removal processes becomes available.

Some communities  presently using extended aeration systems for
waste treatment will not find the model particularly useful.  There
is no existing data for modeling purposes on the performance of
extended aeration with chemical addition for phosphorus removal.
In view  of the additional sludge production it would not appear that
these systems will  be  readily modified at this time.

We believe that substantial reductions in the production of sludge
may be  realized with pure oxygen thus reducing costs of sludge
handling modifications.  The model will be updated if and when
sufficient data are available to substantiate significant removal
of phosphorus by this process.

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                       SECTION III

                     INTRODUCTION

Scope and Purpose

Accelerated eutrophication in lakes and slow moving rivers is  a
contemporary problem involving increased biologic productivity
as a result of increased nutrient enrichment.  Both point and non-
point sources of nutrient addition have been identified.  Suggested
corrective measures have included the reduction of nutrient inflows
by such actions as diversion of wastewater effluents to bodies  of
water with more  assimilative capacity, additional wastewater
treatment to remove nutrients from industrial and municipal ef-
fluents, product modifications such as reducing phosphorus content
of detergents, control of land use practices to reduce nutrient
drainage from fertilizers, and treatment of agricultural drainage.
The first three measures listed above  deal with the control of point
sources while the last two are concerned with non-point  sources.

A basic strategy  of controlling eutrophication is presently linked
closely to the reduction or elimination of phosphorus,  a  nutrient
which does not have a gaseous phase as does nitrogen, and thus
does not replenish phosphorus in water through the atmospheric
gases.  For this  reason, the reduction of phosphorus input to a
body of water is the basic  strategy chosen for the control of eu-
trophication.  There is some indication that the atmosphere may
contain phosphorus contributed by dust particles  or through air
pollution and this may be a significant contribution of nutrients
in some areas.  The specific methods  for achieving phosphorus
removal cannot be adequately specified until the local conditions
have been thoroughly determined and analyzed.

In the program discussed in this report we have dealt primarily
with point sources and in particular the control of point sources
at a municipal waste treatment plant.   The first phase of the
program included a  review of various alternatives for updating
existing treatment plants for phosphorus removal.  We were
concerned with the feasibility of adding equipment to existing
plants  and with isolating the additional capital and operating
costs so that the  specific costs for phosphorus  removal could

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be identified.  We also -were concerned with the possibility that
techniques not presently suitable for routine introduction might
become feasible within the next 5 to 10 years.   Thus, the first
phase was a review of both existing and  possible future techniques
for phosphorus removal.

The second phase of the program involved the formulation of a
computer model for evaluating the  various  strategies for reducing
phosphorus in the effluent of municipal treatment plants. Since
at the present time there  is no national limitation on the use of
phosphorus in detergents, the individual states and municipalities
have been faced with the problem of legislating their own controls.
In many cases this has been done and has affected the  decision to
remove phosphorus by additional waste treatment.   Each of the
possible strategies has an associated cost, thus the objective of
the model is to determine the best strategy on the basis of cost
for controlling effluent phosphorus within some given limit.

The model has been designed specifically for planning purposes
and can be used by municipalities, planning agencies and govern-
ment policy organizations.  Input information is determined  on the
basis of a series of questions and answers  designed to define the
specific set of circumstances in a  given municipality.   A number of
parameters can be varied to simulate possible strategies including
the reduction of phosphorus in detergents and the requirements for
pretreatment of industrial wastes.  Predicted changes in popula-
tion and growth rate can be handled by the model which also  ac-
counts for future additions to plant capacity attributable to the
requirement for phosphorus removal.

The remainder of this report is divided into a number of sections
as follows:  In Section IV the various  strategies used to  control
phosphorus are discussed,  Section V is  a review of the treatment
alternatives available to a municipality including methods which
may not be feasible at the present  time but show some promise,
and Section VI is a description of the phosphate removal strategy
and cost model.  Section  VII presents three case studies we  have
selected to illustrate how the model can be used by local com-
munities.  Section VIII includes the instructions for using the
model along with a complete listing of the program.  The program
listing is  fully documented with comments which reference constants
and program variables including their source.

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                      SECTION IV

          PHOSPHORUS CONTROL STRATEGIES

The primary purpose of this report is to investigate the costs of
various strategies for removing phosphorus from the  effluents of
municipal wastewater treatment plants.   We must assume, therefore,
that a decision has been made to reduce the input of phosphorus as
a result of a desire to curb "cultural eutrophication".

Although our effort is concerned with only the  reduction of phos-
phorus through treatment plants,  several working groups  including
researchers at Utah State University under EPA sponsorship and
Case Western Reserve  University under a grant from the  Rockefeller
Foundation are investigating the overall implications  of phosphorus
cycling in the environment.  Their work will presumably  include an
investigation of the relative quantities of phosphorus introduced
through both point and non-point sources and the rate  of release of
phosphorus from previously deposited bottom  sediments.   Results
of these studies may  affect future eutrophication control strategies,
but for the present we are assuming that a major reduction can be
achieved in the pounds of phosphorus passing daily  through sewage
treatment plants.

Basically,  the three available strategies for reducing or preventing
the impact of phosphorus discharges on lakes  include:

      1.  Removing phosphorus  from wastewater by upgrading pre-
      sent treatment  facilities.

      2.  Reducing the phosphorus content in raw sewage  through
      legislation and  enforcement.

      3.  Diverting wastewater  treatment plant effluents around
      eutrophic receiving waters  or to other waters which have
      adequate assimilative capacity.

These basic strategies are influenced by a number  of factors including:

      a.   The implementation or non-implementation  of local legis-
      lation limiting phosphorus content in detergent  products.

      b.   The present status of local treatment facilities  including
      type of treatment, sludge handling capability, excess capacity
      and degree of over or underloading.

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       c.   Type of waste treated including ratio of domestic to
       industrial wastewater and classification of industrial waste.

       d.   Future growth of the community served and possible re-
       gionalization of treatment in the near future.

       e.   Status of plans for upgrading present facility, or con-
       structing new facilities  for reasons other than phosphorus
       removal.

       f.  Availability of alternate  receiving waters  where phosphorus
       bearing effluents  may be diverted  and be assimilated without
       adverse effects.

       g.   Regional factors such as climate, cost of chemicals, land
       costs,  and transportation.

 Legislation to Limit Detergent Phosphorus

 The absence  of a national regulation on the concentration  of phos-
 phorus in  detergents together  with local regulations passed by more
 than five  states and 50 local governments has  led to both a marketing
 problem on the part of the detergent manufacturers and an enforcement
 problem  in the affected communities.  In Canada,  the  government has
 instituted  phosphorus controls on both the detergent manufacturers and
 the treatment plants.  Phosphorus  concentrations in detergents will
 be limited to  no more than 5 percent after December 31, 1972 (I).  As
 a result,  many of the detergents distributed in Canada now contain
 10-12 percent NTA which is presently banned in the  U. S. (2).  Some
 recent work has shown that NTA is completely biodegradable (3),
 although it apparently is still  unacceptable for medical reasons.
 Other  phosphate substitutes have  tended  to be highly alkaline and
 corrosive. Work is  continuing, however,  at an accelerated pace by
 the major detergent manufacturers.  Proctor and Gamble has re-
 ported expenditures on the order  of $85 million (4) to both reduce
 phosphates in detergents and test the substitutes for safety and ef-
 fectiveness.   Colgate-Palmolive early in 1971 reduced phosphate
 content of all  its detergent products to less than 35%.

 As the detergent manufacturers voluntarily reduce phosphate concen-
 trations in their products, the enforcement costs on the local level
 should decrease and will eventually not be a significant factor.

 Up_g_radi.ng_ of  Treatment Facilities to Include Phosphorus Removal

 The present status of waste treatment  within local communities will
have a significant affect on the strategy for removing phosphates.

                              10

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As we will discuss in the next section,  chemical precipitation methods
of removing phosphorus are  easily implemented and are effective for
80 to 98% removal.  These same techniques can also be used to im-
prove BOD and suspended solids removal in plants which are presently
overloaded.  The cost of implementing the techniques will,  among
other factors, depend on the present chemical dispensing and mixing
facilities, capacity of clarifiers,  sludge handling facilities and
ultimate disposal of sludge.  Some treatment plants  in smaller com-
munities are operated on the extended aeration principle which
requires relatively little sludge handling capacity.  In  other towns
aerated lagoons may provide equivalent secondary treatment but do
not provide adequate sludge  handling facilities.  The addition of
phosphorus removal requirements in these towns would require
relatively major fund! ng for both construction and operating costs.

The 1968 inventory of municipal waste treatment plants (5) showed
that more than 90  percent of the plants constructed were designed
for wastewater flows of less than 5 MGD.   A majority of these plants
were designed for secondary treatment using either trickling filters
or activated sludge.  Most of these plants do not presently provide
for any nutrient removal beyond the residual which in the case of
phosphorus is on the order of 20 to 30 percent.  In many of these
areas the percentage of phosphorus in the wastewater due to the use
of detergents  may vary over a range of 40-75 percent depending on
the classification  and quantity of industrial wastewater treated.  In
towns near the high end of this percentage  range where there is a
minimum infiltration of sewer systems, the regulation of detergent
phosphate will have a major effect on any decision to remove
phosphorus by treatment.

Later in this  report we will  see that the major cost elements in
upgrading treatment plants  for phosphorus removal are the cost
of chemicals, and the additional sludge handling facilities required.
Recent  controversy over the costs of phosphorus removal have been
centered on the issue of whether or not the use of designed excess
capacity in local plants  could be used for phosphorus removal.  In
general, if excess capacity  is provided,  the capital costs for phos-
phorus  removal are calculated  on the assumption that this capacity
is available.  The operation and maintenance costs, however, include
the overall increased effort necessary to operate the plant.   These
assumptions are discussed in greater detail  in Section IV.
                             11

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Effluent Diversion

We have briefly alluded to the impact on present waste treatment
facilities of population growth rates and possible regionalization
of treatment facilities.  Section 208 of the Water Quality Amend-
ments of 1972 addresses the issue of areawide waste treatment
management.   Regional development and implementation of area-
wide  waste treatment management plans is encouraged by the
gove rnment.

In the development of strategies for controlling phosphorus we are
faced with the question of how to determine the future life of  local
plants and the impact of regionalization.  Our model at the present
time  is designed for  a single plant with all the peripheral decisions
of how to upgrade that facility.   With some modifications it could
be designed to handle the same problem for regional organizations.
Often a local community will have little  choice in determining what
water body will receive its treated effluent.   Regional organizations
would have a wider choice, thus effluent diversion becomes a viable
alternative to phosphorus removal by treatment.  In some  temperate
areas spray irrigation may also be a possibility and where facilities
are regionalized and land is available this choice may be a logical
one.

Effluent diversion as a stretegy requires a major effort in planning
and construction.  The Lake  Washington diversion project  in Metro
Seattle  is an excellent example.  The comprehensive plan for the
removal of all treatment plant discharges  from Lake Washington
was approved in October,  1958.  The first ten year stage of the
program required an outlay of $125, 000, 000 (6). Some revisions
and additions  have added another $20, 000, 000 to the project which
has results  in the removal of all treatment plant discharges from
Lake  Washington and the abandoning of  all the ten treatment plants
located on its shores.  New interceptors were constructed and
several large treatment plants  were provided with effluent discharge
into the Duwamish River or  through deep outfalls to  Puget  Sound.

In the case of Lake Washington conditions  improved  markedly.  A
decision was made to divert rather than treat.  If the regional
mechanism had not been approved,  the planning for any alternative
other than treatment would not have been possible.

In the consideration of effluent diversion as a strategy the  major
cost elements are piping and pumping.  Distance to the receiving
                           12

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body and topographic features control these costs.   The problem
becomes more complex,  however, when the economics of scale
of building large regional plants are combined with the costs of
piping and pumping influents over large distances.   As in the case
of Lake Washington and Metro Seattle, the final solution most
likely will involve a consolidation of facilities but is unlikely to
involve one very large  treatment plant serving a large area.

A number  of optimization studies have been made on the problem
of minimizing cost of treatment along river systems receiving
waste treatment effluents.  A recent report (7) discussed the
optimum number and location of treatment plants and uses  as an
example the optimum design of a regional wastewater treatment
system for the Merrimack River Valley.  The program assumes
that liabilities  such as  treatment plants now in operation and
effect of combined sewers can be disregarded.  The method chosen
specifically treats the trade-off between the number of treatment
plants and the extent of sewer systems.  In another recent publi-
cation (8), a computer  program has  been developed to provide
design data and the cost breakdown for  regional sewer systems.
The program takes the specified characteristics for the conveyance
and designs a pipeline  which minimizes the cost of conveyance for
that particular situation.

An effluent diversion strategy would employ both elements mentioned
above.  The optimum number of treatment plants would be an element
of the problem together with the minimum cost of piping and pumping
the effluent. Since this strategy depends on a regional approach, we
have not made  specific provisions  for it in our program.  A  subroutine
could easily be  added if required.
                            13

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                         SECTION V

       TREATMENT ALTERNATIVES FOR REMOVING
             PHOSPHORUS FROM WASTEWATER
The objective of this  study has been to develop a computer program
which would provide a given community with a means for evaluating
various phosphorus control strategies and their associated costs.
To accomplish this objective it was essential that  existing phosphorus
control technology be examined and that methods be selected which at
best could be  implemented immediately and at worst in the very near
future  at existing waste treatment facilities.  The?e methods would
then become the treatment schemes or options available to the
community.

Inherent in the selection of available process options is  a knowledge of
needed design parameters.  While specific values of design parameters
may change with advancements in technology and more reliable measure-
ment of actual field performance, the current "best estimates" are the
minimum required.   Obviously,  the computer program provides for
updating of design parameter inputs as better system knowledge is
obtained.

A review of recent literature is  presented  in this  section in an  effort
to justify the  selection of present phosphorus  removal options deemed
acceptable for immediate implementation.   Although there have been
innumerable studies of phosphorus control technology,  only those most
recent  studies relating to practical application, i.e. ,  feasibility, pilot
plant and demonstration studies  are of interest herein.

Based upon this review, chemical precipitation was selected to be the
most widely accepted means of removing phosphorus.  Because
chemical precipitation provides  many alternatives (both of chemicals
and application points) a discussion follows the literature  review in
which  the specifics of each process option  are presented.
                               15

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                   LITERATURE REVIEW


CHEMICAL PRECIPITATION SYSTEMS

Points of Application and Expected Phosphorus Removals.

The most commonly employed points of application are:

      1)  the primary clarifier (in either conventional or physical-
      chemical systems),  2) the  aeration basin,   3) the secondary
      clarifier and 4) the chemical flocculation unit in  a tertiary
      treatment system.

Removals of phosphorus in primary clarification can be achieved
with any of three cations:  Aluminum (Al 34 \(  Calcium  (Ca^+) or Iron
(Fe2+, Fe^+J.  The most common forms in which these cations are
added are shown below:

      Alum
      Sodium Aluminate
      Lime
      Ferrous Chloride,  Ferrous Sulfate
      Ferric Chloride,  Ferric Sulfate

The chemistry of aluminum and iron reactions with phosphorus are
similar.  Both can be postulated on the basis of a precipitation
reactions involving the formation of aluminum phosphate or ferric
phosphate, and additionally the formation of aluminum or ferric
hydroxide.  The  chemistry of these reactions  is actually quite
complex, serving in part to explain the difficulty accompanying the
estimation of required cation dosages.  The use of the reduced  Torm
of iron (ferrous) is prompted by the availability of pickle  liquor (prini-
pally ferrous sulfate) a waste product of steel mills.  Although
oxidation to Fe^+ does occur,  it is also possible for ferrous phosphate
to precipitate.

The addition of calcium in the  form of  lime results in precipitation of
hydroxyapatite,  Ca10 (PC»4)6 (OH)2, as well as calcium carbonate,
CaCC»3f  and possibly magnesium  hydroxide Mg (OH)2 at very high
pH.  The chemistry of calcium addition is  also complex.  In fact,
recent studies by Ferguson and McCarty (1) and Jenkins,  et al
(2) indicate that precipitation of phosphorus can occur at neutral piJ
conditions when calcium is added in forms other than lime.

In comparing these three cations, aluminum,  calcium and iron, it
may be noted that both aluminum  and iron are added as  salts of
common anions  (SO^' and Cl"),  while calcium is added with
hydroxide ions.   Thus,  aluminum and iron contribute anions to  the
wastewater which may be of concern in the future when water re-use
becomes more prevalent  (3).   In contrast,  lime adds only calcium
because  the hydroxide ions can be easily neutralized in later  stages
of treatment.
                              16

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Chemical addition to the primary clarifier has both advantages and
disadvantages.  In addition to removing phosphorus, chemical
precipitation also enhances both removal of BOD (biochemical oxygen
demand) and suspended solids.  As estimates, the removal of BOD
has been shown to increase from the standard value of 30 per cent tD
about 60 per cent.  Similarly suspended solids removal increases
from 70 per cent to a maximum of about 90 per cent (4). These
additional removals could  provide a measure of  relief to overloaded
secondary facilities.

On the other hand,  because hydrolysis of complex organic and
inorganic phosphorus compounds is  incomplete prior  to biological
treatment, the expected final effluent phosphorus concentration is
quite variable and significantly higher than that achievable in tertiary
phosphorus  removal.  In a review of data available from pilot plant
and full-scale testing, Minton and Carlson (5) report  the results  of
ten researchers and indicate  effluent phosphorus concentrations
ranging from 0. 15 to 2.3 mg / 1 .  The lower values, however,  were
only obtained after filtration.  This  indicates that  some phosphorus
was not readily precipitated or  that  insoluble phosphorus escaped
due to deficiencies in clarification design.

Both aluminum and iron dosages can be expressed as a concentration
ratio of cation to phosphorus  (Al /P  or Fe/P).  Earlier research
results were reported in terms of per cent phosphorus  removal.
However, it was recognized that the phosphorus content of waste-
waters is quite variable both at a given plant and from plant to plant.
Thus,  to specifically state the chemical requirements,  a cation/
phosphorus  ratio is needed.   Again, just as  effluent phosphorus
values were shown to be quite variable, so too were the cation/
phosphorus  ratios as indicated by the data reviewed by  Minton  and
Carlson (5).  The weight ratios of aluminum to P for  two studies
were 1. 5 and 3. 4 while that of three studies of iron were 2.8,  3.1
and  5.8.

The addition of aluminum  as alum will depress pH and may necessitate
the addition of base in a low alkalinity water in order to maximize
phosphorus  removal.  Added as sodium aluminate, pH will tend to
increase which may displace the precipitation reaction  from the
optimal pH.  This is  especially of importance in primary clarifiers
where axial dispersion is  slight thus assuring increased pH near the
point of application (5).  Hence the addition of sodium aluminate  to
primary clarifiers is not recommended.
 In wastewaters of low alkalinity (less than 150 mg/1 as
the addition of lime will increase pH to values greater than 11  before
adequate phosphorus  removal is obtained.  This implies that re-
carbonation, or some other form of pH adjustment will be necessary
prior to biological treatment.  On the other hand,  wastewaters of
higher alkalinity will provide a buffering capacity  sufficient to
prevent the pH from increasing above about 10 while achieving the
                              17

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 required phosphorus removal.  Moreover, tTiese wastewaters usually
 contain significant carbonate alkalinity which enables co-precipitation
 of CaCOs thereby enhancing the settleability of hydroxyapatite.
 However,  if wastewaters have high alkalinity but low hardness (calcium
 and magnesium),  then co-precipitation may not prevail (3).

 Lime treatment of raw sewage result in similar variations in effluent
 phosphorus as observed for aluminum and iron treatment.  Examination
 of extensive field data from a full scale test  at a 2. 0 MGD plant  in
 New Market, Ontario (6) indicate an effluent phosphorus of 2.0 mg/1
 with a lime dosage of 200 mg/1 Ca(OH)2-  In another full scale test
 at Newport,  Vermont  (7),  80 per cent removal of phosphorus (effluent
 concentration unspecified) was  only achieved at dosages greater than
 400 mg/1 (as Ca(OH)2).  The City of Rochester (8) will employ lime
 addition to primary clarifiers and this will be  followed by the activated
 sludge process. A dosage of 125 mg/1 Ca(OH)2 is expected to produce
 a residual soluble phosphorus of 2 mg /1 at a pH of about 10.0.  A
 three month plant scale investigation at Richmond Hill,  Ontario
 indicated that a lime dose of 175 mg/1 produced a pH of 9. 3 and a
 83 per cent removal  of phosphorus.  Plant effluent phosphorus was
 stated to be  0. 9 mg/1 (9).

 From review of various studies on lime addition to the primary
 clarifier, it may be concluded that the dosage  of lime is directly
 related to alkalinity.  Higher alkalinities  require higher lime dosages
 to achieve a given pH.  In fact, lime dosing is independent of influent
 phosphorus concentration and dependent on alkalinity and operation
 pH (10).

 As a practical lower  limit, wastewaters having alkalinity less than
 150 mg/1 as CaCO3 are not suitable for lime treatment because  pH
 will increase to levels greater than 10.0 before effective phosphorus
 removal occurs, and this will be  unacceptable if biological treat-
 ment follows.  To distinguish the lime dosage  required for  moderate
 alkalinity (150-300 mg/1 as CaCOs) from that  for  high alkalinity
 (> 300 mg/I as CaCO3) wastewaters, two levels of lime dose will be
 assumed; moderate alkalinity requires 150 mg/1, while high
 alkalinity requires 200 mg/1.  Further,  based upon field studies the
 achievable total unfiltered effluent phosphorus  is estimated con-
 servatively to be 2 mg/1.

Although lime will be later shown to  offer advantages in sludge
handling,  consideration must also  be given to solids recycle and
prevention of excessive scaling (3).  This may require modification
of the primary clarifier.   Lime recovery is not possible if  lime  is
added to  the primary clarifier because of excessive  amounts  of
contaminants present in the  sludge.  Moreover, special consideration
 should be given to locations where anaerobic  digestion is used for
 sludge handling.  As will be discussed in later sections, lime sludge
could cause digester problems.
                              18

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The combined biological-chemical removal system provides a method
of improving secondary sludge handling characteristics while  simul-
taneously removing phosphorus.   As pointed out by Minton and
Carlson (5),  use of this system also implies that careful consideration
be given to sludge wastage, maintenance of the culture and satisfactory
floe formation (secondary clarification).

Sludge wastage will control the build-up of inorganic precipitates in
the aeration basin.  If build-up becomes significant then a higher level
of solids will be needed.  Survival of the culture may be a factor if
the dosage of aluminum or iron salts depress pH excessively.  For
example,  although BOD removal may still be unaffected,  the rate of
nitrification may be reduced during severe pH depression (11).
Satisfactory floe formation is related to the production of biological
floe in removing chemically precipitated phosphorus.  Polymers
may be needed to assist in achieving good settleability.

Minton and Carlson (5) list results of eight studies of alum, seven of
sodium aluminate  and three of ferric chloride for removal of
phosphorus in a biological-chemical scheme.  Effluent total phosphorus
values range from a low of 0.5 mg/1 to a high of 6.8 mg/1.  These
authors further suggest that without the ability to remove insolubilized
phosphorus,  final  effluent concentrations can be expected to exceed
1. 5 mg/1. With the addition of filtration as a tertiary step, residuals
of 0.5 mg/1 can be achieved.

Minton and Carlson (5) also list  the cation/phosphorus ratio used in
each investigation.  For alum, this value ranged from 0.8 to  2. 1;
for sodium aluminate, from 0.7  to  1.2;  for ferric chloride, from
2.3 to 6.7.  Similar results are  listed in the EPA Process  Design
Manual on Phosphorus Removal  (9).  Based on these reports, it was
concluded that the weight ratio of Al/P be estimated as  1.5/1 and
that of Fe/P as 4/1.

Sodium aluminate should  be added in the aeration basins because
axial dispersion will prevent excessive pH rise. This chemical
may be of interest in wastewaters of low alkalinity.  However,  it has
been  suggested that other means of controlling pH, namely adding a
base  such as soda ash or sodium hydroxide,  should be used in con-
junction with alum, thus  avoiding the use of sodium aluminate (5,9).
In contrast to the  application point of sodium aluminate, it is
recommended that alum and ferric  iron be dosed to the effluent
channel of the aeration basin (5, 9 ).  Minton and Carlson (5) state that
turbid effluents have often been  associated with cation dosing to the
aeration basin itself,  possible because of formation of poorly settling
cation-hydroxide precipitate.

Pickle liquor,  containing iron in the ferrous form,  can be a con-
venient and inexpensive precipitating chemical.  If the dose point pH
is greater than 7, ferrous ion will be advantageous because ferrous
hydroxide is much more  soluble than either aluminum hydroxide or
                              19

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ferric hydroxide and thus not detract from settleability.  Studies
performed by the Detroit Metro Water Department (12) and the
Milwaukee Sewerage Commission (13) indicated that pickle liquor
provided satisfactory removal of phosphorus when added to the
aeration basin.   The addition of pickle liquor  should be made at the
head of the aeration basin to allow time for oxidation of Fe^* to
Fe^+.  Jenkins,  et_al.  (2), however,  point out that ferrous phosphate
may also precipitate.

Although investigated to a lesser extent, the addition of calcium in
forms other than lime has been postulated as  another phosphorus
removal alternative (1,2).  In wastewaters low in magnesium and
carbonate, precipitation  of Ca3(PC>4)2 will occur at pH of 8.  Hence,
calcium could be added to the aeration basin without causing the
excessive pH elevation associated with lime.  Jenkins, et al, (2)
further suggest that solids recycle will enhance the rate  of calcium
phosphate precipitation.  In fact, these researchers have reasoned
that this mechanism may account for high phosphorus removals
presently achieved at specific activated sludge plants that are not
adding any precipitating chemicals.  At the present time there is,
unfortunately, no pilot or full-scale  plant data to substantiate the
success of this process alternative.

In trickling filter plants,  chemicals  should not be added ahead of the
trickling filters (3, 9).  Rather,  chemicals should be  added to the
inlet of either the primary clarifier  or secondary clarifier.  Because
of the many different recirculation schemes in use,  Cecil cautions
that chemical addition after trickling filters be only used where the
recirculation pattern is filter outlet  to primary clarifier inlet,  or
secondary clarifier outlet to primary clarifier inlet (3).

Based on limited data presented in the EPA Process  Design Manual on
Phosphorus Removal (9),  the weight ratios of Al/P and  Fe/P were
determined to be 2.0/1 and 3.5/1 respectively for trickling filter
systems.  The achievable effluent phosphorus  remains the  same as
that of chemical addition to the aeration basin or primary clarifier,
i.e.,  2 mg /I.

Tertiary treatment systems include  both filtration after chemical
addition to the aeration basin, and addition of precipitating chemicals
in a tertiary step followed by filtration.  As mentioned previously,
chemical addition to the aeration basin together with  a final filtration
step after secondary clarification can remove  insoluble phosphorus
such that the final effluent phosphorus concentration is reduced to
0.5 mg/1.

Lime addition in tertiary treatment has been investigated to the
greatest extent, perhaps  as result of the demonstration project at
Lake  Tahoe (14).  Although capital expense is  largest in a tertiary
facility, the effluent phosphorus concentration can be reduced as low
as 0. 1 mg/1.   This is a factor of twenty lower than that achievable
                              20

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with either addition to the primary or secondary system.  In addition,
lime treatment at this application point enables  lime recovery to be
practiced.

In tertiary treatment using lime,  the extent of pH elevation is deter-
mined by the alkalinity.   Thus, moderate to high alkalinity (> 300 mg / 1
as CaCC>3) require a  dosage of lime sufficient to raise pH to about
9.5-10.  Prior to discharge, recarbonation must be used to reduce the
pH to an acceptable level.  This is referred to as single stage recar-
bonation because chemical flocculation is followed by clarification
and then recarbonation prior to filtration.  Lime dosage is difficult
to predict as a function of alkalinity (9).   However, as a "best esti-
mate", for alkalinities between 150 and 300 mg /1 as CaCOs,  a lime
dosage of 200 mg /1 (as Ca(OH)2 is required.  Alkalinities greater
than 300 mg /1 as  CaCO3 will require 265 mg/1  (as Ca(OH)2).  With-
out filtration, the expected effluent phosphorus  concentration is
1.0 mg/1. With filtration, it is 0.5  mg/1.

In contrast, the pH of wastewaters of low to moderate alkalinity (less
than 200 mg/1 as  CaCO^) will increase to values greater than 11
before the lime dosage produces satisfactory phosphorus removal.
Because of the low fraction of CaCC>3 formed in low alkalinity waters,
floe will settle poorly.  Thus a two stage recarbonation process is
selected for production of more CaCO3 precipitate and for depression
of pH to the required final effluent value.  This  process therefore
consists of chemical flocculation,  clarification,  firststage recar-
bonation (to pH of about 10.5),  clarification, second-stage recar-
bonation (to pH of about 7.5) and finally, filtration.  Again, as a
"best  estimate", a lime dosage of 400 mg/1 is required for waste-
waters of low alkalinity (< 150 mg/1 as CaCC>3)  while a lime dosage
of 530 mg/1 is required for moderate alkalinity (150-250 mg/1 as
CaCOs).  Experience with this process is better documented than
single stage recarbonation.   Hence,  the achievable effluent phosphorus
concentration is estimated to be 0. 1 mg/1 rather than 0.5 mg/1.

The addition of aluminum in a tertiary scheme can also produce a
lower final phosphorus concentration than either addition to the
primary or secondary system (9).  On the other hand,  iron salts are
less desirable because of residual iron remaining in the treated
water. Minton and Carlson (5) summarized the findings of five
researchers investigating alum in pilot-scale tertiary treatment.
Filtered effluent phosphorus values ranged from 0.05 to 2.3 mg/1.
Unfiltered effluent phosphorus ranged from 0.27 to 3.0 mg/1.  The
EPA Process Design Manual for Phosphorus Removal (9) suggests
that with proper operation,  effluent phosphorus can be reduced to
0. 1 mg/1 with filtration  and  1. 0 mg/1 without filtration (but with
polymer addition).

Unlike lime,  the recovery of alum has not been shown to be practical.
Hence, alum  addition could only offer an advantage where local costs
of alum are low enough to offset the costs associated with the more
complicated single and two stage lime treatment system.
                              21

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Quantity of Sludge Produced

Wastewater treatment plants precipitating phosphorus by chemical
addition increase the amount of sludge to be handled.  The quantity
of sludge produced is dependent principally on the type and dosage
of precipitant used.  To obtain a first estimate of the additional sludge
mass to be produced by chemical addition, calculations may be made
based upon the stoichiometry of the chemical reactions involved.  This
approach has  been  illustrated for the case of iron addition to raw
wastewater  in the EPA Process Design Manual on Phosphorus Control
(9).

Due to practical factors, stoichiometric  equations can only be used as
a rough guide to sludge production.  The nature of chemical precipi-
tates and their ability to be captured in sedimentation basins,  for
example, are affected by many variables which  cannot be adequately
treated in a theoretical approach.  In the case of lime coagulation,
the actual composition  of the calcium precipitates is not even definitely
established.   Hence, it is more reliable  to employ actual data from
pilot plant or  full-scale testing to predict sludge production from
chemical precipitation.

Available data on sludge production from phosphorus removal systems
is limited, but some values have been reported.  A review article by
Adrian and Smith (15) contains data obtained from 13 case histories.
Tabulations of sludge quantities and densities are presented for
calcium, aluminum,  and iron addition at various points in treatment
systems. Similar  data has been presented by VanFleet et al  (6),  who
documented six recent  case histories in Ontario.  The EPA Process
Design Manual (9)  also includes  data on sludge production at  several
locations.  Other data on sludge  volume produced by chemical pre-
cipitation systems  has  been reported by Schmid and McKinnery (16)
and Jenkins, et al_.   (2)

Sludge Handling

At the outset of phosphorus removal investigations,  little attention
was given to the ultimate fate of  precipitated phosphorus.  Although
there is still very little plant operating data available, recent studies
have dealt more fully with this crucial aspect of phosphorus removal.

In many existing  plants, anerobic digesters are used for  stabilization
of both primary and secondary sludges.  Two factors  are important to
the success of chemical precipitation in such facilities.  First, the
cation associated with phosphorus removal must not interfere with
sludge digestion, and second, phosphorus resolubilization should be
minimal.

Studies by Grigoropoulos,  et aJ (17) have shown that neither alum nor
sodium aluminate (both added to the aeration basin) were detrimental
                              22

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to digester performance.  Further, these researchers concluded
that precipitated phosphorus was not released to the supernatant
during digestion.  In fact, phosphorus present in the primary sludge
was also removed.  Similar findings were reported by Thompson (7).

In full-scale testing, Van Fleet, jet^ aL (6) reported recently that in-
creasing the alum dosage above 150 mg /1 caused a drop in digester
temperature and gas production.  However, below  a dosage of
150 mg / 1,  digestion appeared unaffected.

Malhotra,  et ajl^lS) demonstrated that iron  ohosphate  precipitates
behaved differently  than aluminum phosphate precipitates.  Primary
sludges, with or without  iron (ferrous) precipitated phosphorus
indicated a  significant uptake of phosphorus during digestion.  A
similar observation was  noted by Thompson (7). In contrast,  waste
activated sludge containing mostly ferric phosphate released phos-
phorus upon digestion.   The solubility of ferrous phosphate is  greater
than that of ferric phosphate and could,  as the authors point out,
account for the  release of phosphorus when the  waste  activated sludge
is anaerobically digested.  The work of Singer (19) confirms this
postulation.

It may also be noted that in the event of phosphorus release to the
supernatant, recycle to the primary clarifier would only require
that a greater dosage of precipitating chemical  be used (18). Economic
operation,  however demands that supernatant release be minimized.

In full-scale tests at nine small activated sludge plants in Zurich,
Switzerland, addition of iron chloride to the aeration  basin had no
noticeable  effect on sludge digestion (20).

Sludge handling  of lime precipitated phosphorus by anaerobic digestion
can cause difficulty if the pH of sludge is greatly elevated.  However,
Van Fleet,  et_ al (6) reported that holding of the lime sludge to a depth
of one to two feet in the primary clarifier has solved  this problem in
a full-scale test.

In addition to anaerobic digestion,  the Ontario Ministry of Environ-
ment (6) has provided the results of full scale testing  at several
facilities where vacuum  filtration is in  use. Anaerobic digestion at
six activated sludge plants using various chemical precipitation
options and vacuum filtration at three other plants have been studied.

Tables 1 and 2  summarize the data that is currently available from
these  investigations.  The  increase in sludge volumes as  a result of
chemical precipitation confirm to some  extent "the rule of thumb"
which states that sludge  production will double.  This has been indi-
cated  in the EPA Process Design Manual on Phosphorus Removal (9)
and as well by Minton and Carlson  (5).
                              23

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                                        TABLE  1
  Plant

New Market
(Activated)

Barrie
(Activated
sludge)

N. Toronto
(Activated
sludge)
                    Effect of Chemical Additions for Phosphorus Removal
                                       on Digestion (6)
Flowrate
   MGD

   2.0
  7.5
Chemical

  Lime


  Alum



  Fuels
Dose
mg /e

 200
                           150
  35
   Percent
    w/o
p removal


    3-4
            4.54
   Solids      Sludge
   with       w/o
p removal  p removal
            Ibs/MGD

  10-11       1700
               4.25
Production
   with
p removal


   4900

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                                            Table 2

                       Effect of Chemical Additions for Phosphorus Removal

                                     on Vacuum Filtration (6)
  Plant

W.  Windsor
(Primary)

Little R.
(Activated Sludge)

Little R.

N. Toronto
(Activated Sludge
                                                                            % Solids to
                                                                              Filter
Flow Rate
MOD
24
4
4
Chemical
Alum
Poylmer
Alum
Lime
Dose
mg/1
90
0.4
.50
125
w/o P
removal
11.5
6.2
6.2
withF
remov
7.6
5.7
11.6
7.5
FeCl.
35

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                                                Table 2 --Continued
CT-
               Plant

           W. Windsor
           (Primar y)

           Little R.
           (Activated Sludge)

           Little R.

           No. Toronto
           (Activated Sludge)
    Filter  Yield
     lbs/hr/ftz
 w/o P     with P
removal    removal
  11.3


   5.2


   5.2

  2. 27
 5.8


 4.6


 7.2

4.74
               Filter Cake
                 Solids
           w/oP       withP
          removal    removal
31. 1
19.2
            15.9
                       Sludge Production
                             Ibs/MG
                       w/o P      with P
                      removal     removal
960
           1580
                       1580
2l60
            2440
                        2320

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As noted in Table 2, alum sludges diminished vacuum filtration
yields while both lime and ferric chloride sludges increased filter
yields.  In addition, alum sharply reduced the per cent solids of
both the feed sludge and filter cake while lime increased these
parameters.

In this same field study,  chemical conditioning of alum sludges was
found to be much more difficult at the primary West Windsor primary
plant (chemical costs increased from $3. 10 to  $9.50  per ton of dry
solids).  In contrast, little difficulty was encountered with alum
sludge at the Little River Activated sludge plant (chemical costs
increased  from $16 to $17.96 per ton of dry solids).   Lime sludge
actually reduced chemical conditioning  costs from $16 to $11. 14
per ton of  dry solids.

Pilot plant studies of physical-chemical treatment at the Cleveland
Westerly plant (21) included collection of sludge handling data.  Using
lime addition to the chemical clarifier, per cent solids ranged from
6 to 14 per cent.  Both a vacuum  filter  and a centrifuge were investi-
gated for dewatering of this chemical sludge.  Depending upon
influent per cent solids,  vacuum filtration produced a cake containing
from 14 to 36 per cent solids.  Filter loadings varied from 3 to 19
Ibs/hr/ft   .  Success at higher loadings was attributable to the addition
of polymers (2 Ibs per ton of dry  solids).  Centrifuging produced a
cake  solids ranging from 20 to 28 per cent at a rotational speed of
3500 rev/min.   Polymer addition (1.2 to 1.7 Ibs per  ton of dry solids)
was required.


Novel Modifications of Chemical Precipitation Systems

Sadek (22)  has  reported the use of sacrificial electrodes of either iron
or aluminum to introduce the cation necessary for removal of phos-
phorus.  This system offers the advantage of introducing only the
cation.  In addition, Sadek claims that the evolution of hydrogen gas
at the other electrode can be used to promote flotation of suspended
material in wastewater.

Only  bench-scale testing of this unique  method of chemical precipi-
tation has  been reported.  Although these results were used to
estimate process feasibility and costs,  it is difficult to predict the
future of electro-chemical cation generation without  pilot plant data.
Cecil (3),  however, suggests that further work should be encouraged.

The moving bed filter concept has been pilot plant tested by Johns-
Manville Product Corporation (23).  This process is actually a
tertiary treatment system consisting  of chemical addition,  clarifi-
cation and filtration.  A bed of sand is pulsed upward in an inclined
filter vessel to contact chemically treated wastewater in a  constant
head tank.  Filtered wastewater passes down through the sand-bed.
The top layer of sand that has trapped  chemical floe drops to the
bottom of  the clarifier (constant head tank) and is removed as sludge.
                               27

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This spent sand is then clean and returned to the filter  system while
the wash water containing chemically precipitated phosphorus is
removed for further sludge processing because floe-laden sand is
replaced continually with fresh sand.  Filtration need not be inter-
rupted for  backwashing.

Although the moving bed filter offers the advantage of continuous
operation,  it is a more complex system than conventional filtration.
Moreover, removal of phosphorus should not be expected to be  any
more complete than in other chemical precipitation systems employing
filtration.  Hence, this system does not warrant consideration as a
process option for immediate implementation.


Evaluation of Process Data

As pointed out by Minton and Carlson (5), the method of data reporting
used by researchers investigating chemical phosphorus removal
systems lacks uniformity.  For example, because of the wide
variation in reported biological removals of phosphorus,  the cation/
phosphorus ratio should always be based upon the phosphorus left to
be removed chemically.  Moreover, the  distinction between total
phosphorus residuals and filtrate phosphorus residuals is clouded by
variations  in filter pore sizes  used  by investigators.  Of even greater
concern, some studies  have failed to report the basis on which
effluent phosphorus is measured.

The variability in results is graphically depicted by Minton and
Carlson (5) in a plot of  total phosphorus and filtrate phosphorus as a
function of the aluminum/phosphor us molar ratio.  The data is  widely
scattered,  making selection of a cation/phosphorus ratio difficult.
These authors attribute inconsistencies in part to the lack of corre-
lation with system pH.

Based on this assessment of data by Minton and Carlson (5)  and infor-
mation provided both by the EPA  Process Design Manual on Phos-
phorus Removal (9)  and a review article by Jenkins,  £^£^.(2) four
levels of effluent phosphorus concentration were assumed to be
achievable.  These were discussed  in an earlier section.  To
reiterate:  addition of chemicals to  either the primary clarifier or
aeration basin (or secondary clarifier of a trickling filter plant) will
result in a total phosphorus concentration of 2 mg /1; addition of
chemicals  to the aeration basin followed  by clarification and filtration
will reduce the effluent phosphorus  concentration to 0.5 mg / 1;  and
addition of tertiary chemical treatment will produce the lowest
phosphorus concentration of 0. 1 mg/1 using lime and 0. 3 mg '1 using alum.

Although addition of chemicals to the aeration basin of conventional
activated sludge systems has  been discussed in detail,  there is
little process data available on chemical addition to extended aeration
facilities.  Because primary clarifiers are not usually included in
this form of treatment, chemicals must be added to the aeration
                              28

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basin unless tertiary treatment is proposed.  Several technical
problems may arise in this system, primarily as a result of high per
cent sludge recycle.

It can be postulated that extended aeration systems to which chemicals
are added will show a continual increase in suspended solids.  This
could impede clarification,  increase mixing requirements, and over-
load the sludge recycle system.  Moreover, without sludge wasteing,
pH depression caused by alum or ferric chloride addition could be
severe.  Undoubtedly,  sludge removal will be required at much more
frequent intervals than commonly encountered in extended aeration
plants.

Ewing Engineering Company performed a plant-scale study of alumi-
num (both alum and sodium aluminate) and iron  (waste pickle liquor)
addition to an extended aeration facility (24). Mixed liquor suspended
solids increased from 7000 to a maximum of 11,000 mg/1.   Unfor-
tunately, the period of time was not specified;  however,  it was less
than six months.  Because the alkalinity of the   waste-
water was high (400 mg/1 as  CaCC^),  pH remained between  6.8  and
8.2.  Biological  activity was  not affected measurably by any of the
chemical additions.  However,  solids production increased by about
seven to eight pounds per pound  of phosphorus removed.  This in-
creased the  required sludge wastage by approximately 100 per cent.

From this brief  study of extended aeration systems,  it is apparent
that a more  careful analysis  of chemical addition will be  required
before being implemented on a wide scale.


BIOLOGICAL PHOSPHORUS  UPTAKE

All biological wastewater treatment processes require inorganic nutrients to
sustain growth.   Thus,  it is not surprising that  some  phosphorus removal is
noted in activated sludge and trickling filter  systems.  Nevertheless,  it is
difficult to consider this a technique that will provide a predictable
and significant phosphorus  removal.  Most reports state that the
expected phosphorus removal in a biological system amounts to
about 2 to 3 mg/1 at pH4.   At San Antonio, Texas (Rilling Plant),
Los Angeles (Hyperion Plant) and Baltimore, Maryland (Back River
Plant), 90 per cent phosphorus removal was indicated.  This prompted
 study by the EPA in 12 other activated sludge plants.   All of these
other plants showed erratic removals, with most indicating  very
 little removal (4).

 The luxury biological uptake theory put forth by Levin and Shapiro  (25)
 to  explain biological removals has been refuted by Mulbarger, et^al_(26)
 and Jenkins, et  al (2).  In fact,  these latter  two authors  suggest that
 chemical precipitation of Ca2HPC>4 with the  proper range of pH and
 calcium concentration can  account for a considerable increase of
 phosphorus  removal beyond that characteristics of biological  uptake.
                               29

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Cecil suggests that biological removals of phosphorus cannot be
predicted because the basic mechanism of uptake is not known (3).
He recommends, however,  that operating conditions be maintained
carefully at specific activated sludge plants where biological uptake
has been noted to be significant.

More recently,  Levin,  et aj. (27) reported on pilot plant studies in
Washington,  D. C. in which a controlled process for  biological re-
moval of phosphorus was evaluated.  In this process, activated
sludge withdrawn from the secondary clarifier enters a thickener
and is held for up to 12 hours.   During this time, anaerobic con-
ditions develop and cause the release of phosphorus into the super-
natant. Activated sludge, now, deprived of phosphorus, is returned
to the  aeration basin where luxury phosphorus uptake occurs. Super-
natant from the thickener, containing a high concentration of
phosphorus in a relatively small volume, is then chemically coagu-
lated for ultimate removal of phosphorus.

Results reported by Levin,  e£ a_l (27) were obtained over a relatively
short time (two months). Further,  the objective was somewhat
limited to demonstrating process feasibility rather than optimizing
design.  Several key features of  the process require further study.
These all relate to process stability during sustained operation in
which  sludge characteristics could be affected by changing waste-
water  characteristics and flowrates.  Although this study did evaluate
to some extent variations in process loading, there is still a need
for  collection of data over a longer time period.

Sherrard  and Schroeder (28) lend support to the  luxury uptake theory
with their stoichiometric calculations of cellular phosphorus.  Cell
residence time is, however, very critical to optimal phosphorus
removal.  At low cell residence  times, cell growth rate is maximized
thereby maximizing phosphorus removal.  The initial ratio  of organic
matter to phosphorus was also shown by calculations to affect
biological uptake efficiency.

It may be concluded that biological uptake cannot be put forth as a
generally accepted means of phosphorus removal, but must rather
be considered in conjunction with chemical precipitation (which may
further be enhanced by chemical additions).

ACTIVATED ALUMINA

Activated alumina has been shown to remove phosphorus by a
mechanism best described as a combination of adsorption and ion-
exchange.  In this process, removal of phosphorus causes exhaustion
of the  columnar bed of activated  alumina through which wastewater
is passed. The rate  of exhaustion has been predicted by mathematical
modeling  using synthetic sewage and laboratory  columns (29).   In
considering practical application of this process, the most critical
parameters become  1) length of service provided by a given charge
                              30

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of activated alumina,  2) degree of difficulty in regeneration and
3) interference from other constituents of the waste-water,  e.g. , head
loss in the bed and surface fouling.

Ames (30) reported the results  of laboratory studies in which both
synthetic  sewage and secondary effluent were fed to a column charged
with activated alumina.  Using  secondary effluent,  a steady decline
in phosphorus loading  capacity was noted after  each regeneration
cycle. On Cycle I,  600 bed volumes were treated before significant
phosphorus breakthrough occurred;  however, only 200 bed volumes
could be treated on Cycle V.

The regenerant solution was 1 molar NaOH.  It was concluded that
solids were precipitating  in the column during regeneration thus re-
ducing the efficiency of phosphorus stripping.   An acid  wash with
HC 1 followed by regeneration with a  molar NaOH renewed  the phos-
phorus capacity close  to that originally observed.

It should be noted that a carbon bed was used prior to the activated
alumina column to prevent carryover of organics which had in previous
runs caused a build-up of bacterial slime on the alumina.  Thus,
practical  installation of this process as a tertiary treatment step
would involve more than just an activated alumina column.  Moreover,
the regenerant solution must, of course, be further treated to remove
captured phosphorus.  Ames (30) suggests the use  of lime  in a typical
chemical  precipitation scheme.  The advantage offered by this system
is a much reduced volume.   That is, while phosphorus  is removed
from 600  bed volumes of wastewater, the volume of regenerant to be
treated is  only about 20 bed volumes.

ION EXCHANGE

Most experience with  ion exchange involves strong base anion resins
in the chloride form.  Eliassen et^al^S!) reported  successful appli-
cation of ion exchange following either flocculation and filtration or
filtration  alone.  A conventional activated sludge plant  would therefore
require multiple tertiary units  to achieve phosphorus removal.

Without pretreatment, resin fouling  severly restricts exchange
efficiency (31).  Because regeneration becomes less effective after
each cycle, periodic cleaning of the  resin is required.   Pollio and
Kunin (32) in later studies reported similar results.  Gregory and
Dhond (33) confirmed  Eliassen1 s finding  regarding  preferential
exchange  of sulfate.  That is,  after breakthrough of phosphorus,
sulfate continues to be removed.  Therefore,  wastewaters high in
sulfate limit the effective resin capacity for phosphorus and in
addition,  cause more  chloride ions to enter the effluent water.

In column studies using secondary effluent, a breakthrough of less
than 0. 3 mg / 1  of phosphorus  occurred after  100 bed volumes had
been treated (33).  Although excessive head loss due to clogging by
                               31

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suspended solids did not occur, Gregory and Dhond noted that this may
be a serious problem in plants with poor secondary effluents.  Organic
matter was also removed by the exchange columns, but,  for the
limited number of cycles of operation in this study, phosphorus
removal was not impaired as a result.

Economics and efficiency demand that regenerant volume be mini-
mized.   Gregory and Dhond (33) observed that about four bed volumes
of regenerant were needed for every 100 bed volumes processed. The
waste regenerant solution must then be disposed.  For small volumes,
evaporation may be  practical. Larger volumes warrant  precipitation
for removal of phosphorus.

Gregory and Dhond (38) concluded that ion exchange for phosphorus
removal was of only limited  application due  to economics. Specifically,
they cited its  use in instances where local situations demand a very
high quality effluent; for example, discharge to a recreational lake.
A low concentration of sulfate may also be considered to  be  essential
to economic use of this process.

Envirogenics  (34) investigated a combination resin/iron sorbing
system for phosphorus removal.   In these studies, a cation  exchange
resin (Amberlite 200) was contacted with ferric chloride  such that
the resin surface then held Fe^ + .  Laboratory column studies  indi-
cated substantial phosphorus  removal  capacity.  Regeneration was
accomplished with 0. 1 molar ferric chloride solution.  The  spent
regenerant could, according  to these investigators, be treated with
lime for ultimate precipitation of phosphorus.

A relatively constant regeneration capacity was observed over ten
cycles;   however, an uneconomical amount of ferric  chloride was
required.  A lesser  percentage of resin regeneration was deemed
essential for economic application of this process. The results of
this study cannot be  stated as conclusive because they were  obtained
from a small  laboratory scale investigation  and were not complete.

Reliable cost  projections and actual operation of the  system are
impossible to predict from such limited information.

Finally,  a  similar study reported by Block (35) was aimed at con-
version of a solid adsorbent  to an anion exchanger.   Exchangeable
cations  in vermiculite were replaced by aluminum  ions.  It was
postulated that columnar operation would result in  removal of
phosphorus by an adsorption reaction involving aluminum ions on
the surface of the vermiculite.  However, it was found that
phosphorus adsorption capacity was far  below that  required for
economic operation and this  process was subsequently disregarded.
                             32

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SELECTION OF PHOSPHORUS REMOVAL SCHEME

As shown in the review of literature, phosphorus can be removed by
chemical precipitation, biological uptake, chemisorption and ion
exchange.  The first technique has been repeatedly shown by
laboratory,  pilot plant, and full-scale testing to be the most success-
ful approach.   The other three techniques, while noteworthy,  suffer
both technological and economic drawbacks.

The phosphorus control schemes to be considered herein are restricted
to chemical precipitation.  However, this does not severely limit the
treatment options available.   Foremost,  there are three cations which
can be used: aluminum, iron, and calcium.  These are generally
added in the following  rather  inexpensive chemical compounds:

      1.   aluminum in alum or sodium aluminate

      2.   iron in ferric or ferrous  chloride as well as ferric
          or ferrous sulfafce

      3.   calcium in calcium hydroxide (lime)

In addition to a selection of chemicals, precipitation offers a  choice
of application points;  the most commonly employed are addition
to:  1) the primary clarifier,  2) the aeration basin,  3) the secondary
clarifier, and  4) the  chemical flocculation unit in a tertiary scheme.

Besides process flexibility,  chemical precipitation offers the
advantage of a minimal investment in capital equipment.  Moreover,
the type of equipment  required is already used in water treatment
practice, thus assuring reliability. Essentially, chemical pre-
cipitation does not involve new process technology.

Finally,  in addition to phosphorus removal,  both organics as  BOD
(biochemical oxygen demand), and suspended solids removals are
enhanced.   The process can therefore serve to upgrade existing
plant efficiency.

Biological uptake,  in contrast,  has not been shown to be a reliable
method of phosphorus control.  Although demonstrated at specific
activated sludge  plants, there is little information on design
factors of impact because there is not at present a clear under-
standing of  the mechanism of removal.  It may be concluded that
more operational data must be obtained before this can be
recommended  as a practical  method of phosphorus control.

Chemisorption is the technique or mechanism associated with the
use of activated alumina for phosphorus removal.  Although the
exact removal mechanism is not understood, it is thought to be a
combination of ion exchange and adsorption.  There have been no
reports of pilot plant or full-scale testing with activated alumina.
                               33

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The chief technical disadvantage of the process is the requirement
for regeneration of the alumina bed before exhaustion of phosphorus
removal capacity.

Furthermore,  the added complexity of another unit operation (packed
beds of activated alumina) needs to be carefully considered in light
of the  inherent operational disadvantages associated with backwashing,
bed fouling,  brine disposal,  and multiple-bed rotational schedules.
Aside  from technical drawbacks,  the  capital and operating costs of
the process have not been fully studied.

In pilot plant studies of ion exchange, organic fouling led to reductions
in regeneration efficiency after each cycle and limited the effective-
ness of a given quantity of resin.   Thus, in order for ion exchange to
be  successfully employed, it will be necessary to pretreat wastewater
even after  secondary clarification.  The technical problems described
above  with regard to activated alumina equally apply  to ion exchange.
Consequently,  unless several advanced waste treatment objectives
are sought simultaneously,  ion exchange cannot be considered as a
practical means of phosphorus control.

Process Opt ions

Both application point and chemical added provide options for a given
community.  These are summarized below and are represented
schematically in Appendix A.

Option ] . Addition to the Primary Clarifier

Chemical Alternatives:

      a.   Alum + polymer
      b.   Ferric Chloride + polymer
      c.   Ferrous Chloride +  Lime
      d.   Lime

Option 2. Addition to a Flocculation Basin Prior to Primary Clarifier

Chemical Alternatives:

      Same  as  a, b,  c,  d above

Option 3. Addition to the Aeration Basin

Chemical Alternatives:

      a.   Alum
      b.   Ferric Chloride
      c.   Sodium Aluminate
                              34

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Option 4.  Addition After Trickling  Filter

Chemical Alternatives

      a.   Alum
      b.   Ferric Chloride

Option 5.  Option 3 or 4 plus multi-media filtration

Option 6.  Addition of lime to a Flocculation Basin Following
          Conventional Secondary Treatment

      a.   Single Stage
      b.   Two Stage

Option 7.  Addition of Alum or Ferric Chloride to a Flocculation
          Basin Following Conventional Secondary Treatment

In all of the above options,  it is assumed that the plant is either
already providing secondary treatment or is under an implementation
schedule to  construct these facilities.  This means that the selection
of phosphorus control schemes is not limited to Option 1 or  Option 2
in an existing primary plant.   Where secondary facilities do not
exist,  however, capital costs computed for phosphorus removal will
include those items  needed to acquire a secondary treatment plant.


INPUT DATA REQUIRED FOR PROCESS OPTIONS

General

In order to  compute the costs directly attributable to phosphorus
removal,  the following technical information must be  known for
each process option:

      1.   Achievable Effluent Phosphorus  Concentration
      2.   Chemical Dose(s) Required
      3.   Quantity of Sludge Produced
      4.   Density of Sludge Produced
      5.   Sludge Handling Processes to be used
      6.   Design Factors for  Sludge Handling Equipment

These factors are discussed individually in the following sections.


Achievable  Effluent  Phosphorus Concentrations

Table  3 lists the four levels of phosphorus concentration estimated to
be achievable with the  specific control strategies  listed.  These levels
are attainable throughout the  range  of influent phosphorus concentration normally
found in municipal wastewaters.   Although advantages for Option 3 over Option 1
have been cited,  process reliability dictated that these be rated the same.  The
                              35

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                             Table 3

           Achievable Effluent Phosphorus Concentrations

      Level (rug / 1 as F)               Process Options

             2                        1,  2, 3, 4
             0.5                      5
             0.5                      6 (Lime, one stage)
             0.1                      6 (Lime, two stages)
             0.3                      7 (Alum)

addition of multi-media filtration (Option  5) provides removal of
insoluble phosphorus, while tertiary treatment (Option 6) adds more
process reliability and control and yields the highest quality effluents.


Chemical Dose(s) Required

For both aluminum and iron addition, the amount of cations required
to achieve the effluent phosphorus concentration described  above  is
proportional to the influent phosphorus concentration.  A considerable
variation in weight ratios was found from study to study for each
cation.   However,  for the purpose of a phosphorus control  strategy
program, only a reasonable estimate is necessary.  Table 4 provides
the weight ratios selected for use for both aluminum and iron  in all
options.


                             Table 4

             Cation/Influent Phosphorus Weight Ratios

        Options      Option      Option       Option     Option
         1.2           3           4            5           7

Al       2/1        1.5/1        2/1          1.5/1        2/1
Fe       3.1/1      4/1          3.5/1       4/1


In addition to the cation of choice,  polymer addition is also recom-
mended at a  level of about 0.5 mg / 1.

In contrast to aluminum and iron precipitation, phosphorus precipi-
tation with calcium depends  upon the formation of  more  than one
precipitate.  That is,  calcium carbonate along with calcium hydroxy
apitite precipitation is considered essential to  successful phosphorus
removal.  Moreover,  a pH in the range of 9.5  to 11.5 is also  required
in most applications.  Therefore, inmost cases,  lime [Ca(OH);?]  is
used for calcium precipitation of phosphorus.

The amount of carbonate  contained in a wastewater directly relates
to the alkalinity of the water supply (and possibly to industrial
                              36

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contributors).  At higher alkalinities,  more lime is needed to reach
a given pH because of the  increased buffer capacity.   In these waters,
lime can be added to the primary clarifier in sufficient dose  to
provide phosphorus removal without raising the pH to an unacceptable
level for subsequent  biological treatment.  On the other hand, waters
of low  alkalinity will reach a pH of 11  to  12 for the same applied lime
dose.  This would be unacceptable if biological treatment followed.
Thus,  the phosphorus control scheme  provided herein considers lime
addition to the primary clarifier (Option  1 or 2) to be valid only if
alkalinity is greater  than  150 mg / 1 as CaCO.,.

Similarly, in  tertiary treatment, lime precipitation is influenced by
alkalinity.  High alkalinity waters permit single stage precipitation
while low alkalinity requires two stages with the  second  stage pro-
viding  re-carbonation to lower pH and precipitate calcium carbonate.
An alkalinity greater than 200 mg /1 has been selected for  meeting
the requirements of  single stage treatment.

The  addition of lime or other  salts containing calcium to the activated
sludge system (pH7.5 to  8.5) was not considered herein.  This
process has been suggested by Jenkins _e_^ al^ (2) as an alternative
phosphorus removal method in low alkalinity waters accompanied by
low magnesium concentrations. However,  little  verification of this
approach could be found from either pilot plant or full-scale testing
programs.

Table  5 lists  the lime dosages to be used in the various phosphorus
removal options.
                                Table 5
                             Lime Dosages
   Lime Dose
mg/1 as CaO

      150


      200


      300


      400

      150


      200
      Option

1,2
Alkalinity 150-300

1,2
Alkalinity > 300
6 (Two Stage)
Alkalinity <  150
6 (Two Stage)
Alkalinity > 150
6 (Single Stage)
Alkalinity 200-300

6 (Single Stage)
Alkalinity > 300
                               37

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Quantity of Sludge Produced

Table 6 lists the values selected to represent sludge production for
each cation precipitant and process option.  The values are based
upon data given in the literature,  employing engineering judgment
where divergent results were reported.  As more information becomes
available,  it will be possible to further refine these values.   The numbers
shown in Table 6 are incorporated in TSHEME subroutine of the  model.

                                Table 6

                            Sludge Production
 Cation
Aluminum
Iron
Calcium
Option
 o,
 "1,2
  3
  4
  5
  7
 •A*
 "1,2
  3
  4
  5
 *j»
 ""1,2
  6A(Single Stage)
  6B(Two Stage)
Sludge Produced

5.7 Ib/lb Aluminum
4 Ib/lb Aluminum
3.6 Ib/lb Aluminum
8 Ib/lb Aluminum
3.6 Ib/lb Aluminum

2.4 Ib/lb Iron
2.4 Ib/lb Iron
2.4 Ib/lb Iron
1300 Ib/MG

3000 Ib/MG
3000 Ib/MG
7000 Ib/MG
 Does not include sludge assumed  from added removal of 50 mg/1
suspended solids.

It may be noted that,  although some estimates in Table 6 are ex-
pressed in pounds per million gallons, sludge production was related
to pounds of cation added where possible to account for varying
chemical dosages. Additionally, it should be pointed out the values
presented represent only the  additional chemical sludge produced by
the  precipitation  process;  they do  not include,  for instance, the
additional incremental removal of  organics that would be achieved by
chemical addition to a primary clarifier.

Density of Sludge Produced

To  define the exact magnitude of the additional  sludge handling load
at a treatment plant when phosphorus  removal is instituted, the sludge
density or per cent solids in the  sludge must be stated.  This parameter
can directly affect the efficiency of sludge thickening and dewatering.
In general, addition of iron or aluminum coagulants will cause a
reduction in percentage  solids resulting in a  bulkier sludge and one
which is more difficult to dewater.  Lime addition, on the  other hand,
seems to produce a denser  sludge  while enhancing dewaterability.
                               38

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Estimates of percentage solids in various chemical sludges produced
by the different process options are given in Table 7.  The values are


                             Table 7

                 Per Cent Solids of Chemical Sludges


  Cation                                            % Solids

Aluminum                1,2                             3
                         3, 4, 5, 7                      1.5

Iron                     1, 2 (Pickle liquor)             8
                         1,2                            2
                         3                               1.3
                         4, 5                            1.5

Calcium                 1, 2                            5
                         6A (Single Stage)               4
                         6B (Two Stage)                 3

based on limited information presented in the literature and should
be updated as better data becomes available.

One area of increasing interest regarding sludge production involves
the use of pure oxygen in activated sludge and aerobic digestion
systems.  A recent pilot study on the use of oxygen in conventional
activated sludge processing has  shown that 40-45% less excess
biological sludge is produced corhpared to conventional plug flow.
diffused air aeration (37).  The economic studies indicate that as
plant size increases,  the costs with oxygenation become less than
conventional diffused air.  The authors projected savings of 20% for
a 100 MGD design.

In regard to  filtering characteristics in the  same pilot study mentioned
above,  it was concluded that waste activated sludge from  an oxygen-
ation system can be vacuum filtered directly without  thickening.
Although studies of aerobic digestion were performed only on a
batch basis,  a stabilized sludge  was obtained in 7-9 days  with a
20-30% reduction in volatile suspended solids.

If the pure oxygen systems are used more frequently in the future,
there will undoubtedly be a reduction in sludge handling costs which
will in  turn influence the cost of phosphorus  removal. More infor-
mation is required, however,  on the reduction of chemical sludge
resulting from phosphorus removal by precipitation and coagulation.

Sludge jiandling Process Options

The overall  purpose  of sludge handling processes is  to reduce the
water and organic content of sludges.  To accomplish this purpose,
                              39

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numerous types and combinations of processes may be used.  The
possibilities are so numerous,  in fact,  that for purposes of this  study
it is necessary to delineate only a few of the more typical sludge
handling schemes.  The schemes selected should, however,  be
representative,  of most of those used in practice since process flow
sheets for  sludge treatment tend to  follow similar arrangements.

The sludge handling options designated in this study are shown
schematically in Appendix B and are summarized in Table 8.


                                Table 8

                          Sludge Handling Options

Option 1. Combined handling of all sludge by gravity thickening,
          anaerobic digestion,  and  mechanical dewatering.

Option 2. Combined handling of all  sludge by gravity thickening,
          dewatering, and incineration.

Option 3. Same as Option 2,  except that secondary (biological)
          sludge is thickened by flotation while primary and tertiary
          (if any) sludge is thickened separately  by gravity.

Option 4. Combined handling of all  sludge by gravity thickening,
          anaerobic digestion,  dewatering, and incineration.
Option 5.  Separate handling of tertiary lime sludge by gravity
          thickening,  centrifugation,  calcination, and slaking.
 Additional options may be added in the future if experience
 t.
it.
Design Factors for Sludge Handling Equipment
                                                          warrants
In order to size sludge handling equipment, estimates of equipment
performance with various types of sludge is needed.  Again, little
data is available.  The loading factors developed for the various
sludge handling processes are given in Appendix C.  The values are
based principally on data presented by Smith (36).  Loading factors
presented for vacuum filtration also incorporated the recent work of
Van Fleet, et al (6).
                              40

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                        SECTION VI

  PHOSPHORUS REMOVAL STRATEGY AND COST MODEL



Use of Model

The phosphorus removal model, REMOVE,  is an interactive simula-
tion of the process of removing phosphorus  from the effluents of muni-
cipal wastewater treatment plants.  Included in the model are the inter-
actions between phosphorus  limiting legislation, upgrading of the
treatment plant,  changes in the population of the community, strength
of the influent wastewater  and the effluent objective to be achieved.
The model evaluates for the user a number  of strategies for achieving
the effluent objective and presents least cost alternatives  in terms of
both unit  cost and estimated total costs.

The three major strategies available to a community for the  control of
phosphorus include:

        1.   Legislation to limit phosphorus  concentration in detergents.

        2.   Chemical methods for treating wastewater to  remove
        phosphorus.

        3.   Diversion of phosphorus bearing effluents to receiving
        waters with greater  assimilative capacity.

It is the basic function of the model to evaluate the interactive effects
on cost for  the first two strategies mentioned above.  In the program-
med version of the model  we have not  considered effluent diversion
since this would require the availability of alternate receiving waters.
This option might not  be available to local communities although if
regional  groupings were considered the option might be viable.  The
model can be incorporated in a regional model  if this is desirable.
At the present time, the programmed  version is suited to the evalua-
tion of strategies and  costs on the local level which might be, for
example, the case of a medium-size community on the  shores of Lake
Erie,  faced with decisions on whether to upgrade their  present plant,
limit industrial effluents,  or pass legislation to limit phosphorus in
detergent products  sold in the community.


Model Description

REMOVE consists of a  series of subroutines which correspond closely
to the physical subsections  of the  phosphorus removal problem as
                              41

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shown in Figure 1.  The flow chart for REMOVE,  -which is  shown in
Figure 2, corresponds closely to the major elements in Figure 1.  In
addition, each of the major subroutines is comprised of smaller sub-
routines which can be  easily modified as additional phosphorus  re-
moval and waste treatment process data becomes  available. REMOVE
has been designed to manipulate variables contained in common blocks,
therefore,  many- of the subroutines have no arguments because  the
heart of the program is contained in the common blocks.

The program has been written in Fortran IV and has been run on an
IBM 360/67. A core size  of 288K bytes is  required for execution when
the program is run in  the interactive mode on a time  shared system.
"With some  modifications the program can be run in a "batch" mode
with some reduction in core size.

REMOVE is designed to provide an estimate of the cost to a particular
community of achieving a designated level of phosphorus  removal. The
program begins with the entry of data describing the community in
terms of population and future trends,  the treatment plant in terms
of present size and excess capacity, and the influent wastewater char-
acteristics.  The data can be entered interactively through  subroutine
SYSTEM.

After input data has been entered, the  user has the opportunity  to in-
vestigate various control strategies for achieving  a low phosphorus
concentration in the wastewater  effluent.  Typically,  the  effects on
cost of reducing phosphorus in detergent products, of increasing or
decreasing the  amount of government financing available, or of using
various treatment options  can be investigated.

From the description of the community,  treatment plant, wastewater
characteristics, and desired  strategy the model will design a treat-
ment  plant  incorporating the present plant as described by the user
and will add those processes  or  additional equipment necessary to
achieve the  desired effluent level.  The process options which will
achieve particular effluent levels are described in Appendix A.  Each
process is  sized according to relationships developed in Reference 10
and by our  own work under this contract as described in Section V.
The program converts the sizing information into  construction costs,
operating man-hours,  maintenance man-hours,  and total material and
supply costs for each process.   It is important to  note that  any  increase
in plant capacity dictated by the  population growth of the community and
not by the requirement for additional phosphorus removal is not includ-
ed in the computed cost.  This is achieved in the BUILD algorithm and
subroutine  which is described later.

The majority of the cost relationships  for the processes and equipment
included in the  program were developed for EPA by Black and Veatch,
                             42

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Inc.  (Reference 6).  Costs representing a fixed percentage of construc-
tion and operating and maintenance were not included in the cost calcu-
lations.  These  costs, which include  yardwork, legal, and administra-
tive charges, may increase the total  cost estimate for each phosphorus
removal process by five to ten percent.  The unit treatment costs  on a
cents per  kilogallon of wastewater treated basis are  computed and
printed for each scheme. The user may refer to  the unit cost as a
rough indication of the "figure-of-merit" of a particular  process
scheme.
Modeling Considerations

The model has been developed as a simulation and as such does not
achieve a mathematical optimization.  The user is presented with least
cost alternatives for various removal strategies and from these alter-
natives can optimize his/her decision.

The reader is referred to the Fortran program listing in Section VIII
for the  specific cost equations and sizing relationships chosen.  The
program is fully documented with comments and can be easily under-
stood by readers with  only a limited knowledge of Fortran program-
ming.   In this section  we are presenting some of the basic considera-
tions upon which the simulation is based.

Limiting the phosphorus concentration in detergents has a
significant influence on wastewater phosphorus concentrations  since
almost 50% of phosphorus in wastewater appears to originate from the
use of household detergents.  This number can vary, however, and we
have found that depending on the volume of non-household  waste treated,
the percentage can vary from 10-75%.  If we assume p  to be the
current percentage of  phosphorus in detergents, p^ to be new legisla-
ted percentages of phosphorus and N to be the total amount of detergent
consumed by the sewered population per year, then:
is the total phosphorus reduction achieved by implementing removal
legislation.

Assuming Pc is the current phosphorus concentration in wastewater,
including sources other than detergents, then PT as shown below is
the concentration in the raw sewage which may be achieved by legislation
assuming that W is the amount of wastewater treated per year.
                PT  = P  - N
                  L    c
                              43

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The  cost to society of this legislation will be directly proportional to
the cost difference for a new phosphate substitute detergent.  We will
assume that Ce is the cost of a new phosphate substitute detergent in
dollars per unit weight of  detergent and Cc is the current cost of a
phosphate containing detergent.  The cost to society  of the new deter-
gent will be:
                CT  =  N(C  - C )  - NC
                  L      e    c      s


The differential cost C  may also be the difference in cost between a
high phosphate percentage detergent and a low one.  In the computer
model Cs will be called the DIFCOS.  We are assuming in the develop-
ment of this methodology that each detergent substitute will  have
similar cleaning power per unit weight and that Cs can be estimated
for each town.

We might also add to the above cost, an enforcement cost E, covering
for example, the cost of having officials enforce the legislation.  This
cost can be considered directly proportional to the community's sew-
ered population,  POP.  When we  include the enforcement cost,
becomes
                CT  = NC  + E(POP)
                 L-i     S


Equations for CL and PL are in subroutine DTGLJM of the model.  The
subroutines are listed in alphabetical order in Section VIII.  Values for
Cs and E have been assumed to be $. 02 and $. 40 respectively based on
best available information.  These values may be changed by the user
and we expect that as phosphate substitutes become more widely accep-
ted,  both values will decrease as a result of greater market compet-
ition and a reduced enforcement requirement.

Chemical treatment methods as discussed  in Section V are presently
the only  practical means of phosphorus control at the  waste treatment
plant.  There are N x M treatment possibilities resulting from the
choice of N chemicals (e.g.,  lime, aluminum,  iron) at M points of
application (e. g. ,  primary, secondary, tertiary) within the treatment
plant.  Although two or more chemicals may be used in combination,
it is usually not practical and we may consider  chemical treatment as
a single, discrete variable which we will call T.  Each value T may
assume represents one chemical treatment applied at  one treatment
stage including one value of T  representing the  option  of no chemical
treatment.  Ideally, we would  like to find a functional  relationship
between chemical dosage and phosphorus effluent level for each of the
values of T.  Unfortunately stochiometric relationships for chemical
phosphorus  removal treatments do not accurately predict the treatment
                             44

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plant results.  In addition,  only a limited number of experimental and
actual phosphorus removal applications have been reported in the lit-
erature and those available give  widely varying results.  For these
reasons we have found it impossible to develop a widely applicable
functional relationship giving detailed descriptions  of each procedure.
Rather, we have established for  each value of the treatment variable
a maximum expected value for phosphorus concentration in the  plant
effluent.  This value is called PQut(T).   A list of treatment options and
the value of Pout(T) is given in Appendix A.

The effluent phosphorus concentration will be given by:


                P  ,, = min of [P- ,  P   .(T)l
                 eff          L  L   our  J


In general, treatment will usually be required since a minimum PL
will generally be greater than 2  mg/1 which is the maximum allowable
effluent concentration in many locations.

A cost function relating the cost of chemicals, handling equipment and
storage can also be defined.  These costs will be designated by
and will include amortized equipment cost as well as the costs  for
energy, chemicals, and maintenance.
                Crp(T) = C   .  (W) + C;    (W) + C   .(plf chemical)
                  Tv  '    equip       o+rrv   '    mat H.


 The cost of chemicals will be a function of the level of phosphorus in
 the influent and this in turn is affected by the legislated level of phos-
 phorus in detergent products.  The dosing relationships for the various
 chemicals used in the phosphorus removal treatment have been dis-
 cussed in Section V.  The specific Cation/Influent phosphorus weight
 ratios used in the model and the  lime dosages are summarized in
 Tables 4 and  5 of Section IV.

 The addition of a  chemical treatment scheme for phosphorus removal
 to an existing waste treatment  plant will result in the production of
 additional sludge.   The handling  and processing of this sludge results
 in additional costs.   The amount of additional sludge, which we will
 call S(W, T, PL),  will be a function of the wastewater volume (W), the
 chemical treatment method (T),  and the phosphorus concentration in
 the wastewater influent (PL)-  The equations for determining the
 additional sludge  produced are  contained in subroutine SIZE and in-
 corporate data presented in Table 6 of Section V.  In this subroutine
 the size of equipment required to handle additional sludge produced
 as  a result of both the phosphorus removal requirement and increased
 population are determined.   P-^ is a function of the detergent limiting
 legislation so that the amount and therefore  the processing cost of
                              45

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additional sludge will depend on the legislation variable (pi) as well as
the treatment variable (T).  The cost function itself will be a  simple
summation of amortized capital costs,  operating and maintenance costs,
and materials costs for various types of sludge handling equipment.
This function will take into account the  excess capacity of a plant and
future growth of the community over a given time horizon.  This cost
function is represented by Csige(pj, T):


        C,  (p., T) = C   .  (S) + C ,   (S) + C   .(chemical, S)
         slgevrl'       equip      o+mv      mat'


Equations for determining Cgjee(pi> T) are contained in subroutine  TRT2.
Table 9 lists the cost functions together with  their  location in the pro-
gram listing.

The costs attributable to phosphorus removal will  depend on size rela-
tionships developed in SIZE and in the BUILD subroutine which deter-
mines whether or not excess plant capacity can be  used, and if not,
whether or not the plant expansion is  chargeable to phosphorus removal
or to  increasing population.

Solid waste disposal  assumes that there is at least one sink available
with the capacity to accept the minimum amounts of solid waste output
from the treatment plant.  The capacity of each  sink N is defined as
Pss(n) and the  cost of transporting the solid waste  is a function of dis-
tance from the plant  to the  sink and is Css(n):
       C  (n) = C    • DIST(n) •  S(W, T,PT )
         S S       S S                      1_(


where Css equals unit transportation costs,  and DIST(n) is the distance
to sink n.  The Css(n) equation is contained in subroutine SSKCST.

Although the model is a  simulation and not a linear programming model,
we can define what might be called an objective function for phosphorus
reduction.  Cost minimization will result when values of the variables
Pi (legislation), T (chemical treatment),  and m (selection of sink) are
in the  right combination to minimize the total cost:
       Total Cost = CL(PI) + CT(T) + Cgx  (pr T) + C
ss
The minimization is carried out by the  user interacting with the simu-
lation model under the constraints that:
                             46

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                          Table  9

                 COST FUNCTION LOCATOR
Cost Term
CT(T)
C    .  (W)
 equip

C    (W)
 o+mv
                   Name

                   Cost of Phosphorus
                   Limiting Legislation
                   Total Cost of Liquid Treatment

                   Amortized Cost of Equipment
                   for  Liquid Treatment
                   Operating and Maintenance Cost
                   of Liquid  Treatment
Subroutine Location

    DTGLIM

    TRT1
    CONCST
Cequip(S)
C   4-(Pn» chemical) Cost of Chemicals for Liquid
 mat  1            Treatment
                   Total Cost of Sludge Handling

                   Amortized Cost of Equipment
                   for Sludge Handling

                   Operating and Maintenance Cost
                   for Sludge Handling
      chemical, S)  Cost of Chemicals for Sludge
                   C onditioning
                   Cost of Solid Waste Disposal
 'mat
C   (n)
  ss
     TRT1


     TRT1

     TRT2

     CONCST


     TRT2

     TRT2

     SSKCST
                              47

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       Peff < Paink(m) °r  mU ^iW' POut(T>J < Psink
-------
if the allowable effluent concentration is 2 mg/1,  treatment schemes
achieving effluent levels lower than 0. 5 mg/1 will not be chosen.

A loop is then entered and disposal costs are calculated for each of
the treatment schemes selected.  A long report may be printed for
each scheme showing for each process within the treatment scheme
the construction cost,  amortized cost, year process is first needed,
and the periodic operating costs.   Several short report formats may
also be selected which summarize cost information for each treatment
scheme.

A number of subroutines  enter into the above cost calculations.  The
subroutine,  TRTMNT,  first calls SCHOSE to select the  sludge handling
scheme most compatible  with the input data describing the existing
waste treatment plant.  A list of the sludge handling schemes incor-
porated within the model  is presented in Appendix B.  SIZE is then
called to compute for each time period of the control strategy the  size
of each piece of equipment {or process) required by the  eligible treat-
ment scheme with and without phosphorus removal being considered.
BUILD then determines,  based on the present size of equipment cur-
rently in the treatment plant, how  much additional  equipment will  be
needed,  at what time,  and whether or not the cost will be assessed to
the phosphorus removal requirement.  TRTMNT then calls SIZE again
and computes the  operating and maintenance costs,  and material costs
for each process required for each time period.  SIZE is called at this
time because some of the operating and maintenance costs depend  on
the design size as determined by BUILD and some  on the actual  oper-
ating time the equipment is used.  After the O&iM and material costs
are calculated the construction costs are determined by CONCST.   The
flow chart for the computation of costs in TRTMNT is shown in Figure
12.

Subroutines, LSKCST  and SSKCST, compute the disposal costs for
liquid and solid effluent from the plant.  LSKCST is not activated in the
model at the present time since it involves the effluent diversion
strategy.  If it were to be activated, it would examine the maximum
assimilative capacity for phosphorus for each of several possible  re-
ceiving bodies of water and would  select those  sinks capable of assim-
ilating the phosphorus effluent over the whole time horizon.   It would
then determine the sinks  resulting in the lowest pipe and pumping
costs.  The effluent would be routed to those sinks with acceptable
assimilative capacity and lowest piping and pumping costs.  SSKCST
chooses the lowest cost solid waste sink for  each time period.  To be
eligible  a sink must have  sufficient capacity  for the solids over the
entire time period.  The least costly eligible sink would be the one with
the lowest transportation cost which generally would be the site closest
to the treatment plant.

Finally, for each particular treatment scheme REPORT prints a sum-
mary of the costs.  After printing the  costs for one treatment scheme
                              49

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the program returns to compute costs for the next eligible scheme and
continues until all eligible schemes have been costed.

After all treatment schemes eligible under a particular control strategy
have been evaluated,  the program will ask the user if another control
strategy is desired.  If so,  the program variables are reinitialized and
control returns to STRTGY.  If not,  the program is ended.
ASSUMPTIONS AND LIMITATIONS

Cost Data

The accuracy of cost predictions for each of the strategies evaluated
by REMOVE depends to a large degree on the validity of sizing and cost
data incorporated in the  SIZE, CONCOS, and TRTMNT subroutines.
Cost data for most of the processes and manpower  requirements is
from a study performed  for EPA by Black and  Veatch,  Inc. {Reference
6).  In several cases cost data has also been used from the COST2
computer program developed by Smith and Eilers (Reference  10) and
the Process  Design Manual for Phosphorus  Removal (Reference 12).
Comments incorporated  in the subroutine program listing refer to the
source of the particular  cost equations.

All cost and  labor data is keyed to standard indexes which update  the
cost data to the present time.  The EPA "Sewage Treatment Plant Con-
struction Cost  Index", the U. S. Department of Labor "Index  of Whole-
sale Prices and Prices Indices",  and the Department of Labor "Employ-
ment and Earning Statistics" have been used for this purpose.

The information developed in Reference 6 for estimating costs and man-
power  requirements was  intended to  be applicable to average  situations
throughout the  United States.   When a cost estimate is prepared for
broad applicability, however,  it can  only be regarded as being suitable
for preliminary estimates of what might be  considered average situa-
tions.  The cost data and manpower requirements for estimating  oper-
ating costs were  based on the experience of the investigators,  extensive
data concerning design details, and actual construction costs  during the
period 1950 to  1968.  This information was  supplemented by field visits,
and the examination of operating and maintenance  records.

From the extensive data acquired by Black and Veatch, graphical cost
relationships were developed.   These are plotted in a log-log format in
Reference 6.  Much of the graphical  information was  later converted by
Smith and Eilers (Reference 10 and 15) to exponential equations by
linear  and polynomial curve fitting.  This is the form of the equations
appearing in the CONCOS and TRTMNT subroutines.
                              50

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It should be recognized that in the development of average cost data
it is impractical to recognize all variations of design occurring among
individual projects.  Variations in cost from one specific project to
another can be attributed to differences of design details,  construction
site  conditions, and the economic climate at the time the bids are taken.
Differences in costs will  tend to be minimized if many different com-
ponents and processes are involved in the construction project due to
the tendency for composite estimates to vary less than the individual
components.  For this reason we would estimate that the variation in
actual construction cost data  compared to estimates provided by
REMOVE will tend to be more pronounced  in small projects involving
relatively little additional equipment.  In these cases, however,  the
cost of chemicals  will usually be the dominant factor in  phosphorus
removal costs and the overall cost estimate  should be a valid one.

Several processes included in the TRTMNT subroutine do not have cost
equations in the program listing.  They may easily be added as valid
cost data becomes available.   We were  not able in the course of this
contract to find information on these processes  which would lend itself
to curve fitting techniques.   The affected processes include aerobic
digestion, waste stabilization ponds,  sodium hydroxide  feeding and
storage, and fluidized bed incineration.  Except for aerobic digestion,
which is being used more frequently now, the other  processes will not
appear frequently in treatment plant flow sheets.


Valid Ranges for Design  Parameters Calculated by REMOVE

As discussed above, the  mathematical cost relationships used in
REMOVE have been developed from linear and polynomial curve fitting
techniques.  The cost calculations are valid only over the range of the
regression data points used to generate the data points.  Where  the
cost relationships are linear, some extrapolation above and below the
data points  may be reasonable.  The range of validity of the cost cal-
culations for the various processes  is given in Table 10. Costs  of some
supplies, such as chemicals  for phosphorus removal are directly input
by the user if the  assumed value is not correct  for the particular area
or region in question.

If the  user selects design parameters which are outside the range shown
in Table 10, the program will print  a warning message.  If the user is
satisfied that a linear extrapolation is involved  or that the input value is
just barely out of the valid range,  the program can  be continued satis-
factorily.


Assumptions Concerning Additional Capacity and Input Information

The model  is based on the following assumptions concerning the addition
of sludge handling equipment as a consequence  of increased sludge pro-
duction.
                               51

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                          Table 10
        CONSTRUCTION COST - VALID RANGES FOR
                    SIZING PARAMETERS
Process Name

Raw Waste Pumping
Pre Treatment
Flocculation Basin
Before  Primary
Primary Settler

Primary Sludge Pump
Trickling Filter
Aeration Basin
Diffused Air System

Mechanical Aeration

Secondary Settler

Recirculation
Pumping (1)
Chlorination Feeding
System
Chlorination Contact
Basin
Multi Media Filtration
Recirculation
Pumping (2)
Anaerobic Digester
Sludge Drying Beds
Vacuum Filter
Centrifuge
Multiple Hearth
Incineration
Recarbonation Basin (1)
Recarbonation Basin (2)
Tertiary Settler (1)

Tertiary Settler (2)

Gravity Thickener
Recalcination
Independent Sizing
    Parameter

Initial Firm Capacity
Maximum Capacity
Maximum Capacity

Surface Area  of
Settler
Initial Firm Capacity
Media Volume
Liquid Volume
Initial Firm Blower
Capacity
Total Installed
Capacity
Surface Area  of
Settler
Maximum Capacity

Average Chlorine
Use
Liquid Volume

Maximum Capacity
Maximum Capacity

Sludge Volume
Surface Area  of Beds
Filter Area
Firm Capacity
Capacity

Liquid Volume
Liquid Volume
Surface Area  of
Settler
Surface Area  of
Settler
Surface Area
Maximum Capacity
Units

MGD
MGD
MGD
GPM
Thos Cu Ft
Thos Cu Ft
Thos CFM

HP

Thos Sq Ft

MGD

Ibs/day

Thos Cu Ft

MGD
MGD

Thos Cu Ft
Thos Sq Ft
Sq Ft
GPM
Lbs  dry
solids/hr
Thos Cu Ft
Thos Cu Ft
Thos Sq Ft
Valid
Range

.5-300
1-200
1-200
Thos  Sq Ft     1-30
30-5000
3-9000
3-4000
.02-200

20-5000

1-30

.5-300

20-8000

3-300

1-200
.5-300

30-6000
7-4000
80-6000
1. 5-700
700-
30, 000
1-400
1-400
1-200
Thos Sq Ft     1-200
Thos Sq Ft
MGD
.02-20
1-200
                             52

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       1.   Existing equipment will be operated up to the maximum
       nominal time before any new equipment is constructed.
       Nominal values selected for the various units  have been sel-
       ected from Reference  10.

       2.   When additional sludge handling units are constructed,
       the  sizing will be performed as follows:

           a.  The maximum size needed with phosphorus removal
           is determined.  This will occur sometime within the
           chosen time horizon.

           b.  The time when present capacity will be exceeded is
           determined.

           c.  The maximum size needed during the chosen time
           horizon is constructed at the time when present capacity
           is first exceeded.

       3.   Existing equipment used for sludge handling is assumed
       to be  in sufficiently good  condition to  be operated throughout
       the  chosen time horizon.   The user of the model may wish to
       shorten the time horizon  if it is expected that major changes
       will be necessary to existing equipment.

       4.   Sludge handling schemes will generally be chosen to
       include the following processes:

           a.  thickening

           b.  digestion

            c.  dewatering

           d.  incineration

If there is  no existing sludge  thickening provided at a treatment plant,
the model assumes that gravity thickening, as a minimum,  will be
required.   If there are no provisions for sludge drying,  the model assumes
that vacuum  filtrating will be required.   Anaerobic digestion capacity
will not be increased by the model as it is  assumed that alternatives to
this process are  available which will result in lower cost.  This may
include dewatering and incineration of partially stabilized sludges.   It
is  also expected that aerobic  digestion will be used more frequently in
the future.  The model will calculate costs associated with landfill
disposal of digested dewatered sludges in addition to incineration.   We
expect, however,  that incineration may increase in popularity.  The
costs of land spreading digested sludges is not included in the model.
                             53

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At the present time the model will include the cost of upgrading a pri-
mary- treatment plant to secondary treatment as a cost associated with
phosphorus removal.  If this is not desired,  the strategy can be run
twice in the following manner.

The upgrading is performed on the present primary treatment plant
and all costs of the particular strategy are calculated.  Then using the
secondary treatment sizing parameters selected by the model as input
data to the model, the strategy is run again, this time assuming that
the plant has secondary treatment.  The cost of phosphorus removal
without the cost of upgrading to secondary treatment is the  result
achieved in the second  run.

As with the primary upgrading costs,  the cost of adding  chlorination
to plants not having this equipment will also be charged to phosphorus
removal.   These decisions were made by the EPA program monitor
early in the project.  If the user does not wish to include these costs,
the long printout  may be requested and the unit cost of chlorination
subtracted from the unit cost summary.

The model is presently restricted to the treatment and sludge handling
schemes shown in Appendices A  and B. The process schematics shown
will be suited to most treatment  plant configurations although occasion-
ally variations  such as  a two-stage  trickling filter may require modifi-
cation of the model.
                             54

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Ul
Ul
fl> hrt
3 H..
3 OTQ
               Sewered
              Population
              Phosphate
              Detergent
                Usage
 Phosphate
Legislation
Phosphorus
   From
  Industry
                              Industrial
                                Waste
                              Treatment
                                    High
                                    Phosphorus
                                    Content
                                    Liquid
                   PHOSPHORUS
                   REMOVAL

                   MODEL
                                  Energy

                                      Chemicals

                                          Labor
                                                                            Additional
                                                                            Equipment
                                        LIQUID

                                     TREATMENT

                                                                       -3
                                                                          CUD
                                                                          w
                                                   v
                                                   QO
                                                   '
                                        SLUDGE

                                    TREATMENT
                                                                            Waste
                                                                 I  Transportation
                                                                                     ^-*
                                                                             Effluent
                                                                            Diver sion
                                                                         Phosphorus
                                                                         Content
                                                                         Licluid

-------
Subroutine Descriptions and Flow Charts
REMOVE
   THIS IS THE MAIN PROGRAM. IT USES A COMPLETE DESCRIPTION OF
   A COMMUNITY AND A DESIRED (INPUT 8V USER) PHOSPHORUS CONTROL
   STRATEGY TO COMPUTE THE COSTS OF DIFFERENT TREATMENT SCHEMES
   WHICH ACHIEVE A GIVEN PHOSPHORUS EFFLUENT LEVEL. A REPORT ON
   THE COSTS FOP EACH SCHEME IS THEN PRINTED.
   NOTE It THIS PROGRAM WAS DESIGNED TT RUN ON AN IBM 360/67
   TIME SHARING SYSTEM.  S" ECIFICALLYt THAT OF, INTERACTIVE
   DATA CORP., WALTHAM, MASS. (617-890-1234).
   A CORE SIZE OF 238K BYTES WAS REQUIRED FOR EXECUTION.
   NOTE 21 THE BASIC STUCTURE OP THE COST EQUATIONS WAS TAKEN
   FRCM RFF. 10 AND FOR THIS WE ARE EXTREMELY GRATEFUL TO
   RICHARD EILERS AND ROBERT SMITH OF EPA-CINCINNATI FOR THEIR
   FINE WORK WHICH WE BUILT UPON.

COMMON BLOCKS:
   PRGCNT - CONTAINS PROGRAM CONTROL VARIABLES
   PRNTR  - CONTAINS PRINTOUT CONTROL VARIABLES
   SCHEME - CHARACTERISTICS OF LIQUID TREATMENT SCHEMES

SUBROUTINES CALLED:
   LCHOSE  - PICK LIQUID TREATMENT SCHEME
   LSKCST  - COMPUTE COST OP FEASIBLE LIQUID SINK (dummy for now)
   REPORT  - PRINT SUMMARY OF COST INFO FOR SCHEME
   SSKCST  - COMPUTE COSTS Oc FEASIRL^ SOLID SINKS
   STRTGY  - INPUT CONTROL STRATEGY
   SYSTEM  - INPUT DESCRIPTION OF COMMUNITY, SEWAGE, PLANT
   TOTMNT  - COMPUTE COST OF LIQUID AND SLUDGE TREATMENT
REFERENCES:
   1. MONOGRAPH
                NO. 9, 'ENVIRONMENT REPORTER', DOYLE, KATHLEEN
       .t
          20 AUG 71.
   2. 'CHEMICAL HANDBOOK MANUAL OF CURRENT INDICATORS',
      STANCFHPD RESEARCH INSTITUTE, AtJG 71.

   3. PRIVATE COMMUNICATION WITH LARRY COX OF EPA-WASHI NGTON ,
      O.C. ON II SEP 72.  HE SAID THAT SUFFOLK COUNTY, NY WAS
      PLANNING ON $.*O/CAPITA/YR.

   4. «NCWS RELEASE CF FRIDAY, 1 MAY 70', U.S. OF.PT OF INTERIOR
      FWQA.
                          56

-------
5. «REPORT TO OECD WORK GROUP ON DETERGENTS'* BUNCH, ROBERT
   L. , SEP 71.

6. 'ESTIMATING COSTS AND MANPOWER REQUIREMENTS FOR
   CONVENTIONAL WASTFWATER TREATMENT FACILITIES', PATTERSON,
   W.L. AND BANKER, R.F. OF BLACK 6 VF.ATCH, CONSULTING
   ENGINEERS, F.PA REPORT NO. 17090 DAN.

7. MYSELF

8. 'SFWAGE TREATMENT PALNT CONSTRUCTION COST INDEX', EPA-

   TFFICE OF WATER PROGRAMS.

9. 'WHOLESALE PRICES AND PRICE  INDICES -  INDUSTRIAL
    COMMODITIES', U.S. DEPT. OF LABOR.

10.  'COST2', A COMPUTER PROGRAM BY RICHARD EILERS OF
     EPA-CINCINNATI, OHIO.  'COST2' COMPUTERIZES THE  GRAPHS  OF
     REFERENCE 6.

11.  PRIVATE COMMUNICATION  WITH  W.C. KRUMRI OF  PROCTER
     C GAMBLE, CINCINNATI,  OHIO  (513-562-2859)  ON  6  SEP  72.
     HE SAID THAT  ANY NUMBER FROM -.05(FOR  SQOIUM  CARBONATE)
     TO +.26CFOR CITRIC ACID) WAS VALID BECAUSE NO ONE
     SUBSTANCE HAS BEEN ACCEPTED AS A' PHOSPHATE SUBSTITUTE.

12.  'PROCESS DESIGN MANUAL FOR  PHOSPHORUS  REMOVAL*,
     BLACK 6, VEATCH, CONSULTING  ENGINEERS,  EPA  REPORT
     NH. 17010-GNP.

13.  'COST AND PERFORMANCE  ESTIMATES FOR  TERTIARY  WASTEWATER
     TREATING PROCESSES', SMITH, ROBERT AND MCMICHAFL,  WALTER
     F., EPA-CINCINNATI, OHIO,  JUN 69.

1*.  'EMPLOYMENT £ EARNINGS STATISTICS -  HATER, STEAM,
     £  SANITARY SYSTEMS  (SIC <»94-497)', U.S.  OEPT. OF  LABOR.

15.  'PRELIMINARY  DESIGN AND SIMULATION OF  CONVENTIONAL
     WASTEWATER RENOVATION  SYSTEMS USING  THE  DIGITAL
     COMPUTER*, POBEO.T  SMITH,  EPA- CINCINNATI,  MAR 68.
     THIS  REPORT PROVIDES A THEORECTICAL  BACKGROUND  FOR
     RFFFRENCE 6.
                        57

-------
NUMERIC
CONSTANTS'
.020825 =
.029

.075
.123
.125
.232    *
.4902
.6
.7
        .7457
       1.506
       2.27
       2.6
       2.89
       3.95
       4.?2
       5.4
       5.4
       6.
       7.48
       8.33
      11.
      24.
      30.
      60.
     180.

     365.
    1440.
    2000.
   43560.
PCUNDS/GAL FOR LIQUID POLYMER
ASSUMED RATIO OF TRICKLING FILTER SLUDGE
WASTING STREAM VOLUME TO INPUT VOLUME
POUNDS PF AIR/CUBIC FOOT
POUNDS OF C02/ CUBIC FOOT
ENDCGENQUS RESPIRATION CONSTANT AT 20C
POUNDS OP 02/ POUND 0^ AIR
PQUNDS/GAL FOR LIQUID ALUM
ASSUMED FRACTION OF MLVSS WHICH APE ACTIVE
ASSUMED RATIO OF MIXED LIQUOR VOLATILE
SUSPENDED SOLIDS TO MLSSAR
KILOWATTS/HPRSEPOWER
WQO-STP INDEX FOR JAN 71 NATIONAL AVERAGE $
POUNDS OF FECL2/PGUND OF FE
POUNDS/GAL FOR FECL2
POUND OF FECL3/ POUND OF F£
OOUNDS/GAL FOR FECLS
POUNDS OF NAAL/POUNO OF AL
PCUNOS/GAL FOR ALUM
(ASSUMED) POUNDS/GAL FOR NAAL
ASSUMED DEPTH OF TRICKLING FILTER MEDIA
GALLONS/CUBIC FOOT FOR WATER
POUNDS/GAL FOR WATER
POUNDS OF ALUM/POUND OF AL
HOURS/DAY
DAYS/MONTH
MINUTES/HOUR
ASSUMED CONCENTRATION OF SUSPENDED SOLIDS IN
TRICKLING FILTER SLUDGE WASTING STREAM
DAYS/YEAR
MINUTES/DAY
POUNDS/TON
SQUARE F5F.T/ACRE
AUTHOR:
   CAVID A BARNES   19DEC72
   RCNALC CRNER
   JBF SCIENTIFIC CORP.
   2 RAY AVENUE
   BURLINGTON, MA  01803
   (617-273-0270)
                          58

-------
         f REMOVE  J
           SYSTEM
            STRTGY
            LCHOSE
DO FOR ALL ELIGIBLE SCHEMES
   NO
            TRTMNT
            LSKCST
            SSKCST
            REPORT
  END
   OF
 SCHEME
DO-LOOP
            Figure 2
               59

-------
                            YES
                            YES
                         USER
                       SELECTS
                         LONG
                        PRINT-
                         OUTS
                         USER
                          TRY
                       ANOTHER
                       STRATGY
                     Figure 2 (cont. )
SYSTEM
PURPCSt:
   SYSTEM  CALLS  THE  SUBROUTINES WHICH  READ IN A DESCRIPTION OF
   Tt-F TCTAL  WASTE  SYSTEM. THIS DESCRIPTION! CONSISTS OF THE
   CHARACTERISTICS  CF ThE COMMUNITY,  THE  INFLUENT SEWAGE,
   THE TREATMENT PLANT.

SLeKGLTINES CALLED:
           -  RE ACS  IN DESCRIPTION OF  COMMUNITY
           -  REACS  IN JESCRIPTICN OF  INFLUENT SEWAGE
   PLANT   -  RE/iDS  IN' DESCRIPTION OF  TREATMENT PLANT
CAl.LEC 3Y:
   Ff EMGVE
- THE MAIN  PROGRAM
AUTHC'fc :
   CAVIC A  BAF.NFS
         05CCT72
                          60

-------
                       (  SYSTEM  J
                          CMMNTY
                          SEWAGE
                           PLANT
                        f RETURN  J
                                                   Figure 3
SYSTEM and its three (3) subroutines CMMNTY,  SEWAGE, and
PLANT have the  function of reading in and storing large  amounts
of information into selected common blocks whose variables des-
cribe the  community and its treatment plant.

Each variable is  filled in the following manner:
   "-H
   o
  C C 3
  * C 0
  — .1-1 J_l
  4J ac o
  
-------
                      c
    STRTGY
                        INTIME
                        EFFLIM
                        DTGLIM
 INTIME
INDLIM
i

                     (  RETURN
                                             Figure 4
PURPOSE:
   IMI-ME &EAOS  IN A DESCRIPTION OF  THE  TIME  HORIZON DESIRED-
   IT THEN CALLS SP^NC TO COMPUTE  THE  SEVERED POPULATION FOR
   EACH TINC PERIOD.

COMMCN PLCCKS:
   PPGCNT - CONTAINS PRCGKAM CONTROL VARIABLES
   TIMC    - PARAMETERS OF  TIME  HCRIZCN

SLBRCLTINES CALLED:
   SPFMC  - CCMPUTES SEhEfcED POPULATICN  FOR  ALL  TIME PERIODS

CALLEC 8Y:
   ST&TGY  - CONTkUL STRATEGY CALLING  ROUTINE
ALTHGI' :
   DAVI'J A B
06nCT72
                          64

-------
 SPFNC
                     f  INTIME  J
                      READ IN:

                      1.  Number of
                         Years in
                         Time Horizon
                      2.  Size of Each
                         Time Period
                       COMPUTE
                   MAXIMUM NUMBER
                   OF TIME PERIODS
                        SPFNC
                      C RETURN  J
                                              Figure 5
     SPFIVC COMPUTES  THE  SIZIE OF ThP SEWERED  POPULATION OVE* ALL
   TIKE PEKIUCS  OF  A GIVEN CCNTRCL STRATEGY.

CGMMCN flLCCKS:
   SEhPOP  - THE Sf-bEREO POPULATICN
   T1M£    - PARAVIPTFRS  OF TIME HCRIZCN

CALLtC BY:
   INT IMF.  - READS  IN TIME HGklZGK OF CONTROL  STRATEGY

AUTHCP:
   CAVIC  A BARNES   060CT72
                           65

-------
              ( SPOPFNC J
                /GO TOV
               \FNCTYPX
        linear 5%
           linear
      exponential
piece-wise linear
                                       B
                                                   D
                 Figure 6
                    66

-------
             B
     COMPUTE SLOPE
     FROM FIRST TWO
    VALUES OF SPOPIN
DO FOR ALL TIME PERIODS
     COMPUTE SEWPOP
  FOR THIS TIME PERIOD
     NO
               YES
        C RETURN  J
                                  SLOPE = .05
                                    J
         Figure 6 (cont. )
              67

-------
             c
  COMPUTE EXPONENTIAL
  CONSTANT FROM FIRST
  TWO VALUES OF SPOPIN
DO FOR ALL TIME PERIODS
    COMPUTE SEWPOP
  FOR THIS TIME PERIOD
     NO
         END OF
         DO-LOOP
               YES
       ( RETURN  J
      Figure 6 (cont. )
            68

-------
               D
 DO FOR ALL TIME PERIODS
DO FOR EACH TIME INTERVAL
              IF
            TIME
         PERIOD LIES
            WITHIN
          INTERVAL
                                 COMPUTE SLOPE
                                   AND INITIAL
                               POPULATION VALUE
      NO /END OF
          DO-LOOP
      COMPUTE SEAVPOP
    FOR THIS TIME  PERIOD
     NO
                 YES
        rRETURNS
        Figure 6 (cont. )
               69

-------
POPULATION GROWTH FUNCTIONS
 present
                                    linear:

                                       PT
                                    t = T - T
            - PO
         T2 - TO
                  t + P
0
                                            0
                                    exponential:
                                    t = T - T     P   = P(1 +
         Q
K = ex - 1
                                                        Q
                                    piecewise linear fit:
                                    T <  T.
                                   t=T- T
                                     T   T. -  T.
                                               i- 1
                            70

-------
DTGLIM
PUP PCSF: :
   CTCLIM
       INITIALIZES THE  INFLUENT-HALF OF IELIMT TO  'PINPS1
DTP.GLIM KEACS  IN THE  PROPOSED LEGISLATIVE LIMITS ON THE
        US CONTENT OF  DETERGENTS AND THE I VPLENENT AT ION
        FOk EACH TIME  PERIOD THE INFLUENT-HALF OF  IELIMT
        COSTS  OF NCN-PHCSPHATE SUBSTITUTES ARE COMPUTED.
       DTGIIV  ASSUMES  THAT PYEAR V»ILL INCREASE EACH
       TIME IT IS  READ  .IN.
       THE
       BLOCKS:
   OTRGNT -  CHARACTERISTICS OF DETERGENTS AND USAGE
   lELl^T -  INFLUENT  AND EFFLUENT LII-ITS
   PRC-CNT - CONTAINS  PROGRAM CONTROL VARIABLES
   LIQUID -  LIQUID  INFLUENT INFCPfATICN
   SEkvPQP -  THE  SF.UERED  POPULATICN
   TI^E   - PARAMETERS CF THE TIME HCRIZQN

C&LLEC BY:
   STRTGY -  CONTROL  STRATEGY CALLING ROUTINE
AUTHOR:
   DAVID  A  BARNES
                  11CCT72
                            71

-------
              f  DTGLIM  J
               INITIALIZE
            IELIMT = PINPS
               PSUBCS  = 0
NOTE:  DTGLIM
assumes that 'PYEAR1
will increase each
time it is read in
                READ IN
          PCNTNT AND PYEAR
                       = VALID NUMBER
            CHANGE PYEAR
           TO A TIME PERIOD
                COMPUTE

           1.  New influent P level

           2.  Annual substitution cost
DO FOR ALL REMAINING TIME PERIODS
                  SET

           1.  New influent level
           2.  Substitution cost for
              this time period
                 Figure 7


                   72

-------
DTGLIM
                  NO
                     Figure 7 (cont.)
 EFFLIM
 PLRPCSE:
    EFFLIM READS  IN THE PHOSPHORUS  EFFLUENT  LIMITS  AND
    CONSTRUCTS THE EFFLUFNT-HALF  OF  IELIMT
    NOTE: EFFLIM  ASSUMES  THAT  'EYEAR1  hILL  INCREASE
    EACH T IME IT  IS READ  IN.
    VCN BLCCKS:
    IELIMT - LIMITS OK  INFLUENT/EFFLUENT  PHOSPHORUS
            CONCENTRATIONS
    PRGCNT - CONTAINS PROGRAf  CONT«CL  VARIABLES
    SEfcPOP - THE  SEWERtO  POPULATICN
    TIME  - INFC  ABOUT  THE  TIME  HCRIZON
 CALLEC  BY:
     STKTGY -  THE  CONTROL  STRATEGY  CALLING ROUTINE

 AUTHCP :
     DAVIC A  BARNES    UCCT72
                            73

-------
             (  EFFLIM  )
                READ IN
                ELIMIT,
                 EYEAR
       NOTE: EFFLIM
       assumes that EYEAR
       will increase each
       time it is read in
  =OTHER
'00  ' X         *\
    ' (  RETURN  }
                     = VALID NUMBER
            CHANGE EYEAR
          TO A TIME PERIOD
DO FOR ALL REMAINING TIME PERIODS
        SET EFFLUENT LEVEL
        FOR THIS TIME PERIOD
         NO
                END OF
               DO-LOOE
                    YES
                Figure 8
                   74

-------
INDLIM
PURHCS6:
   INOLIM REACS IN LEGISLATED RESTRICTIONS  CN INDUSTRIAL
   PHCSPHOF-US EFFLUENT.  THE CORRESPONDING  CHANGES ARF THEN
   MACE TO THE INFLUENT-HALF OF  IF.LIMT.
       BLOCKS:
   INDSTY - INDUSTRIAL EFFLUENT  LEVFLS
CALL6C 3Y:
   STRTGY - THE CONTPCL STRATEGY  CALLING ROUTINE

AUTHOR :
   CAVIC A BARNES    113CT72
                     (  INDLIM J
                        DUMMY
                       FOR NOW
                     f RETURN  J
                        Figure 9
                           75

-------
 LCHOSE
   LCKlSt  1^3 KS  iS  ELIGIBLE  FCfi  C CNS I DEkATJ CN THOSE  LIQUID
   FUAFMtNT  scHi, ves UHICH WILL:
   1. ACHItVt;  TH[,:  O^SIRL'J MINF^UM  r-h'f-LUL'M PHOSPHORUS  LfcVtL
   2. ACHltVE  A  LEVEL CLOSE  TO  THAT  CFSIREO.

   MCN BLCCKS:
   IELIMT  - LIMITS  "N INFLUIfM/FFFLUfEM PHOSPHORUS
   PR'jCNT  - CONTAINS PHCGRAM CUNTRCL  V^RIAQLES
   LIOU1C  - LIQUID  INFLUENT  INFC
   SCHrMF  - I NFL AECUT  L I QU I C TREATMENT SCHtMES
   TlVb    - INFC: AbCUT  TIME  HC-PIZCN
   TPLANT  - INFG ^BCLT  TKEATi^FNT  PLANT PROCESSES
CALL EC ev:
   »fc:MG\/f. -  THE  VAIN P^CGRAM

AUTHCR :
   CAVID A  3AK\nS    12UCT72
                          76

-------
          (  LCHOSE  )
    DO FOR ALL TIME PERIODS
   FIND MINIMUM PHOSPHORUS
   EFFLUENT LEVEL REQUIRED
             END O
            DO-LOOP
DO FOR ALL TREATMENT SCHEMES
            WILL THIS
         SCHEME ACHIEVE
     THE MINIMUM AND IS ITS
           VALUE THE
           CLOSEST TO
             MINIMUM
                                   SET CLOSENESS
                                       FACTOR
              END O
              O-LOOE
              Figure 10
                 77

-------
   DO FOR ALL SCHEMES
     MARK AS ELIGIBLE
THOSE SCHEMES THAT WILL:


  1.  Achieve min.'eff. P

  2.  Lie within closeness
     factor
      IF   \       /IF
 ALKALINITY\ YES / SCHEME IS
INTO PRIMARY;?—(EITHER, LIME
  SETTLER /   \TO PRIMARY,
   IS < 150/       \OR 1-STAGE
                    TERTIARY
                                           SCHEME
                                              IS
                                           MARKED
                                             NOT
                                          ELIGIBLE
              Figure 10 (cont. )
                    78

-------
         IF
     SCHEME IS
     SUCH THAT
 ADDITION OF ALUM
 OR FECL3 WOULD
    DEPRESS THE
    ALKALINITY
       BELOW
        50.
  MARK
 SCHEME
   NOT
ELIGIBLE
         IF
    SCHEME CAN
HAVE ALTERNATIVE
    EQUIVALENT
     PROCESSES
                           CHOOSE AND ADD
                             PROCESS SO AS
                          TO CLOSELY  MATCH
                       PRESENT CONFIGURATION
       END O
       O-LOOP
       RETURN
       Figure 10 (cont.
          79

-------
 TRTMNT
PUPPCSE:
   TRTMENT IS THE MAIN COST COMPUTING SUBROUTINE.  IT FIRST
   DETERMINES WHAT ADDITIONAL (IF ANY) SLUDGE HANCLING
   hGUIPKENT IS REQOIREC RY THE COMBINATION CF THIS TREATMENT
   PLANT AND ELIGIBLE TREATMENT SCHrME.  THEN PCR  FACH TIME
   PER IOC THE FALLOWING WILL BE COMPUTED.
   1. SIZE AND CCST OF ADDITIONAL EOUIPMENT
   2. OPERATION AND CAINTAINENCE COSTS
   3. MATERIAL AMD SUPPLY COSTS.
   NJTfc: THE ABOVE CCSTS ARE ONLY THOSE ATTRIBUTABLE TO
         PHOSPHORUS REMOVAL

COMMON BLCCKS:
   SCKMfc - INFO ABQLT LIQUID TREATMNET SCHtMES
   TPLANT - INFO. ABOUT LIQUID T»EATMfcNT PROCESSES
   TlNf.    - PARAMETERS CF TIME HORIZON

SLBRCLTINES CALLED:
   BUILD
   SCHOSf
   SIZE
   TRT1
   TRT2
   CCNCST

CALLEC BY:
DETERMINES MAXIMUM SIZE OF ADDITIONAL EQUIPMENT
CHOOSES SLUDGE HANDLING PROCESSES
COMPUTE INDEPENDENT SIZING PARAMETERS FOR  PROCESSES
COMPUTES 0 I * COSTS
COMPUTES OEM COSTS
CCMPUTS CONSTRUCTION COSTS
          - THE MAIN FPCGRAM
AUTHOR:
   CAVIL A BARNES
        120CT 72
                          80

-------
      (  TRTMNT J
         SCHOSE
DO FOR ALL TIME PERIODS
              YES
DO FOR ALL TIME PERIODS
           SIZE
   COMPUTE O&M AND
MATERIAL COSTS FOR EACH
   REQUIRED PROCESS
    NO
  SUBROUTINES
  TRT1 & TRT2
               YES
 COMPUTE CONSTRUCTION
     COSTS FOR EACH
    REQUIRED PROCESS
SUBROUTINE
  CONCST
        ( RETURN J
         Figure 11
             81

-------
SCHOSE
PUKPCSE:
   SCHOSc PICKS THE  SLUCGE  HANDLING  PROCESSES (EQUIPMENT) WHICH
   ,iRF CCTh:
   1. NtCESSARY FOR  A PARTICULAK  LIQUID  TREATMENT SCHEME
   2. CCNFCRM MOST CLOSELY  WITH THE  PRESENT PLANT CONFIGUR AT ICN
SCHOSE ALSC CONSTRUCTS A COMPLETE  LIST OF  NECESSARY EQUIPMENT
F'JK THIS STRATEGY
CCMPCN BLCCKS:
   PHGCNT - PROGRAM CCNTROL
   SCHEME - REQUIRED LIOUIO
   SLGSCM - REQUIRED SLUOGE
   TFLANT - CHARACTERISTICS
                 VARIABLES
                 HANDLING EQUIPMENT
                 HANCLING EQUIPMENT
                 GF TREATMENT  PLANT
                           PROCESSES
CftLLEC PY:
   TSTMNT -

AUTHCR:
   L^AVIC A
 THE MAIN COSTING SUBROUTINE
flARNES
120CT 72
                          82

-------
 CHOOSE THICKENING
       PROCESS
  CHOOSE DIGESTION
       PROCESS
          IF
      CHEMICAL
    CONDITIONING
       NEEDED
PICK CHEMICAL
  PROCESSES
CHOOSE INCINERATION
       PROCESS
       TERTIARY
         LIME
     PICK
 R EGA LI NATION
   PROCESS
             NO
        Figure 12
           83

-------
                 TURN 'ON' PROCESSES
                   COMMON TO ALL
                 TREATMENT SCHEMES
                 TURN 'ON' PROCESSES
                 REQUIRED FOR THIS
                 TREATMENT SCHEME
TURN 'ON1
FOR SLUDG1

PROCESSES
£ HANDLING

                     ( RETURN J

                    Figure 12 (cont. )
SIZE
PURPOSE:
   SIZE COMPUTES FOR  TH«E  CURRENT TIME PERIOD (TP), THE
   INDEPENDENT SIZING  PARAMETERS FOR EACH PROCESS WITH/WITHOUT
   PHCSPHORUS REMOVAL  TREATMENT.

CCMNCN BLOCKS:
   IbLItfT - INFLUENT  ANC  EFFLUENT LIMITS
   LIQUID - LIQUID  INFLUENT  INFORMATION
   PKGCNT - PROGRAM CONTROL  VARIABLES
   SCHEME - INFC ABCUT  LIOUIC  TREATMENT SCHEMES
   SLCHAR - SLUDGE,LIQUID,CHEMICAL CHARACTERISTICS
   SLGSCK -REQUIRED SLUUGE  HANDLING EQUIPMENT
   SLLDGE - SLUDGE  INFORMATION
   SEksPOP - THE SEWERFD POPULATION
   TIME   - PARAMETERS  OF TIME HORIZON
   TPLANT - CHARACTERISTICS  OF TREATMENT PLANT PROCESSES
SUBROUTINES CALLED:
   TSCHME(ES) -  INITIALIZES
                   IN  CRDER  TO  SIZE WPARM
CALLEC BY
   TRTMNIT
- THE MAIN COSTING  SUBROUTINE
AUTHOR:
   DAVIC A BARNES
          120CT72

                84

-------
                    f  SIZE (ipn
                                 ES = Current
                                     Eligible
                                     Scheme
                       TSCHME
                        (NONE)
                      SIZE ALL
                 REQUIRED PROCESSES
                                 WITHOUT
                                 PHOSPHORUS
                                 REMOVAL
                                 TREATMENT
                     TSCHME(ES)
                      SIZE ALL
                REQUIRED PROCESSES
                                i WITH
                                ! PHOSPHORUS
                                [REMOVAL
                                ' TREATMENT
                    f  RETURN]

                       Figure 13
TSCHME(ES)
   TSCHME  INITIALIZES  ALL  THE DOMAIN VARIABLES NECESSARY  TO
   SUE WPARM(J)  (THE  INDEPENDENT SIZING PARAMETER WITH
   PHTSPHCPUS  REMOVAL  TREATMENT FCR E/CH PROCESS(J))•  THIS  IS
   JCNE FOR  A  PARTICULAR ELIGIBLF TREATMENT SCH^MEttS).

   MCN  BLOCKS:
   LICUIL  -  LUUIO INFLUENT INFCRMATICN
   PRGCNT  -  PROGRAM CCNTROL VARIABLES
   SLCHAft  -  SLUDGfcfLlOUlU.CHfcPICAL CHARACTERISTICS
   SLUDGE  -  SLUOGt CHARACTERISTICS
   TPLANT  -  CHARACTERISTICS CF TPCATMENT PROCESSES
    LEL
    SIZE
- THE INDEPENDENT  PARAMETER  SIZING SUBROUTINE
 ALTHf> :
    i-wn
 b A ft N E S
130CT72
                          85

-------
                                            ES = Number of
                                                 Eligible
                                                 Scheme
                                        INITIALIZE ALL
                                      DOMAIN VARIABLES
                                        FOR SCHEME ES
                             n
                                         f RETURN  J
                       Figure 14
 BUILD
PURPOSE:
   BU1LC DETERMINES THE MAXIMUM  SIZE  CF  THE  NECESSARY
   ACDIT ICNAL EQUIPMENT NEEDED FOR  EACH  PROCESS AND THE
   PE«IOC WHEN AODITICNAL  EtiUIP^ENT  IS FIRST NEEDED.
                                             TIME
       CLOCKS:
   PKGCNT - PROGRAM CQNTKOL
   TIME   - INFC ABCUT TIME
   TPLAM - CHARACTERISTICS
   TKTCST - TREATMENT CCSTS
                VARIABLES
                HCRIZCN
                CF THE TREATMENT
                FOR EACH PROCESS
PLANT PROCESSES
FOR EACH TIME
CALLED BY:
   TRTMNT -
THE MAIN COSTING SUBROUTINE
AUTHOR :
   DAVID A BAHNES
        19DEC72
                          86

-------
                     C  BUILD  )
                DO FOR ALL PROCESSES
                  DETERMINE AMOUNT
                      TO BE  BUILT
                   FOR THIS  PROCESS
                      USING BUILD
                      ALGORITHM
                   N0 XEND or
                        JO-LOOP,

                             YES

                      ( RETURN  J
                        Figure 15


PICTORIAL REPRESENTATION OF BUILD ALGORITHM



P   = Present Plant sizing parameter for a process

B   = Size to be built

W   = Size needed with Phosphorus Removal

"WO =  Size needed without P removal

NOTE: Assume W > WO always
Case 1:
P = 0
                                                  B
                                                      i.e. B = W
                                  P    \VO   "W
                            87

-------
Case Z:
                   WO
W
B = (#, because present size is
       large enough
Case 3:
                               B
                          W
          B = W-P,  i.e. the excess
                    capacity, P-WO,  is
                    utilized for Phos.
                    removal
Case 4:
                   WO
W
B = W-WO,  i. e. the amount,
           WO-P,  which is also
           required is not caused
           by Phos.  removal,
           but by population
           growth, and therefore
           its cost is not charged
           to Phos. removal
                              88

-------
TRT1
PURPOSE:
    THE COSTS ARE COMPUTED FOR EACH PROCESS WHICH IS
    BEING USED FOR THE CURRENT TREATMENT SCHEME IN
    THE FOLLOWING MANNER:

    1.  COSTS WHICH DEPEND ON THE SIZE OF THE PROCESS

       A. IF P  <  0, THEN COST = F(B)
       B. IF TP < TPFADD,  THEN COST = 0
       C. IF TP^TPFADD,  THEN COST = F(P + B) - F(P)


    2.  COSTS WHICH DEPEND ON ACTUAL USAGE OF THE
       PROCESS

       A. IF P<0, THEN COST = F(W)
       B. OTHERWISE, COST  = F(W) -  F(WO)

P  =  PPARM    = PRESENT  SIZE OF  PROCESS
B  =  BPARM    = SIZE REQUIRED TO BE BUILT BY TIME
                   PERIOD 'TPFADD1
W  =  WPARM   = SIZE REQUIRED WITH PHOSPHORUS REMOVAL

WO =  WOPARM  = SIZE REQUIRED WITHOUT PHOSPHORUS REMOVAL

(SEE COMMON 'TPLANT' FOR ADDITIONAL EXPLANATION)
TRT2



PURPOSE:
   TRT2  IS SIMILAR TO TRT1.

COMMON BLOCKS:

SUBROUTINES CALLED:

AUTHOR:
   DAVID A. BARNES 30 NOV  72
                           89

-------
CONCST
PURPOSE:
   CGNCST COMPUTES CONSTRUCTION COSTS FOR EACH PROCESS
   MOTE: FOR MOST PROCESSES THE EQUATIONS ARE FROM REF. 10

COMMCN BLOCKS:
   LBRCST - COST OF LABOR
   SCHEME - INFO ABOUT LIQUID TREATMENT SCHEMES
   TIME  - TIME HORIZON INFORMATION
   TPLANT - CHARACTERISTICS OF TREATMENT PLANT PROCESSES
   TRTCST - TREATMENT COSTS
   TSCST  - TIME AND SPACE DIFFERENCE COSTS

CALLED BY:
   TRTMNT - THE MAIN SIZING AND COSTING ROUTINE

REFERENCES:

AUTHOR:
   DAVIG A. BARNES 30 NOV 72
                          90

-------
LSKCST


PUKPGSt:
   LSKCST CHOOSES  A  LIQUID SINK kITH  A  LARGE  ENOUGH
   ASSIMILATIVE  PHOSHHJRUS CAPACITY.   IT  THTN COMPUTES THE
   PUVD  AND  PIPE -fctCUIRfcMENTS.  ANC THEM  CALCULATES THE CHST
   OF  Thf? SINK  FU» EACH TIME PFRITO.

CQVMCN BLOCKS:
   f'NGCST -  OELIVEREC CCSTS Cf ENtSGY  FOkMS
   IcLlMT -  INFLUENT/EFFLUENT LIVITS
   LIQUID -  -LiaUIO -INF.LLENT INFCRfATICN
   LSINK  -  CHARACTERISTICS GP LICUIC  SINKS
   PRGCNT -  PROGRAM CONTROL VARIABLES


CALLEC BY:
           -  THE  MAIN PKCGRAM
AUTHOR:
       L1  A  BARNES   12GCT72
                     (  LSKCST J
DUMMY
FOR
NOW


                     f RETURN  J
                        Figure 16
                           91

-------
SSKCST
PUKPCSE:
   SSKCST COMMUTES THE COST CF TRANSPORTING THE SOLID WASTE
   FHC^ THE TREATMENT PL^NT TO A SINK WITH SUFFICIENT CAPACITY.
   THIS IS DC3Nc FOR EACH TIVE PERIOD.

CCMNIGK BLOCKS:
   PRGCNT - PROGRAM CCMTRDL VARIABLES
   3SINK  - CHARACTtRlSTICS CF THE SCLIO SINKS

CALLEC BY:
   ^E^OVt - THE PAIN PKCGRAM

AUTHCP :
   C4VID A BARNES   120CT72
                          92

-------
       f  SSKCST J
DO FOR ALL TIME PERIODS
             I
 DO FOR ALL SOLID SINKS
     REDUCE CAPACITY
      OF CHOSEN SINK
    COMPUTE COST FOR
      THIS TIME PERIOD
     NO
                 ES
         ( RETURN  J
                                  NO
             CAN
      AMOUNT OF SOLID
WASTE FOR THIS TIME PERIOD
      BE PUT INTO  THIS
             SINK
             IS
         THIS SINK
            THE
           LOSEST
       PICK THIS SINK
     SET  NEW CLOSEST
           END OF
           0-LOOP
                                  Figure 17
              93

-------
                  A SUMMARY
                  TKL7ATMENT
        OF  THE  COSTS
        SCHEME,
ASSOCIATATEO WITH
 REPORT
PLRFCSE:
   PtFCRT PRINTS
   EACH ELIGIBLE

CCMMCN BLCCKS:
   9TRGNT - DETERGENT  INFORMATION
   LBRCST - CCST OF  LABCR
   LIQUID - INFO. ABCUT LIQUID  INFLUENT
   PRGCNT - CONTAINS PROGRAM  CONTROL  VARIABLES
   SCHEMF - INFC ABOUT LIQUID TREATMENT SCHEMES
   SLiVvPOP - THE SEWERED POPULATICN
   TIMt   - PARAMETEFS OF  TIME  HCPIZON
   TPLANT - CHARACTERISTICS CF  TREATMENT PROCESSES
   TRTCST - TREATMENT CCSTS

C.HLEL BY:
   RtMOVF - THE MAIN PKCGfcAM

ALTHCR:
   CAVIC A 3ARNFS    130CT72
REINIT
   RFINIT REINITIALIZES  ALL  THfc  VARIABLES NECESSARY TO TRY A
   New PHOSPHORUS CCNTPCL  STRATEGY.
       BLCCKS:
CALLtC HV:
   RENGVfc - THE MAIN  PRCGRAM
   DAVID A tiAKNES
130CT72
                          94

-------
Common Block Descriptions
CCWMCN BLCCK:
   ChfCST
PUR PCSE :
   CONTAINS
'DELIVERED COST QF CHEMICALS
VAR IAELES;
ALLMCS
CI12CS
FECLCS
L IMEC5
NAALCS
NAGHCS
PCKLCS
POLYCS
»
t
- COST
- COST
- COST
- COST
- COST
- COST
- COST
- COST

OF
OF
OF
OF
OF
OF
DF
GF

ALUM
CARBON
FERRIC
LIME
SODIUM
SODIUM
PICKLE
POLYMER


0
C

A


10X1
HLOR

LUMI
HYCRQ
L



OF.
IDE

NATC
XIDE
IQUCR


AUTHOR:
   RCN CPNFK
    10 CCT 72
       BLCCK:
   01PGNT

PURPOSE:
   CCNTAINS Df-TEKGtNT  INFORMATION
   DIFCOS
   OTP.GUS
   ErtFCST
   PORATQ
   PCTRG
   FPRATC
   PRESPC
 DIFFERENTIAL CCST OF  PHOSPHATE SUBSTITUTF (WL3)
 ANNUAL PEt< CAPITA DETERGENT  USE (LBS/CAP/YR)
 ANNUAL PER CAPITA ENFORCEMENT COSTS OF P BAN  U/C4
 RATIC P^OSPHATL-  TO  CETtRCENT * RIGHT
 WEIGHT P IN ScWAGE  CUE  TC DETERGENTS (LBS)
 RATIC PhCSPHORUS TC  PHOSPHATE
 PPFSfiMT P CONCENTRATION IN JfcTERGLNTS (KATI01
   r»SUBCS(TP) - COST  OF  P SUBSTITLTe FOK EACH TlVt  PERIOD  ($)
AUTHOR:
   PCN
    10 CCT 72
                           95

-------
COVCN 3LCCK:
   FNGCbT
   CONTAINS DELIVERED  CCSTS  Uf  ENERGY SUPPLIES

VAR TABLES :
   bLFCGS - ELECTRICITY  COST (t/KKHR)
   GILCCS - OIL COST          U/GAL  )
   GASCOS - GAS COST          ($/CU.FT)

AUTHOR :
   RCN CKNEK    10 GCT  72

    /E;NGCST/ ELECOS, CILCCS, GASCCS
 CCMMCN  BLOCK:
    Ifc'LIMT

 u 1 10 p f c r •
    CONTAINS INFLUcNT ANt EFFLUENT  CONCENTRATIONS
    OF  FHCSPHJKUS


 VARIFLWT(I,J1 -  I-l:  INFLUENT  CCNCtNTKAT ION (MG/L)
    IrLir^UtJ)    J = is  E|=FLUEKT  CGNCENTRATION (MG/L)

                   j   :  TIME  PEFUCC
    tFF    - cFFLUENT CONCENTRATION INDEX
           - INFLUENT CQNCENTKAT I CN INDEX
 AUThCR:
    RCNCFNtF.     10  GCT  72
                         96

-------
CC.MMCN ciLCCK:
   INCSTY

PURPCSEi
   CCMA1NS  INDUSTRIAL  FHCSPHCHUS  INFCRMAT I CN . This common block
   is unused since it is referenced only by the dummy subroutine INDLIM.
VARIABLES:
   INDSTYUiJ) -  1=1:  LBS  P/DAY  OUTPUT OF INDUSTRY J
                  I=2i3:  8  CHARACTER NAME FOR INDUSTRY J
   LEGINP      -  LEGISLATED P LEVEL FOR INDUSTRY  (MG/L)
AUTHOR:
                 10  CCT  72
CCMMCN BLCCK:
   L3&CST
   CONTAINS LAtJCP. COSTS


VARIABLES:
    )H*    - DIRECT  HOURLY  RATE:   U/HK)
    IOPRAC - INDIRECT  FRACTION OF DIRECT LABOR


AUTHCR:
    RCN  CFNEK     10  GCT 72
       BLOCK:
   LIGUID
PURPOSE:
   CONTAINS

VARIABLES:
   ALKIPS
   BODIPS  •
   MLSSAR
   NH3IAR  •
   PINPS
   QAVE
   QPEAK
   SSINPS
   TBOCAR
THE CHARACTERISTICS OF LIQUID  INFLUENT  SEWAGE.
 ALKALINITY CONC. INTO PRIMARY  SETTLER (CAC03 MG/L)
 BOOS CONC. INTO PRIMARY  SETTLER  (MG/L)
 MIXED LIQUOR SUSPENDED SOLIDS  IN AER. PROC.  (MG/L»
 NH3 CONC. INTO AERATION  PROCESS  (MG/L)
 PHOSPHORUS CONC. INTO PRIMARY  SETTLER (MG/L)
 PRESFNT AVERAGE DAILY ^LOW  (MGD)
 PRFSENT PEAK DIURNAL FLOW  (MGD)
 SUSPENDED SOLIDS CONC.  INTO PRIMARY SETTLER  (MG/L)
 TOTAL CHANGE IN RODS ACROSS AF.RATION PROCESS
 (FRACTION REMOVED)
AUTHCP:
   DAVID  A  BARNES
        26 DEC  72
                           97

-------
COMMC3N BLOCK:
   PRNTR

PURPOSE:
   PRNTR CONTAINS VARIABLES  CONTROLLING THE PRINTOUT
VAR TABLES:
   IPASS  - =1,
                    PASSES  THRU  ELIGIBLE
             FIRST SET OF
             SCHEME LOOP
         =?, TO GET SELECTED  LONG  PRINTOUTS
ISELCT(J) - NUMBERS OF SCHEMES SELECTED  FOR  LONG  PRINTOUT
             FOLLOWING SHORT  OR SUPF.RSHORT
             PRINTOUT OF ALL  ELIGIBLE  SCHEMES
I SHORT - = ON, FOR SHORT OR SUPERSHQRT  PRINTOUT
         = DFF, FOR LONG PRINTOUT
[SKIP  - SET TO ON MRST TIME THRU REPORT
         SET TO OFF BY REMOVE
ISUPFF - =ON» COP SUPFRSHOPT  PRINTOUT
         -OFF, OTHERWISE
AUTHOR:
   CAVIC
A BARNES
                  4- JAN 73
                         98

-------
COMMON BLCCK:
   LSINK
PURPOSE;
   LICU I C
       SINK COSTS
VARIABLES:
   3ESTLS(TP)
   L ICSNKU , J)
              ORDINAL OF LIQUID  SINK  USED FOR TIME PF.RICD TP
              1=1: ASSIMILATIVE  CAPACITY OF SINK J (LBS
              1=2: HEAD LCSS  TC  SINK  J (FT)
              1=3: DISTANCE  TC  SINK J (FT)
LSNKCS(TP)  - COST UF LIQUID  SINK  USEC FOR TlMc PERIOD TP
       CPNEK
              10 OCT  7?
     N BLCCK:
   f»*GCNT
   PRGCNT CONTAINS  V^RI^BLE  USED E3Y THE PROGRAM REMOVE
   AND  ITS SUBROUTINES  TO  CONTROL THE FLGrt CF DFClilCNS
VARIABLES
   ITYPE  -
IGOTO  -

lANSwR -
ANSWER -
      - DO-LOOP V^RAIELE  (SCHtVE  NUMBER)
         KIND OF VALUE OF  TYPED  IN  ANi«F*S
                 1  IMTEGEP
                 2  FLCATIKG  PCINT
                 3  ALPHANUMERIC
                 COMPUTED  GG TC  TO  SIMULATE
                 FP.CM SU6RCTUlNt:S
F1XFO =
FLUTE =
ALPHA =
UStD IN
RETUkWS
WILL
WILL
                                                MULTlLE
CCNTAIN
CONTAIN
FIXcD
FLOAT
VALUE
VALUE
                                   TYPED
                                   TYPED
                                            IN
                                            IN
                          99

-------
CCNMCN bLCCK:
   SOtME

PUrtPLSE:
   CONTAINS PARAMETERS  FGk FHCbPHOPUS REMOVAL  SCHEMES

VAK IflBLES:
   f!LG3TY(J) -  = ON  IF  SCHEME J IS ELIGIBLE,  = CFF  OTHERWISE
   L-OUIP(K) - EQUIP(K)=CN IF PR.CCESS K  IS NtCESSARY FOR THIS
   STRATEGY, = OFF  IF NL)T
   ^/JXSCM - THE MAXINUM NUMBER OF SCHEMS, MAX  VALUE OF J
   MINtFP(J) -  MINUMUM  ACHIEVABLE EFFLUENT  P CONC.  FOR
                SCHEME  j
   SChfcMEl I.J)  -  I  PARAMETERS FCR J SCHEMES
                  I  REPRESENTS REQUIRED  LIQTC EQUIPMENT FOR
                  SCHEME J - SEE COMMON  /TPLANT/

   J   \AMF     DESCRIPTION OF SCHEME
   i    ALPYP6   ALUM +  POLYMER TC PRIMARY SETTLER
   2   FCPYPS   FERRIC  CHLORIDE + POLYMER TT  PRIMARY SETTLER
   3   FCLMPS   FEKP.OLS  CHLQRIDt + LINE  TC PRIMARY SETTLER
   •+   LlVt:PS   LIWE TO  PRIMARY SETTLER
   j   /.LPYFd   ALUM *  PGLYMER TC FLGCCULATICN  BASIN
   O   FCPYPri   FCKf 1C  CHLORIDE + POLYMcR TO FLOCC.  BASIN
   7   FCL^HB   FtRRCUS  CHLORIDE * LIME  TO FLOCC.  BASIN
   ii   LlVfrJ   LIME TO  THE FLCCCULATICN BASIN
   '•J   ALL*A3   ALUM Th" THE AERATION BASIN
   10  P-FCLA6   FFP.SIC  CHLORIDE TO AERATION  BASIN
   11  \AAL.rA-i   SHOIUM  ALUMINATE TC AERATION BASIN
   12  ALArtMF   ALJM TO  £cP. fcASIN + VULTI-MECIA  FILTRATION
   13  FCA6MF   FfcRklC  CHLORIUE TO AER.  HASIN * MULTI-MSDIA FIL,
   If  NA-lfcMF   SODIUf-1  ALUMINATH TC AER.  BASIN  *  MIJL-MED FILTR.
   Lb  /SLLMTF   ALUM AFTER TRICKLING FILTER
   16  FECLTF   FERRIC  ChLORlCt AFTER TRICKLING FILTFR
   17  ALTFMF   ALUM AFfHR TRICKLING FILTER  * fUL-MEU FILTR.
   18  FCTFMF   FtRRIC  CHLQRIUL AFTER TRK.FIL.  *  MUL-^fcD FILTR,
   19  ALFcAS   ALUM TO  FLOCC. AFTER CONVENT ICNAL  SECONDARY
   ^0  FCFBAS   FbCLH T2 FLUCC. wFTfiK CONVENTIONAL STCCNCARY
   21  L1FBAS   LIME( 1-STAGF. )  TC FLCCC  AFTER CONVEM. SfcCCNCAftY
   22  L2FBAS   L IMF (2-STAGE)  TC FLOCC  AFTER CONVEN. ScCONCARY
   23  NfMt     NO  CHfMICALS ADDru FOR PhCSPHGRUS  REMOVAL

AUTHCf-:
   PCN CRNEF     10  CCT  72
                          100

-------
C L M v C N 3LCCK:
   SL
   ::NTAINS  INFCHMATICN  ABOUT PRESENT AND FUTURE  SEWERED
   POPULATION.
   -\CfYP  -  THT-  TYPE  OF  FUTURE SEWERED POPULATION  GROWTH FUNC
            = 1  ASSUMED LINF.AR 5 PtRCNT GROWTH RATE
            = 2  LINilAK
            = 3  FXPCNEINiTI AL
            =^  PieCE-^ISE LINEAR

   SPGPIN(IfJ)  -  THE SEWERED POPS AND YEARS  READ  IN

                  1=1  THE SEwERFC POP
                  1=2  THE YEAR
                  J     THF. OKCINAL FOR PGP  AND VALUES KEAO IN

   SSUPUP  ,-l   -  ThE  YtAR INOEX

 AUTrtJH :
   CAVIC  A  fiAKSF.S   03QCT72
                           101

-------
CUVMflN BLOC
SLCHAP
PURPOSE:


CONTAINS
STREAMS
VARIABLES
AARATC
ADDSSR
\LKIAR
30DIAR
C020
FCVFD
FFP.ATC
LBNVPS
LBIVVSS
LBNVTS
LRVPS
LBVSS
L3VTS
LIMEPD
L IMETD
LMVFD
PALUM
PC02
PFECL
PLIMF
PNAAL
PNAGH
PCLYD
PPOLY
°PCKL
"YFTD
PYVFD
QPSLGF
OSSLGE
OTGTAL
QTSLGE
SRALF
SRALP
SRCAT
SRCATA
SRC ATS
SRFEF
SPrEP
SPL IMF
SRTLIM
TLBNV?
TLBPS
TLPSLG
TLBSS
*
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
-
K:


CHARACTERISTICS OF THE SLUDGE, LIQUID* AND CHEMICAL
DURING PLANT OPERATION.

POUNDS OF ALUM (OR NAAD/POUND OF AL
ADDITIONAL SUSPENDED SOLIDS REMOVAL (MG/L)
ALKALINITY IN AERATION PROCESS (MG CAC03/L)
BOC5 INTO AERATION PROCESS (MG/L)
C02 DOSE IN RECARBONATION (L9S C02/MR. GAL.)
<=ECL3 DOSAGE FOR VACUUM FILTER (L9S/TON)
POUNDS OF FFCL3 (OP PCKD/POUND OF FE
POUNDS OF NON-VOLATILE PRIMARY SLUDGE (LRS/DAY)
POUNDS OF NON-VOLATILE SECONDARY SLUDGE (LBS/DAY)
POUNDS OF NON-VOLATILE TERTIARY SLUOGt (LBS/DAY)
POUNDS OF VOLATILE PRIMARY SLUDGE (LBS/DAY)
POUNDS OF VOLATILE SECONDARY SLUDGE (LBS/DAY)
POUNDS OF VOLATILE TFPTIARY SLUDGE (LBS/DAY)
LIME PRIMARY DOSAGE (MG/L)
LIME TFRTIAPY DOSE (MG/L)
LIME DOSAGE FOR VACUU* FILTER (LBS/TON)
TOTAL AMOUNT OF ALUM USED FOR 1 TP (LBS)
TOTAL AMCUNT OP C02 USTD CQR 1 TP (LBS)
TOTAL AMOUNT OF FECL USED FOR i TP (LBS)
TOTAL AMOUNT OF LIME USED IN 1 TP (L5S)
TOTAL AMOUNT OF NAAL USED FOR 1 TP (LBS)
TOTAL AMOUNT OF NAOH USED FOR 1 TP (L8S)
POLYMER PRIMARY DOSAGE (MG/L)
TOTAL AMCUNT OF POLY USED F3R i TP (LBS
TOTAL AMOUNT OF PCKL USED FQR 1 TP (L3S
POLYMER DOSE FOR FLOTATION THICKENER (LBS/TON)
POLYMER DOSE FOR VACUUM FILTRAT ION (LBS/TON)
VOLUME OF PRIMARY SLUDGE (MGD)
VOLUME OF SECONDARY SLUDGE (MGD)
VOLUME OF TOTAL SLUDGE (MGD)
VOLUME OF TERTIARY SLUDGE (MGD>
SLUDGE RATIO IN TRICKLING FILTER (LBS/LB AL )
SLUDGE RATION IN PRIMARY (LBS/LB AL )
SLUDGE RATIC FOR CATION (LBS SLUOGE/LBS CATION)
SLUDGE RAT 1C IN AERATOR (LBS/LBS FE)
SLUDGE RATIO IN SECONDARY EFFLUENT (LBS/LB CATION)
SLUDGF RATIO IN TRICKLING FILTER (LBS/LB FE )
SLUDGE RATIO IN PRIMARY (LBS/LB FE)
SL'JOGF RATIO FOR LIME (LBS SLUDGE/MG)
SLUDGE RATIC PQR LIME (TERTIARY) (LBS SLUOGE/MG)
TOTAL POUNDS OF NON-VOLATILE SLUDGE (LBS/DAY)
TOTAL POUNDS OF PRIMARY SLUDGE (LBS/DAY)
TOTAL POUNDS OF ALL SLUDGE (LBS/DAY)
TOTAL POUNDS 0* SECONDARY SLUDGE (LBS/DAY)
102

-------
TL8TS
TLBVS
TSETUC
WQLBSS
WOPALM
WOPC02
WOPFC
WOPLIM
WOPNAL
WOPNOH
WOPPLY
WOTL9S
WOPPCK
WRALA
WKALF
WRALP
WRALS
WRCAT
WRCATS
WRFF.A
WRFEF
WRFEP
            TOTAL POUNDS OF TERTIARY
            TOTAL POUNDS OF VOLATILE
            TERTIARY SETTLER UNDERFLOW
            = TL8SS (WITHOUT
                    {WITHOUT
                    (WITHOUT
                    (WITHOUT
                    (WITHOUT
                    (WITHOUT
                    (WITHOUT
                    (WITHOUT
PALUM
PC02
PFFCE
PLIME
PNAAL
PNAOH
PPOLY
P
P
P
P
P
P
P
P
          SLUDGE (LBS/OAY)
          SLUDGE (LBS/DAY)
        DENSITY (FRACTION)
REMOVAL) (LBS/DAY)
         (LBS)
         (LBS>
         (L3S)
         (LBS)
         (LBS)
         (L3S)
         (LBS)
AUTHOR:
   CAVID
                      REMOVAL)
                      REMOVAL)
                      REMOVAL)
                      REMOVAL)
                      REMOVAL)
                      REMOVAL)
                      REMOVAL)
   TOTAL POUNDS OF SLUDGE WITHOUT P REMOVAL
   = PPCKL (WITHOUT P REMOVAL (LBS)
   WEIGHT RATIO AL/P IN AERATOR
                AL/P IN TRICKLING FILTER
                AL/P IN PRIMARY
                AL/P TO SECONDARY
                OF CATION TO  PHOSPHORUS
                OF CATION TC  PHOSPHORUS  IN SEC.
                FE/P IN AERATOR
                FE/P IN TRICKLING FILTER
                F
-------
COMMCN  BLCCK:
    SLLCGE

PURPOSE:
    CUNTAINS CHARACTERISTICS  OF  SLUDGE.
    IABLES:
    ASC   -  ACTIVATED  SLUOGE  DENSITY (FRACTION)
    FLOTUC -  FLOTATION THICKENER  UNDERFLOW SLUDGE DENSITY (FRAC)
    GPAVUD -  GRAVITY THICKENER UNDERFLOW SLUOGE  DENSITY (FRAC)
    HPDFT -  OPERATING  HOURS  PEP DAY FCK FLOTATION THICKENER
    HPDVF -  OPERATING  HOURS  PER CAY FOR VACUUM FILTER
    PSETUC -  PRIMARY SfcTTLER  UNDERFLOW SLUDGE DENSITY (FRAC)
    PSRMVE -  SOLIDS REMOVAL  IN PRIMARY St-'TTLEP (FRACTION)
    VFPSLG   - VOLATILE FRACTION FOR PRIMARY SLUDGF (FRACTION)
    VSANR^   - VOLATILE SLUDGE REGAINING AFTER ANAEROBIC
              DIGESTICN (FRACTION)
    VSARM -  VOLATILE SLUCGE  REMAINING AFTER AEROBIC DIGESTION
    (FRAC1 ICN)
 AUTHOR :
    DAVID A  RARN6S   03QCT72
CCMMCN BLCCK:
   SSINK

PUkPCSE:
   SCLID SINK CHARACTERISTICS

VARIABLES:
   t3cSTSS(TP) - ORDINAL OF  SCLID  SINK  USED  AT  TP
   CAP    - CAPACITY  INDEX
   OIST   - DISTANCE  INDEX
   MAXSS  - MAXIMUM NUMBER  CF~ SCLID  SINKS
   SCLSNK(ItJ) - 1=1: CAPACITY OF  SINK J
                 1-2: DISTANCE TO  SINK J
   SSCQST(TP) - COST OF SOLID  SINK USED AT  TP  ($)
   SlnASTHTP) - SOLID *A$TE FROM  TREATMENT  PLANT  AT  TIME  TP
                                                       (TONS)
   TPNCST - TRANSPORTATION  CCST OF SCLID *ASTE  (S/TOM/MILEJ

AITHCP :
   RCN CRNER    10 OCT 72
                          104

-------
CCMMCN BLCCK:
   TIME

PIRPOSE:
   CCNTAINS  INFORMATION  ABOUT  TIME HCRUON CF CONTROL STRATEGY
   NICYRS   - NUMBER  OF  YEARS FCR CONTROL STRATEGY
   MAXTP   - MAXIMUM NUMBER  CF TIMF PERIODS = NCYEARS/TPSI ZE
   TPSIZE  - SIZE  OF TIME  PERIOD STEPS (FRACTION OF YEARS)
   TP     - THE  CURRENT TIME PERICD

ALTHOP:
   uAVIQ A 8ARNES    03CCT72
CC^NCN  BLCCK:
    TPLANT

PURPCSE:
    CCNTAINS TREATMENT PAKAHETEHS CCK  TREATMENT  PROCESSES

VARIABLES:
    TPLANT(ItJ)  - I  PAf-AMb'TERS FCK TREATMENT  PPQCESS J
  J    VARIAELE    DESCRIPTION

  1    PwFLJVF     FAW WA5TEWATFR PUMPING
  2    PRfcT«T     PRELIMINARY TREATMENT
  3    PRMSET     PRIMARY SETTLES
  4    PSPUMF     PRIM^kY SLUDGE PUMPING
  5    TRKFTR     TRICKLING FILTER (SINGLE  MEDIA)
  6    JERBSN     AEHATICN BASIN
  7    CIF^IR     DIFFLS=0 AIR SYSTEM
  3    NCHAEK     MECHANICAL AE^TICN
  9    FLOCCP     FLOCCULATION BEFORE  PRIMARY
10    SECSET     SECONDARY SETTLER
 11    RE1PMF     RECIP.CULATICN PUVFING
32    CLFerr     CHLORINE FEEC SYSTFW
 13    CLB£SN     CHLOKINATUN CONTACT  6ASIN
1^    MILFTF     MULT-MErCIA FILT?«
 1.5    RE2PMF     HEC I5CULATILN PUMPING
16    CRVTKN     GRAVITY THICKNER
 17    FLCTKN     AIR FLGTATION ThICKNcR
Id    ANAC1G     ANAb'RO-JIC DIGtSFICN
 19    AERCIG     AEKCPIC CIGF.STICN
 20    CRYEfcC     SLULGF. DRYING BcO
21    SLCTNK     SL'JOGi HOLDING TfiNK
22    VACFTP     VACUUM FILTER
                          105

-------
23
24
25
26
27
28
29
30
31
32
33
34
35
36
37
30
39
40
41
42
43
44
45
CENFUG     CENTRIFUGE
MHINC      MULTIPLE  HEARTH  INCINERATOR
FBINC      FLU10IZED BED  INCINERATOR
kSPCND     WASTE STABILIZATICN  PCND
SLGCCN     SLUDGE  LAGOCN
RECREl     Kt-CARBINATICN
RECPE2     RE-CAP3INATICN
TERST1     TERTIARY  SETTLER
TERST2     TERTIARY  SETTLER
ALUMFS     ALUM
FECLFS     FERPIC  CHLORICE
LIMEFS     LIME
PCLYFS     POLYMER
CG2FS      CO 2
NAALFS     SODIUM  ALUMINATE
PCKLFS     PICKLING  LIQUOR
NADHFS     SODIUM  HYDROXIDE
RECALC     RECALCINATICN
FLGCCT     FLOCCLLATION BEFORE  TtRTIARY
FEEDING
FEEDING
FEEDING
FEEDING
FEEDING
FEEDING
FEEDING
FEEDING
AND
AND
AND
AND
AND
AND
AND
ANO
STORAGE
STORAGE
STORAGE
STORAGE
STORAGE
STCRAGE
STCRAGE
STORAGE
 I

 i
 2
 3
 4
 t)
 6
 7
 8
 9
10
11
12
13
14
•» 5
16
       ERS  FOR  TREATMENT  PROCESSES
     VAPIAELE    DESCRIPTION
PNAPfc
PNAME
AMRATE
   IFE
    BASE
    APV/R
    PA K M X
    M IN h V
    MAXPV
              CHARACTER DESCRIPTION OF PROCESS
              CHARACTER DESCRIPTION OF PROCESS
                        DESCRIPTION OF PROCESS
                        RATE
                        LIFETIME
                12
                12  CHARACTER
                AMORTIZATION
                AMORTIZATION
                                                     FOR CCSTS
           PRESENT  INDEPENDENT SIZING PARAMETER
           PRESENT  DESIGN PARAMETER
           INDEPENDENT  SIZING PARAMETER WITHCUT P REMOVAL
           INDEPENDENT  SIZING PAKAMETER WITH P REMOVAL
           DESIGN  PARAMETER fclTH P REMOVAL
           INDEPENDENT  SIZING PARAMETER TO BE BUILT
           AMAXK WC^ARMf PPARV) ,  USED BY C-«-M COST EQS.
           INITIAL  ASSUMt'J VALUE CF PVAR
           FOUt<  CHARACTER DESCRIPTION OF PAkN1
           MINIVLM  USABLF VALUE  CF BPARV
           MAXIMUM  USA3LE VALUE  CF PPARM
                         106

-------
DESCRIPTIONS AND DIMENSIONS OF PARM AND VAR FOR EACH
PROCESS FOLLOW:
   PARM = INDEPENDENT SIZING PARAMETER
   VAR. = DESIGN VARIABLE
                 INITIAL FIRM CAPACITY (MGD)
                 MAXIMUM CAPACITY (MGO>
                 SURFACE AREA CF SETTLER (THOS. SQ. FT.)
                 DESIGN OVERFLOW RATE ( GPO/SQ.FT. )
                 INITIAL FIRM CAPACITY (GPM)
                 OPERATING HOURS < HOURS/DAY)
                 PEDIA VOLUME (THOS. cu. FT.)
                 HYDRALIC LOADING (MGO/ACRE)
                 LIQUID VOLUME CTHOS. cu. FT.)
                 DETENTION TIME (HOURS)
                 INITIAL FIRM BLOWER CAPACITY  (THOS. CFM)
                 OIFFUSER EFFICIENCY  (FRACTION)
                 TOTAL INSTALLED CAPACITY (HP)
                 TRANSFER EFFICIENCY  (LBS 02/HP-HR)
                 MAXIMUM CAPACITY (MGD)
                 SURFACE AREA OF SETTLER CTHOS. SQ. FT.)
                 OFSIGN OVERFLOW RATE  (GPD/SO.FT.)
                 MAXIMUM CAPACITY (MGD)
                 AVERAGE CHLORINE USE  (LBS/DAY)
                 CHLORINE DOSAGE  (MG/L)
                 LIQUID VOLUME  (THOS.  cu. FT.)
                 CHLORINE CONTACT TIME  (MINUTES)
                 CAPACITY  (MGO)
                 MAXIMUM CAPACITY (MGD)
                 SURFACE AREA  (THOS.  so. FT.)
                 DESIGN LOADING  RATE  (LBS/SQ.FT.)
                 SURFACE AREA  (SQ.  FT.)
                 LOADING RATE  ( LB/HR/SQ .FT . )
                 SLUDGE  VOLUME  (THOS. CU.  FT.)
                  DETENTION TIME (DAYS)
                  SLUDGE  VOLUME  (THOS. CU.  FT.)
                  DETENTION TIME (DAYS)
                  SURFACE  AREA  OF BEDS (THOS. SQ.  FT.)
                  REQUIRED  OEO  AREA  (SQ.FT. /CAPITA)
                  SLUDGE VOLUME (THOS. cu.  FT.)
                  DETENTION TIME (HOURS)
                  FILTER AREA (SQ. .FT.)
                  LOADING RATE  (L8S/HR/SQ.FT. )
                  PI^M CAPACITY (GPM)
                  OPERATING TIME (FRACTION OF DAY)
                  CAPACITY (LBS DRY SOLIDS/HR)
                  OPERATING TIME (HOURS/DAY)
                  CAPACITY (LBS DRY SOLIDS/HR)
                  OPERATING TIME (HOURS/DAY)
RWPUMP:
PRETRT:
PRMSET:

PSPUMP:

TRKFTR:

AERBSN:

DIFAIR:

PCHAER:

FLCCCP:
SEC SET:

RE1PMP:
CLFEED:

CLBASN:

MULFTP:
RE2P"P:
GRVTKN:

FLOTKN:

ANADIG:

AERDIG:

CRYBED:

SLDTNK:

VACFTR:

CENFUG:

MHINC:

FBINC:

PARM -
PARM -
PAPM -
VAR -
PARM -
VAR -
PARM -
VAR -
PARM -
VAR -
PARM -
VAR -
PARM -
VAR -
PARM -
PAP.M -
VAP -
PARM -
PARM -
VAR -
PARM -
VAR -
PARM -
PARM -
PARM -
VAR -
PARM -
VAR -
PARM •
VAR -
PARM •
VAR -
PAPM •
VAR -
PARM •
VAR -
PAPM
VAR -
PARM
VAR -
PARM
VAR -
PARM
VAR -
                          107

-------
  fcSPOND: PARM •
          VAR -
  SLGCCN: PAPM
          VAR -
  RECRBi: PARM •
          VAP -
  RECRE2: PARM •
          VAP -
  TER STl: PARM •
          VAR -
  TERST?: PARM •
          VAR -
  ALUMFS: PARM
          VAR -
  FECLFS: PARM •

  LIMEFS: PARM •
          VAR -
  POLYFS: PARM •
          VAR -
  C02FS  : PARM •
          VAP -
  NAALFS: PARM •
          VAR -
  PCKLFS: PARM •
          VAR -
  NAOHFS: PARM •
          VAR -
  RECALC: PARM •
  FLOCCT: PARM -
VAXP  - MAXIMUM
                   •  SLUDGE  VOLUME  (THOS.  CU.  FT.)
                     DETENTION  TIME  (DAYS)
                   •  SLUDGE  VOLUME  (THOS.  CU.  FT.)
                     DETENTION  TIME  (DAYS)
                   -  LIQUID  VOLUME  (THOS.  CU.  FT.)
                     DETENTION  TI^F  (MINUTES)
                   -  LIQUID  VOLUME  (THOS.  CU.  FT.)
                     DETENTION  TIME  (MINUTES)
                   •  SURFACE AREA OF  SETTLER  (THOS.  SQ.
                     DESIGN  OVERFLOW  RATE  (GPD/SQFT)
                   •  SURFACE AREA OF  SETTLER  (THOS.  SQ.
                     DESIGN  OVERFLOW  RATE  (GPD/SQFT)
                   •  CHEMICAL USAGE  (LBS AL/DAY)
                     COST OF CHEMICAL  ($/LB  ALUM)
                   •  CHEMICAL USAGE  (LBS FE/DAY)
                     COST OF CHEMICAL ($/L8 FECL3)
                   •  CHEMICAL USAGE  (LBS CAD/DAY)
                     COST OF CHEMICAL ($/LB CAO)
                   -  CHEMICAL USAGf  (LBS/OAY)
                     COST OF CHEMICAL ($/LB POLY)
                   •  CHEMICAL USAGE  (LBS/OAY)
                     COST OF CHEMICAL ($/LB CQ2)
                   •  CHEMICAL USAGE  (LBS AL/DAY)
                     COST OF CHEMICAL ($/LB NAAL)
                   •  CHEMICAL USAGE  (LBS FE/DAY)
                     COST OF CHEMICAL ($/LB FECL2)
                   •  CHEMICAL USAGE  (LBS/DAY)
                     COST OF CHEMICAL (t/LB NAOH)
                   •  MAXIMUM CAPACTIY (MGD)
                     MAXIMUM CAPACITY (MGD)
                   NUMBER OF PROCESSES
                                                 FT.)

                                                 FT.)
AUTHCP
   PON
OPNER
             10 OCT 72
   MCf\ BLCCK:
   T4TCST
   TREATMENT COSTS. FOP 45  PROCESSES  OVER  20  TIME  PERIODS

VAR IABLES :
          - OPERATING MAN-HOURS
          - MAINTAINENCE  MAN'-HCURS
   IMS    - TOTAL MATERIAL  AND  SUPPLY  COST
   CCNCQS - CCKSTKUCTKJN  COST
   AMCOST - AMOKTIZEC CCNSTRUCTIQN  COST  FROV TIME PERIOD
                                  TPFAUD  TO  NAXTP
   TPFAOL - TIME PERIUJ WHEN  FlkST  ADDITIONAL AMOUNT OF
                                  tQUIPMENT  IS NFtCEC
AUTHOR:
   PCfv CRNER    10 CCT 72
                          108

-------
       BLCCK:
   TSCST

PURPOSE :
   TlfE ANC LOCATION DIFFERENCE COSTS - MULTIPLIERS TO CONVERT
   TO PRbSENT LOCAL $

VARIABLES:
   CNSTRC - (WQO-STP INUGX I /100.
   MATRLS - NIATFRIAL CJST MULTIPLIER
   KCN CRNEK    10 CCT 12
                         109

-------
                       SECTION VII

                       CASE STUDIES


The primary purpose of the computer model is to assist local
communities in evaluating the costs of various strategies undertaken
to reduce effluent phosphorus.  In order to demonstrate how the
model can be used by a community we have  performed three case
studies which are presented in this  section.  Each case  is designed
with a different size community in mind.  The cases  include:

      1.  A community of approximately 50,000 population
          presently operating a 5 MGD secondary trickling
          filter treatment plant.

      2.  A medium size city of approximately 200, 000 population
          operating a 20 MGD secondary activated sludge treat-
          ment plant,

      3.  A large city of approximately 500,000 population
          operating a 50 MGD primary treatment plant.

In each case we have assumed that the average per capita generation
of liquid waste is 100 gallons per day and that peak flow is 80% of
the average.  It is also assumed that sludge disposal facilities of
sufficient capacity to handle all sludge generated during a 20 year
assumed time  horizon are available v/ithin a distance of 5 miles
from the treatment plant.  Although we have not done so in these
cases,  it is possible to limit and disperse sludge disposal facilities
if desired.

The treatment plants in each community had available the following
process equipments adeouately sized to treat the present influent
load assuming that phosphorus removal was not required:

       1.  Raw waste pumping
      2.  Pre-treatment facilities
      3.  Primary  settler
      4.  Primary  sludge pumping
      5.  Chlorination
      6.  Gravity thickener
      7.  Sludge holding tank
      8.  Vacuum filter

In addition to the above,  the'trickling filter plant had a  secondary
settler, and recirculation pumping.   The activated sludge plant had
an aeration basin, mechanical aeration, secondary settler,  and re-
circulation pumping.

Each case study was examined over a 20 year time horizon.  In these
case studies we assumed that the populations were constant over the
                              111

-------
time horizon.  However,  the program can accept linear, exponential,
and piece-wise linear growth predictions.  Cost estimates were
generated (and appear in  Tables  11,  12 and 13 for each  case) for six
different combinations of  events.  These combinations can be viewed
as "strategies".  Costs of achieving phosphorus effluent concentrations
of both 2.0 mg/1 and 0.5  mg /1 were examined.  For each of these
effluent requirements the effect of federal and state governments
financing 80% of the construction costs was examined as was the
additional effect of restricting phosphate detergents.  The detergent
restriction evaluated in these cases consisted of a total  ban  on the use
of phosphates in detergents assuming a national detergent consumption
of 16 Ibs/capita/year.  The model can also accept various percentage
decreases in phosphate consumption assuming a zero ban is not  feasible.

It was also assumed that  there would be no enforcement cost to  the
consumer since detergent manufacturers have recently  complied with
most phosphate restrictions and are anticipating further reductions in
the future.

Case 1 - 5 MGD Trickling Filter Plant

For this case we found that a phosphorus effluent level of 2. 0 mg/1
can be achieved at a minimum cost of 4.6 cents/1000 gallons using a
treatment scheme of alum added after the trickling filter.  This is
shown as scheme 1 5 in Table 11. (See Table 14 for a list of treatment
schemes).  The minimum cost was achieved assuming that all phos-
phate detergents would be banned  and the federal and state governments
would finance 80% of the required construction costs. As can be seen
from Table 11, this  scheme would  also be the  most cost  effective if
there were no ban on detergent phosphates and government financing
was not available.

We can also see from Table llthat reducing the effluent phosphorus
from 2.0 to 0.5 mg/1 resulted in  a different treatment scheme being
selected.  In this case scheme 17 also included the addition of alum
after the trickling filter but, in addition, required that a multi-media
filter be added to the alum treatment process.

The costs of  the feasible  treatment schemes capable of  achieving 2.0
and 0.5 mg/1 phosphorus effluent requirements are shown in Table 11.
The long printouts for schemes  15 and  17,  showing in detail the
equipment and operating costs for the individual processes,  are
shown in Figures 18 and 19.  The information shown in these tables
and figures is available to the program user as part  of the computer
output format.

Case 2-20 MGD Activated Sludge Plant

For this case we found that the minimum cost of achieving a 2.0 mg/l
phosphorus effluent was 4.0 cents/1000 gallons achieved with the
                             112

-------
                    Table 11
                5 MGD TRICKLING FILTER PLANT
             TREATMENT COSTS IN CENTS/1000 GAL.
P            2      2      2     0.5    0.5    0.5
GOVFF              .8     .8             .8     .8
RESTRICT                 yes                   yes

SCHNO
1
2
5
k
5
6
7
8
9
10
11
12                              18.9   1U.5   10.2
13                              16.6   12.1    9.1
U                              21.7   17.1   11.5
15         7.7    6.7    U.6
16         S.2    7.3    4.8
17                              15.7   10.0    iti
18                              1U.9   11.2    7.7
21                              15.3   10.5   11.2
NOTES:
1. P = Phosphorus effluent  level  In mg/1 .
2. GOVFF * Fraction of construction cost  financed
           by federal and stdte governments.
3. RESTRICT = Restrictions  on phosphate  detergents.
U. SCHNO • Treatment  scheme number.
5. 	 » Lowest  treatment cost.
13.9
10.0
17.8
13.1
lit. 8
11.0
18.8
11*. 0
12.5
10.0
15.1
11.9
8.4
15.0
10.9
12.3
8. R
15.3
11.2
10.6
8.U
13.5
8.U
6.6
13.7
11.7
8.8
7.0
1U.O
12.1
7.5
6.3
8.8
                       113

-------
                                    Figure 18

                        5 MGD Trickling Filter Plant


                              CASE  1
 LIQUID  TREATMENT SCHEME =    15
 AMORTIZATION  RATE =0.05 AMORTIZATION LIFETIME  =20  0
 FRACTION  OF  CONSTRUCTION COST FINANCED BY GOVERNMENT
                                        = .0
 PROCESS  NAME
RAW WSTE  PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE  PMP
TRKLNG  FILTR
SECY SETTLER
RECIRC  PMPNG
CHLORNE FEED
CHLORNE BASN
GRAV THICKNR
SLGE HLD  TNK
VACUUM  FILTR
ALUM FEEDING
FECL FEEDING
LIME FEEDING

TOTALS =
 CONSTRUCTION
COSTdOOO $ )

        0.0
        0.0
        0.0
        0.0
        0.0
        0.0
        0.0
        0.0
        0.0
       31*.821*
       15.61*9
      101*.751
       1*9.858
       1*5.525
       15.901

       2G6.507
SIZING
PARAMETER
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.022
0.987
39.600
62U. 750
61*. 565
71*6.367


MGD
MGD
TSF
GPM
TCP
TSF
MGD
*/D
TCF
TSF
TCF
SQFT
#/D
#/D
*/D
AMORT
(10
















IZED
00 $
0
0
0
0
0
0
0
0
0
2
1
8
1*
3
1
21
COST
/TP)
.0
.0
.0
.0
.0
.0
.0
.0
.0
.791*
.256
.1*06
.001
.653
.276
.385
                                                                            YEAR PROCESS
                                                                            FIRST NEEDED
199U
199U
199U
1991*
1991*.
199U
199U
199U
1971*
197U
1971*
1971*
1971*
0
0
0
0
0
0
0
0
0
0
0
0
0
0
1971*.0

-------
                       Figure 18 (cont. )
                             PERIODIC OPERATING  COSTS
PROCESS NAME
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
TRKLNG FILTR
SECY SETTLER
RECIKC PMPNG
CHLORNE FEED
CHLORNE BASN
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
ALUM FEEDING
FECL FEEDING
LIME FEEDING
 OPERATING MAN-HOURS
  (MAN-HOURS/TP)
AVE.    MAX.    MIN.
               MA I NTAI NANCE MAN-HOURS
                  (MAN-HOURS/TP)
                AVE.    MAX.    MIN.
0.
0.
0.
0.
0.
0.
0.
0.
0.
2.
18.
665.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
2.
18.
665.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
2.
18.
665.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
1.
11.
80.
11*73.
600.
1578.
0.
0.
0.
0.
0.
0.
0.
0.
0.
1.
11.
80.
1473.
600.
1578.
0.
0.
0.
0.
0.
0.
0.
0.
0.
1.
11.
80.
1473.
600.
1578.
TOTALS
665.
685.
6S5.
5742.
3742.
3742.

-------
                                      Figure 18 (cont. )
 PROCESS NAME
 RAl,' V.'STE  PMP
 PRE TRETMENT
 PRIM SETTLER
 PRMYSLGE  PMP
 TRKLNG  FILTR
 SECY SETTLER
 RECIRC  PMPNG
 CHLORNE FEED
 CHLORNE BASN
 GRAV  THICKNR
 SLGE  HLD TNK
 VACUUM FLITR
 ALUM  FEEDING
 FECL  FEEDING
 LIME  FEEDING

TOTALS =

MATER

AVE.
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0,0
0.0
S.C7
51*. 57
51CC.75
7SS72.UU
;
-------
                    Figure 18 (cont. )
                             UNIT COST DATA
                          (CENTS/1000 GALLONS)

PROCESS NAME   AMORTIZATION   LABOR   MATERIAL & SUPPLY   TOTAL
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
TRKLNG FILTR
SECY SETTLER
RECIRC PMPNG
CMLORNE FEED
CHLORNE BASN
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
ALUM FEEDING
FECL FEEDING
LIME FEEDING

TOTALS =
TIME
PERIOD
1
2
3
k
5
G
7
o
9
10
11
1 2
13
14
15.
16
17
18
19
20
SINK
USED
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
  TOTALS =

UNIT COSTS
TOTAL UNIT
       0.0
       0.0
       0.0
       0.0
       0.0
       0.0
       0.0
       0.0
       0.0
       0.15
       0.07
       0.1*6
       0.22
       0.20
       0.07
        0.0
        0.0
        0.0
        0.0
        0.0
        0.0
        0.0
        0.0
        0.0
        c.oo
        0.01
        0.19
        0.37
        0.15
        0.39
       1.17        1.10

        SOLID SINKS COSTS
                AMOUNT
                   (TON
SOL
S)
IT 10
1*10
1*10
IrlO
U10
1*10
1*10
1*10
1*10
1*10
1*10
1*10
1*10
1*10
1*10
1*10
1*10
1*10
1*10
1*10
IDS
. I; 6
.1*0
AC
.l*G
.1*0
.1*0
AG
.IrG
. to
. 46
. ^G
AC
.l*G
.1*6
.1*6
.1*6
.1*6
. i*6
.1*0
.1*0
COST
(S/TP)
102G1
10201
10261
10201
1U2G1
1 0 2 G 1
102G1
102G1
10261
102G1
10201
10201
10261
1 0 2 G 1
10201
10201
10201
10201
102 G 1
10261
.50
.50
.50
.50
. 50
.50
.50
.50
.50
.50
.50
.LG
.50
.50
.50
.50
.50
.50
.50
.50
8209.17
                      205220.12
o.n
0.0
0.0
0.0
0.0
0.0
0.0
o.n
0.0
o.co
0.00
0.17
U.32
0.16
0.1G
0.0
0.0
0.0
0.0
0.0
o.c
o.n
o.n
o.o
O.li
0.08
0.82
U.31
0.51
0 .C>2

7.09
FOR SOLID WASTE DISPOSAL (CENTS/10CO  GAL
COST (CENTS/1000 GAL) = 7.G6
                                ) =
                          117

-------
                                             Figure 19

                                    5 MGD Trickling Filter Plant


                                       CASE   1
          LIQUID  TREATMENT SCHEME =    17
          AMORTIZATION RATE =0.05 AMORTIZATION LIFETIME =20.0
          FRACTION  OF  CONSTRUCTION COST FINANCED BY GOVERNMENT
                                                         .0
00
          PROCESS  NAME
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
TRKLNG FILTR
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASN
MUL-MED FLTR
RECIRC PMPNG
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
ALUK FEEDING
FECL FEEDING
LIME FEEDING
                CONSTRUCTION
               COSTC1000  $  )
  0,
  0,
  0,
  0,
  0,
  0,
  0,
  0,
  0,
595,
124,
 30,
 27,
157,
 49,
 US.
0
0
0
0
0
0
0
0
0
028
588
645
753
691
858
525
                                18.908
si z inn
PARAMETER
0.0
0.0
0. 0
0.0
0.0
0.0
0.0
0.0
O.C
5.000
9.000
0.205
3.193
88.G87
624.750
83.588
965.279


MGD
r-:cn
TSF
n PM
TCF
TSF
MGD
#/D
TCF
MGD
MGD
TSF
TCF
SOFT
#/D
#/n
*/D
AMORT 17.
(1000

















EP COST
$ /TP)
0.0
0.0
0.0
0.0
O.C
O.C
0.0
0.0
0.0
47.747
9.997
2.1*59
2.227
12.654
4.001
3.653
1.517
                                                                                    YEAR PROCESS
                                                                                    FIRST NEEDED
1994
1994
1994
1994
1994
1994
1994
1994
1994
1074,
1974,
1974,
1974,
1974,
1974,
0
0
0
0
0
0
c
0
0
0
0
0
0
0
0
1974.0
1974.0
         TOTALS
                     1049.994
                                         84.255

-------
                    Figure 19 (cont. )
                              PERIODIC OPERATING COSTi
PROCESS  NAME
RAW WSTE  PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE  PMP
TRKLNG FlLTR
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASN
MUL-MED FLTR
RECIRC PMPNG
GRAV THICKNR
SLGE HLD  TNK
VACUUM FlLTR
ALUM FEEDING
FECL FEEDING
LIME FEEDING
  OPERATING MAN-HOURS
   (MAN-HOURS/TP)
 AVE.    MAX.    MlN.
        MA INTAI NANCE  MAN-HOURS
            (.MAN-HOURS/TP)
         AVE.     MAX.     MIN.
0.
0.
0.
0.
0.
0.
0.
0.
0.
1672.
597.
16.
57.
U28.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
1672.
597.
IB.
57.
1«»28.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
1672.
597.
16.
57.
li»28.
0.
0.
0.
0.
0.
0.
0.
c.
0.
0.
0.
0.
0.
519.
7.
33.
171.
1U73.
600.
1660.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
519.
7.
33.
171.
1473.
600.
1660.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
519.
7.
33.
171.
1<*73.
eoo.
1660.
TOTALS
3769.    3769.
3769.
1*1*61*.
i*<*6l*.
l*i*6«*.

-------
                            Figure 19 (cont. )

                    PERIODIC OPERATING COSTS
 PROCESS NAME
 RAW WSTE  PMP
 PRE TRETMENT
 PRIM SETTLER
 PRMYSLGE  PMP
 TRKLNG  FILTR
 SEC SETTLER
 RECIRC  PMPNG
 CHLORNE FEED
 CHLORNE BASN
 MUL_MED FLTR
 RECIRC  PMPNG
 GRAV THICKNR
 SLGE HLD TNK
 VACUUM  FLITR
 ALUM FEEDING
 FECL FEEDING
 LIME FEEDING

TOTALS =
MATER

AVE.
0.0
0.0
0.0
0.0
0.0
0.0
o.o
0.0
0.0
8013.89
4312.23
51.20
171.56
6882.15
78872.UU
3881.48
3696.66
105881.50
IAL ft SUPPLY
( $ /TP)
MAX.
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
8013.92
4312. 2k
51.20
171.56
6E82.18
78872.69
3881.U9
3696.66
105881.81
                                       COST
    MIN.

    0.0
    0.0
    o.o
    0.0
    0.0
    0.0
    0
    0
    0
 8013
 4312
   51
  171
 6882,
78872,
 3881,
 3696,
0
0
0
92
24
20
56
18
69
49
66
LABOR COST
(AVERAGE)
(1000S/TP)

     0.0
     0.0
     0.0
     0.0
     0.0
     0.0
     0. 0
     0.0
     0.0
                        TOTAL  OiM
                       (1000S/TP)
     7,
     5,
                                       105881.81
   594
   072
 0.105
 0.410
 7.262
 6.693
 2.725
 7.541

37.402
 0,
 0,
 0,
 0,
 0,
 0,
 0.
 0,
 0.
15.
 9.
 0.
 0,
14.
85.
 6.
0
0
0
0
0
0
0
0
0
608
384
156
582
144
565
607
                11.238

               143.283

-------
                     Figure 19 (cont. )
                             UNIT COST DATA
                          (CENTS/1000 GALLONS)

PROCESS NAME   AMORTIZATION    LABOR   MATERIAL & SUPPLY   TOTAL
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
TRKLNG FILTR
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASN
MUL-MED FLTR
RECIRC PMPNG
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
ALUM FEEDING
FECL FEEDING
LIME FEEDING

TOTALS »
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
2.62
0.55
0.13
0.12
0.69
0.22
0.20
0.08
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
O.U2
0.28
0.01
0.02
0.1*0
0.37
0.15
O.Ul
U.62        2.05

  SOLID SINKS  COSTS
TIME
PERIOD
1
2
3
1*
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
SINK
USED
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
AMOUNT SOLIDS
(TONS)
912.13
912.13
912.13
912.13
912.13
912.13
912.13
912.13
912.13
912.13
912.13
912.13
912.13
912.13
912.13
912.13
912.13
912.13
912.13
912.13
COST
($/TP)
22803.3U
22803.31*
22803.31*
22803.31*
22803. 3U
22803.3U
22803.31*
22803.3U
22803.31*
22803.3U
22803.31*
22803.31*
22803.31*
22803.314
228-03.31*
22803. 3U
22803.31*
22803.31*
22R03.3U
22803.3U
   TOTALS  «

 UNIT  COSTS
 TOTAL UNIT
                      182U2.66
1*56066.31
                                            0.0
                                            0.0
                                            0.0
                                            0.0
                                            0.0
                                            0.0
                                            0.0
                                            0.0
                                            0.0
                                            0.1*1*
                                            0.2U
                                            0.00
                                            0.01
                                            0.38
                                            I*.32
                                            0.21
                                            0.20

                                            5.80
                         0.0
                         0.0
                         0.0
                         0.0
                         n.o
                         o.o
                         o.o
                         o.o
                         n.o
                         3.U7
                         1.06
                         0.11*
                         0.15
                         1.1*7
                         I*.91
                         0.56
                         0.70

                         12.U7
            FOR  SOLID  WASTF.  DISPOSAL  (CENTS/1000   GAL.)
            COST (CENTS/1000 GAL)  -13.72
                        1.25
                           121

-------
 addition of ferric chloride to  the aeration basin.   This  is shown as
 scheme JO in Table  12.  This scheme is also the least  cost treatment
 method when government financing is available and there is no  limi-
 tation on detergent phosphates.

 When an effluent phosphorus concentration of no more than 0.5  nig / 1
 was required, the best treatment scheme was the addition of  a  multi-
 media filter to the ferric chloride process. This scheme is number
 13 in  Table  12.

 When there is no  detergent phosphate limitation the best scheme
 became the single stage tertiary lime process shown as number 2].
 This scheme also remained the best choice if there was no government
 financing.  This fact resulted from a balancing of two effects.  The
 capital costs for the tertiary lime process were a larger fraction of
 the total costs than was the case for  the ferric  chloride process.
 This resulted in a greater increase for the lime process when govern-
 ment financing was  reduced.  However,  the sludge disposal costs
 for the ferric chloride process were 0.9 cents/1000 gallons while
 they were essentially zero for the lime process  since the lime  sludge
 was recalcined and  thus reused.

 There was an additional consideration in this case due  to chemical
 costs.  The cost of  new lime was less than 0.5 cents/1000 gallons
 while  the cost of ferric chloride was on  the order  of 4.  cents/1000
 gallon. Although much more lime is used than ferric chloride,  the
 ferric chloride was not recalcined and the overall chemical cost was
 always greater than  the lime.

 The long printouts of the lower cost treatment schemes including
 schemes  10,  13, and 21 are presented in Figures  20, 21,  and 22.


 Case 3-50 MOD Primary Plant

 In this case it was assumed that the treatment plant would require
 upgrading  to secondary treatment and that the costs of this upgrading
would  be included in  the phosphorus removal cost.

In this case we evaluated the two options  of either upgrading with a
trickling filter or an activated sludge process.  For  the case  of a
total phosphate ban and 80% government  financing the least cost
 scheme was the addition of alum after a  trickling filter.  This scheme
is shown as number  15 in Table 13.   When no government financing
was available and the phosphate ban was lifted,  the addition of alum
after the aeration basin of an activated sludge  plant became
 equivalent in cost to  the alum-trickling filter scheme.

 When the  effluent  limit was reduced to 0.5 mg / 1,  scheme 17 which is
 the addition of a multi-media filter after alum addition  to the trickling
filter effluent, was the lowest cost scheme. With no  phosphate
                              122

-------
                    Table 12
P
GOVFF
RESTRICT

SCHNO
1
2
3
4
5
6
7
8
9
10
11
12
13
II*
15
ID
17
18
21
               20 MGD ACTIVATED SLUDGE PLANT
             TREATMENT COSTS IN CENTS/1000 GAL.
11.2
 7.9
 8.4
          2
         .8
11.0
 6.1*
 7.U
          2
         .8
        yes
11.1
7.6
16.5
9.8
11.7
8.1
17.1
10.4
8.5
9.9
6.5
13.9
8.6
10.1
6.7
14.2
8.9
8.0
6 . 4
4.8
12.7
9.5
6.7
5.1
12.9
9.7
5.0
6.4
4.4
       0.5
                     13.U
                     11.3
                     16.3
0.5
 .8
                     10.9
                      8.8
                     13.S
0.5
 .?
yes
                     7.0
                     6.0
12.3
15.6
Ut
8.9
10.0
£i±2
6.3
6.6
7.1
NOTES:
1.  P  «  Phosphorus effluent  level  in me,/1 .
2.  GOVFF  =  Fraction of construction cost  financed
            by  federal and state  governments.
5.  RESTRICT  =  Restrictions  on  phosphate  determents.
4.  SCHNO  =  Treatment  scheme number.
5.  	  *  Lowest  treatment cost.
                       123

-------
                                           Figure 20
                                   20 MGD Activated Sludge Plant

                                       CASE   2
           LIQUID TREATMENT SCHEME  =     10
           AMORTIZATION RATE  =0.05  AMORTIZATION LIFETIME =20.0
           FRACTION OF CONSTRUCTION COST FINANCED BY GOVERNMENT
IN)
           PROCESS NAME
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
AERTN BASIN
MECH AERATN
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASN
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
FECL FEEDING
LIME FEEDING
                CONSTRUCTION
               COSTUOOO  $  )
  0,
  0,
  0,
  0,
  0,
  0,
  0,
  0
  0
  0
 38
  0
 98
115
0
n
o
o
o
o
o
o
o
o
16.3
0
759
133
SIZING
PARAMETER
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.51*6
0.0
31*. 950
641*6.578


MGD
MGD
TSF
RPM
TCF
HP
TSF
MGD
#/P
TCF
TSF
TCF
SOFT
#/D
                                  36.171
          251*1.481  */D
AMORT
(10















IZED
00 $
0
0
0
0
0
0
0
0
0
0
3
0
7
9
2
COST
/TP)
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.062
.0
.925
.239
.903
                                                      YEAR PROCESS
                                                      FIRST NEEDED
199
199
199
199
199
199
199
199
199
199
197
199
197
197
U
k
k
i*
I*
i*
l*
k
k
k
k
k
k
k
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
                                                         1971*.0
           TOTALS =
                       288.226
                                          23.128

-------
                                         Figure 20 (cont. )
                                                     PERIODIC  OPERATING COSTS
ro
                       PROCESS NAME
RAW WbTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
AERTN BASIN
MECH AERATN
SECY SETTLER
RECIRC PI-'.PMG
CHLORNE FEED
CHLORNE BASN
GRAV THICKNR
SLGE HLD INK
VACUUM FILTR
FECL FEEDING
LIME FEEDING
                  OPERATING  MAN-HOURS
                   (MAN-HOURS/TP)
                AVE.     MAX.     MIN.
        MA INTAI NANCE  MAN-HOURS
           (MAN-HOURS/TP)
         AVE.    MAX.    MIN.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
1*1.
0.
3013.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
J*l.
0.
3013.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
Ul.
0.
3013.
0.
0.
0.
0.
0.
0.
c.
0.
0.
0.
0.
0.
23.
0.
3T9.
2881*.
2009.
C.
0.
0.
c.
0.
0.
0.
0.
0.
0.
23.
0.
3H9.
288U.
2009.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
23.
0.
359.
2S8U.
2009.
                       TOTALS =
               3055.
3055
3055.
52£i».
52£i*.

-------
                           Figure 20 (cont. )

                     PERIODIC  OPERATING  COSTS
PROCESS NAME
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
AERTN BASIN
MECH AERATN
SECY SETTLER
REG IRC PMPNG
CHLORNE FEED
CHLORNE BASN
GRAV THICKNR
SLGE HLD TNK
VACUUM FLITR
FECL FEEDING
LIME FEEDING
 MATERIAL a SUPPLY
       ( $ /TP)
AVE.        MAX.
            COST
                                            MIN.
LABOR COST
(AVERAGE)
(1000$/TP)
 TOTAL OekM
(1000$/TP)












17
299
9
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
88.
0.
365.
353.
722.
0
0
0
0
0
0
0
0
0
0
kQ
0
26
00
P2
0
0
0
0
0
0
0
0
0
0
88
0
17365
299353
9722
•
•
•
•
•
•
•
*
*
*
*
•
*
•
•
0
0
0
0
0
0
0
0
0
0
uo
0
30
06
£5
0
0
0
0
0
0
0
0
0
0
88
0
17365
299353
9722
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
. **o
.0
.30
.06
.85
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
15.
13.
9.
0
0
0
0
0
0
0
0
0
0
290
0
362*
101
121*
0
0
0
0
0
0
0
0
0
0
0
0
32
312
18
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.378
.0
. 729
.1*53
.8U7
TOTALS
326529.56   326529.56
                                  37.873

-------
Figure 20 (cont. )
           UNIT  COST DATA
        (CENTS/1000 GALLONS)
PROCESS NAME
RAW t'JSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
AERTN BASIN
MECH AERATN
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASN
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
FECL FEEDING
LIME FEEDING
TOTALS -
AMORT
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
a.
0.
IZATI
0
C
r>
C
0
0
u
0
0
0
ou
0
11
13
01*
32
SOL
TIME SINK
PERIOD USED
1 1
2 1
3 1
i* 1
5 1
6 1
7 1
£ 1
9 1
10 1
11 1
12 1
13 1
1U 1
15 1
16 1
17 1
18 1
19 1
20 1
TOTALS =
AN'OU
NT
















in
so
ON
















SI
LI
LABOR
































0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
NKS
n
S
r
. o
. ')
.0
n
la
.0
">
.0
.0
.0
.00
.0
.21
.18
.12
.52
COS
















TS
M

















ATE

















COST
(TONS) («/









































5
255
255
255
255
255
255
255
255
255
255
255
255
255
255
255
255
255
255
255
255
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
3.
1079.
9
9
9
q
9
9
9
9
9
9
9
9
9
9
9
9
3
9
q
9
U
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
7
5









































12
638
638
638
638
638
633
638
658
638
638
638
638
638
638
638
638
638
638
638
638
769
1*9
1*9
!*9
1*9
1*9
1*9
1*9
1*9
1*9
1*9
1*9
1*9
1*9
1*9
1*9
U9
1*9
1*9
1*9
1+9
85
TP)
.36
.36
.35
.36
.36
.36
.36
.36
.36
.36
.36
.36
.36
.36
.36
.36
.3C
.36
.36
.36
.00
                    MATERIAL A SUPPLY   TOTAL

                          0.0
                          o.o
                          o.o
                          o.c            o. --i
                          o.o            n. o
                          u.n            0.0
                          o.o            o. n
                          o.o            r-, c
                          o.o            n. o
                          o.o            o.o
                          0.00           0.05
                          o.o            o.o
                          0 . 2 U           n . 5 C
                          I*. 10           U.i*l
                          0.15           H.30

                          U.U7           5.31
UNIT COSTS FOR SOLID WASTE DISPOSAL  (CENTS/1000   GAL.)
TOTAL UNIT COST (CENTS/1000 GAL) = 6.18
                                     =  D.S7
      127

-------
                                  CASE
                                                Figure 21

                                        20 MGD Activated Sludge Plant
         LIQUID TREATMENT  SCHEME  =    13
         AMORTIZATION RATE  =0.05  AMORTIZATION LIFETIME =20.0
         FRACTION OF CONSTRUCTION COST FINANCED BY GOVERNMENT
                                                       =  .0
00
         PROCESS NAME
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
AERTN BASIN
MECH AERATN
SECY SETTLER
RECIKC PMPNG
CHLORNE FEED
CHLORNE BASH
MUL-MED FLTR
RECIRC PMPNG
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
FECL FEEDING
LIME FEEDING
                CONSTRUCTION
               COSTUOOO  $  )
   0
   0
   0
   0
   0
   0
   0
   0
   0
   0
1C70
 372
  59
  53
 339
 118
  1*2
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.251*
.327
.732
.183
.398
.005
.581
SIZING
PARAMETER
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
o.o
0.0
20.000
38.000
1.712
11.1*50
320.500
GG1G.OG2
32U1.200


MGD
MGD
TSF
GPM
TCF
HP
TSF
MGD
#/D
TCF
MGD
MGD
TSF
TCF
SQFT
#/D
#/D
AMORTIZED COST
  (1000 S /TP)

         0.0
         0.0
         0.0
         0.0
         0.0
         0.0
         0.0
         0.0
         0.0
         0.0
       150.075
        29.877
         £*.703
         U.2G8
        27.234
         9.1*69
         3.1*17
                                                       YEAR PROCESS
                                                       FIRST NEEDED
1991*
1991*
1991*
199U
1991*
1991*
1991*
1991*
1991*
1971*
1971*
197U
1971*
197t*
1971*.0
197U.0
         TOTALS =
                                                              229.153

-------
                                          Figure 21 (cont. )
                                                  PERIODIC OPERATING COSTS
sO
                     PROCESS NAME
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
AERTN BASIN
MECM AERATN
SECY SETTLER
RECIRC PMPNG
CMLORNE FEED
CHLORNE BASN
MUL-MED FLTR
RECIRC PMPNG
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
FECL FEEDING
LIME FEEDING
                  OPERATING  MAN-HOURS
                   (MAN-HOURS/TP)
                AVE.    MAX.    MIN.
MA I NT A I NANCE MAN-HOURS
   (MAN-HOURS/TP)
AVE.
         MAX.
                                                                             MIN.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
3772.
1153.
126.
95.
5927.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
3772.
1153.
126.
95.
5927.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
3772.
1153.
12C.
95.
5927.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
971.
69.
59.
727.
2927.
2107.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
971.
69.
59.
727.
2927.
2107.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
971.
09.
59.
727.
2927.
2107.
                     TOTALS
11072.  11072.  111)72.
                                       CS59.
       6859.
                GS59.

-------
                           Figure 21 (cont. )
                 PERIODIC OPERATING COSTS
PROCESS NAME
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
AERTN BASIN
MECH AERATN
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASN
MUL-MED FLTR
RECIRC PMPNG
GRAV THICKNR
SLGE HLD TNK
VACUUM FLTER
FECL FEEDING
LIME FEEDING
      MATERIAL ft SUPPLY COST
            ( $ /TP)
     AVE.        MAX.
                                            MIN
                       LABOR COST
                       (AVERAGE)
                       (1000$/TP)
                        TOTAL O&M
                       (1000S/TP)










2G3
SO
2
1*
3U2
3072
123
0
0
0
0
0
0
0
0
0
0
87
78
68
02
1U
23
99
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.56
.01
.39
.13
.87
.00
.70
0
0
0
0
0
0
0
0
0
0
20387
8078
268
U02
31+211*
307223
12399
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.59
.03
.39
.13
.87
.06
.75
0
0
0
0
0
0
0
0
0
0
2G387
8078
268
1*02
31*211*
307223
12399
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.59
.03
.39
.13
.87
.00
.75
0
0
0
0
0
0
0
0
0
0
17
9
0
0
30
13
9
.0
.0
.0
.0
.0
.0
.0
.0
.0
.0
.13
.61*
.88
.70
.22
.29
.57










2
U
3
0
9
(*
o
L.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
1*3.
17.
X •
1.
61+.
320.
21.
0
0
0
0
0
0
0
0
0
0
520
722
151
102
1*1*1*
517
972
TOTALS =
33S973.G2
388973.75
388975.75
81.U5I*
1*70.1+27

-------
                  Figure 21 (cont. )

                             UNIT COST DATA
                          (CENTS/1000 GALLONS)

PROCESS NAME   AMORTIZATION   LABOR   MATERIAL & SUPPLY   TOTAL
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
AERTN BASIN
MECH AERATN
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CULORNE BASN
MUL-MED FLTR
RECIRC PMPNG
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
FECL FEEDING
LIME FEEDING
TOTALS =

TIME SINK
PERIOD USED
1 1
2 1
3 1
k 1
5 1
6 1
7 1
£ 1
9 1
10 1
11 1
12 1
13 1
Ik 1
15 1
16 1
17 1
18 1
19 1
20 1
0.0 0.0
0.0 0.0
0.0 0.0
0.0 0.0
0.0 0.0
0.0 0.0
0.0 0.0
0.0 0.0
0.0 U.O
0.0 0.0
2. 06 U.23
Q.kl 0.13
0.07 0.01
O.OG O.C1
0.37 0.1*1
0.13 0.18
0.05 0.13
3.1U 1.12
SOLID SINKS COSTS
AMOUNT SOLIDS COST
(TONS) (S/TP)
5107.95 12769S.G9
5107.95 127698.69
5107.95 12769S.G9
5107.05 127698. C9
5107.95 127G9S.G9
5107.95 127698.69
5107.95 127698.69
5107.35 127698.69
5107.95 127694}. 69
5107.95 127698.69
5107.95 127698. G9
5107.95 127698.69
5107.95 127698.69
5107.95 127698.69
5107.95 127698. GO
5107.95 127G95J.G9
5107.95 127698.69
5107.95 127698.09
5107.95 12769S.69
5107.95 127698.59
  TOTALS -

UNIT COSTS
TOTAL UNIT
                                            0.0
                                            0.0
                                            0.0
                                            0.0
                                            0.0
                                            0.0
                                            0.0
                                            0.0
                                            0.0
                                            0.0
                                            0.36
                                            0.11
                                            0.00
                                            0.01
                                            0.1*7
                                            I*.21
                                            0.17
                                            5.33
         102158.87   2553966.00

FOR SOLID WASTE DISPOSAL (CENTS/1000
COST (CENTS/1000 GAL) -11.33
 0.0
 0.0
 0.0
 0.0
 0.0
 0.0
 0.0
 0.0
 0.0
 0.0
 2.6ii
 0.65
 0.08
 0.07
 1.2G
 U.52
 0.35

 9.58
                                                  GAL.)
1.75
                         131

-------
                                Figure 22.  20 MGD Activated Sludge Plant
                                        CASE  2
          LIQUID TREATMENT SCHEME  =     21
          AMORTIZATION RATE =0.05  AMORTIZATION  LIFETIME  =20  0
          FRACTION OF CONSTRUCTION COST  FINANCED  BY  GOVERNMENT
                                                       = .0
PO
          PROCESS NAME
RAW WSTE  PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE  PMP
AERTN BASIN
MECH AERATN
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASN
MUL-MED FLTR
RECIRC PMPNG
GRAV THICKNR
SLGE HLD  TNK
VACUUM FILTR
RECARBONATN1
TER SETTLER1
FECL FEEDING
LIME FEEDING
C02  FEEDING
RECALCINATN
FLOCC -TRTRY
                 CONSTRUCTION
                COSTC1000  $  )
   0
   0
   0
   0
   0
   0
   0
   0,
   0,
   0,
1870,
 372,
   0,
   0.
   o(
  85.
 374.
   0.
  82.
  27.
 456.
 355.
.0
,0
,0
,0
,0
,0
,0
,0
,0
,0
 254
 327
.0
 0
 0
 288
 382
 0
 873
 699
 965
 555
S 1 7. ! .NG
PARAMETER
0.0
0.0
0.0
0.0
o.n
0.0
0.0
0.0
0.0
0.0
20.000
38.000
0.0
0.0
n.o
55.704
2fc.571
0.0
871*6.1*96
0.190
20.000
20.000


MGD
MGD
TSF
G PM
TCF
HP
TSF
MGD
*/P
TCF
MGD
MGD
TSF
TCF
SQFT
TCF
TSF
#/D
*/D
*/n

MGD
AMORTIZED COST
  (1000 $ /TP)

         0.0
         0.0
         0.0
         0.0
         0.0
         0.0
         0.0
         0.0
         0.0
         0.0
       150.375
        29.377
         0.0
         0.0
         0.0
         6.841*
        30.042
         0.0
         6.650
         2.223
        36.668
        28.531
                                                                                     YEAR PROCESS
                                                                                     FIRST NEEDED
                                                                                        1994
1994
1991*
1994
1994
1994
1994
1994
1994
1974
1974
1994
1994
1994
1974
1974
1994
1974
1974
1974
,0
,0
,0
,0
 0
,0
 0
 3
 0
 0
 0
 0
 0
 0
 0
 0
 0
 0
 0
 0
 0
                                                                                        1974.0
          TOTALS  =
                     3625.344
                                                                       290.909

-------
                     Figure 22 (cont. )
                             PERIODIC  OPERATING  COSTS
PROCESS NAME
RAW WSTE Pf-'P
PRE TRETMENT
PRIM SETTLER
PRKYSLGE PMP
AERTN BASIN
MECH AERATN
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BA3N
MUL-MED FLTR
RECIRC PMPNG
GRAV THICKNR
SLGE HLD TNK
VACUUM FlLTR
RECARBONATN1
TER SETTLER1
FECL FEEDING
LIME FEEDING
C02  FEEDING
RECALCINATN
FLOCC -TRTRY
   OPERATING MAN-HOURS
    (MAN-HOURS/TP)
  AVE.    MAX.    MIN.
MA I NTA I NANCE MAN-MODRS
   (MAN-HOURS/TP)
 AVE.    "AX.    N'IN.
0.
0.
n.
0.
o.
0.
0.
0.
0.
n.
3772.
1153.
0.
0.
0.
0.
1932.
0.
0.
69 8.
8625.
0.
n.
0.
n.
0.
0.
0.
0.
0.
0.
0.
3772.
1153.
0.
0.
-o.
0.
1932.
C.
0.
698.
8625.
0.
n.
0.
n.
0.
0.
0.
0.
0.
0.
0.
3772.
1153.
0.
0.
-0.
0.
1932.
0.
0.
69?.
8G25.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
971.
0.
0.
0.
n.
1072.
coo.
2563.
590.
I* 3 8 0 ,
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
971.
0.
G.
-0.
0.
1072.
600.
2563.
590.
1*380.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
0.
971.
0.
0.
-G.
0.
1072.
600.
25 C 3.
590.
4380.
0.
TOTALS =
16180.  16180.  16180.  10175.  10175.  10175.

-------
                            Figure 22 (cont. )
 PROCESS NAME
 RAW  WSTE  PMP
 PRE  TRETMENT
 PRIM SETTLER
 PRMYSLGE  PMP
 AERTN BASIN
 MECH AERATN
 SECY SETTLER
 RECIRC PMPNG
 CHLORNE FEED
 CHLORNE BASN
 MUL-MED FLTR
 RECIRC PMPNG
 GRAV THICKNR
 SLGE HLD  TNK
 VACUUM FILTR
 RECARBONATN1
 TER  SETTLER1
 FECL FEEDING
 LIME FEEDING
 C02   FEEDING
 RECALCINATN
 FLOCC  -TRTRY
MATER

AVE.
0.0
o.n
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
26587.56
8078.01
0.0
0.0
0.0
0.0
3766.37
0.0
331*61.12
70695.UU
1191*93.12
11604.89
IAL * SUPP
( $ /TP)
MAX.
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
0.0
26387.59
8078.03
0.0
0.0
0.0
0.0
3766.38
0.0
331*61.18
70695. C2
1191*93.37
11601*. 92
                      PERIODIC OPERATING COSTS
                      LY COST       LABOR COST
                                    (AVERAGE)
                              MIN.  (1000$/TP)
                  TOTAL OfiM
                 (1000$/TP)
                              0
                              0
                              0
                              0
                              0
                              0
                              0
                              0
                              0
                              0,
                          26337,
                           8078,
                              0,
                              0,
                              0,
                              0,
                           3766,
                              0,
                          331*61,
                          70695.
                         1191*93,
0
0
0
0
0
0
0
0
0
0
59
03
0
0
0
0
35
0
IS
62
37
 0
 0
 0
 0
 0
 0,
 0.
 0,
 0,
 0,
17,
 9,
 0.
 0,
 0,
 0,
13.
 2.
11.
 5.
59.
0
0
0
0
0
0
0
0
0
0
132
6l*U
0
0
0
0
6U7
725
6UO
81*9
076
  0
  0
  0
  0
  0
  0
  0,
  0,
  0,
  0,
 1*3,
 17,
  0,
  0,
  0,
  0.
 17.
  2.
 U5.
 76,
178,
0
0
0
0
0
0
0
0
0
0
520
722
0
0
0
0
1*11*
725
102
51*5
569
                          llfcOU.92
         0.0
            11.605
TOTALS =
2731*86.50   2731*87.00    273«*87.00
       119.715
           393.201

-------
                     Figure 22 (c o nt.
                             UNIT C^ST  n.ATA
                           ( CENTS/ 10 00  GALLONS)

PROCESS NAME   AMORTIZATION    LABOR    MATERIAL  ft SUPPLY   TOTAL
RAW ','

0
n
23
13
r
v;
ij
n
o
19
nu
1C
OK
11
r\
V,
f*\
o
n
0
•^
L'
Q
n
o

Ci
r
r>
o
1
n
r>
r
0

0
n
n
1
0
.0
.0
.0
n
• tj
.n
n
• I*
» i J
r
• •.
.0
.0
.36
.11
.0
.0
. i)
.0
.05
0
• v
.U6
.97
.fit
.1C
3.99
                     1.6U
                                             3.75
                                                            0.0
                                                            0.0
                                                            o.o
                                                            0 . 0
                                                            o.o
                                                            0.0
                                                            o.o
                                                            n.n
                                                            o.o
                                                            o.o
                                                            2.T5
                                                            O.R5
                                                            ii. 0
o.o
fi.PQ
O.G5
0.04
r.. 71
i.os
2.^5
0.55

Q.37
                    >OLID  SINKS  COSTS
TIME
PERIOD
SINK
USED
  TOTALS =
                 AMOUNT  SOL IDS
                    (TONS)

                          0.0
                   COST
                   (S/TP)

                     0.0
UNIT COSTS FOR SOLID  WASTE  DISPOSAL (CENTS/1000  GAL.)
TOTAL UNIT COST  (CENTS/1000 RAD  = 9.37
                                                    0.0
                           135

-------
detergent limitation,  scheme 21 which is single stage tertiary lime,
became the best choice.

The long printouts in these cases  show the  interesting  relationship
between capital costs, chemical costs, and operation of the plants.
They are  shown in Figures 23,  24, and 25.
                             136

-------
                    Table 13
                    50 MOD PRIMARY PLANT
             TREATMENT COSTS IN CENTS/1000 GAL.

P            2      2      2    0.5    0.5    b.5
GOVFF              .8     .8            . fc      . S
RESTRICT                 yes                  yes

SCHNO
1
2
3
k
5
6
7
8
9
10
11        15.5    12.1     7.6
12                              15.0    11.7     7
13                              13.0     9.7     7
1U                              17.G    1U.G     9
15          8_JL    &&    JL.J.
16          9.1     7.2     U.9
17                              12.1*     S.7
18                              13.G     9.8     6.7
 21                              ifiJL    Ul     7.3
 NOTES:
 1.  P  *  Phosphorus  effluent level  in mr/1 .
 2.  GOVFF  » Fraction  of construction cost  financed
            by federal  and state governments.
 3.  RESTRICT = Restrictions on phosphate deterrents
 U.  SCHNO  » Treatment scheme number.
 b.  	 =  Lov;est treatment cost.
15.0
9.5
lb.2
11.6
13.5
9.9
18.6
12.0
10. G
8^5
10.8
7.5
1U.8
9 . i>
11.0
7.7
1U.9
9.7
9.1
7.1
7. it
5.8
13.5
10. U
7.6
6.0
15.7
10. C
6.2
5.2
                        137

-------
                                 Figure 23.  50 MGD Primary Plant
                                      CASE
            LIQUID TREATMENT SCHEME  =     10
            AMORTIZATION RATE  =0.05  AMORTIZATION LIFETIME =20.0
            FRACTION OF CONSTRUCTION COST FINANCED BY GOVERNMENT
                                                       = .0
OJ
co
            PROCESS NAME
RAW WSTE PMP
PRE TKETMENT
PRIM SETTLER
PRMYSLGE PMP
AERTN BASIN
MECH AERATN
SECY SETTLER
RECIMC PN'PNG
CHLORNE FEEH
CHLORNE BASN
GRAV THICKNR
3LGE HLD INK
VACUUM FILTR
FECL FEEDING
LIME FEEDING

TOTALS =
                CONSTRUCTION
               COSK1000  $  )
0.
0.
0.
0.
167U.
371.
799.
1*65 .
0.
0.
52.
0.
ise.
336.
66.
0
0
0
0
708
'JUfi
331
798
0
0
!*80
n
U32
751
R81

PA




1








16
F,
SIZING
1AMETER
0.0
o.r,
O.G
0.0
F. 7 1 . 1 2 2
69U.16G
71.U2Q
50.GCO
0.0
0.0
1.289
0.0
S7.375
116.UU5
353.695


MGD
f'.CD
TSF
npM
TCF
HP
TSF
MTD
#/n
TCF
TSF
TCF
SOFT
*/p
#/D
AMORTIZED COST
  (1000 $ /TP>
YEAR PROCESS
FIRST NEEDED
                                  3931.329




1




0
0
0
0
5U
30









3
C
3




1
2

1
1*
7
0
0
u
0
2
7
5
5
.C
.0
.y
.0
. 3
.1*
.1




8
0
1*
.37
.0
.0
.2
.0
.5
.0
.3
. ^4


1

5
2
G
6




l*
8
1
7


1

3
2
7
2
                       199(4.
                       199U.
                       199U.
                       199U,
                       197U,
                       1071*.
                       197U,
                       197U.
        0
        0
        0
        0
        0
        0
        0
        0
        0
   199t*.0
   197U.0
   1991*.0
   1971*.0
   1971*.0
   1971*.0

-------
                                         Figure 23 (cont. )
                                                    PERIODIC OPERATING COSTS
OJ
vO
                       PROCESS  NAME
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMY3LGE PMP
AERTN BASIN
MECH AERATN
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASN
GRAV THICKNR
SLGE HLD TNK
VACUUM FlLTR
FECL FEEDING
LIME FEEDING
                  OPERATING  MAN-HOURS
                   (MAN-HOURS/TP)
                 AVE.     MAX.     MIN.
                          MA INTAINANTE MAN-HOURS
                             (MAN-HOURS/TP)
                           AVE.     MAX.     MIN.
0.
0.
0.
0.
0.
51«i*2.
3(481.
0.
0.
0.
73.
0.
6897.
0.
0.
0.
0.
0.
0.
0.
31*1*2.
31*81.
0.
0.
0.
78.
0.
6R97.
0.
0.
0.
0.
0.
0.
0.
3UU2.
31*81.
0.
0.
0.
78.
0.
BF07.
C.
0.
0.
n.
c.
0.
0.
2133.
191*9.
1133.
0.
0.
1*3.
0.
862.
1*996.
2UOf .
0.
0.
0.
0.
0.
2133.
19J*9.
1133.
0.
0.
1*3.
0.
862.
U906.
2i*OG.
0.
0.
0.
0.
0.
2133.
19U9.
1133.
0.
0.
«i3.
0.
fc62.
t»93P.
2i*nc.
                      TOTALS -
1389?.   1389?.  13898.  13522.  13522.
                                                       13522.

-------
                           Figure 23 (cont.
                     PERIODIC  OPERATING COSTS
PROCESS NAME
RAW WSTE  PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE  PMP
AERTN BASIN
MECH AERATN
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASN
GRAV THICKNR
SLGE HLD  TNK
VACUUM FILTR
FECL FEEDING
LIME FEEDING

TOTALS =








113
7
10




39
748
24
9u?
MATER

AVE.
0.0
0.0
0.0
o.o
0.0
I22.no
493. 70
396.82
0.0
0.0
166.03
0.0
537.44
382.00
307.07
4U5.00
IAL ft SUPPLY
( $ /TP)
MAX.
0.3
0.0
0.0
0 . G
0.0
118122.06
7493.71
10396. 24
0.0
0.0
166.05
0.0
39537.49
748382.50
24307.11
948405. 5C
COST

M 1 M .
0.0
0.0
0.0
0.0
0.0
118122.06
7493. 71
10396. 84
0.0
0.0
166.05
0.0
39537.49
748322.50
24307.11
948405.56
                                                   LABOR COST
                                                   (AVERAGE)
                                                   (1000$/TP)
       TOTAL  O&M
      (1000S/TP)
                                                        0
                                                        0
                                                        0
                                                        0
                                                        0.
                                                       25,
                                                       24,
                                                        5,
                                                        0,
                                                        0,
                                                        0.
                                                        0.
                                                       35.
                                                       22,
                                                       10,
,0
,0
 0
 0
 0
 325
 C65
 149
 0
 0
 548
 0
 242
 C96
 930
   0
   0
   0
   0,
   0,
 143,
  32,
  15,
   0,
   0.
   0.
   0.
  74.
 771.
0
0
0
0
0
447
159
54G
0
0
714
0
779
078
                                                      124.555
  35.237

1072.960

-------
                     Figure 23 (cont. )
                             UNIT COST DATA
                          (CENTS/1000 GALLONS)

PROCESS NAME   AMORTIZATION   LABOR   MATERIAL A SUPPLY   TOTAL
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE Pf-'.P
AERTN BASIN
MECH AERATN
oECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASN
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
FECL FEEDING
LIME FEEDING
TOTALS =
TIME SINK A?
PERIOD USED
1 1
2 1
3 1
4 1
5 1
6 1
7 1
8
9
10
11
12
13
14
15
16
17
18
19
20
1
1
1
1
1
1
1
1
1
1
1
1
1
0.0
0.0
0.0
0.0
0.74
0.17
0.35
0.20
0.0
0.0
0.02
0.0
0.07
0.15
0.03
1.73
SOLID
.'.OUNT SO
(TONS)
G38
63S
638
638
638
638
638
63
63
63
63
63
63
a
8
S
8
8
8
638
63
63
63
63
63
8
S
n
c
8
P
u
C38
S
L
k
4
4
4
k
4
4
4
4
4
4
4
4
4
4
4
4
4
4
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
INKS
IDS
.94
.94
.94
.94
.94
'.94
.94
.94
.34
.94
.94
.94
.94
.94
.94
.94
.94
.94
.0
.0
.0
.0
.0
.14
.14
.03
.0
.0
.00
.0
.19
.12
.06
.GS
cos
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
TS
596
596
596
59P
596
59&
596
596
59 6
59 f,
59 f-
596
596
5^6
596
596
596
596
596
596
COST
$/TP)
23.50
23.50
23.50
23.50
23.50
23.50
25.50
2
2
3.
3.
23.
2
3.
23.
2
2
2
2
2
2
2
2
3.
3.
3.
3.
3.
3.
3.
3.
50
50
50
50
50
50
50
50
50
EC
50
50
50
                                            0.0
                                            0.0
                                            0.0
                                            0.0
                                            O.C
                                            0.65
                                            0.04
                                            0.06
                                            0.0
                                            0.0
                                            0.00
                                            0.0
                                            0.22
                                            4.10
                                            0.13

                                            5.20
  TOTALS =

UNIT COSTS
TOTAL UNIT
         127698.75   3132463.DC

FOR SOLID WASTE DISPOSAL (CENTS/1000  HAL )
COST (CENTS/1000 GAL) = 8.48
                                                           0.0
                                                           O.P
                                                           O.Q
                                                           o.o
                                                           0. 74
                                                           0.95
                                                           0.53
                                                           0.29
                                                           0.0
                                                           0.0
                                                           0.03
                                                           0.0
                                                           0.4£
                                                           4.37
                                                           0.22

                                                           7.61
                                                          0.87
                          141

-------
                             Figure 24.  50 MGD Primary Plant
                            CASE   3
LIQUID TREATMENT  SCHEME  =    lb
AMORTIZATION  RATE  =0.05  AMORTIZATION LIFETIME =20.0
FRACTION OF CONSTRUCTION COST FINANCED BY GOVERNMENT
                                          .0
PROCESS NAME
RAW WSTE PKP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
TRKLNG FILTR
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASN
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
ALUM FEEDING
FECL FEEDING
LIME FEEDING
 CONSTRUCTION
COSTdOOO $ )
        0
        0
        0
        0
     3659
      799
      652
        0
        0
        0
        0
        0
      287
       1*5
       7k
.0
.0
.0
.0
.099
.531
.002
.0
.0
.0
.0
.0
.187
.525
.509
S 1 Z 1 NG
PARAMETER
0.0
0.0
0.0
0.0
2613.600
71.1*29
75.000
0.0
0.0
0.0
0.0
0.0
621*7.1*92
6U5.Rl*fi


MGD
MGD
TSF
GPM
TCF
TSF
MGD
#/D
TCF
TSF
TCF
SOFT
#/D
#/D
7U63.672
AMORTIZED COST
  (1000 $ /TP)

         0.0
         0.0
         0.0
         0.0
       293.618
        61*.11*1
        52.319
         0.0
         0.0
         o.o
         0.0
         0.0
        23.0U5
         3.653
         5.979
                                                                           YEAR PROCESS
                                                                           FIRST NEEDED
199U
1991*
1991*
199U
197U
1971*
1971*
199U,
199U,
1991*,
199U,
199U,
1971*,
1971*.
197U.
0
0
0
0
0
0
0
0
0
0
G
0
0
0
0
TOTALS
      5517.6U1

-------
                                         Figure 24 (cont. )
                                                   PERIODIC OPERATING COSTS
to
                      PROCESS  NAME
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
TRKLNG FlLTR
SECY SETTLER
RECIRC Pf.PNG
CHLORNE FEED
CHLORNE BASN
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
ALUM FEEDING
FECL FEEDING
LIME FEEDING
                  OPERATING  MAM-HOURS
                   (MAN-HOURS/TP)
                 AVE.     MAX.     MIN.
MA INTAI NANCE MAN-HOURS
   (MAN-HOURS/TP)
 AVE.    MAX.    MIN.
0.
0.
0.
0.
3295.
31*81.
0.
0.
0.
0.
0.
1*528.
0.
0.
0.
0.
0.
0.
0.
5295.
31*81.
0.
0.
0.
0.
0.
1*528.
0.
0.
0.
0.
0.
0.
0.
3295.
31*81.
0.
0.
0.
0.
0.
1*528.
0.
0.
0.
0.
0.
0.
0.
183C.
191*9.
U5G.
0.
0.
0.
0.
562.
52UG.
969.
21*8*4.
0.
0.
0.
0.
1830.
191*9.
11*56.
0.
0.
0.
0.
5f:2.
52Ufi.
969.
21*81*.
0.
0.
0.
0.
1830.
191*9.
ll*5G.
0.
0.
0.
0.
562.
521*6.
9G9.
2t*8U.
                     TOTALS -
              11303.  11303.   11303.   IkkSS.   11*1*95.   1UI*95.

-------
                           Figure 24 (cont. )
                                     PERIODIC OPERATING  COSTS
 PROCESS  NAME
RAW WSTE  PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE  PMP
TRICING FILTR
SECY SETTLER
RECIRC FEED
CHLORNE FEED
CHLORNE BASN
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
ALUM FEEDING
FECL FEEDING
LIME FEEDING
      MATERIAL * SUPPLY COST
            ( $ /TP)
     AVE.        MAX.
                                            MIN.
LABOR COST
(AVERAGE)
(1000$/TP)
                                                               TOTAL O&M
                                                              (1000$/TP)
0.0
0.0
o.n
0.0
2919.70
7U93.70
10396. S2
0.0
0.0
0.0
0.0
23292.32
788727.00
29381.19
28553.50
0.0
0.0
0.0
0.0
2919.70
7U93.71
10396.SU
O.C
0.0
0.0
0.0
23292.36
738727.56
299F.1.20
28553.52
0.0
0.0
0.0
0.0
2919.70
7U93.71
10396. 8U
0.0
0.0
0.0
0.0
25292.36
788727.56
29981.20
28553.52
0.0
0.0
0.0
0.0
23.279
2k. 665
6.611*
0.0
0.0
0.0
0.0
23.118
23.829
lt.U02
11.282
0. 0
0.0
0.0
0.0
26.199
32.159
17.010
0.0
0.0
0.0
0.0
U6.I+10
812.556
3i+. 383
39.c36
TOTALS =
S0136U.19   89136U.81   89136U.81
   117.188
1008.552

-------
                    Figure 24 (cont. )
                             UNIT POST DATA
                          (CENTS/1000 GALLO'JS)

PROCESS NAME   AMORTIZATION   LABOR   MATERIAI ft SUPPLY    TOTAL
RAW rt'STE PMP
PRE TRETMENT
PRIM SETTLER
PRI-1YSLGE PMP
TRKLNG FILTR
SECY SETTLER
RECIRC PMPNG
CHLORME FEED
CHLORNE BASN
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
ALUM FEEDING
FECL FEEDING
Lli".E FEEDING
TOTALS =

TIME SINK
PERIOD USED
1 1
2 1
3 1
I* 1
5 1
6 1
7 1
8 1
9 1
11) 1
11 1
12 1
13 1
14 1
15 1
16 1
17 1
18 1
19 1
20 1
O.C
0.0
0.0
O.C
1.G1
0.35
0.29
0.0
0.0
0.0
0.0
0.0
0.13
0.02
0.03
2.U3
SOLID SINKS
AK.OUNT SOLIDS
(TONS)
U10U. 61
1*101*. 61
1*101*. 61
t*io«*. r>i
1*101*. 61
UOi*. 61
1*101*. F>1
1*101*. 61
1*101*. 61
1*101*. 61
i*ini*.6i
1*101*. 61
1*10 I*. Cl
1*101*. 61
l*10U. 61
l*10U. 61
U10U. 61
UlOl*. 61
UIQU. 61
1*101*. 61
0.0
0.0
0.0
0.0
0.13
0.1U
0.01*
0.0
u.o
0.0
o.n
0.13
0.13
O.R2
0.06
0.61*
CO?TS
COST
($/TP)
102615.12
102615.12
102615.12
102615.12
102615.12
102615.12
102615.12
102615.12
102615.12
102615.12
102515.12
102615.12
102C15.12
102615.12
102615.12
102615.12
102615.12
102615.12
102615.12
102615.12
   TOTALS
                     82091.9U   2052301.00
                                            0.0
                                            0.0
                                            0.0
                                            0.0
                                            0.02
                                            o.ou
                                            O.QC
                                            0.0
                                            O.C
                                            O.C
                                            0.0
                                            0.13
                                            I*. 32
                                            0.16
                                            0.16

                                            U.C8
0.0
0.0
o.n
n.o
1.7!
0,
0,
n,
o,
n
o
o
                                                             53
                                                             38
                                                             0
                                                             0
                                                             0
                                                             0
                                                             25
                                                             58
                                                             21
                                                             25
                                                           7.35
UNIT COSTS FOR SOLID WASTE DISPOSAL  (CENTS/1000   GAL.)
TOTAL UNIT COST (CENTS/1000 GAL) = 8.51
                                                           0.56
                            145

-------
                          Figure 25.  50 MGD Primary- Plant
                      CASE  3

LIQUID TREATMENT SCHEME =     21
AMORTIZATION RATE =0.05 AMORTIZATION  LIFETIME  =20.0
FRACTION OF CONSTRUCTION  COST  FINANCED  BY  GOVERNMENT
                                          .0
PROCESS NAME
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
AERTN BASIN
MECH AERATN
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASN
MUL-MED FLTR
RECIRC PMPNG
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
RECARBONATN1
TER SETTLER1
FECL FEEDING
LIME FEEDING
C02  FEEDING
RECALCINATN
FLOCC -TRTRY

TOTALS =
 CONSTRUCTION
COSTdOOO $ )
0.
0.
0.
0.
1674.
378.
799.
465.
0.
0.
4115.
759.
0.
0.
0.
173.
799.
0.
153.
45 .
522.
595.
0
0
0
0
70S
94P,
331
798
0
0
578
593
0
0
0
254
331
0
233
65F
194
094
SIZING
PARAMETER
0.0
0. 0
0.0
0.0
1671.122
694. 166
71.429
50.000
0.0
0.0
50.000
90.000
0.0
0.0
0.0
139.260
71.429
0.0
2186C.230
0.474
50.000
50.000


MGD
MOP
TSF
fiPM
TCP
HP
TSF
MGD
#/n
TCF
MGD
MGD
TSF
TCF
SQFT
TCF
TSF
*/D
#/D
*/D

MGD
                                                       AMORTIZED COST
                                                         (1000 $ /TP)
YEAR PROCESS
FIRST N'F.EDED
                    10482.703
0
0
0
0
134
30
64
37
0
0
330
60
0
0
0
13
64
0
12
3
41
47
Ski
.0
.0
.0
.0
.384
.408
.141
.377
.0
.0
.247
.952
.0
.0
.0
.902
.141
.0
.296
.604
.903
.752
.16E
                                                                              1094,
                                                                              1994,
                                                                              1994,
                                                                              1994,
                                                                              1974,
                                                                              1974,
                                                                              1974,
                                                                              1974,
                                                                              1994,
                                                                              1994,
                                                                              1974,
                                                                              1974,
                                                                              1994,
                                                                              1994,
                                                                              1994,
                                                                              1974,
                                                                              1974,
                                                                              1994,
                                                                              1974,
                                                                              1974,
                                                                              1974.0
                                                                              1974.0
                                                                    0
                                                                    0
                                                                    0
                                                                    0
                                                                    0
                                                                    0
                                                                    0
                                                                    0
                                                                    0
                                                                    0
                                                                    0
                                                                    0
                                                                    0
                                                                    0
                                                                    0
                                                                    0
                                                                    0
                                                                    0
                                                                    0
                                                                    0

-------
 PROCESS  NAME
 RAW WSTE  PMP
 PRE TRETMENT
 PRIM  SETTLER
 PRMYSLGE  PMP
 AERTN BASIN
 MECH AERATN
 SECY SETTLER
 RECIRC PMPNG
 CHLORNE FEED
 CHLORNE BASN
 MUL-MED FLTR
 RECIRC PMPNG
 GRAV THICKNR
 SLGE HLD TNK
 VACUUM FILTR
 RECARBONATN1
TER SETTLER1
 FECL FEEDING
 LIME FEEDING
C02  FEEDING
RECALCINATN
 FLOCC  -TRTRY
        Figure 25 (cont.)
                PERIODIC

   OPERATING MAN-HOURS
     (MAN-HOURS/TP)
  AVE.    MAX.    MIN.
OPERATING COSTS

 MA INTAI NANCE MAN-HOURS
    (MAN-HOURS/TP)
  AVE.    MAX.    MIN.
0.
0.
0.
0.
0.
31*1*2.
31*81.
0.
0.
0.
6U58.
2211.
0.
0.
0.
0.
31*81.
0.
0.
808.
12106.
0.
0.
0.
0.
0.
0.
31*2*2.
31*81.
0.
0.
0.
6U58.
2211.
0.
0.
-0.
0.
31*81.
0.
0.
808.
12106.
0.
0.
0.
0.
0.
0.
31*1*2.
31*81.
0.
0.
0.
61*58.
2211.
0.
0.
-o.
0.
31*81.
0.
0.
808.
12106.
0.
0.
0.
0.
0.
0.
2133.
19U9.
1133.
0.
0.
0.
16U3.
C.
0.
0.
0.
191*9.
600.
3070.
1*31.
10950.
0.
0.
0.
0.
0.
0.
2133.
191*9.
1133.
0.
0.
0.
161*3.
0.
0.
-0.
0.
191*9.
fiOO.
5070.
1*31.
10950.
0.
0.
0.
0.
0.
0.
2133.
19U9.
1133.
0.
0.
0.
16U3.
0.
0.
-0.
0.
19U9.
600.
3070.
1+31.
10950.
0.
TOTALS
319&7.   31987.  319E7.  2385E.  23S58.  2385S.

-------
                                          Figure 25 (cont. )

                                              PERIODIC OPERATING COSTS
00
               PROCESS NAME
 RAW WSTE  PMP
 PRE TRETMENT
 PRIM SETTLER
 PRMYSLGE  PMP
 AERTN  BASIN
 MECH AERATN
 SECY SETTLER
 RECIRC PMPNG
 CHLORNE FEED
 CHLORNE BASN
 MUL-MED FLTR
 RECIRC PMPNG
 GRAV THICKNR
 SLGE HLD TNK
 VACUUM FILTR
 RECARBONATN1
TER SETTLER1
 FECL FEEDING
 LIME FEEDING
C02  FEEDING
 RECALCINATN
FLOCC -TRTRY
MATER

AVE.
0.0
0.0
0.0
0.0
o.o
116122.00
7U93. 70
10396.82
0.0
0.0
58605.25
10396.82
0 . 0
0.0
0.0
0.0
7U93.70
0.0
83652.50
141*110.25
282007.00
23624.37
IAL & SUPPLY
( $ /TP)
MAX.
0.0
0.0
0.0
0.0
0.0
118122.06
7493.71
10396.81*
0.0
0.0
58605.35
10396.81*
0.0
0.0
0.0
0.0
7493.71
0.0
83652.81
141*110.69
282007.12
23024.1*1
COST

MIN.
0.0
0.0
0.0
0.0
0.0
118122.06
71*93. 71
10396. 81*
0.0
0.0
58605.35
10396.8U
0.0
0.0
0.0
0.0
71*95.71
0. 0
83652.81
11*1*110.69
282007.12
23621*. 1*1
LABOR COST
(AVERAGE)
(1000S/TP)

     0.0
     0. 0
     0.0
     0.0
     0.0
    25.525
    21*.665
     5.1!*9
     0. 0
     0.0
    29.335
    17.506
     0.0
     0.0
     0.0
     0.0
    21*.665
     2.725

     5.626
   101*. 732
     0.0
                                                                               TOTAL  O&M
                                                                              (1000$/TP)
   0,
   0,
   0,
   0,
   0,
11*3,
 52,
 15,
   0.
   0,
 87,
 27.
   0.
   0.
   0.
   0.
 52,
   2,
 97.
1U9.
386.
0
0
0
0
0
1*1*7
159
546
0
0
91*0
903
0
0
0
0
159
725
537
736
739
                                                                                 23.621*
              TOTALS -
                             745902.37
                           745903.37   71*5903.37
   253.672
999.571*

-------
                    Figure 25 (cont. )
                             UNIT COST DATA
                          (CENTS/1000 GALLONS)

PROCESS NAME   AMORTIZATION   LABOR   MATERIAL & SUPPLY   TOTAL
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
AERTN BASIN
,MECH AERATN
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASN
MUL-MED FLTR
RECIRC PMPNG
GRAV THICKNR
SLGE HLD INK
VACUUM FILTR
RECARBONATN1
TER SETTLER1
FECL FEEDING
LIME FEEDING
C02  FEEDING
RECALCINATN
FLOCC -TRTRY

TOTALS =
         0.0
         0.0
         0.0
         0.0
         0.71*
         0.17
         0.35
         0.20
         O.C
         0.0
         1.81
         0.33
         0.0
         0.0
         0.0
         0.08
         0.35
         0.0
         0.07
         C.02
         0.23
         0.26

         i*.Gl
              0.0
              0.0
              0.0
              0.0
              0.0
              O.ll*
              Q.Ik
              0.03
              0.0
              0.0
              0.16
              0.10
              0.0
              0.0
              0.0
              0.0
              O.li*
              0.01
              0.08
              0.03
              0.57
              O.C

              1.39
0.0
0.0
o.o
0.0
0.0
0.65
0.04
0.06
0.0
o.n
0.32
0.05
0.0
0.0
0.0
o.n
0.01*
0.0
O.U6
0.79
1.55
0.13

(4.09
0.0
0.0
0.0
0.0
Q.7k
0.95
0.53
0.29
0.0
0.0
2.29
O.U9
0.0
0.0
o.n
o.os
0.53
a.ni
o.ro
n.8U
2.35
n.39
TIME
PERIOD
SI NK
USED
  TOTALS =
   SOL IP SINKS COSTS

AMOUNT SOL I OS        COST
   (TONS)           ($/TP)

         o.o          o.n
UNIT COSTS FOR SOLID WASTE DISPOSAL (CENTS/10flO  GAL.)
TOTAL UNIT COST (CENTS/1000 GAL) =10.00
                                                  0 . 0
                         149

-------
                                          TABLE 14
NO.
  1
  2
  3
  4
  5
  6
  7
  8
  9
 10
 11
 12
 13
 14
 15
 16
 17
 18
 19
 20
 21
22
23
SYMBOL
 ALPYPS
 FCRYPS
 FCLMP
 LIME PS
 ALPYFB
 FCPYFB
 FCLMFB
 LIMEFB
 ALUMAB
 FECLAB
 NAALAB
 ALABMF
 FCABMF
 NAABMF
 ALUMTF
 FECLTF
 AKTFMF
 FCTFMF
 ALFBAS
 FCFBAS
 LIFBAS
 L2FBAS
NONE
                                    TREATMENT SCHEMES
            SCHEMES
                                                                   APPENDIX A
                                                                       OPTION
                                                                     DIAGRAM
                                                                          EFFLUENT
                                                                         PHOSPHORUS
                                                                             (mg/L)
 Alum & Polymer to Primary Settler
 Ferric Chloride &  Polymer to Primary Settler
 Ferrous  Chloride & Lime to Primary Settler
 Lime to  Primary Settler
 Alum & Polymer to Flocculation Basin
 Ferric Chloride &  Polymer to Flocc.  Basin
 Ferrous  Chloride & Lime to Flocc.  Basin
 Lime to  the Flocculation Basin
 Alum to  the Aeration Basin
 Ferric Chloride to Aeration Basin
 Sodium Aluminate to Aeration Basin
 Alum to Aer.  Basin &  Multi-Media Filtration
 Ferric Chloride to Aer. Basin & Multi-MediaFil.
 Sodium Aluminate to Aer. Basin & Mul-Med Fil.
 Alum After Trickling Filter
 Ferric Chloride After Trickling Filter
 Alum After Trickling Filter & Multi-Med Filtr.
 Ferric Chloride After Trk.  Fil. & Mul-Med Fil.
 Alum to Flocc. After Conventional Secondary
 Fecl3 to  Flocc. After Conventional Secondary
 Lime(l-Stage) to Flocc After Conven. Secondary
 Lime(2-Stage) to Flocc  After Conven.  Secondary
No Chemicals Added for Phosphorus Removal
1
1
1
1
2
2
2
2
3
3
3
5-A
5-A
5-A
4
4
5-B
5-B
7
7
6-A
6-B
2
2
2
2
2
2
2
2
2
2
2
0. 5
0. 5
0. 5
2
2
0. 5
0. 5
0. 3
0. 3
0. 5
0. 1

-------
                       SECTION VIII

       OPERATING MANUAL FOR  THE PHOSPHORUS
            REMOVAL COST MODEL (REMOVE)
General

This manual describes how REMOVE functions and explains how to
interpret the results provided.  The manual should be used in con-
junction  with the descriptive data provided in the other sections of this
report.  REMOVE is an interactive program which means that it is
designed to 'hold a conversation with the user'.   The program will ask
questions of the user and perform certain operations based on the
responses.  The program asks the user to describe his/her community
and treatment plant.   It then inquires about the control strategy the
user wishes to evaluate in achieving phosphorus removal. The program
then chooses all the various treatment schemes which are to be con-
sidered  in a particular strategy and starts calculating costs for the
first one.  Certain errors are detected if input data is  outside the
range  of the cost functions  in the model and,  if they are,  error messa-
ges are  printed during the cost computations.  (See ERRORS section for
further explanation. )  The user is then asked what type of printout is
desired  and the printout begins.  Following the printout,  the next treat-
ment scheme from the list  of eligible schemes is considered and its
costs are printed out.  This is done for each eligible treatment scheme.
Control  then returns to the strategy design portion of REMOVE.  The
user may then evaluate additional strategies.   Detailed explanations of
the questioning and printout follow.


Questioning Procedure

Every variable, whose value is to be set  by the user, is  input in the
following manner:  (NOTE:  In demonstrating computer/user interaction
all computer responses are underscored. )

VNAME = C/R

Where VNAME is the name of the variable and C/R is  a  carriage
return.  The user then may type: q, a, m, or a valid input value,
followed by a C/R.

q - tells the program that the user did not understand what is wanted
and results in the long form of the question being printed.  Sometimes,
following the long form,  certain keywords, enclosed in parentheses,
will be printed. These keywords further clarify what type of value is
expected by the program and are explained in the KEYWORDS section.
                              151

-------
a - tells the program to set the variable to the assumed value.  The
assumed values are given in the 'VARIABLES section and  represent the
'best known value' at the time the program was last updated.

m - tells the program that the user discovered a mistake  in a pre-
viously input variable and desires to return to the beginning of this
block of variables.  (WARNING - be careful about using this as it can
result in a lot of repeat typing. ) If return is not as far back as desired
then the program must be restarted from the beginning.

valid input value - results in the variable being set to that value.
(WARNING  - due to IBM limitations on word length, no more than 8
characters  are accepted. )  (WARNING - there are no checks on the
reasonableness  of the input values,  i.e., a number may be ridicul-
ously large  or small and will be accepted as valid. )

non-valid input value - results in the question being repeated.

Below is an example of a sample question period.

       ELECOS=
       q                     (Long form of question is desired)
       ELECTRICITY COST ($/KWHR)
       a                     (Assumed value is input)
       q
       DIRECT HOURLY LABOR RATE ($/HR)
       ew3                  (Non-valid response,  question is
                             repeated)
       DHR =
       4. 05                  (User inputs Labor Rate other than
                             assumed)
       IDFRAC =

The questioning procedure for the variables describing the treatment
plant is slightly different than above.  The treatment  plant consists of
a number of processes about which the user can input two pieces of
information;  the present size (PPARM) and the present loading rate
(or design  variable, PVAR).  So, for the treatment plant, the program
will print the treatment process  name and ask that PPARM and PVAR
be input.  A list of the processes and the present size (PPARM) and
design variable (PVAR) parameters is presented later in this  section.


PRINTOUT

There are  three (3) types of printout available for each treatment
scheme.  They are known as SUPERSHORT, SHORT,  and LONG.
The program will ask the user if he/she desires a short printout.
                             152

-------
If the answer is 'yes1, then the program will ask if a  supershort print-
out is desired.   Printing then begins.   Following the printout for all
eligible schemes,  the user  is asked if he/she desires to select up to
five (5) schemes for the LONG printout.  The most advantageous use
can be made of this feature by first printing all  schemes under the
SUPERSHORT  option and  then selecting a few for detailed examination.
A  complete description and example of each type of printout follow
below.

SUPERSHORT  -
        The output consists  of two lines:
        LIQUID TREATMENT SCHEME = schno
        TOTAL UNIT COST (CENTS/1000 GAL)  = xx. xx
        Where,  schno = number of the treatment scheme,
                       see SCHEME section for further
                       explanation,
               xx. xx = total  unit cost

LONG -
        The output consists of:
        1.   Treatment scheme number.
        2.   Miscellaneous
            a.   Amortization Rate and Lifetime for all equipment
            to  be built.
            b.   Per cent of construction cost financed by federal
            government.
            c.   BODS and  suspended solids  removal in the primary.
        3.   Construction information for each process in the treat-
        ment plant:
            a.   process  name,
            b.   construction cost in $1000,
            c.   sizing parameter, i. e. , the amount to be built,
            d.   amortized cost  in $1000 per time period,
            e.   the year in which the additional equipment to be
            built will be  first needed,
            f.   total for construction cost and  amortized cost.
        4.   Periodic Operating  Costs for each process:
            a.  process name,
            b.  operating  man-hours, average, maximum, minimum.
            The max & min are useful when sewered population is
            growing to get an idea of just how much costs will in-
             crease  as  time goes on. ,
             c.  maintainance man-hours,
             d.  material & supply costs in $ per time period,
             e.  average labor cost computed from the average
             operating &  maintainance man-hours, and the  direct fe
             indirect labor  rates,
             f.   total O & M cost which is the sum of the average
             labor cost and material & supply cost,
             g.  total for each of the  above.
                              153

-------
       5.   Unit Cost Data in CENTS/1000 GALLONS for each
       process:
            a.   amortization,
            b.   labor,
            c.   material fc supply,
            d.   total of a. , b. ,  and c.  for each process,
            e.   column totals of a. , b. , c. , and d.
       6.   Cost of Substitutes  of Phosphate Detergents:
            a.   average,  maximum,  and minimum cost in $ per
            time period,
            b.   average unit cost in cents/1000 gal.
       7.   Solid Sink Costs for each time period:
            a.   time period,
            b.   number of the sink used for that time period,
            NOTE:  If sink number  - 99, then all the sinks have
            been used up and the waste is being dumped in  the
            backyard.  See also ERRORS section.,
            c.   amount of solids sent to the sink,
            d.   cost in $ per time period,
            e.   totals for amount of solids and cost,
            f.   average unit cost in cents/1000 gal.

SHORT -
       The output consists of the titles and column totals from the
       LONG printout.

KEYWORDS

FLOAT - a floating  point number is desired, i. e. ,  a number -with a
decimal point.   For example,  5.7,  35.26, 23., .02.  If no decimal
point is input,  then the number input will be converted to floating
point,  e. g. , 38 will become 38.

FIXED - an integer  is expected, i. e. ,  no decimal point.  If a decimal
point is typed the number  will be considered invalid and the question
will  be repeated.

FRACTION - a  decimal fraction is  expected, e. g. , . 52, .  02.  A num-
ber greater than one will not be trapped and most probably will result
in invalid results.  FRACTION is used most often to signify that a
fraction is desired and not a percentage.   For example, activated
sludge density  is usually expressed as  a percent, i.e., 5%,  this means
that  the program would expect 5% to be input as . 05.

others - other  keywords usually indicate the dimensions of the vari-
ables.   For example:

       $/CAP/YR -  Dollars  per capita per year (This type of operation
                     is always equivalent in the report to $/CAP« YR)
       MG/L - Milligrams per  liter
                              154

-------
VARIABLES

This section contains a list of all the variables whose values may be
input by the user.  They are listed alphabetically within each group
consisting of variables common to an input subroutine.  The variable
name,  a  description, dimensions, and assumed value are given for
each variable.  Test methods for variables requiring measurement
are referenced to Standard Methods, 13th Edition.

NOTE;  If a variable deals with a treatment process  which is not to be
considered, then the assumed value may be used safely.

***** Subroutine CMMNTY

CNSTRC
The WQO-STP Construction Cost Index
Dimensions = Index  divided by 100.
Assumed Value = 1. 714 for MAY 72

DHR
Direct hourly labor  rate.  Average  labor rate for personnel working
at the treatment plant including supervisory personnel.
Dimensions = $/Hour
Assumed Value = 3.95 for MAY 72 (S.I. C. 494-497)

ELECOS
Delivered cost of electrical power
Dimensions = $/KWHR
Assumed Value = .01

FNCTYP
A number representing the type of sewered population growth function
desired.
Dimensions = none
Assumed Value =  1
Allowable input =  1  (linear growth rate  of 5%)
                  2  (linear growth rate  calculated  from
                    present pop. and one future  pop. )
                  3  (exponential growth rate  calculated from
                    present pop. and one future  pop. )
                  4 (piece-wise linear growth function rate
                    from present pop.  and up to four future
                    pop.  values)

GOVFF
 Fraction of construction cost that will be financed by the federal and
 state governments.
 Dimensions  = none
 Assumed Value = 0.
                              155

-------
IDFRAC
Indirect labor fraction.   Indirect labor costs include those labor
related costs paid by the utility other than salaries,  wages and other
direct compensation.  Examples  of indirect labor costs include social
security; contributions to pension,  retirement,  or welfare funds; and
premiums paid  on hospitalization, health,  life,  and workmen's com-
pensation insurance.  The costs are specified as a fraction of the base
wage and generally  average about 15%.
Dimensions - none
Assumed Value  = . 15 (i. e. 15%)

MATRLS
Wholesale Price Index for Industrial Commodities
Dimensions = Index divided by 100.
Assumed Value  = 1. 176  for MAY 72

SOLSNK(CAP)
Capacity of solid waste sink.  Capacity should be  given in terms of the
estimated tons a solid waste disposal area will  take before it is filled
to capacity.  It  can  be estimated  by determining how many years  of
useful life are left times the annual tonnage of sludge material trucked
to the site.
Dimensions = Tons
Assumed Value  = large (i.e.  10  billion)
Special Input - 99-  will cause the subroutine to  end input for solid sinks,
Note:  Up to fifteen  (15)  solid sinks may be input.

SOLSNK(DIST)
Distance to solid sink (solid waste disposal site)
Dimensions = Miles
Assumed Value  = 0. (which results in  zero cost)

SPOPIN(SPOP)
The  size of the  sewered population.  This number  is usually given in
survey or engineering reports generated by regional planning agencies
and represents the  present population  served by sewers feeding the
treatment plant.
Dimensions - Capita
Assumed Value  = none
Note:  This is input  after FNCTYP and up to five (5)  population values
may be input.
Note:  The first SPOPIN input must be the  present population and year.

SPOPIN(YEAR)
The  year corresponding to the sewered population  of SPOPIN(SPOP).
This number is  the  year of the present sewered population estimate
and must be entered.  It forms the base for the FNCTYP growth
functions.
                             156

-------
Dimensions = Year (e. g.  1980. )
Assumed Value = none
Special input - 0. will cause the  subroutine to proceed to the nrxt
variable.   This is used to input less  than 5 values for a piece-vise lim. .r
growth function,  [corresponding SPOPIN(SPOP)  must be set to /.erol

TRNCST
Transportation costs for  solid wastes
Dimensions = $/Ton-Mile
Assumed Value = 5.

*****  Subroutine SEWAGE

ALKIPS
Alkalinity  into the primary settler (Standard Methods, 102)
Dimensions = Milligrams/Liter
Assumed Value - Z01.

ASD
Activated  sludge  density.  Ratio of weight of dry  sludge  to weight of
wet sludge.  Test method 224G,  (Total Residue).
Dimensions = none (Note: 5% is input as .05)
Assumed Value = . 01

BODIPS
BODS  into the primary settler (Standard Methods,  219)
Dimensions = Milligrams/Liter
Assumed Value = 200.

FLOTUD
Air flotation sludge thickener underflow density (Standard Methods,
224G)
Dimensions = none (Note: 5% is input as . 05)
Assumed Value = .05

GRAVUD
Gravity sludge thickener underflow density (Standard Methods, 224G)
Dimensions  = none (Note; 5% is input as  . 05)
Assumed Value = . 08

HPDFT
Maximum allowable  operating hours per day for  the air flotation
thickener. This number is  set  by the  superintendent of the treatment
plant  and  represents the time available for an operator  to run the process
or the maximum time per day the  superintendent is willing to run the
equipment in view  of maintenance  considerations.  For  instance, the
assumed value of 8 hrs/day is based on a one shift operation.  To raise
this number would either involve an additional shift or possibly over-
time hours.
Dimensions  = Hours/Day
Assumed Value = 8.
                              157

-------
 HPDVF
 Maximum allowable operating hours per day for vacuum filter (see
 above)
 Dimensions = Hours/Day
 Assumed Value =  8.

 MLSSAR
 Mixed liquor suspended  solids in the aeration process (Test method
 224C,  Total Suspended Matter)
 Dimensions - Milligrams/Liter
 Assumed Value =  2000.

 NH31AR
 NH3 concentration into the aeration process (Standard Methods,  212)
 Dimensions = Milligrams/Liter
 Assumed Value =  0.

 PINPS
 Phosphorus concentration into the primary settler (Total Phosphorus -
 Standard Methods, 223C)
 Dimensions = Milligrams/Liter
 Assumed Value =  10.

 PSETUD
 Primary settler underflow sludge density (Standard Methods, 224G)
 Dimensions = none (Note: 5% in input as . 05)
 Assumed Value =  .05

 PSRMVE
 Fraction of suspended solids removed in primary settler.  This is the
 ratio of suspended solids in the  effluent from the primary settler to the
 suspended solids in the influent.
 Dimensions = none
 Assumed Value =  . 5

 QAVE
 Average daily flow
 Dimensions =  Million Gallons/Day
 Assumed Value =  10.

 QPEAK
 Peak diurnal flow
 Dimensions = Million Gallons/Day
 Assumed Value =  19.

 SSINPS
 Suspended solids into the primary settler (Standard Methods, 224C)
 Dimensions = Milligrams/Liter
Assumed  Value =  200.
                            158

-------
TBODAR
Total change in BODS across aeration process
(i.e.,  the fraction removed)
Dimensions = none
Assumed Value = . 85

VFPSLG
Volatile fraction of primary sludge (Standard Methods,  224G Volatile
Residue)
Dimensions = none
Assumed Value = . 78

VSANRM
Volatile sludge fraction remaining after anaerobic digestion (Standard
Methods,  224G Volatile Residue)
Dimensions = none
Assumed Value = . 5

VSARM
Volatile sludge fraction remaining after aerobic digestion (Standard
Methods,  224G Volatile Residue)
Dimensions = none
Assumed Value = . 5

*****  Subroutine PLANT

AMRATE
Amortization rate for all equipment to be built
Dimensions - none
Assumed Value = . 05 (i. e. , 5%)

AMLIFE
Amortization lifetime for all equipment to be built
Dimensions = years
Assumed Value = 20.

The following variables describe  the equipment (processes) comprising
the treatment plant.  For each process there are two variables which
describe it.

PPARM
The present independent sizing parameter
Dimensions =  see below for a particular process
Assumed Value = 0.
Special Input - 99.  indicates the end of process description data and
execution proceeds to the next subroutine.
              - -1.   indicates that the plant is to have this process but
its present size is set to zero.
                              159

-------
PVAR
The present design variable
Dimensions  = see below for a particular process
Assumed Value =  see below for a particular process
Note:  If PPARM = 0. ,  then PVAR is set to its assumed value
automatically.  In some cases, there will be no  PVAR for a particular
process.   Although the program does not in these cases need this value
to calculate  costs, the program due  to programming limitations will
request a  value.  The assumed value which is zero can be safely-
entered.
PROCESSES -
 1
 2
 3
 4
 5
 6
 7
 8
 9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
24
25
26
27
28
29
30
31
32
33
34
35
RWPUMP
PRETRT
PRMSET
PSPUMP
TRKFTR
AERBSN
DIFAIR
MCHAER
FLOCCP
SECSET
RE1PMP
CLFEED
CLBASN
MULFTR
RE2PMP
GRVTKN
FLOTKN
ANA DIG
AERDIG
DRYBED
SLDTNK
VACFTR
CENFUG
MHINC
FBINC
WSPOND
SLGOON
RECRB1
RECRB2
TERST1
TERST2
ALUMFS
FECLFS
LIMEFS
POLYFS
RAW WASTEWATER PUMPING
PRELIMINARY TREATMENT
PRIMARY SETTLER
PRIMARY SLUDGE PUMPING
TRICKLING FILTER (SINGLE MEDIA)
AERATION BASIN
DIFFUSED AIR SYSTEM
MECHANICAL AERATION
FLOCCULATION BEFORE  PRIMARY
SECONDARY SETTLER
RECIRCULATION PUMPING
CHLORINE FEED SYSTEM
CHLORINATION CONTACT BASIN
MULT-MEDIA  FILTER
RECIRCULATION PUMPING
GRAVITY THICKNER
AIR FLOTATION THICKNER
ANAEROBIC DIGESTION
AEROBIC DIGESTION
SLUDGE DRYING BED
SLUDGE HOLDING TANK
VACUUM FILTER
CENTRIFUGE
MULTIPLE HEARTH INCINERATOR
FLUIDIZED BED INCINERATOR
WASTE STABILIZATION POND
SLUDGE LAGOON
RE-CARBCNATION
RE-CARBONATION
TERTIARY SETTLER
TERTIARY SETTLER
ALUM
FERRIC CHLORIDE
LIME
POLYMER
FEEDING AND
FEEDING AND
FEEDING AND
FEEDING AND
STORAGE
STORAGE
STORAGE
STORAGE
                            160

-------
36
37
38
39
40
41
CO2FS
NAALFS
PCKLFS
NAOHFS
RECALC
FLOCCT
CO2
SODIUM ALUMINATE
PICKLING LIQUOR
SODIUM HYDROXIDE
RE CALCINATION
FLOCCULATION BEFORE TERTIARY
FEEDING AND STORAGE
FEEDING AND STORAGE
FEEDING AND STORAGE
FEEDING AND STORAGE
DESCRIPTIONS AND DIMENSIONS OF FARM AND VAR FOR EACH
PROCESS FOLLOW:

 FARM = INDEPENDENT SIZING PARAMETER
 VAR = DESIGN VARIABLE
RWPUMP:  PARM - INITIAL FIRM CAPACITY (MGD).  The total
           capacity of the original installation with the largest pumping
           unit out of service.  If a plant had three raw waste pumps
           each with 1 MGD capacity, the initial firm capacity would be
           2 MGD.
PRETRT:  PARM - MAXIMUM CAPACITY (MGD)
PRMSET:  PARM - SURFACE AREA OF SETTLER (THOS.  SQ. FT.)
           VAR - DESIGN OVERFLOW  RATE (GPD /SQ. FT. ) Design
           flow divided by surface area of the settler.
           Assumed value for VAR = 700.
PSPUMP:  PARM - INITIAL FIRM CAPACITY (GPM) Same as above.
           VAR - OPERATING HOURS  (HOURS/DAY)
           Assumed value for VAR = 4.
TRKFTR:  PARM - MEDIA  VOLUME (THOS.  CU. FT. ) Media depth
           multiplied by surface  area.
           VAR - HYDRAULIC LOADING (MGD/ACRE)
           Assumed value for VAR - 5.
AERBSN:  PARM- LIQUID VOLUME (THOS. CU.  FT.)
           VAR - DETENTION TIME (HOURS)
           Assumed value for VAR = 6.
DIFAIR:    PARM - INITIAL FIRM BLOWER CAPACITY (THOS. CFM)
           The total capacity of the original installation with the largest
           blower  unit out of service.
           VAR - DIFFUSER EFFICIENCY (FRACTION) Ibs oxygen
           absorbed divided by Ibs of oxygen supplied.
           Assumed value for VAR = . 05
MCHAER:  PARM - TOTAL INSTALLED CAPACITY (HP)
           VAR - TRANSFER EFFICIENCY (LBS 02/HP-HR) (Number
           specified by supplier  of the  aeration equipment)
           Assumed value for VAR = 3.5
FLOCCP:  PARM  - MAXIMUM CAPACITY (MGD)
SECSET:  PARM  - SURFACE AREA OF SETTLER (THOS. SQ. FT.)
           VAR  - DESIGN OVERFLOW RATE (GPD/SQ. FT.  )
           Assumed value for VAR = 700.
RE1PMP:  PARM  - MAXIMUM CAPACITY (MGD)
CLFEED:  PARM  - AVERAGE CHLORINE USE (LBS/DAY)
           VAR  - CHLORINE DOSAGE  (MG/L)
           Assumed value for VAR = 8.
                            161

-------
CLBASN:   FARM-  LIQUID VOLUME (THOS. CU.  FT.)
           VAR - CHLORINE CONTACT TIME (MINUTES)
           Assumed value for VAR - 15.
MULFTR:  FARM -  CAPACITY  (MGD).  Limited cost data is available
           on multi-media filter installations.  The cost information
           used by the program is a function of the effluent passed
           through the filter.  The number requested is the flow rate
           of secondary effluent through the filter.
RE2PMP:  FARM -  MAXIMUM CAPACITY (MGD)
GRVTKN:  FARM -  SURFACE AREA (THOS. SQ.  FT.)
           VAR - DESIGN LOADING RATE (LBS/DAY/SQ.  FT. )
           Assumed value for VAR = 20.
FLOTKN:  FARM-  SURFACE AREA (SQ.  FT.)
           VAR - LOADING RATE (LB/HR/SQ. FT.)
           Assumed value for VAR = 2.
ANADIG:   FARM -  SLUDGE VOLUME (THOS. CU. FT.)
           VAR - DETENTION TIME (DAYS)
           Assumed value for VAR = 15.
AERDIG:   FARM -  SLUDGE VOLUME (THOS. CU. FT. )
           VAR - DETENTION TIME (DAYS)
           Assumed value for VAR = 15.
DRYBED:  FARM -  SURFACE AREA OF BEDS (THOS.  SQ. FT. )
           VAR - REQUIRED BED AREA (SQ.  FT./CAPITA) Sludge
           bed loadings are computed on a per capita basis. Typical
           ranges for chemical  sludges are 2. 0 -  2. 5 for open beds
           and 1. 25  - 1.5 for covered beds.
           Assumed value for VAR =2.3
SLDTNK:   FARM =  SLUDGE VOLUME (THOS. CU. FT. )
           VAR - DETENTION TIME (HOURS)
           Assumed value for VAR = 4.
VACFTR:  FARM -  FILTER  AREA (SQ.  FT.)
           VAR - LOADING RATE (LBS/HR/SQ. FT. )
           Assumed value for VAR = 4. 5
CENFUG:  FARM -  FIRM CAPACITY (GPM) Rated capacity of the
           centrifuge.
           VAR - OPERATING TIME (FRACTION OF DAY)
           Assumed value for VAR = 34.
MHINC:    FARM -  CAPACITY  (LBS DRY  SOLIDS/HR)
           VAR - OPERATING TIME (HOURS/DAY)
           Assumed value for VAR = 8.
FBINC:    FARM -  CAPACITY  (LBS DRY  SOLIDS/HR)
           VAR - OPERATING TIME (HOURS/DAY)
           Assumed value for VAR = 8.
WSPOND:  FARM -  VOLUME OF SLUDGE (THOS.  CU. FT.)
           VAR - DETENTION TIME (DAYS)
SLGOON:   FARM -  SLUDGE VOLUME (THOS. CU. FT.)
           VAR - DETENTION TIME (DAYS)
           Assumed value for VAR = 0.
                            162

-------
RECRB1:   FARM- LIQUID VOLUME (THOS.  CU. FT.)
           VAR -  DETENTION TIME (MINUTES)
           Assumed value for VAR = 30.
RECRB2:   FARM- LIQUID VOLUME (THOS.  CU. FT.)
           VAR -  DETENTION TIME (MINUTES)
           Assumed value for VAR = 30.
TERST1:   FARM - SURFACE AREA OF SETTLER (THOS.  SQ. FT.)
           VAR -  DESIGN OVERFLOW RATE (GPD/SQ.  FT.)  Flow
           volume divided by surface area of the settler.
           Assumed value for VAR = 700.
TERST2:   FARM - SURFACE AREA OF SETTLER (THOS.  SQ. FT.)
           VAR -  DESIGN OVERFLOW RATE (GPD/SQ.  FT.)
           Assumed value for VAR = 700.
ALUMFS:  FARM - CHEMICAL USAGE (LBS AL/DAY)
           VAR -  COST OF CHEMICAL ($/LB ALUM) The cost
           desired is the dollars per pound of dry alum charged to the
           treatment plant.  If the plant receives liquid alum, the
           charge should be converted to a dry alum basis assuming
           that liquid alum has a density of 11.1  Ib/gal at 60°F and
           there are  5. 4 Ib dry alum per gallon of liquid.
           Assumed value for VAR = . 03
FECLFS:  FARM - CHEMICAL USAGE (LBS FE/DAY)
           VAR - COST OF CHEMICAL ($/LB FECL3)
           Assumed value for VAR = . 042
LIMEFS:   FARM - CHEMICAL USAGE (LBS CAO/DAY)
           VAR - COST OF CHEMICAL ($/LB CAO)
           Assumed value for VAR = . 01
POLYFS:  FARM - CHEMICAL USAGE (LBS/DAY)
           VAR - COST OF CHEMICAL ($/LB POLY)
           Assumed value for VAR = 1.5
CO2FS:    FARM - CHEMICAL USAGE (1000  cu. ft.  min)
           VAR - COST OF CHEMICAL ($/LB CO2)
           Assumed value for VAR = . 023
NAALFS:  FARM - CHEMICAL USAGE (LBS AL/DAY)
           VAR - COST OF CHEMICAL ($/LB NAAL) The cost
           desired is the dollars per pound of dry sodium aluminate
           charged to the treatment plant.  Liquid sodium aluminate
           has considerable variation in density and viscosity, thus
           the manufacturer's data should be checked to convert the
           cost of liquid sodium aluminate to an equivalent dry cost.
           Assumed  value for VAR = . 12
PCKLFS:  FARM - CHEMICAL USAGE (LBS FE/DAY)
           VAR - COST OF CHEMICAL ($/LB FECL2)  .
           Assumed  value for VAR = . 04
NAOHFS:  FARM - CHEMICAL USAGE (LBS/DAY)
           VAR - COST OF CHEMICAL ($/LB NAOH)
           Assumed  value for VAR = 0.
RECALC:  FARM - MAXIMUM CAPACITY (MGD)
FLOCCT:   FARM - MAXIMUM CAPACITY (MGD)
                             163

-------
***** Subroutine INTIME

NOYRS
Number of years in desired time horizon
Dimensions - Years
Assumed Value  = 20

TPSIZE
Size of time periods in desired time horizon
Dimensions = Years
Assumed Value  = 1.

***** Subroutine EFFLJM

ELIMIT
Desired phosphorus effluent limit
Dimensions = Milligrams/Liter
Assumed Value  = 99.
Special Input - 99. indicates end of effluent data and execution continues
with the next subroutine.
Note:  Up to 20 limits  and years  may be input

EYEAR
Year of effluent implementation
Dimensions = Years
Assumed Value  = 0.
Note: Subroutine EFFLIM expects EYEAR to increase each time it is
input.

***** Subroutine DTGLJM

DIFCOS
Differential cost between old and new detergents. This number is the
difference in cost between a new detergent product replacing a phos-
phate containing detergent as a result of local legislation.  The new
product may contain no phosphate or it may contain some reduced
amount depending on the legislation.   DIFCOS is the extra cost of
replacing one pound of phosphate with a substitute.
Dimensions = $/Pound Detergent
Assumed Value  = .02

DTRGUS
Annual per capita detergent usage
Dimensions = Pounds/Capita/Year
Assumed Value  = 27.
Note:  27. is equivalent to 90% of phosphorus in influent wastewater
resulting from detergents.
Use  16. to get 50%.
                            164

-------
ENFCST
Enforcement cost of phosphate restrictions
Dimensions = $/Capita/Year
Assumed Value = .4

PC NT NT
Proposed legislated phosphorus content in detergent.    Up to five values
are accepted.  The variable PYEAR requests the year of implementation
of the legislative restrictions.
Dimensions = none  (Note:  3% is input as . 03)
Assumed Value = 99.
Special Input -  99.  indicates end of limit data and execution proceeds to
read in the next variable.

PRESPC
Present legislated phosphorus content in detergents.  If the community
has passed legislation limiting phosphorus  in detergents, what is the
percent allowed?
Dimensions = none
Assumed Value = .  1 (i. e.  10%)

PYEAR
Year of implementation corresponding to a PCNTNT
Dimensions = Year (e. g. ,  1982. )
Assumed Value  = 0.
Note:  DTGLIM expects PYEAR to increase in value each time it is
input.
ERRORS
 1.     Since linear and polynomial curve fitting techniques were used
 to obtain the mathematical cost relationships that are used in the pro-
 gram, the cost calculations are valid only over the range of the re-
 gression data points used to generate the cost equations.   If an input
 value to the construction cost equations lies outside this range, a
 warning message is printed.  This informs the user that the construc-
 tion cost,  operating and maintainance man-hours, and material &
 supply costs may be inaccurate for this process.  The warning message
 is of the form:

 ***** WARNING - THE VALUE  OF THE SIZING PARAMETER
 FOR PROCESS 'pname' = pvalue LIES OUTSIDE  THE RANGE
 minvalue TO maxvalue

 where:  pname  = name of process
        pvalue  = value of parameter
        minvalue = minimum value  of range
        maxvalue  = maximum value of range
                              165

-------
2.      Because it is possible to run out of capacity in the solid sinks,
a warning message will be printed when this occurs.  The message is
of the form:

***** WARNING - ALL, SOLID SINKS ARE COMPLETELY FILLED
SCHEME

The following chemical treatment schemes have been selected to pro-
vide varying levels of phosphorus in the effluent.
       1
       2
ALPYPS
FCPYPS

FC LMPS
4
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
21
22
23
LIME PS
ALPYFB
FCPYFB
FCLMFB
LIMEFB
ALUMAB
FECLAB
NAALAB
ALABMF
FCABMF
NAABMF
ALUMTF
FECLTF
ALTFMF
FCTFMF
ALFBAS
FCFBAS
L1FBAS
L2FBAS
NONE
ALUM + POLYMER TO PRIMARY SETTLER
FERRIC CHLORIDE + POLYMER TO PRIMARY
SETTLER
FERROUS CHLORIDE + LIME TO PRIMARY
SETTLER
LIME TO PRIMARY SETTLER
ALUM + POLYMER TO FLOCCULATION
BASIN
FERRIC CHLORIDE + POLYMER TO FLOCC.
BASIN
FERROUS CHLORIDE + LIME TO FLOCC.
BASIN
LIME TO THE FLOCCULATION BASIN
ALUM TO THE AERATION BASIN
FERRIC CHLORIDE TO AERATION BASIN
SODIUM ALUMINATE TO AERATION BASIN
ALUM TO AER. BASIN + MULTI-MEDIA
FILTRATION
FERRIC CHLORIDE TO AER.  BASIN +
MULTI-MEDIA FIL
SODIUM ALUMINATE TO AER.  BASIN +
MUL-MED FILTR.
ALUM AFTER TRICKLING FILTER
FERRIC CHLORIDE AFTER TRICKLING
FILTER
ALUM AFTER TRICKLING FILTER +  MUL-
MED FILTR.
FERRIC CHLORIDE AFTER TRK. FIL.  +
MUL-MED FILTR.
ALUM TO FLOCC. AFTER CONVENTIONAL
SECONDARY
FECL3 TO FLOCC. AFTER CONVENTIONAL
SECONDARY
LIME (1-STAGE) TO FLOCC AFTER CONVEN.
SECONDARY
LIME (2-STAGE) TO FLOCC AFTER CONVEN.
SECONDARY
NO CHEMICALS ADDED FOR PHOSPHORUS
REMOVAL
                           166

-------
                            LONG  PRINTOUT  EXAVPLE
 LIQUID  TKEATMENT SCHEME =    17
 AMORTIZATION RATE =0.05 AMORTIZATION LIFETIME  =20.0
 FRACTION  OF  CONSTRUCTION COST FINANCED BY GOVERNMENT
 PROCESS  NAME
RAW WSTE  PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE  PMP
TRKLNG FILTR
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASM
MUL-MED FLTR
RECIRC PMPNG
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
ALUM FEEDING
FECL FEEDING
LIME FEEDING
CONS
COST(

















TRUCTION
1000 $ )
0.0
0.0
0.0
0.0
11*31. 811
0.0
0.0
0.0
0.0
1870.2511
372.327
0.0
56.1*05
0.0
IOC. 520
1*5.525
1*7.318
S 1 Z 1 NC
PARAMETER
0.0
0.0
0.0
0.0
101*5.1*1*0
0.0
0.0
0.0
O.P
20.000
38.000
0.0
12.796
0.0
21*93.000
5314.353
3865.117


MOD
MGD
TSF
RPM
TCF
TSF
MGD
#/D
TCF
MGD
MGD
TSF
TCF
SOFT
#/D
#/0
*/D
AMORT
(10

















IZED
00 $
0
0
0
0
119
0
0
0
0
150
29
0
1*
0
8
3
3
COST
/TP)
.0
.0
.0
.0
.708
.0
.0
.0
.0
.075
.877
.0
.526
.0
. 51*8
.553
.81*5
                                                      YEAR  PROCESS
                                                      FIRST NEEDED
                                                         199*4
                                                         199U
                                                         1991*
                                                         199U
                                                         1974
                                                         199U
                                                         1991*
                                                         199U
                                                         1991*.
                                                         197li.
                                                         197U,
                                                         1991*,
                                                         1971*.
                                                         1991*.
                                                         197U.
                                                         1971*.
                     ,0
                     ,0
                     ,0
                     ,0
                     ,0
                      0
                      0
                      0
                      0
                      0
                      0
                      0
                      0
                      0
                      0
                      0
                                                         1971*.0
TOTALS
3990.760
320.231

-------
                                                 PERIODIC  OPERATING  COSTS
oo
                    PROCESS NAME
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
TRKLNG FILTR
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASN
MUL-MED FLTR
RECIRC PMPNG
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
ALUM FEEDING
FECL FEEDING
LIME FEEDING
                 OPERATING MAN-HOURS
                  (MAN-HOURS/TP)
                AVE.    MAX.    MIN.
                         MAINTENANCE MAN-HOURS
                            (MAN-HOURS/TP)
                          AVE.    MAX.    MIN.
0.
0.
0.
0.
1UU9.
0.
0.
0.
0.
3772.
1153.
0.
13U.
1*391.
0.
0.
0.
0.
0.
0.
0.
UU9.
0.
0.
0.
0.
3772.
1153.
0.
131*.
U391.
0.
0.
0.
0.
0.
0.
0.
UU9.
0.
0.
0.
0.
3772.
1153.
0.
13U.
1+391.
0.
0.
0.
0.
0.
0.
0.
925.
0.
0.
0.
0.
0.
971.
0.
80.
536.
3012.
765.
2182.
0.
0.
0.
0.
925.
0.
0.
0.
0.
0.
971.
0.
80.
536.
3012.
765.
2182.
0.
0.
0.
0.
925.
0.
0.
0.
0.
0.
971.
0.
80.
536.
3012.
765.
2182.
                   TOTALS =
10898.   10898.   10898.    81*70.    8U70
                                                       8U70.

-------
                                          PERIODIC OPERATING COSTS
vO
               PROCESS NAME
RArt WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
TRICING FILTR
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASN
MUL-MED FLTR
RECIRC PMPNG
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
ALUM FEEDING
FECL FEEDING
LIME FEEDING
                      MATERIAL  &  SUPPLY  COST
                            ( $ /TP)
                     AVE.         MAX.
                                                            MIN,
LABOR COST
(AVERAGE)
(1000$/TP)
                                                                               TOTAL O&M
                                                                              (1000$/TP)
0.0
0.0
0.0
0.0
1819. 01*
0.0
0.0
0.0
0.0
25175.88
7707.08
0.0
1*86.36
2161*1*. 56
301004.00
11*813.01
11*107.63
0.0
0.0
0.0
0.0
1819.0U
0.0
0.0
0.0
0.0
25175.92
7707.10
0.0
1*86.36
2161* k. 59
30100U. 37
11*815.06
1U107.67
0.0
0.0
0.0
0.0
1819. 01*
0.0
0.0
0.0
0.0
25175.92
7707.10
0.0
1*86.36
2161* l*. 59
30100i*.57
14813.06
1U107.67
0.0
0.0
0.0
0.0
10.0tt6
0.0
0.0
0.0
0.0
15.961
8.985
0.0
0.901*
20.852
12.7U5
3.239
9.233
0.0
0.0
0.0
0.0
11.865
0.0
0.0
0.0
0.0
1*1.137
16.692
0.0
1.390
i*2.i*97
313.71*9
18.052
23.31*0
               TOTALS
               386757.50   386758.00   386758.00
                                                                      81.961*
               1*68.721

-------
                             UNIT COST DATA
                          (CENTS/1000 GALLONS)

PROCESS NAME   AMORTIZATION   LABOR   MATERIAL & SUPPLY   TOTAL
RAW WSTE PMP
PRE TRETMENT
PRIM SETTLER
PRMYSLGE PMP
TRKLNG FILTR
SECY SETTLER
RECIRC PMPNG
CHLORNE FEED
CHLORNE BASN
MUL-MED FLTR
RECIRC PMPNG
GRAV THICKNR
SLGE HLD TNK
VACUUM FILTR
ALUM FEEDING
FECL FEEDING
LIME FEEDING

TOTALS «
                   0.0
                   0.0
                   0.0
                   0.0
                   1.61*
                   0.0
                   0.0
                   0.0
                   0.0
                   2.06
                   0.1*1
                   0.0
                   0.06
                   0.0
                   0.12
                   0.05
                   0.05
0.0
0.0
0.0
0.0
0.11*
0.0
0.0
0.0
0.0
0.22
0.12
0.0
0.01
0.29
0.17
o.oi*
0.13
                  i*.39         1.12
                    SOLID  SINKS  COSTS
TIME
PERIOD
1
2
3
i*
5
6
7
8
9
10
11
12
13
11*
15
16
17
18
19
20
SINK
USED
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
1
AMOUNT SOLIDS
(TONS)
36l*8.5it
36U8.5I*
361*8.51*
361*8. 5k
361*8.51*
361*8.51*
361*8.51*
361*8.51*
361*8.51*
361*8.51*
36U8.51*
361+8.51*
361*8.51*
361*8.51*
361*8.51*
36U8.51*
36U8. 51*
361*8.54
36i*S.5l*
3Gl*8.5i»
COST
<$/TP)
91213.1*1*
91213.U1*
91213.1*1*
91213.1*1*
91213.1*1*
91213.1*1*
91213. 1*1*
91213.1*4
91213.1*1*
91213.1*1*
91213.1*1*
91213.1*1*
91213.1*1*
91213.1*1*
91213.i*£*
91213.i*U
91213.1*1*
91213.1*1*
91213.1*1*
91213.1*1*
  TOTALS  -
                     72970.69   182^*265.00
0.0
0.0
0.0
0.0
0.02
0.0
0.0
0.0
0.0
0,3i*
0.11
0.0
0.01
0.30
l*.12
0.20
0.19

5.30
 0.0
 0.0
 0.0
 0.0
 1.80
 0.0
 0.0
 0.0
 0.0
 2.62
 0.61*
 0.0
 0.08
 0.58
 l*.t*2
 0.30
 0.37

10.81
UNIT COSTS FOR SOLID WASTE DISPOSAL (CENTS/1000  GAL.)
TOTAL UNIT COST (CENTS/1000 GAL) =12.06
                                                       =  1.25
                         170

-------
ERRATA SHEET FOR THE PROGRAM LISTING

NOTE:  Statement # n-fm means Fortran statement number n + m lines

Subroutine:  CQNCST

       Statement # 6790 + 1
       should read X = TPLANT (BPARM, RECALC)
       Statement # 6790 4 2
       should read 'REF.  13', not "REF. 12'

Subroutine:  SIZE

       Statement # 4000 + 22
       which reads 'PFECL = PFECL + WRFEP* , . . '
       should be replaced by the following 6  lines:

C     FE CAN BE ADDED AS EITHER FECL3 OR FECL2
C     IF FECL3,  THEN FFRATO =  2.89
C     IF FECL2,  THEN FFRATO ^  2. 27
       FECON = WRFEP * IELIMT(INF,  TP) * FFRATO * CON
       IF (FFRATO .EQ. 2. 89) PFECL = PFECL + FECON
       IF (FFRATO .EQ. 2. 27) PPCKL - PPCKL + FECON


 Subroutine: TSCHEME

       Statement # 5700
       Insert before this  statement the followinq line:

       RETURN
                              171

-------
FILF:
                         PI
                                                     INTERACTIVE DM* CORPORATION
C
c
C
c
c
c
c
c
c
c
c
c
c
c
c
c
c
8LCCK DATA


   PURPOSE :
      BLOCK OfTA CONTAINS  DAT!

      VARIABLES IN NAVPC


   roMvcf^ PLCCKS:
                                 S"UTcv'\TS  USED TO INITIALIZE
      PRGCNT
      SCHEME
      SF.WPDP
      SSINK
      TPLANT
                INFLUr*lT/rFFLUENT  I NCC2MA TI CN
                CONTAINS  P^UGKAM CDNTRCL  VARIABLES
                INFO APGUT  LIQ'MS  TREATMENT  SCHPMES
                THE: SCWEREO  PQOULATICK
                SOLID SINK  INP3RMATION
                THE TREATMENT  PLANT  CHSR ACTFR IS TIC5
    AUTHCP :

       DAVID A 5APNES    171CT7?
      COMMON /IELIMT/  IFLIMT(?,?0)

     1 ,  INF,  EFF


      REAL  IELIMT

      INTtGEO  EFF
              /P:
-------
       BLKCAT
                   pi
                                                      INTERACTIVE DATA CORPORATION
      CCMS'CN  /TPLfiNT/ TPL4NTJ 16,45)
1
2
3
4
5
6
7
8
9

I
2
3
4
5
6
, RVWlvp,
, ^Cn*':Efif
, RFPPMF,
, VACCTR,
, REC»32,
, CC2FS .
, PNAME ,
, WVAR .
, MAXP
INTEGER Rwi
t DIC4 TRt
, GRVTKT. ,
, CEMFUC,
, TERST2,
, PNAME ,
, WVA3 ,
PRFTOT,
CLOCC°,
GRVTKN,
CE^FIJ^>»
TE^STI ,
NA4LCS ,
t M r A T c ,
6 P A t M ,

P^-'SET ,
sscsrr.
PS°IJMP,
TRKPT3
A?on,SN.
^FlPyP, CLFLEC, CL8ASN,
PL^TKN, iMADir,, AFDOIG, ORYBEC,
MHINC ,
TFR3T2,
PCKLFS,
AMLIFc,
3ASF ,

CRINC , WSPONC, SLGCCN,
AL'JMFS,
FECLFS, LI"rcS,
DIFAIP
MULCT«
SLDTNK
PFCf31
POLYPS
NiQHFs, PECALC, PLTCCT
PPAR" ,
PVAR , WGPAP.M,
APVA^ , PA3MX , MIN^V ,



WPAPM
MAXRV

>UNP, PRETRT, PRESET, PSPUMP, TRKFTP, AERRSN
FLOCCP,
FLCTKN,
FBINC ,
ALUMFS,
AMR ATE.
BPARM ,
SECSET,
AMAHI G,
WSPGNO,
FECLFS,
AML i FE ,
FLOCCT,
»FIPMP,
AERDir,,
SLGCCN,
"OLYPS,
PPARM ,
9ASE ,
CLFEED
CPYBSP
"ECR Bl
C02FS
PVAR
APVAR
CLflASN,
SLOTNK,
RECRP2,
PCKLFS,
WOPAPM,
PARMX
RE2PMP
VACFTR
TERSTl
RECALC
WPARM

C
c
C
c
c
c
c
c
          ****?  I r L 1 v T «:-•
            INf/l/, Lr~l2l
   ***** PkGCNT  *****
DATA FIXFD/1/, FLCTF/2/,  ALPHA/3/
DATA YES/3HYFS/f  NO/2HNC/
CATA GN/1/ , OFF/0/

   ***** SEfcDCP  *****
DATA YFAR/2/i SPOP/1/,  MAX°v/5/
    ***** SSIM<  *****
 OATA CAP/I/, CIST/2/,  MAXSS/15/

    ***** SCI-EME  *****
 OATA MAXSCM/25/
    SCHEME NAMES  AND NU«BE*S
 DATA ALPYPS/1/,  FCPYPS/2/,  FCLMPS/3/, I
1 ,  FCPYFB/ 6/,  FCLMFV  7/f  LlMEFB/ 8/,
2 ,  NAALAB/11/,  ALABMF/12/,  FCA8MF/13/,
3 ,  FF.CLTF/16/,  ALTFMF/17/,  FCTFMF/1B/,
4 ,  ll?BtS/21/,  L2FP.AS/22/,  ^nNIE/23/
    LljUir fftATMFNT PP^CESSCS FOP FACH
 :ATA >c»-t*;
-------
Fir
3LKCAT
                         PI
                                               INTERACTIVE DATA CC&POPATION
c
c
c
c
      DATA SCHEME(1,13)  /!'»/,  S-.HE-r ( 2, 13) /15/, SCHCME<3,13> /33/

      DATA SCHE*Ed,l  /!«/,  SCH?'iE < 2, U) /15/, SCHEMEI3.U) /37/
      DATA SCHEME (I,1 5)  /3?/t  SCH=M= ( 2 ,'. 5 1
      DAT* SCKEȣd,l6)  /33/,  SCHEV=(2,16!
      DATA SOFMEd.17)  /IW,  SCHE«E(2,m  /15/, SCHFME(3,17) /32/
     I  , SCHEME!*,17)  /5/
      DATA SCHFMEd,l3)  /!<»/,  SCHevP(2,18)  /15/, SCHEME(3,18) /33/
      CATA SCt-EME(l,i9)  /1V,  SCHE"=<2,19> /15/, SCHFCE(3,19) /30/
     1 , SCHEME(*»19>  /32/,  SCH = l«E(5,19) Ml/
      DATA SCHEMEd.201  /I*/,  SCH£MF(2,20) /15/, SCH£ME(3,20) /30/
     1 , SCHFMECV,20)  /•?•;/,  SCH5ME(5,20I /41 /
      CATA SCHEM!?d,21t  /I'*/,  SCHEMF(2,2l) /15/, SCHFME(3,2l) /28/
     1 , SCHEVE(4,21)  /30/,  SCH:ME(5,21) /34/, SCHEME(6,2l)  /36/
     2 , SCHEV£<7,21)  /41/
      DATA SCHtMFd,22)  /I*/,  SCHEME«2,22) /15/, SCH?ME<3,22) /28/
     I , SCH£ME(4,22)  /29/,  SCHuV?(5,221 /30/, SCHEMF(6,22)  /31/
     2 , SCHEME! 7,22)  /34/,  SCH?^EH,22) /36/, SCHEME!9,22)
         MINIMUM ACHIEVABLE  EFFLUENT p LEVELS FOR EACH SCHEME
      DATA MIN£FP(  D/2./,
           MINEFP(
     2
     3
     -%
     5
     6
     7
"IMEFP(
MINEFp<10)/2./, MIME'Pdl)/2./
MINEFP(13)/.5/, MINEcP(l^)/.5/
MINEFPJ16I/2./, M!NEcP(17)/.5/

M^EFP(22)/.l/, MINE-P(23)/10./
   **.*+ TPLANT  *****
                                      MINEFPJ 9)/2./
                                      MINEcP(12)/.5/
                                      MINEFP(l5)/2./
      DATA MAXPM5/
      DATA
             PROCESSES  NAMES AND NUMBERS
                PRETRT/2/,  PRMSET/3/,
                                                        TRKFTR/5/
1 AE13SN/ 6/
2
3
4
5
6
••
a
0
t
o
,
RElPMP/U/t
GRVTKN/16/
SLOTNK/21/
WSPCNC/26/
TERST2/31/
C02FS /36/
FLOCCT// 9/,
^UL"TR/l*/,
AERDIG/19/,
MHINC /2W»
PECR92/29/,
LIMEFS/34/,
NtOHFS/39/,

SECSET/10/
RE2PMP/ 15/
ORYBED/20/
FBINC /25/
TESST1/30/
PCLYFS/35/
RECALC/40/

PPARM/6/, PVAC/7/
f

BPARM /d/,
MAXRV/16/
BASE /12/

«=0». PRINTOUT
OATATPLANT11,
OATATPLANT(1,
OATATPLANT(I,
OiTATPLANTd,
OATATPLANT(1,
DATATPCANTd,
                   /,TPLANT(2,
                 E  /,TPLANT(2,
         3)/«HPRIM/,TPLANT(2.
                                    1 )
                                                     TPLANTO ,
PMP/
                     5)/4HTP.KL/.TPLANT(2i
                     6)/4HAERT/,TPLANT(2,
                                          SFT/,
                                               TPLANT(3t
                                            C/,TPLANTC3,
                                                                3IMHTLEP/
                                                                      PMP/
                                                         6J/AHSIN  /
                                    174

-------
                                               INTERACTIVE  DAT*  CORPORATION
DATATPLANT.d ,  7) /4MQ IFF/, TPLAMT ( ? ,  7>/4HUSF.D/,
DATATt>LANT( 1,  8 ) /4HM?r H/, Tt>L ANT ( 2 ,  81/4H AFP/.
OATATPLANT( 1,  9 ) /4HFLOC/, TPL ANT (2 ,  9)/4HC -P/,
DATATPLANTd.lOJ/'tHSEC Y/, TPL ANT ( 2 , 10 > /4H S'T/,
DATATOLANTl 1, 11 J/4HP.FC I /, TPLAMTl 2, ll)/4HRC P/f
DAT/T°LANT(
DATATPLANT
OATATPLANT
DATATPLANTC
DATATPLANT(
OATATPLANT<
OATATPLANTJ
DATATPLANT(
OATATPLANT(
OAT AT PL ANT (
5 , 1 3 J / 4HCHLH/,
 , I 4 ) MHMUL-/,
 ,15)MHRECI/,
1 , 16) MHGR AV/,
1,17)/4HFLOT/,
1,1B)/4HANA /,
1,19)/4HAER /,
1,20)/4HSLGE/,
1, 21 ) /4HSLGF/ ,
1,22 IMHVACU/,
                          TPL ANT ( 2,
                          TPL ANT ( 2,
                          TPLA'IT(2,
                          TPL ANT ( 2,
                          TPLANT(2,
                          TPL ANT ( 2 ,
                          TPL ANT( 2t
                          TPLA\'T(2,
                          TPL4NT ( 2,
                          TPLAMT( 2,
                                           = /,
                                   14 )/4H*1ED /,
                                   15)/4HRC P/,
                                   16)/4H THI /,
                                   17)/4H TMI/,
                                   13 1/4HOI GF_/,
                                   19) /4HDIGE/,
                                   20)/4H DRY/.
                                   2 I ) MH HLD/,
                                   22 )MHIH F/,
                                          PEE/,
                                          FEE/,
                                          FEE/,
                                          FEF/,
                                          FEE/,
                                          FEE/,
OATATPLAMT(l,24J/4HNtUL-/,TPLANT(2,^	,
DATATPLANT(l,25)/4HFLUD/,TPLANT<2,25)/4H-3ED/,

OATATPLANT«l,27)/4HSLGE/,tTPL4NT(2,'27)/4H LAG/!
OATATPLAMT(1,28)/4HRECA/,TPLANT(2,28)/4HR30N/,
DATATPLANT(l,29)/4HRECA/,TPLANT(2,29)/4HRfiON/,
OATATPLAMT(1,30)/4HTER  /, TPL ANT ( 2, 30) MHS^TT/,
DATATPLANT1l,3i)/4HT5R  /,TPLANT I 2,31)/4HS^TT/,
OATATPLANMI,32)/4HALUM/,TPLANT(2,32I/4H FEE/,
OAT/>TPLANT(1,33)/4HFECL/,TPLANT(2,33)/4H
DATATPLANT<1,34)/4HLIME/,TPLANT(2,34)/4H
DATATPLANT(1,35)/4HPOLY/,TPLANT(2,35)/4H
DATATPLANT(1,36)/4HC02  /,TPLANT(2,36)/4H
OATATPLANT<1,37)/4HNAAL/,TPL4NT(2,37)/4H
DATATPLANT<1 ,38 )/4HPCKL/,TPLANT(2,38)/4H
OATATPLANT»1,39)/4HNAOH/,TPLANT(2,39)/4H . l.u,,
DATATPLANT(1,40)/4HRECA/,TPLANT(2,40)/4HLCIN/,
DATATPLANT
-------
Fill?: OI.K.CVT
Ff-TPAN  PI
INTERACTIVE CA"M
PATA
04TA
OATA
PATA
DATA
D4T/S.
TATA
TATA
CAT*
CATA
OATA
DATA
DATA
DATA
OATA
DATA
OATA
DATA
DATA
OATA
OATA
DATA
CATA
DATA
CATA
DATA
OATA
DATA
DATA
OATA
S
DATA
OATA
CATA
DATA
DATA
OATA
DATA
DATA
DATA
DATA
OATA
DATA
DATA
DATA
DATA
DATA
OATA
DATA
OATA
DATA
CATA
OATA
OATA
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLAVT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPL4NT
TPLANT
TPLANT
( 12,16
(13,17
( l ? , \ a
(13, 19
(13,20
(13,21
(13, 72)
(13,23)
(13,24)
(13,25)
(13,26)
(13,27)
(13,28)
(13,29)
(13,30)
(13,31)
(13,32)
(13,33)
(13,34)
(13,35)
(13,36)
(13,37)
(13,38)
(13, 3S)
(13,40)
(13,41)
(13,42)
(13,43)
(13,44)
(13,45)
/20./
/2. /
X1 5./
/I1)./
/?.3/
/4./
/4.1)/
/ .34/
/8./
/8./
/O. /
/O./
/30./
/30./
/TOO./
/700./
/.03/
/.042/
/.Ol/
/1.5/
/.023/
/.12/
/.04/
/O. /
/O./
/O./
/O./
/O./
/O./
/O./






























IZING PARAMETER UNITS US
TPLANT
TPLANT
TPLANT
(14,1)
(14,3)
(14,5)
TPLANT (14, 7)
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
TPLANT
(14,9)
(14,11)
(14,13)
(14,15)
114,17)
(14,19)
(14,21)
(14,23)
(14,25)
(14,27)
(14,29)
( 14,31)
(14,33)
(14,35)
(14,37)
(14,39)
(14,41)
(14,43 )
(14,45)
/4Hwf»0 /
/4HTSF /
/4HTCF /
/4HTCCM/
/4HHGC /
/4HMGD
/4HTCF
/4HMGD
,
ff
,
,
t
/,
/.
/,
/4HSCPT/,
/4HTCF
/4HTCF
/4HGpM
/4HK/D
/4H
/4HTCF
/4HTSF
/4H "*/D
/4H  /4HMGD
                                    TPLANTU4,16>
                                    TPLANH 14.18)
                                    TPLANT(14,20)
                                    TPLANT(14,22»
                                    TPLANT(14,24)
                                    TPLANT(14,26)
                                    TPLANT(14,23)
                                    TPLANT(14,30)
                                    TPLA'4T( 14*32)
                                    TPLANTC14,34)
                                    TPLA»iT( 14, 36)
                                    TFL6-\T(14,33)
                                    TP>LANT( 14,40)
                                    fPLANT(!4,42)
                                   /4HK/H
  AND MAXIMUM VALUES FOR VALID RANG?  FOR CONSTRUCTION EO.
                                   /4HTCF
                                   /4HTSF
                                   /4HK/D
                                   /4H#/0
                                   /4HK/0
                                   /4H«/D
                                   /4H
                                   /4H
                      176

-------
PILE: RLKDAT
                  PI
                                               INTERACTIVE DATA CCRPORATICN
CAT*
DATA
DATA
DATA
OATA
DATA
DATA
DATA
D4TA
OATA
DAT*
DATA
OATA
OATA
OATA
DATA
OATA
OATA
DATA
OATA
OATA
DATA
DATA
DATA
DAT*
DATA
DATA
DATA
OATA
DATA
OATA
DATA
DATA
DATA
OATA
DATA
DATA
DATA
DATA
DATA
DATA
DATA
OATA
DATA
DATA

END
           TPLAMT(15,2)
           TPLANT(15,3)
           TPLANT(15,5)
           TPLANT(i5,6)
           TPLANT(15,7J
           TPLANT(15,8)
           TPLANT(15,9)
           TPLANT (15, 10)
           TPLANT(15,1U
           TPLANT( 15,12)
           TPLANTU5.14)
           TPLANT (15,15)
           TPLANTU5, 16)
           TPLANT (15,17)
           TPLANT (15,1*)
           TPLANT(15,19)
           TPLANT(15,20)
           TPLANT (IS, 21)
           TPLANTU5.22)
           TPLANT<15,23)
           TPLANT(15,24)
           TPLANTU5.25)
           TPLANT (15, 26)
           TPLANT(15,27)
           TPLANT(15,28)
           TPLA\T(15,29)
           TPLANT(15,30)
           TPLANTU5.31)
           TPLANT (15, 32)
           TPLANT(15,33)
           TPLANT(15,34)
           TPLANT(15,35)
           TPL/SNTU5.36)
           TPLANT(15,37)
           TPLANT(15,38)
           TPLANT(15,39)
            TPLANT (15,43)
            TPLANT(15,45) /O./,
              6,1) /1000./
/I./, TPLANT(16,2) X200.X
/I./, TPLANT<1<,,3) X200.X
X30./, TPL4NTU6.4) /5000.X
/3.X, T°LANT<16,5) X9000.X
X3.X, TPLiNT(16,6) X4000.X
/.02/, TPLANT(16,7) /200.X
X20.X, TPLANT(16,8) /5000./
/I./, TPLANT(16,9) /200.X
 /I./, TPLANT(16,10) X200.X
 X.5X, TPLANT(16,1J.) X300.X
 /20.X, TPLANT(15,12) /8000.X
 X3.X, TPLANT(16,13) X300./
 /I./, TPLANT(16,14) X200.X
 /.5/, TPLANT(16,15) X300.X
 X.02X, TPLANT(i6,16) /20.X
 /O./, TPLANT(16,17) X1.EIOX
 /30.X, TPLANT(16,18) /6000./
 XO.X, TPLANT(16,19) X1.E10X
 /7.X, TPLANT(16,20) /4000.X
 /I,/, TPLANT(16,2!1 X1000.X
 X80.X, TPLANT(16,22) /6000./
 /I.5/i TPLANT(16,23) /700.X
 X700.X, TPLANT(16,24)  X30000./
 XO.X, TPLANT(16,25) XI.E10/
 XO.X, TPLANT(16,26) X1.E10X
 X30./, TPLANT(16,27) X30000.X
 XI.X, TPLANT(16,28) X400.X
 /l.X, TPL4;JT(16,29) X400.X
 XI.X, TPLANT(16,30) X200.X
 XI.X, TPLANTU6.31) X200.X
 XO.X, TPLANT(i6,32) X1.S10X
 XO.X, TPLANT(16,33) X1.E10X
 XO.X, TPLANT(16,34) X1.EIOX
 XO.X, TPLANT(16,35) X1.510X
 XO.X, TPLANT(16,36) X1.EIOX
 XO.X, TPLANT(16,37) X1.EIOX
 XO.X, TPLANT(16,38) X1.EIOX
 XO.X, TFLANT(16,39) X1.E10X
 XI.X, TPLANT(16,40) X200./
 /l.X, TPLANT(16,41) /200.X
 /O./, TfLANT(16,42) /1.510/
 XO.X, TPLANT(16,43) XUEIO/
 /O.X, TPLANT(16,44) X1.E10X
        TPLANT(16,45) X1.E10X
                               177

-------
FRF:
                         PI
                                            INTERACTIVE CAT* CORPORATION
                r  PUILO
C
c
C
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
   SUILD DETERMINES THC "4XMU*  SIZE  0=  THf  NECESSARY

   ADDTTJC\AL EQUIPMENT NtcOEP FOR  EACH  PROCESS  ANC THF TIME

   PFRIOC WHjN ADDITIONAL  iiQUI P*::NT  IS  = IRST NEEDED.
       BLOCKS:
   PRGCNT - PROGRAM CONTROL

   TIME   - INC0 ABOUT TIME

   TPLANT - CHAPACTEPISTICS

   TRTCST - TREATMENT COSTS
VtRI A1!' PS
HCRIZCN

OF THE TREATMENT

FOR FACH PROCESS
PLANT PROCESSES
FOR EACH TIME
CALLED BY:
   TRTMNT - THE MAIN COSTING  SOBROUTINE


AUTHOR:
   TAVID A fJARNES   19DEC72
      COHMCN  /PRGCNT/  IGOTO,  IANSWR,  FIXED, FLOTE, ALPHA

      I  , YES,  NO,  CN,  OFF

      2  , ISCH*
      3  , IDUHMY,  CUVMY


      EQUIVALENCE  ( I ANSWS,ANSWEHI


      INTEGER  FIXED,  FLCTE,  ALPHA

      INTEGER  YES,  ON, OFF


      COMMON  /TIME/  NOYRS,  MAXTP,  TPSIZE, TP


      INTEGER  TP
CCMMQN /TPL*^T/ TPLANTJ 16,45)
1 RWPUKP,
2
3
it
5
6
7
8
q
MCHAER,
PE2PMP,
VACFTR,
RECRB2,
C02FS ,
PNA^E ,
WVAfi ,
MAXP
PRETRT,
FLCCCPi
GRVTKN,
CENFUG,
TFPST1,
NAALCS,
AMRATE,
EPARM ,

PRESET,
SECSET,
FLOTKN,
MHINC ,
T6RST2,
PCKLFS.
A^LIFE,
BASE ,

PSPUMP,
RE1PMP,
ANAOIG,
FBINC ,
ALUMFS,
NAHHFS,
PP4RM ,
ADVAR ,

TRKFTP,
CLFEEO,
AEPOIG,
WSPCNC,
FECLFS,
RFCALC,
PVAR ,
PARMX ,

AERBSN,
CLBASN,
ORY8ED,
StGOCN,
LIMEFS,
FLOCCT
WOPARM,
MINRV ,

OIFAIR
MULFTR
SLOTNK
RECR31
POLYPS

WPARM
MAX^V

INTEGER RWPUMP, PRETRT, PRESET, PSPU"P, TPKFTR, AERBSN
1 DIFAIP,
2 GP.VTKNt
3 CENCUG,
4 TERST2,
5 PNAME ,
6 WVAR ,
FLGCCP,
FLCTKN,
FSINC ,
ALUMFS,
AMRATF,
BPARM ,
SECSET,
4NAOIG,
WSP3ND,
FECLFS,
AMLIFF,
FLHCCT,
BE1PMP,
AEHOIG,
SLGCCM,
POLYPS,
PPARM ,
S»SE ,
CLFEEO,
QRY3ED,
PECRBl,
CC2FS ,
PV4R ,
ftPVAR ,
CLBASNt
SLOTNK,
RECRB2,
PCKLFS,
WOPAPM,
PARMX
RE2PMP
VACFTR
TERST1
RF.CALC
WPARM

      COMMON  /TPTCST/  OMH^S ( 45, 20 1 ,  MMHPS ( 45, 20) ,  T«SU5,20),  CONCOS(45)

      1               ,  AMCQSTU5), TPFADO(45I
                                      178

-------
FILF: BUILD
               FORTRAN  PI
                                               INTERACTIVE O'TA
                                                                     F. AT I CN
      PEAL M1HRS
      INTFGER TPFflCC
C
c
C
c
c
c
1000
c
c
c
C
C
C
4COO
c
c
    ***************************************************************
    ****************                                ****************
    ****************     STAFT FXECUTICN            ****************
    ****************                                ****************
    *******,****»****¥********************************+*************

 CCNTINUE

    COMPUTE  ADDITIONAL  SIZE  NFEDEC TC BE BUILT
    FOR  EVERY  PROCESS
 00 4000 IP  »  ItMAXP
 IF (TP  .LE. 1)   TPPADDUP)  « *AXTP + 1
 TPLANTCSPARK,IP)  - 0.
 TPLANT(BASEiIP)  - AMAX1(TPLANT(WOP ARM,IP),TPLANT("PARM, I P) )
 8  - TPLANT(kPARM.IP)
 IF JTPLANT
-------
      CyMC!TY    FCrTFiN  f>\                           INTERACTIVE ^flTA CCJl'Pn'U T I ON
C
C
C           CMMMTY  Rfc'AOS  IN VALUE"; rOP THE VA^IA^LES  WHICH DFSCPIRE THT
C           COVVU.MTY.   THES^ INCLUDE SUCH 1REAS  AS:  SEW5"'EO POPULATION,
C           ENERGY-,  TCANSPOaTAMnN-COSrS, LIOUIO AN^ S3LID
C           SINKS.
C
c        CO""":N  PLOCKS:
C           ENGCST   - DtLIVcSED COSTS Oc  ENEPGY  FORMS
C           INDSTY   - INPORMATIPN A30UT INDUSTRIAL  PHCSPHO^US EFFLUENTS
C           LRPCST   - COSTS TF LA^G'?  (DIRECT  AND  INDIRECT)
c           LSINK    - CHARACTFRISTICS OF  LIQUID  SINKS
C           PRGCNT  -  CONTAINS PROGRAM CONTROL  VARIABLES
C           SEWPOP   - THE SFWERED PTPULATICN
C           SSINK    - CHARACTERISTICS OF  SOLID rfASTE  SINKS
c           TSCST    - TIME AND SPACF  DIFFERENCE  COSTS
c
C        CALLED  BY:
C           5YSTEP
C
c        AUTHOR:
C           DAVID A  BARNES   190EC72
C
c        ---------------------------------------------------------------

      COMMON /ENGCST/ ELECOSt OILCCSt GASCCS

      COMMON /INPSTY/ INDSTY ( 3, 20 >,  LEGINP

      REAL  INCSTY,  LEGINP

      COMMON /LBRCST/ OHO , IOFRAC,  GOVFF

      REAL  tDFRAC

      COMMON /LSIM
-------
= ILF:  CV^'TY    FORTRAN  PI                           INTERACTIVE DATA CORPORATION


       CCHKON  XSSINK/ T^NCST, SV.ASTE(20), SCLSMK ( 2 , 1 5 ) , SSC^ST(20)
      I              . 9ESTSS(20), CAP, DIST, MAXSS
       INTEGt.A  EcSTSS, CAP, OIST

       CCMMON  /TSCST/ CNSTRC,

       REAL
1010   FORMAT!IHO,/IX,«CC^UNITY CHARACTERISTICS')
3051   FORMATdH ,'ELECOS='I
3054   FORMATdH , • EL5CTR 1C I TY CCST ! S/KWH') • )
3151   FORMATdH ,«riLCOS=«)
3154   FORMAT! IH ,'QIL COST !$/GAL)')
3251   FORMATdH ,'GASCOS='J
3254   FOPMATdH ,«GAS COST 
-------
FILF:
                                                     INTERACTIVE  DAT4  CP?PCRATI»1N
CTSTS Afc f NOT
                   AT  PRESENT
C        THi FCLLr*/ING
      GO TO 4CCO
3150  POINT 3151
3152  CM.L RL:AniN(PLOTF )
      GOTO (2153, 3000, 3155, 3150, 315S),  IGOTO
3153  PRINT 3154
      GO TO 3152
C        NPT LSED YET
3155  CILCCS = DLC^Y
      GO TO 3157
3156  OILCCS = ANSWER
3157  CONTINUE
3250  PRINT 3^51
3252  CALL R E 4C IN( FLOTE )
      GOTO (3253,3000,3255,3250,3256),  IGOTO
3253  PRINT 5254
      GC TO 3252
C        NOT tSEO YET
3255  G4SCOS
      GO TO 3257
3256  G&SCOS = A
3257  CONTINUE
*000  CONTINUE
C        PEAO IN LAPPR COSTS
*050  PRINT 
-------
FILE:
               FORTRAN  PI
                                               INTERACTIVE  DATA
5057
C
5110

5111

5112
5113

5114
5150
5152

5153

5156

5155
C
5157
5250
5252

5253

5255
C
5256
5257
C
 5300
 6000
 6050
 4052

 6053

 C
 6055

 6056
 6057

 6110
 6150
 6152
CCNTINUE
   SET NC OF PHTMTS TO BE READ  IM  FOR EACH TYPE OF
IF(FNCTYP.EC.1)SO TO 5110
IF(FNCTYP.eC.2.OR.CNCTYP.ro.3JGC TO 5111
IF(FNCTYP.EC.4)GO TO 5112
GP TH 5050
LIM = I
GO TC 5113
LIM = 2
GO TO 5113
LI^ = 5
CCNTINUF
LI"1 = 0
LIMl = LI^l  +  I
PP INT 515.1
CALL REACINfFLOTE)
GO TO (5153,5000,5155,5150,5156),   IGOTO
P?INT 5154
GC TC 5152
SPOPlM(litIl»l) =  ANSWER
GO TO 5157
GC TO 5150
   NO DEFAULT  VALUE  FOR  SPCPIN
CONTINUE
PPINT 5251
CALL REACIN(FLOTE)
GO TO (5253,5000,5255,5250,5256),   IGOTO
PRINT t>254
GO TO 5252
GO TO 5250
   NO DEFAULT  VALUE  FOR  SPCPIN
SPOPIN(2tLII*l) =  ANSWER
CTNTINUE
   CHFCK  HC  OF ENTRIES
IF UIM.EQ.LINl)   GO TO  5300
   IF PIECE-WISE  LINEAR  ALLOH
.EG. 5 .OR. ANSWF« .50. 0.
 THiN
)   GO
 IF  UIM1
 GC  TO
 CONTINUE
 CONTINUE
 P^INT  6051
 C»LL P-EADIMFLOTE)
 GD  TO  (6053,6000,6055,6050,6056),  IGOTO
 PSU!T  6054
 GC  TO  6052
    5.  I/TGN-1ILE FROM REF. 7
 TRNCST =  5.
 GO  TO  6057
 TCNCST =  ANSWER
 CCNTINUE
 LIM1  = 0
 Livi  = LI"!  + 1
 PSU
-------
FILE: CVVIMY   F?,MMN   PI                           INTERACTIVE DAT* CORPORATION
6153  P  (WOg-STP  INOCX FOR  MAY 72)/100.  FROM REF. 8
7055  CNSTRC =  1.714
      GC TO 7057
7056  CNSTRC =  ANSWER
7057  CONTINUE
7150  PF IMT 7151
7152  CALL REACIN(FLOTE)
      GO TO 47153,7000,7155,7150,7156),   IGOTO
7153  PMNT 7154
      GO TO 7152
C        1.176  f-RCM REF. 9
7155  MATfLS *  1.176
      GO TO 7157
7156  MATRLS *  ANSWER
7157  CONTINUE
C
C        FND C* SUBROUTINE CMWNTY
      RrTURN
      END
                                    184

-------
FILF: C7NCST   FGF.TPA'J   PI
                                            INTERACTIVE  DATA  CCSPOSATION
      SCBRHUTINF CCKCST
C
c
C
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
   CflNCST COMPUTES CONSTRUCTION COSTS FOR EACH  PROCESS

   NOTE: FCR MOST PROCESSES THE EQUATIONS A*E FROM
                                            10
       BLOCKS:
   LSPCST - COST OP LA30R

   SCHEME - INFO ABOUT LIQ'JIO TRFATMENT  SCHEMES

   TIME  - TIME HORIZON  IN=0<>M£TIGN

   TPLANT - CHARACTERISTICS OF  TREATMENT  PLANT  PROCESSES

   TSTCST - TREATMENT COSTS

   TSCST  - TIME AND SPACE DIFFERENCE  COSTS


CALLEC BY:

   TRTMNT - THE MAIN SIZING AND COSTING  ROUTINE


REFERENCES:
AUTHOR:
   DAVID A.
BARNES 30 NOV 72
      CCMMCN  /LBPCST/ DHR, IOFRAC, GOVF<=


      REAL  ICFPAC


      COMMON  /SCHEME/ SCHEME I 25,25), ELG9TY(2r>» MINEFP125).  VAXSCM

      I  ,  ALPYPSf  FCPYPSt FCLMPSt LI"FPSt ALPYFBt FCPYFBi FCLMFP,
      2  t  ALUMA6,  FECL49, NAALAB, AL4B«P, FCABMr, NAABMF, ALUMTFt  FECLTF

      3  ,  ALTFNF,  FCTFMF, ALFBASt FCFBASt L1FBAS, L2FBAS, NONE
      4  f  FQUIPCtSI


       INTEGEk ELGBTY, EQ"JI«>f SCHEME

       INTEGER ALPYPSt FCPYPSt FCL««PS. ALPYFBt  FCPYFfl,  FCLMF3t ALUMA3
      1  t  FECLA8,  ALA«3MF, FCABMF, ALUMT^t FECLTF, ALTFMF, FCTFMF,  ALFBAS

      2  ,  FCFBAS
       REAL  MINEFP


      CCMVON  /TIVE/ NOYRS, MAXTP, TPSIZ6,  TP


       IMTFGER TP


       COMMON  /TPLANT/
1
2
3
*
5
6
7
8
9
RWPUMP,
MCHAER,
RE-2PMP,
VACPTfl,
PPCRB2,
C02FS t
PNA^E ,
HVAP, t
MAXP
PRET^T,
FLCCCP,
GRVTKNf
CENFUG,
TERSTL,
NAALPS,
/MPATt,
PPA-.M ,

PRMSET,
SECSFT,
FLOTKNf
MHINC t
TE^ST2,
PCKLFSf
AMLIFE,
BASE t

PS^U«*P,
RfclPMP,
AN A DIG,
FBINC ,
AL'JMFS,
NAQHFSt
l>Pi*M t
APVAR t

TRKFTft,
CleEEO,
AE^DIG,
WSPONO,
FECLFS,
RECALC,
PVAP .
PAP MX t

AERBSN,
CLBASN,
DRY^ED,
SLGOCN.
LIMEFSt
FLOCCT
WOPARH,
MINPV t

OIFAIR
MULFTR
SLOTNK
RECPBl
POLYPS

WPAOM
MAXRV

                                     185

-------
 CILE:  C'lNCST   CGRT&A-VJ   Pi                            INTERACTIVE DA T \  COR POP AT ION
                                                 TRKFTR ,
      1  ,  CICMR| FLC'CCP,  SrCSF.T, ^ETP^P, CLFrEl1,  CLBASN, RE?PMP
      2  ,  CRVfKh, FLCTKN,  ANACIC, A^OIO, DOY^SO,  SLOTNK, VA^.FTR
      3  ,  CENFUG, FBIMC  ,  WSPOND, SLGCCN, RECFP1,  RrC»B2, TERST1
      4  ,  TE^ST?, *LUV1CS,  F£CLCS, POLYPS, CC2FS ,  PCKL^S, RECALC
      5  ,  PNi«E , JMCAT&i  A^LIFE, °PARv  , pvA1?   ,  WOPARM, WPAPM
      6  i  V»VA=   , PPAKM  i  FLCiCCTt BASE   , A°VAR ,
       COMMON /TRTCST/ OMHO'i ( 
C
C         PRELIMINARY TREATMENT
6030   1C  < TPL ANTt 9P4RM, PP.ETRT)  .LE. 0.)  00 TO  6050
       X = ALOG(TPLANT(9P«RH|PRETRT))
       CONCDS(PRtTRT)=EXP(3.2597l6*.6l915l«X)
C
C         PRIMARY SETTLFR
605C   IP  ING
6070   1C  < TPL ANT ( PPARw.PSPU'-IP)  .LE. 0.)  GO TO  60
-------
FILE: CQNCST   FORTRAN   PI
                                                     INTERACTIVE DATA CORPORATION
6110   tc  (Tf'LiNTtSPiSM, ATR3SM)  ,L = .  0.)   GC TO 6130
       X * ALOG(TPL AKT (Ro fls.M, AER4SN > >
C
C        CIFFLSFC AIR  SYSTEM
6130  IF (TPL ANT(BP^M,r>IFAIR)  .L5.  0.)   GC TO 6150
      X = ALPG(TPLANT(«PAPM,OIF A 13))
      COMCOSIDIFAIR)=EXP(4.145454+.633339*X+.031939*X**2-.0024!9*X**3>

C        MECHANICAL  AERATION
6150  Ic 
-------
 FILM  CaNCST   crpTR*N  PI                           INTERACTIVE DATA CORPORATION
 C         Al*  FLOTATION
 6330  IF  ( TPL^r.'TJ PP*=M,FL'JTKN )  .L~.  O.J   GC  TH 6350
       X = AtOG
C
C         VACUU^ FILTER
6430   I^  ITPLANTiecAP^.VACFT?) .LF-. 0.)   GC  TO  6450
       X*  ALOG(TPLANT(BPARH,VACCTR))
       CONCOS( VACFTK) = EXPO.238028 + . L94537* X+. 033313*X**2)
C

6450   IF  (TPLANT(FPAR^,CENFUGI .LE. 0.)   GO  TO  6470
       X »  ALCGITPLANT(RPARf1,CENcUr,) )
       CONCOS(CcNFLG)=EXP(4.528439*.049867*X+.053l98*X**2)
C
C         KULTIPLE-HEARTH INCINERATION
6470   1=  CTPLANT(ePtRM,«HINC  I .LE. O.J   GC  TO  6490

       CONCOSCMHINC )=EXP(2.377364».5989a6*X)
C
C         FLUICIZEC-BE') INCINE"ATION
64<)0   ic  ( TPLANTIPPAR^.FBINC  ) .LE. 0.)   GC  TO  6510
       X «  ALOG(TPLAMT(i
C	      NO  dATA FOU
       C")NCOS(F?INC ) = 0.
C
C         WASTE  STABILIZATION FCND
6510   1=  CTPL ANTlEPA^.wSPQMD) .L=. 0.)   GC  TO  6530
       X »  ALOG(TPL4M
C	      MH  TSTA FOR

C
C         SL'JDGE LAGCCN
6530   1=  ( TPLANT«?PA?M,SLGr)nN) ,LE. 0.)   GC  TO  6550
                                      188

-------
FILE:  C.WST    CGFTFA^  PI                           INTERACTIVE  OA.T4 CORPORATION


       X  =  ALTG( TPLANTJ PP/1P.M, SLG1CN) J
       CmCOSCSLOCfN)  = EXPM. 375449+. 394996*X+.014726«X**2)
c
C         RE-CiRSCMZATION
6550   IP AP«,LIM?«=S) .L = . 0.)  00 TO  6690
       X  =  ALOG(TPLANT(BPA3M,LIMITS))
       CONCGS(LI"EFS)=eXP(-1.900487*.670797*X)
C
C         POLYMER  FEEDING ANO STORiGc
6690   IF  (TPHNTAKy,PCLYFSr .LE. 0.)  GO TO  6710
       X  =  ALOGITPLAN'TtBPASM, PCLYFSM
                                    189

-------
     :  CJNC5T    -TPTPAM  PI                           INTERACTIVE DATA
C
C        CAP.4CN CIOXnF FfETIMG ANO STORAGE
6710   Ic < TPL4NT< pn/^,CD2FS » .L?. 0.)   GC  TT  6730
       X =  AL1G(TDL£\T( R%rtMiCC2(:S  ))
C        ASSUMED SAME tS OIFFLSFC AIR
       CCNCCS( CC?FS )= = XP(4.l45454f..633339'''X*.031939*X**2-.0024 19*X**3»
C
C        SODI'J" UUMINATr P'FDING AND STORAGE
6730   IF AL = S ) .L^:. 0.)   GC  TO  6750
       X -  AL:>G  »  200. *X**. 5 * 1.506/1.2984
C
C        FL^CCtLATICN BEFOPE TERTIARY
6810   IP ITPLANT(BPA?M,FLOCCT) .LE. 0.)   GC  TO  6330
       X =  AL3G(TPLA\T(9P*o.M,cLCCCT) )
C        PQUAMCN  FR01  RF.F. I2i P. 5-6f TA«?LE
       CPNCTS(FLOCCT)  =  EXPC4. 06044*. 56209*X)
6830   CONTINUE:
c
C        Cr>NV?°T NATIONAL  AyfPA3E J4N 71  DOLLARS TO PRESENT LCCAL OOLLA"
C        USING  ^CC-STP  COST INDEX
C        CCMPIJT: FEMJCIC  A^cdTI^co CONSTRUCTION COSTS FOR EACH
C        PROCESS
C
       00 7500 IPrfQC  = lt"iXP
       IF (E3UIPC IP80C)  .EO. nFF)  GG TO 7500
       CONCOS( IFROC) = CONCHSJ IP-»CC) * ( CNSTRC /1.506)  * (l.-GOVFF)
       RATE =
                                     190

-------
FILE: CCNCST   FORTRAN  »l                           INTERACTIVE  DAT\  CORPORATION


      RTON = < l.**4T6)«*TPl ANTI iMLI-Ei IP3CC)
      AMCCST( IP'.'JC) = CONCOSC IPOOCI*CPC*TPSIZE
7500  CCNTINJF
C
C        END Oc SLfle OUTING CONCST
      RETURN
      END
                                     191

-------
      r»T<-,LIv   "C^T-AM   PT                            INTERACTIVE  DAT4  C0=. PHB AT ION


      SlBKO'JTIMt
C
C
C           3TGLI*  INITIALIZES TH£ t NF1_UENT-H4L= 0?  IFLI**T  TO
C           OTRGLI*  R?ACS  IN THE  PROPOSED LEGISLATIVE  LIMITS ON  THE
c           PHCSPH^SUS  CCNTFNT cf DETER^E\TS t\o THC  IMPLEMENTATION
C           TIMES.   pnc  EACH Tl^if P = KIOO TH= INFLUENT-HALF
C           ANC  ThF  CISTS  OF N 3^- PHDSPHiTE SUBSTITUTES  45E  COMPUTED
C           NOT= :   CT5LI"  ASSUMES THAT PY?AR WILL  INCPEASF  EACH
C                   TIME  IT IS PEAO IN.
C
C        CO^CN  BLOCKS:
C           OTRGNT  - CHARACTERISTICS OF OETERGtNTS  4KO USAGE
C           IcLIMT  -  INFLUENT AND EFFLUENT LIMITS
C           PSGCNT  - CONTAINS P*CCF,A*» CONTROL V»»IABLES
C           LICUIO  - LIQUID INFLUENT IMFCdmiT HN
C           SEU?CP  - THE  SFWEREO POPUL4TICN
C           TIME    - PARAMETERS 0? THE TIME HORIZON
C
C        CALLEC  BY:
C           STRTGY  - CONTROL STFAT=GY CALLING ROUTINE
C
C        AUTHOR:
C           04Vn A  B4FNES   11JCT7?
c
c
      CrwMQV /DT^GNT/ OT3GUS, POR4TO, PPRSTO, CIFCOSf  P^ESPC
     i               , PDTRG t ENFCST,  PSu5CS(20)f PCNTNT

      REAL LEGPC

             /IELIMT/ IELIMT(2,?0)
      1 , INF,

      REAL IELIMT
      INTEGER EFF

      CCHMCN /LI3UIC/  ALKI°St  BOOIPSt MLSSAR, NH3IAR,  PINPSt
      1                t  QPEAK,  SSINPSt TB30AR

                   NH3IA3
                       F'JCTYP,  SPC?IN(2t5), SEWPOP<20»
     1 i YEA^, SPCP,  MAXPV

       INTF3E-? YEAE,  S?CP,  CNCTY">
      CC*yCN /P^GCNT/  I30TO,  lA'JS i~ .,  CIXFO, FLQTE, ALPHA
      1  t YESi  IO,  CN,  OFF
      2  t ISCHM
      3  * IC'-I^Y,  C'.
      EQUIVALENCE  I l

      INTEGER  FIXED,  CLOT£,  SLPHi
                                    192

-------
FILE: rir,l
               cC«TPflM   PI
                                                     INTERACTIVE  DATA  CO«Pn»ATION
1010
1951
1954

2051
2054

2151
2154
2251
2254
2651
2654
3051
3054

4051
4054
3510

C
C
c
c
c
c
1000
1500
C
C
1900
1950
19*2

1953

1955

1956
1957
2000
C
      COMMON  /TIME/ NHYRS,  WAXTP,  TPSIZE, TP

      INTEGER  TP

      FCSM«T(1H  ,'OETERGrNT RETSICTIONS1)
      FC?VAT(1H  ,
      FORMAT dH  , *CC  YOU  Wi'.'T TO IMPLEMENT PHOSPHATE OETERfJENT  PESTHICTI
      ONS?  ( Y-:S  Uf-  NO) • )
             (1H
              (If^
     1RGNT)')
      FGPMATI 1(-
      cPRMATdH
             I1H
             ;IH
      FORMATdH
      FCRMATdH   »PC£:sENT  P CONCENTRATION IN CETEP.GENTS  (RATIO)*)
      FORMAT  (1H  ,'PCNTNT=')
      FORMAT  CM  ,'PGOPOSEO LEGISLATED PHCSPHCRJS CONTENT  IN  DETERGENTS
     KFLrAT.FRAO* )
      FORMAT  (lr|  ,«PYEAPsf)
      FORMAT  (1H  f'YEA5  OF IMPLE^cNTATI1N (FLOAT)*)
      FORMAT  (IH  ,'PCNTNT  IS  TOO LAfvGE, PESURMIT PCNTNT  *  PYEAR* )
            •CIFFERFNTIAL  COST BETWEEN OLO E NEW DETERGENT  ( J/LB  OT

            •CTPGUS=«)
            •ANNUAL  PER,  CAPITA OCTfRGENT USE (L BS/CAP/Y",) • )

            •AMN'JAL  PE?  CAPITA ENFORCEMENT COST OF P  BAN  (i/CAP)')
            *"RESPC=*)
   ****************
   ****************
   ***«*********#**
                              START EXECUTION
****************
****************
*************««;*
             >***
CCNTINUE
P^INT  1010
DO  1500 TP  *  l.MAXTP
ISLI^TCINF.TP)  »  PINPS
PSUBCS(TP)  «  0.
CCNTIN'JE

    ASK USER  IF  HE/SHE OESIRSS TO TRY DETERGENT  CONTROL  STRATEGY
'CCNTIN'JE
PhU.T  1<3U
CALL RCACIN(ALPHA)
GO  TO  (1953,1900,1955,1950,1956),  IGOTO
PRINT  1954
GO  TO  t<>52
I/«NSW3 a  NC
GC  TO  1957
CCNTINUE
       IP  (IANSKS  .SO.  YES)   GC TC 2000
       IF  (IANSK*  .EO.  NT)
       GO  TCI  1900
               IN  DETF9GENT
                                     193

-------
FILF: HTGLM    eCRTP.AN   f>i                           INTERACTIVF OST4 CCRPOPATIOM
2050   PC[Nr  205]
2052   CALL =PACIN(FLOT&)
       G'J  TO  ( 2053 ,2000,2055,2050,2056) ,   IGOTG
2053   P=MMT  2054
       GC  TO  2052
C         .0?  */LB  cp^M  5FF. l.»P. 15 AMO  "-PP  II.
C         ASSUMING  TH5T  1  13 OF D€TERGF.NT  CONTAINS  0.4 LB OP PHPSPHATE OK
C         ITS  SUBSTITUTE
2055   DISCOS  =  .02
       GO  TO  2057
2056   CIPCOS  =  ANSWER
2057   CONTPJJP
2150   PPINT  2151
2152   CALL PE4CIN(CLCTF)
       GO  TO  (2153,2000,2155,2150,2156),   IGOTO
2153   PRINT  2154
       GO  TC  2152
C         27  L8S/CAPITA/V=4R F^CM P-EF. 2
2155   OTRGUS  =  27.
       GC  TO  2157
2156   DTRGUS  =  AMSKER
2157   CONTINUE
2250   P3INT  2251
2252   CALL R £ AC IN ( FLOTF )
       GO  T'J  (2253,2000,2255,2250,2256),   IGOTO
2253   PRINT  2254
       GO  TO  2252
C         *.40/CAPITA/YEAR  FROM REF. 3
2255   ENCCST  -  .40
       GO  TO  2257
2256   ENFCST  =  AMSWEP
2257   CONTINUE
C         PORATO =  WEIGHT  RATIO Or PHOSPHATE TO  DETERGENT
C         .4 FPCM "EF. 4
       PDRATO  =  .4
C         PPRATO =  WEIGHT  KATIC Or PHOSPHORUS  TC PHOSPHATE
C         .25  FROM  REF.  5
       PPRATO  =  .25
2t50   PRINT  2651
2C52   CALL HPACIN(FLDTE)
       GOTO  (2653,7000,2655,2650,26561,   fGQTQ
2653   PRINT  2654
       GC  TO 2652
C         NEGATIVE  NUMBER  WILL  CAUSE PRESPC=t>DR AT3»PPRATO IN «CTGLIM«
2*55   PRESPC  =  -1.
       GO  TO 2657
2656   PRESPC  =  ANSWEP
2657   CONTINUE
C
C         RF.Ai) IN LEGISLATED PHOSPHORUS CONTENT
3050   P',INT  305'
3052   CALL ° E AC IN ( FL CTF »
       GO  TO  ( 3053 ,10 >0,30->5, 3050, 3056),   IGOTO
305?   PRINT  3054
       GO  TC  3052
                                     194

-------
FILt: OTf.LIM   =ORTSAN   PI                            INTERACTIVE  DATA  CCPPORiTICN


3055  PCNTNT = 99.
      GO TO 3057
3056  PCNTMT = ANSWER
3057  CHNTINUE
C        IF PCNTMT   = 99.,  THEN END OF LEGISLATION DATA SO 3ETURN
      IF(  PCNTNT  ."FQ. 99. )   nfT'JSN
C
C        FEAT  IN  IMPLEMENTATION y^A* ASSOCIATED WITH  PCNTNT
4050  PRINT 4051
4052  CALL = EAriMcLOTn
      GOTO (4053f 1000, 4055, 4C50, '.056),  IGOTO
4053  PRINT 4054
      GC TO 4052
4055  PYEA* =  0.
      GC TO 4057
4056  PYEAR =  ANSV«SP
4057  CONTINUE
C
C        CHANGE YEA" OF IMPLEMENTATION TO  A TIME  PERIOD
      ICTP *  IPYSAft  - SPCPIN(YciP,lll/TPSIZE
C
C            IF PRESENT  P CONC. IS UNKNOWN, USE  ASSUMED VALUE
      IP (PRSSPC  .LT. 0.)   PRESPC = PORATC*PPRATO
C
C        COMPUTE  INFLUENT  PHOSPHC3US RESULTING  F^OM  DETERGENTS IN
C        (PQ'JNOS/tAYI
      POT^G «  OT5GUS/365.  * PRESPC * SEWPOPdl
C
C        COMPUTE  NEW P  CONCENTRATION "ESULTING  FROV  LEGISLATION
      PLEGRT   =  (PRESPC -  PCNTNT  J/fRESPC
      IF  (PLEGRT  .LT. O.I   P3IMT  3510
      PINNEW  = P^PS - t»!>TSG*PLSGKT/(QAV5*a.33l
C
C        COMPUTE  ThF ANMUiL PER  CAPITA   COST  OF NON-PHOSPHATE SUBSTITUTE
      PCOST  *  CDIFCCS*DTRG'JS + tNFCST )*TPSI ZE
C
C        FILL  INFLUENT HALF OF IELIMT
C        AND  STORE SUBSTITUTION  COSTS  FO1*  EACH TI"E  PERIOD
      00 4500  TP  = ICTP,MftXTP
       I6LIMT(INF.TP) * PINNEW
      PSUBCS(TP»  = PCOST * SEWOOP(TP)
4500  CCNTINUE
C        PEAD IN  KEXT LEGISLATED 0  CONTENT
      GO  TO  3050
C
C         ENO  OF  SUBROUTINE OTGLIV
       END
                                     195

-------
FILF: EFCLIM    CCFTFAN   PI                          INTERACTIVE 04Ti CORPORATION


      SLFP.;iuriNf
C
C        PURPOSE:
C           EFFLIM  RfcAOS  IN THE PHOSPH03US EFFLUENT LIMITS AND
C           CONSTRUCTS  THE E=FLUENT-HALC OF IELIMT
C           NOT = :  cF<=LlM  ASSUMES TH4T 'CYEAR' WILL INCREASE
C           fACH  TIME  IT  IS "EAO IN.
C
C        COMMCK  BLOCKS:
C           IELIMT  - LIMITS ON INFLUENT/EFFLUENT PHOSPHORUS
C                   CONCENTRATIONS
C           LIQUID  - LIQUID INFLUENT INFORMATION
C           PRGCMT  - CONTAINS PROCr.A,1'! CJNTRQL VARIABLES
C           SEWOOP  - THE  SFWEPE^ POPULATION
C           TIME  - INFJ  ABTUT THE TIME HCRIZON
C
C        CALLEC  BY:
C           STRTGY  - THE  CONTROL STRATEGY CALLING ROUTINE
C
C        AUTHOR:
C           TAVIO A BARNES   I10CT7?
C
C
      CCMMON  /IFLIMT/  IELIMT<2,20>
     I  i INF, tFF

      REAL  IELIMT
      INTEGER EFF
              /LIQUID/  ALKIPSi  9QCIPS,  MLSSA^, NH3IAR, PINPS, GAVE
     1                ,  QPEAK,  SSINPS,  TBOOAR

      REAL WLSSAR,  NHSIAR

      COMMON  /P^GCNT/  IOOTO,  IANSWB ,  FIXED, FLOTE, ALPHA
     1 , YES, NO, CN,  OFF
     2 , ISCHM
     3 , IDUMMY, DUMMY

      EQUIVALENCE  ( I ANSwR , VJShE* I

      INTEGER FIXEC,  CLOTP,  ALPHA
      INTEGER YES,  CN,
              /S=*POP/  rNCTYP,  SPCPIN«2,5I, SE«POP
-------
F IL F : 2 ' ~ L I v
                                               INTFPACTIV? DATA CC\P0^4TIOS
3054

C
C
c
c
c
c
1000
1500
C
c
2050
205?

2053

2055

2056
2057
C

C
C
3050
3052

3053

3055

3056
3057
C
C

C
C
 4500
 C
 C
              ( 1H
              (Iri

             : ***J
                     LIMIT  I"?LEMENTATIOM (FLOAT)')
   *»**»**«***«=****
   *•»"***«**"****""
                              STt-.T EXFCUTICN
                                                          ****** «**#**«:***
                                                          K,*»r-* ***********
DC 150i> TP =
ICL I'^TI =Fr ,T
CCNTIN'Jt
   PE«0 IN PRC^SED  EFPLUrNT  LIMIT ON PHCSPHQ^US
PRINT ?051
CALL REACIN(FLnTE)
GO TO (2053 (!000, 2055, ?050t2056»,  IGOTO
PRINT 2054
GO TO 2052
CLIMIT =  "59.
GO TO 2057
ELICIT =  AT4SKER
CCNTINUE
   «?ETUON IF  ELIMIT  =  99. = ENC OF DATA
IF lELI^IT  .cO.  99.)  RFTURN
   READ  IN  I^PLE^NTATICN YPA?  ASSOCIATED  WITH ELMIT
PPINT  ^OV.
CALL RE4CIMFLOTE )
GO TO  <3053,1000,3055,3050,3056),   IGOTC
PQTNT  3054
GC TO  3052
EYEA*  =  0.
GO TO  3057
EYEAR  =  ANShE"
CONTINUE

   CHANGE YEAP QP IMPL E *c "IT AT I ON  TO A TI^E  P=RIOD
 ICTP = (EYEAR - SPOPIN(YFAE,1))/TPSIZc
    FILL EFFLUENT H*LF CF  IELIMT
 DO 4500 TP = ICTP.MAXTP
 IELIMT(EFF,TP) = ELICIT
 CONTINUE
    PEAO IN K£XT EFFLUENT
 GO TO 2050
    END OF SUBROUTINE
 END
                                      197

-------
FILf: I'iC>LI*    ^JFTRA'!   Pi                            INTEPACTIVF  DATA
c
C
C            INCLI"'  fcE.irS  IN LFGISL&TFO =ESTP I CTIOMS  CN  INDUSTRIAL
c            pHrsPHOsus  Ef-PUJENT.  TH~ CORRESPGNOING  CHANGES  SRE  THEN
C            MftDF  TO  THE  INCLUFMT-HALF 3F lELI^T.
C
c        CCHMCN BLOCKS:
C            INDSTY  - INDUSTMil EPFL'JENT LEVELS
C
C        CALL?C 3Y:
C            STRTGY  - THE  CONTROL STRATEGY CALLING ROUTINE
C
C        AUTHOR:
C            DAVID A BARNES   110CT72
C
c
              /INOSTY/ INCSTY(3,20l, LEGINP
      REAL  INCSTY,  LEGINP
Q        »*»»»***********

c        **»*»»*».*******    STA^T EXECUTION             ****************
£        **«t*»»a**« * «:«* 4*
r

C

C
C        END  OF  SLBPCUTIN'E INCLIM

      RETURN

      END
                                     198

-------
FILf:  !NTI"r    -nKT->AN  Pi                            I^ERACTIVE  DATi
c
C
c            INT:«F = -AOS  IN  A  OFSCFIPTIJN  oc  THE
C            IT ThE.-J C4LLS  SP = MC  TQ COMPUTE  THE  SEWEPrD PnpiJl AT IOM F -Jr«
C            EACH TIMF PEPIOT.
C            INTIT ALSl'' t-EAOS  IN TH= GOVERNUFNT FJNA^.'CIMO  FACTOR.
C
C         00*"^ BLCCKS:
C            L>?t*
           ****************     STAPT cX£CUTIrlN             ****************
           **-B »»» *********                                 ****************
                                       199

-------
FILE: INTIWE   c:PTpi'.|  PI                           INTERACTIVE OAT4
                                       *»****»
C
1000  CCATtNJc
C
C        PP4D  IN NUMBER DF YEARS  IN  TIM?  hCSI
2050  P"IMT 2051
2052  CALL p=ACiN
-------
FILr: LCHOSfc
                                            INTERACTIVE  DATA  CORPORATION
      SLBPQUTUE  LC»-nS =
C
c
C
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
   LCHDSE "AUKS AS ELIGI3L5 COR CONSIDERATION THOSc  LIQUID

   TREATMENT SCH=MPS KHICH WILL:

   1. &CHIEV? THE DESIRED 1R4IMUM  EFFLUENT  PHOSPHORUS  LEVEL

   2. ACHIEVE A LEVEL GLOSS TO THAT  DESIRED.
COMMCN BLOCKS:
   PRGCNT

   LICUIO

   SCHEME

   TIME

   TPLAMT


CALLED 3Y:
            LIMITS CN I NFUJENT/ tF FLUENT  PHOSPHORUS

            CONTAINS PROGRAM CONTROL  VARIABLES

            LICUIO INFLUENT  INFO

            IMC0 ABOUT LlCLJIC  TREATMENT  SCHEMES

            INFO ABOUT T!"=  HORIZON

            INFO ABOUT TREATMENT  PLANT  PROCESSES
          - THE MAIN
AUTHOR:
   DAVIH A BARNES
                    28 0":C 72
              /IELIMT/ IELIMT(2,20)

          INF,  EFF
       REAL  IELIHT

       INTEGER EFF


       COMMON /LIQUIO/
              ALKIES,

              QPEAK,
                               SSINPS,
MLSSAR,

TBODAR
                                      NHSIARt PINPSt GAVE
       REAL MLSSAR, NH3IAR
       COMMCN /PKGCNT/ I GOTO, IANSWP, FIXED, FLOTE,  ALPHA

      1 t  YES. NTi CN, Occ

      2 ,  ISCHM

      3 f  IDUM-Y, CUMMY


       EQUIVALENCE ( IANSW* , ANSfcEP.)


       INTEGER FIXED, FLOTE, ALPHA

       INTEGER YESt CN, OFF


       COMMON /SCHEME/ SCHEME 125,25), ELGBTY125),  MINEFPC25).  MAXSCM

      I ,  ALPYPS, FCPYPS, FCLMPS, LIMEPS,  ALPYFB,  FCPYFB, FCL^FB, LIMEFB

      2 ,  ALU^AB, FF.CLAB, N»ALAR, ALABMF,  FCABMP,  NAA«?HF, ALUMTF, FECLTF

      3 t  ALT-MF, FCTFMF, ALC3AS, FCFBAS,  L1FBAS,  L2FBAS, NCNE
       INTEGER. ELG8TY, E<3UI»,  SCHF*«5
       INTEG!=» ALPYPS, FCPYPS,  FCL^PS,  ALPYF3,  FCPYFB, FCL^F'J, ALUMA3

      1 , FECLAB, ALA9MF,  FCAB"F,  AL'JMTF,  FECLTF,  AL^FVP, FCTFMF, ALFBAS

      2 t FCF3AS

       REAL MINEFP
                                      201

-------
                  PI
INTERACTIVE OAT^t CC3PORCT I O'J












CPHVCN /TirF/ rJYRS, ViXT?, TPSI?f. TP
INTfG^-. TP
criMON /TPLANT/ TPLANT( 16,45)
1 , FWP(JWP| P3ETRT, °RMSETi PS°'JvPt T"KFTR,
2 , McmEa, FLTCCP, SPCSET, RF.IP.MP, CLFEEr/,
3 i RE2PMP, G3VTKN, FLDTKN, AN49IG, AEPDIG,
4 , VACFTR, CENFUG, «MI MC , F6I.NC , WSPONO,
5 , PECSE2, T-R5T1 , TERST?, AL'J^FS, CECLFS,
6 , C02FS , N4ALFS, PCKLFS, NA1HFS, RECALC,
7 , PN«'1E , *^PATfi A"LIFE» PPARV , PVAF. ,
8 , WVAO , np/fcH , 64SE , APVAF. , PAP.MX ,
<3 , MAXP



AERBSN, DIFAIR
CLSASN, MULFTR
HPY3ED, SLOTMK
SLGOGN, RECKB1
LIMEFSt PCLYFS
FLOCCT
WOPARM, WPARM
^IIN'JV , M6XRV

INTEGER P*PUWF, PRETkT, PRESET, PSPUMP, THKFT* t AERBSN






C
C
c
c
c
c
1000


1500

C
c


2000

C
c
c




3000
C
C
C
i , DICAIC, FLPCCP, S^CSET, C.EIPMP, CLFEEO,
2 , GRVTKN, FLCTKN, ANACIG, AE3EIG, CRYBEO,
3 , CFNFUG, F^INC , XSPOMDi SLGOCN, PECRB1,
4 , TE3ST2, ALUMFSt FECLFS, POLYPS, CC2^S ,
5 i PNAME , AMRATE, AMLIFE, PP&RM , PVAR ,
6 , WVAR , 6PARM , FLOCCT, BASE , APVAR ,
»*t*B«*»*»t«-»*5*******<-*»»**************
*****4**»*»**#** STAPT EXECUTION
****»*r»*****«**
***«****»**************«'********* *******

CONTINUE
DO 1500 ISC = It^AXSCM
ELGeTYdSCI = OFF
COMINUE
EFPMIN = 99.

FIND NINIfUM PHOSPHORUS EFFLUENT DESI?.EO
DO 2000 TP = l.MAXTP
IF (IELICT(EFF,TP) .LF. FFP^IN) EFPMIN = t
CONTINUE
DELMIN = 99.

SEARCH ALL LIQUID T"»FATMENT SCHEMES FC*
EFFLUENT LEV^L ATTA INA3 I LTY CLOSEST TO °
DC 3000 ISCH = l,l"^XSCv
HELTA = l»ISEPP( ISCH) - ECP"IN
IF 
-------
FILE:  LrHCSf    FORTRAN  PI                            IMTE&ACTIVE OAT* CO=PO°.ATION
       SCHfMf ( ILIQ.ISCH) -
       IF  (TPLANT
-------
FILC: LSKTST   FCRTkA'l   PI                           INTERACTIVE DATA CORPORATION


      SUPPOUTIN5 LSKCST
C
c        PU°POSE:
C           LSKCST CHOOSES  A  LtOUID  SINK WITH A LARGE ENOUGH
C           ASSIMILATIVE  PHOSPmRUS  CAPACITY.  IT THEN COMPUTES THF
C           PUKP ANC PIPE REQUIRE ME'JTS.   AND THEN CALCULATES THS COST
C           OF THE SINK  PIP  FACH  TI'^E  PERIOD.
C
C        COMMON BLOCKS:
C           ENGCST - DELIVERED  COSTS OF  ENERGY FCR^S
C           IF.LIMT - INFLUENT/EFFLUENT LIMITS
C           LICUID - LIOUID INFLUENT IMFCRKATICN
C           LSINK  - CHARACTERISTICS OF  LIQUID SINKS
C           PRGCNT - PROGRAM CCNT*1L VARIABLES
C           SEWPOP - THE SEWEREO  POPULATION
C
C        CALL=C BY:
C           REMOVE - THE MAIN PRCS, MLSSAR, NH3IAR,  PINPS,  GAVE
      1                , OPEAK,  SSINP?, TBODAR
       REAL  MLSSAR,  NH3IAR

       CCMMON  /LS^K/ LIQSNK(3,201, LSNKCSI20I, BESTLS(20J

       REAL  LISSNK,  LSNKCS
              /PRGCNT/ IGCTQ, IANS»
-------
FILF: LSKCST    FORTRAN  PI


C
£        ****************
C        »*««»»**»»**«***
C        ********+******»

C
C
C        END OF  SUBROUTINE LSKCST
      RETURN
      END
                       INTERACTIVE DATA CCRPCFATION
ST4PT EXECUTION
                           ««****** *****«*^
     206

-------
         .'.f. T
                                                      INTERACTIVE  CAT4 COrPOATION
       SU6r~!UTINE  PLANT
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
       "L4NT RFAOS IKJ VALUES Cc  VARIABLES  WHICH DESCRIBE THE

       SEWftGE Ta=ATMf.NT PL&KT.

       NOTE: THE ASSUMFO WLU5S  PC&  'APVAP',  'MINRV't AND

       ARE FCCM *EF. 10.


       MCN BLOCKS:

       CHKCST - CONTAINS DELIVERED CCSTS OF  CHEMICALS

       PRGCKT - CONTAINS PROGRAM CONTROL VARIABLES

       TPLANT  - DESCRIPTION fie  TFcATMENT  PLANT
    CALLED BY:
       SYSTEf


    AUTHOR:

       DAVID A BAPNES    060CT72
              / CHPCST/ LI«OCSt ALUMCS .  POLYCSt  FECLCSt NAALCSt PCKLCS

                     , NAOHCS, C02CS
       P«=AL LIMECS, NAALCSt MACHCS
 CCMKC'J /PF.GCNT/  IGOTO,

1 , YES, NO, CNt  OFr

2 t ISCH"

3 t IOUXMY,
       EQUIVALENCE ( I ANSHP .ANSWER )


       INTEGER FIXEC, FLCTE,  ALPHA

       INTEGER YES, CN, OFF
              /TPLANT/ TPLANT ( 16,^5)
                                       FIXED,  FLCTEt ALPHA
1 ,
2 t
3 t
4 ,
5 ,
6 ,
7 ,
8 ,
Q ,
RWPJPP,
VCHAEF,
PE2PMP,
VACFTR,
PECRB2,
Cr12FS ,
PNA-4E ,
KVAR ,
MAXP
PRF.TRT,
FLCCCP,
GRVTKN,
C5NFJG,
TErSTl,
NAALFS,
AMRATE,
B°#RM ,

PR SET,
SECSET,
FLOTKN,
MHINC ,
TEBST2,
PCKLFS,
AMLIFE,
BASE ,

PS°UMP,
RFipju-p,
ANADIG,
FBINC ,
ALUMFS,
NiOHFS,
PP4RM ,
APVAP ,

TRKFTR,
CLFEED,
AERDIG,
WSPONO,
FECLFS,
RECALC,
PVAR ,
PARMX ,

AER3SN,
CL9ASN,
DRY3EO,
SLGOCN,
LIMEFS,
FLOCCT
WO"ARM,
MINRV ,

DIrAIR
»
-------
PILE:  PLA'T     FCCTf4N  PI                           INTERACTIVE CATA CORPORATION
 1010   FOP" AT ( 1 HO, 'QfSCC I PT ION Or PB5SE*iT  TREATMENT  PL^NT1//
      1  •  Scl  OPF.FftTING M4NLIAL F JP ni«FNS!CNS  OF  PAR^.ETEkS FTS EACH PROC
      2FSS' I

 2i5i   FORMAT  IH  ,»PP4~M=M
               H  , 'PRESENT INDEPENDENT SIZING  PARAMETER FOR COSTS')
1351
       FORMAT
1551
       FORMAT
275'   FORMAT
IH
IH ,'AMCmiZATnN P-ATfc  FCR  ALL  ECUIPMF.NT TO 35 BUILT')
IH ,'AKLIFE='I
IH ,'AMORTIZATION LIFETIME  FOR  ALL  EQUIPMENT TO RE BUILT")
IH ,«PVAS=»)
275'.   FOP"'AT(1H ,'PRESENT DESIGN PARAMETER1)

f         *»»»*»***»*»«»*«*«**»«'*»**««*****»*«*»*«t
^         ***rt *»*»*«.******                                ****************
C         ***n»*******«***    START EXECUTION             ****************
C
C
C
1000   CrNTI.MME
       PRINT  1010
C
C         RK40  IN AMORTIZATION e\T=
1350   PRINT  1351
1352   CALL R€ACIN(CLOTEI
       GO  TO  (1353,1000, 1355, 135f), 1356) ,   IGOTO
1353   PRINT  135<*
       GC  TO  1352
1355   4RATE  =  .05
       GO  TO  1357
1356   APATfc  =  ANSUFR
1357   CCNTINJ5
C
C         FtAD  IN AMOP.TI ZATIG^ LIFETIME
1550   PRINT  1551
155?   CALL REACIM "L'JTE I
       GO  TO  <1553 ,1000, 1555, 155l>, 1556) ,   IGOTQ
1553   PRINT  155*
       GC  TC  1552
1555   4LIer  =  20.
       GC  TO  1557
1556   ALIFF  =  ANSfc£P
1557   CCKTINUE
       DO  1900  IPRCC  =  1,MAXP
       TPLANT< AMP.ATE, IPROC)  * ARATE
       TPLANT(AML IFE,IPRQC)  = ALIFE
       TPLANT(PV4R,IP50C)  =  TPLANT(APVAR,IPROC)
1<300   CONTINUE
C
C         PE^^  IN PARAMETERS FCR TREATMENT PROCESSES
       00  3000  IPROC  »  l.MAXP
       POINT  2010,  (TPL4NTUf 1PR3C),J = 1,3)
r
C         READ  IN PRESENT  INDSPESDENT  SIZING PARAMETER
2150   PFINT  2151
                                     208

-------
FILF
               CDRTRAN  PI
                                              INTERACTIVE DATA CORPORATION
2152

2153

2155

21*6

2157

C
C
2750
275?

2753

2755

2756
2757
3COO
3500
C
C
C
C
C
C
CALL
GO TO «2153, 1000, 2155, 215J, 2156) ,  IGTTO
PRINT 2154
GO TO 215?
TPLflNTCPPARP, IPROC) » 0.
GO TO 2157
IF (ANSWER  .EO. <59.)  GO TC 3500
TPLANTCPPARf , IPPOC) = A\SWFR
CCNTINUE
IF 
FECLCS = TPLANT(PVAR.PECLFS)
LIMECS * TPLAMT
-------
FILE:  F.E/iOl\    FCRTRAM  PI                          INTERACTIVE  DATA  CORPORATION


               NE  REA3INC ITYPE)
C
C
C            REJOIN REA1S IN ANSWERS INP'JT SY THE USER.   tFTEH
C            EXAMINING THF  VALUF TY»EO iNt THE S'JBROTUIN?  SETS  *IGOT1»
C            S3  THAT ON RETURN TO TH= CALLING ROUTINE A CORRECT
C            PRANCh CAN OCCUR.  (USING "IGOTO* AND A COMPUTED GO  TO
C            IS  A  CLUMSY WAY OF GETTING AROUND THE IMCCKPAT IB IL IT I ES
C            BETWEEN I3M ANO CPC WITH RESPECT TC MULTIPLE  RETURNS
C            «=RCM  A SUBROUTINE.)
C            I TYPE  HAS A VALUF 0^ :
C             FIXED = 1 = INTEGER VALUE IS EXPECTED
c             FLOTE = 2 = BLOATING POINT VALUE EX°ECTEC
C             ALOHA - 3 = ALPHANUMERIC EXPECTED
C            IGCTC  CAN BE SET Tp:
C             1  =  PRINT FULL EXPLANATION OF QUESTION IF A  *Q* WAS  INPUT
C             2  =  GO TO BEGINNING OF CALLING SU8RQTUINE IF  A  *M*  WAS
C                 INPUT
C             3  -  USE ASSUMED VALUF OF VARIABLE IF AN *A*  WAS INPUT
C             4  =  REPEAT E°.IEF QUESTION 3ECAUSE INCORRECT  VALUE
C                 hAS INPUT
C             5  =  CORRECT INPUT, F.ET'JRN AND CONTINUE PROCESSING
C
C        COMVCN BLOCKS:
C            PRGCNT - PROGRAM CONTROL VARIABLES
C
C
c
C
C
C
C
C
C
C
C
C
C
c
      COMMON  /PRGCNT/  IGTTO, IANSW( FIXED, FLCTE, ALPHA
     1 , YES, NO,  ON,  0"
     2 , ISCHM
     3 , ID'J^Y,  CUMVY

      EOUIV«LENCE  ( I ANSWP , ANSWE' )

      INTEGF^ FIXEC, FLCTE, ALPHA
      INTEGER YES,  CN, OFF


      CIMENSICN ISTCStdOl
      REAL*S  INTYPF, M/1HM/, C/1H3/, A/IHA/
      LOGICAL*! D<8)
C        D  IS A ?U^^Y  V^IA^LE TC ALLOW US T0 COUNT BYTES
      INT£G£R*2 ITF^P, ID=C/l"./, I3L4NK/1H /, NEG/1H-/
CALLED BY:
CVMNTY
OTGLIM
E<=FLIM
INDLIM
INTIME
PLANT
SEWAGE
AUTHGP:
DAVID A

- READS
- REAOS
- READS
- READS
- REAPS
- F.EAOS
- READS

3ARNES

IN
IN
IN
IN
IN
IN
IN



DESCRIPTION OF
REST* ICTIONS ON
EfFLUENT RESTRI

COMMUNITY
DETERGENT
CTIONS OF


PHOSPHATES
PLANT
INDUSTRIAL EFCLUENT RESTRICTIONS
Tl«E HCRIZQN
DESCRIPTION OP
DESCRIPTION CF

130CT72

TREATMENT
SEWAGE



PLANT



                                    210

-------
FILf:
               =fPT3AN  PI
                                                     INTERACTIVE  DMA  CCR"OP AT I ON
     1 , NUMS( 10) /lHOf 1H1, IH2 , 1H3? lH4,lH5flH6, lH7ilH8f IH9/
C        THE CCMMCN  'JUS«/yt  j 5 ijs = n  TC  p^CE  CONSECUTIVE  STORAGE  IF
C         THS  JURE1!
      COMMON

2010  FPf»WAT< Afl)
                     D, INTYPE, ITFMP
C
C
C
C
C
C
C
2050
C
 2C70
 C
 3COO
 C
 4COO
 C
 C
 C
 C
 C
 C
         ft****************************** ****** ft*?*** ****** **************
          **«****<-****«4*t
                              START  5XECUTICM
                                                         ****************
                                                         ****************
 4030
 C
          READ  IN INPUT VALUE IN *4* FOPMAT
      READ  (5t2010tEND=5000) INTYPE
          CHECK  FOR 1ST ANH CNLY CHARACTER EQUAL TO *0*t *»<*t OR *A*
       IF  I INTYPE .NF.  Q»   GO TO 2050
          RETIJRK TC PRINT  FULL EXPLANATION QF QUESTION
       IGOTO =  1
       RETURN
       IF  (IMTYPE .ME.  *}   GO TO 2070
          RETURN TO BEGINNING CF CALLING SUBROUTINE
       IGOTO -  2
       RETURN
       I=( INTYPE .N?. A)  G3 TO 3000
          RETURN TC USE ASSUMED VALUE OF VARIABLE
       IGOTG *  3
THEN RETURN
       CCNTIN'J5
          IF ALPHANUMERIC INPUT WAS EXPECTECi
       IF tITYPE .NE. ALPHA)  GC TO 4000
       ANSWER * INTYPE
       IGOTO » 5
       RETURN
       CONTINUE
          CONVERT *A* FORMAT NUMBER  READ  IN  TO  AN INTEGER OR
          FLOATING NUMBER

       NSIGN » 0
       1PLACE * 0
       ITEMP » IBLANK
          DETERMINE NUMBE" Oc  CHARACETERS TYPED INt VALIDITY OF
          CHARACTER!  AND  START  CONVERSION
       CO 4200 I - S,J6
           SHICT BYTE TO  LFFTMCST  POSITION OF ITEMP
       0(17) * C(I)
          CHECK FCR NEGATIVE  SIGN
       IF UTEMP .NE. NEC)   GC TO  4030
       NSIGN » 1
       GO TO 4200
       CONTINUE
          CHECK FOR BLANK MEANING  END OF
       IF (IT^MP .EQ.  ISLANKJ   GO  TO 4300
          CHECK FOR DECIMAL  PCINT
                                      211

-------
 FRF:  «FADI\'    FORTRAN  PI                           INTERACTIVE OATI CORPORATION

       IP  (ITS'tp ,N5.  IQ£C)  <-,o TC
       IPLiCF  = 1-8
       Ic  (ITYP? .FQ.  CLCTE)   GC TT 4200
          ERR1R -  OECIHiL  POINT IN AN INTEGER
       IGOTO  =  4
C         CHECK  FOR VALID N'JMEOJC C
4040   03  4100 J =  1,10
       Ie  UT6MP . EQ.  N'JVS
-------
FILF: REMOVE   FCRTP4M   P!                           INTERACTIVE DATA CCfPOP. AT ION
C
C
C           THIS  IS THE  MAIN  PROGRAM.  IT  USFS A COMPLETE DESCRIPTION OF
C           A COVyWITY  AMD  A DESI&50  (INPUT BY USER) PHOSPHORUS CCNiTROL
C           STRATEGY  TO  COMPUTE  THE COSTS CF DIFFERENT TREATMENT SCHEMES
C           •JHIO  ACHIFVE  A  GIVEN PHOSPHORUS EFFLUENT LEVEL. A REPORT  C'J
C           THE CCSTS FQC  EACH SCHF^E  IS  THEN PRINTED.
C           NOT1;  I! THIS P^CGPA" WAS DESIGNED TO "UN ON AN I«M 360/67
C           TIMr  SHfKINj SYSTEM.  S°EC I FI CALL Y, TH4T OF, INTERACTIVE
C           DATA  COfP.t  WALTHtw, MASS. < 6 1 7-890-1234 ) .
C           * CORE SIZE  OF 28flK  3YTES  WAS REQUIRED FOR EXECUTION.
C           NOT?  2: THE  BASIC STUCTIJGE CF THE COST EQUATIONS WAS TAKEN
C           p!
-------
 PILE: RevrvF    PCRTKAN   PI                           INTERACTIVE DAT*


 c
 C            7.  MYSFLF
 c
 C            8.  'SEWAGE  TPb'ATMFNT  PALNT CONSTRUCTION COST  INDEX',  *PA-
 C               OFFICE OF  WATER  PROGRAMS.
 C
 C            9.  'WHHLESALE PRICES  AND PRICE INDICES  - INDUSTRIAL
 C                CPrtfdQITieS'i U.S.  OEPT.  OF LABOR.
 C
 C            10.  'COST2',  A  COMPUTER PROGRAM BY RICHARD EILERS OF
 C                EPA-CINCIWATI, OHia.  'COST21  COMPUTERIZES THE GRAPHS OF
 C                REFERENCE 6.
 C
 C            II.  PRIVATE  COMMUNICATION  WITH W.C. KRUMRI OF PROCTER
 C                £ GAMBLE, CINCINNATI,  OHIO (513-562-2859) ON 6 SEP 72.
 C                HE  SAID  THAT ANY  NUMBER  FRC* -.05IFOR  SOOIUM CARBONATE!
 C                TO  +.26{FO»  CITKIC  ACIOI  W&S VALID  BECAUSE NO ONE
 C                SU3STANCF HAS BEEN  ACCEPTED AS A PHOSPHATE SUBSTITUTE.
 C
 C            12.  'PROCESS  DESIGN MANUAL FOR PHOSPHORUS  REMOVAL1,
 C                BLACK C VEATCH, CONSULTING ENGINEERS,  £PA PEPCW
 C                NO. 17010-GNP.
 C
 C            13.  'COST AND PERFORMANCE  ESTIMATES FOR TERTIARY WASTEWATER
 C                TREATING  PROCESSES',  SMITH, ROBERT  AND MCMICHAEL, HALTER
 C                F., EPA-CINCINN4TI,  OHIO,  JUN  69.
 C
 C            1*.  'EMPLOYMENT  f. EARNINGS STATISTICS - WATER, STEAM,
 C                C SANITARY  SYSTEMS  (SIC  V»4-*97I«,  U.S. DEPT. OF  LA90R.
 C
 C            15.  'PRFLIMIN4RY DESIGN  AND  SIMULATION  OF  CONVENTIONAL
 C                WASTEWATER  "^NOVATION  SYSTEMS  USING THE DIGITAL
 C                CCMPUTER',  ROBERT SMITH,  EPA-  CINCINNATI, MAR 68.
 C                THIS REPORT  PROVIDES  A THEORECTICAL BACKGROUND FOR
 C                REFERENCE 6.
 C
 c        NUMEPIC CONSTANTS:
 C                .020825  -  POUNOS/GAL  FOR  LIQUID POLYMER
 C                .029     »  ASSUMED  RATIO  CF TRICKLING  FILTER SLUDGE
 C                          WASTING  STREAM  VOLUME TO INPUT VOLUME
 C                .075     »  PCCNDS OF  AIR/CUBIC FOOT
 C                .123     »  POUNDS OF  C02/  CUBIC FOOT
C                .125     *  ENOC1ENOUS  RESPIRATION CONSTANT AT 20C
C                .232     *  BOUNDS OF  02/  POUND OF AIR
 C                .4902    *  PCUNDS/GAL  FOR  LIQUID ALUM
C                .6        ASSUMED  FRACTION Oc MLVSS WHICH ARE ACTIVE
 C                .7       * ASSUMED  RATIO  OF MIXED LI3UCR  VOLATILE
 C                           SUSPENDcO  SOLIDS TO *LSSA<*
 C                .7457    *  KILP4ATTS/HORSEPOWER
 C                1.5Q6     =  WOO-STP  INDEX  FCP JAN 71 NATIONAL AVERAG= %
 C                2.27      *  POUNDS Oc  FFCL2/POUNO OF FE
 C                2.6       »  POUNDS/GAL  FQR  CECL2
 C                2.8S      *  i>CUNO  OF  FECL3/ POUND Oc FC
 C                3.95      *  POUNDS/GAL  FOR  FECL3
 C                4.22      *  POUNDS CT= NAAL/POUNC Oc  AL
                                    214

-------
FILE:
                        PI
                                            INTERACTIVE DAT\  CORPORATION
C
c
C
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
       5.4

       5.4
       6 .
       7.48

       8.33

      11.

      ?4.

      30.

      60.
     180.


     365.
PCUN'JS/G*L FOR ALUM
(ASSUMED) PCUNOS/GAL FOR NAAL
ASSUME1!) OcPTH CF TRICKLING  FILTER
GALL1MS/CU3IC "90T FQC WATER
PCUNOS/GAL FOR WATER
POUNDS OF ALMM/POUNO OF AL
HOURS/DAY
DAYS/M3NTH
                                  MEDIA
    2000.
   43560.
ASSUMED CONCENTRATION OF SUS^END^D SOLIHS
TRICKLING FILTER SLUDGE WASTING STREAM
OAYS/YFSR
MINUTES/OAY
PCUNOS/TON
SQUARE FEET/ACRE
AUTHCR:
   TAVID S BA'NES   09 FEB 73
   SCNSLD CRNEH
   JPF SCIENTIFIC CORP.
   2 PAY AVENU?
   aUPLINGTON, *!A  01803
   (617-273-0270)
      COMMON  /PRGCNT/  I GOTO ,  IANSWP,  FIXED, FLOTF., ALPHA

      1  t Y5S,  NO,  CN,  Occ

      2  , ISCHM

      3  t IOUVMY,
      EQUIVALENCE  ( IANSWS , ANSWER )
       INTEGER
       INTEGER
     FIXED, FLCT-,
     YES, CN, OFF
 ALPHA
      CPMMCN  /PRNTR/  ISHCKT,  ISUPER, ISKIP, IPASS, ISELCT(5)
       COMMON  /SCHEME/  SCHEME{25,25), ELGBTY(25),

      1  ,  ALPYPS,  FCPYPS, =CLMPS,  LI^EPSt ALPYPB,
      2  ,  ALUMAP,  FECLA9, NAiLAB,  ALAfiMF. FCA5««F,

      3  ,  ALTFKF,  FCTF^F, ALF3AS,  FCFBAS, LIFSAS,
      4  ,  FQUIP145)
                                         MINEFPC25),  MAXSCM
                                                 FCLMFB,  LIMEFB
                                                 AL'JMTF,  FECLTF

                                         L2FBAS, NONE
       INTEGER  ELGPTY,  6CUIP, SCHEME
       INTfGE"  ALPYPS,  CCPYPS, FCLMPS, ALPYF3, =CPYFB, FCLMC3, ALUMA3
      i  ,  FECLAB,  ALABMF,  FCAB^F, ALUMTF, FECLTF, ALTFI-F, FCTFMF, AL=RAS
      2 ,  FCFPHS
       REAL  MINEFP
 1010   FORMAT  IIHO.'THIS is THE PHOS°HCSUS REMOVAL MODEL*)
 6551   CORMAT  (IH ,'S=LECT?'»
 6554   FORMAT  (IH .•OU YOU WISH 4 SELECTED LONG PRINTOUT?  (YES OR N0»«)


 6754   CDR"AT  ( IH ,»MJM?ER QC SCHEME TO BE LHNG PRINTED  (FIXED)1)
                                     Z15

-------
 FILE: orvpvr    COET3AN  °1                           INTERACTIVE DATA CORPORATION
 7651   =3^MAT  ( 1HO, •
 7854   rns.vflT  (IHO.'CC  V.1U WISH TC TSY ANOTHER CONTROL STRATEGY (YES OR N
      10) •)
 9010   FORMAT  
                                    216

-------
                  Tii-j  PI                          INTERACTIVE DATA CORPORATION


      GO TC 6^52
6555
      GT TT 6S57
C556  CnNTINUc.
6557  CONTINUE
      je (IANSW9 .FC. YES)  r.C TC 6700
      IF (IANSV>B .EQ. MO)  GC TC 7BOO
      GO TO fcSCO
C
C        S?T UP SELFCTfO LONG PRINTOUT
6700  CONTINUE
      isnrm = CCF
      ISUP5R = OFF
      ISKIP = CPF
      OC 6600 1-1,5
      ISELCT(I) = 0
6600  CONTINUE
      LIM  * 0
6710  LI*  = LI? *  I
6750  ORIKJT 6751
6752  CALL * c AT. IN ( F IXEO )
      GO TO (6753,1000,6755,6750,6756),   IGOTO
6753  PSINT 6754
      GO TO 6752
6755  ISELCT(LIM)  =  0
      GC TO 6757
6756  ISELCT(Ll*»  =  lANSh1*
6757  CONTINUE
      IF 1 ISILCTJLIM  .NT-. 99 .AND. LIM .LT. 5)  GO TC 6710
      GO TO 3000
C
C        ASK USER  IF HE/SHE DESIPES TO TRY ANOTHER CONTROL STRATEGY
 7800  CONTINUE
 7650  PRINT  7851
 7852  CALL  Re AC IN(ALPHA)
      GO TO  (7853,1010,7855,7850,7856),  IGOTO
 7653   PRINT  7P54
      GO  TO  7952
 7655   IANSWR  -  NO
      GO  TO  7657
 7856  CONTINUE
 7657  CONTINUE
       IP  (IA.NSKR  .FC. YES)  GO TO  2000
       IF  (IANSfc°.  .EC. NO)  GO TO 9000
       GC  TO 78CO
 C
 C        ENO CF PROGRAM
 C        PRINT END
 4000   CCNTIN'J5
       PRINT 9010
       CALL EXIT
       5ND
                                     217

-------
FILE:
                FORTRAN  PI
                                               INTEPACTIVF DATA  CORPORATION
C
c
C
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
A SUMMARY
T*E4TMtNT
OF THE COSTS

SCHEME.
                     ASSOCIATATEO  WITH
                  PEPTRT
   PIRP.-SF :
      REPORT  PRINTS

      EACH  ELIGIBLE


   COMMCN  BLOCKS:
      OTRGNT  -  DETERGENT INFORMATION

      L8RCST  -  COST  Oc  LA'iO"
      LICUlC  -  INFO. ABfUT LIOUID INFLUENT

      P3GCNT  -  CONTAINS  PROGRAM C3NTPOL VARIABLES

      PRNTR   -  CONTAINS  PRINTOUT CONTROL VARIABLES
      SCHEME  -  INFC  ABOUT  LIO'JIC TREATMENT SCHEMES

      SEtePOP  -  THE SEWETD POPULATION

      SLCHAR  -  SLUDGEt  LIQ'IID CHARACTERISTICS

      SLtOGE  -  SLUPGE INFO

      SSINK   -  SOLIO SINK  INPQRWATICN
      TIWE    -  PARAMETERS  OF TIME HORIZON

      TPLANT  -  CHARACTERISTICS OF TREATMENT PROCESSES

      TRTCST  -  TREATMENT COSTS


   CALLEC  BY:
      REMOVE  -  THE MAIN  PRCGPAV
   AUTH3R:

      DAVID A 3ARNFS
26
COMMON /CTKGNT/
                       DTRT.US.  PCR4TH, PPRATO,  DIFCOSi  PRESPC

                       PDTRG ,  ENCCST,  PSUBCS(20)f  PCNTNT
      REAL


      COMMON  /LPRCST/  DHR ,  ICFPACt GOVFF
      CCMMON  /LIQCIC/  ALKIPSi  BOOIPS, MLSSAIf NH3IAR,  PINPS,  GAVE

     1                ,  QPEAK,  SSINPS, TBODAft
      REAL  MLSSAR,
      COMMON  /PRGCNT/  TGOTOf IANS4F* FIXEOt FLQTEf  ALPHA

      I , YES,  NO,  CK.,  OFF

      2 , ISCHM

      3 , IQiJw^Y,  CU"^Y


      PQUIVALENCE  ( IANSW" , AN SnE" )


      INTEGFR  FIXED,  cLCTt,  ALPHA

      INTFGF'<  VrS, CfJ, OFF


      COMMCN  /PRNTR/  ISHQRT, ISJPER, ISKIP, IPASS,  ISELCTI5I
                                     218

-------
FILE:
          c">PT(.AN  PI
                                                INTERACTIVE DATA CORPORATION
 COMMON /SCHEME/ S CHFv|E( 25 , 2 5 ),  ELG6TYC25),  MINEFPK25I, «AXSCM
1 , ALPYPS, FCPYPS,  FCLMPS,  LIMFPS,  ALPYFB,  FCPYFB,  FCLMPB,  LIMEFB
2 , ALUMAE, FECLAH,  NAALA6,  ALAB-F,
3 , ALTFVF, FCTFMF,  ALCBAS,  FCF3AS,
4 , FQUIPU5)
                                                  NAABKF,  ALUMTF,  FECLTF
                                                  L2FBAS,  NONE
 INTFGER FLGPTY, EQUIP,  SCHEME
 INTEGER ALPYPS, FCPYPS,  FCL^PSi  ALPYF9,  CCPYFB,  FCLMF3, ALUMA9
1 , FECL4B, ALAPMF,  FCABMF,  ALUMTF,  FECLTF,  ALTFMF, FCTFMF,  ALC8AS
2 t FCFRAS
 REAL MINEFP

 CCMKON /SEHPCP/ FNCTYP,  SCOPIN(2,5I,  SEWPDPI20J
1 , YEA\, SPOP, MAXPV

 INTEGER YEAP, SPOP, FNCTYP
COMMON /SLCHAP/
1
2
3
4
5
6
7
8
9
LBNVTS
PC02
OSSLGE
TLBSLG
WftPFC
PLIME
SRFE"=
WRFEA
C020
L6VPS ,
PFECL ,
CTOTAL,
TLBSS .
VGPLIM,
PYFTO ,
WPFEF ,
AARATO,
SRTLIM,
AOOSSR,
L8VSS ,
PNAAL ,
OTSLGE,
TLBTS ,
WOPNAL,
PYVFD ,
SRFEP i
FFRATO,
TSfrTUC,
ALKI/P FCVFD ,
LBVTS
PNACH
SRCAT
TLBVS
WOPNGH
PPOLY
SPALP
SRCATS
LI^ETO
LIMEPO,
PCLYD ,
SRLIME,
WGLBSS,
WOOPLY,
SRALF ,
WRALP ,
WRCATS,
BCDIAR,
LBN VPS,
LMVFC ,
PPCKL ,
TLBNVS,
WOPALM,
WCPPCK,
SRCATA,
WRFEP ,
WRALS ,
WOTLBS
LBNVSS
PALUH
QPSLGE
TLBOS
WOPC02
WRCAT
WRALF
WALA
W9FES

 REAL       LBNVPS, LBNVSS,  LBNVTS,  LBVPS ,  LBVSS ,  LBVTS
1 ,  LIMF.PC, LMVFO , L
 COMMON /SLUDGE/ ASP    ,  FLOTUO,  GRAVUO,  HPDFT ,  HPHVF , PSETUO
I              t PSRMVE,  V^PSLG,  VSANR«1,  VSARM

 COMMON /SSUK/ TPNCST,  SWASTE(20),  SOLSNK< 2,15) ,  SSCOST(20)
1             , 9ESTSS(20),  CAP,  OISTi  M4XSS
 INTEGER BESTSS, CAP, OIST
COMMON /TI
INTEGER TP
"E/ NQYRS, M4XTP, TP$IZE, TP
COMMON /TPLANT/ TPl
1
2
3
5
6
7
8
q
RWPU^P,
MCHAER,
VACFTR,
PECRB2,
CC2FS ,
PNAMS ,
WVAR ,
MAXP
PRETRT,
FLOCCP,
GRVTKN,
CENFUG,
TFRST1,
NAALFS,
AMRATE,
PPARM ,

.ArjT(16,<
PRMSET,
SECSET,
FLOTKK,
MHINC ,
TERST2,
PCKLFS,
AMLIFF,
?ASF ,

t5)

^ E l P y p ,
A.NAOIG,
CBINC ,
NAOHFS,
PPA'w ,
APVAR ,


TRKFT»,
CLFEED,
AEROIG,
WSPONO,
FECLFS,
REC.ALC,
PVAP ,
PARMX ,


AERBSN,
CLBASN,
DRY3ED,
SLGOCN,
FLOCCT
WOPARH,
MINRV ,


OIFAIR
MULFTR
SLOTNK
RECR31
PCLYFS

WPA«1
MSXRV

 INTEGER RWPUMP, PRETRT, PS«SET,  PSPUMP,  T8KFTR,  AERBSN
1 ,  OIFAIR, FLCCCP, SECSET,  REtPvP,  CLFEEO,  CL3ASN,  RE2PMP
                               219

-------
      FtPr".T
                        PI
                                                INTERACTIVE DAT\ COSPORATIOr4
 COMMCN /TSTCST/ 0MH3S ( 45 , 20 I •  >'"HRS ( 45 , 20) ,
i              , AMCOSTJ45),  T=FAOD(45)

 REAL MMHPS
 INTEGER TPFiOC
      DIMENSION LPRAVEK5), SPAVE
           LFRAVE
                                                   TM«5(45,20)f CONCOS(45)
1551
1554
1151
1154
2010
2020
2025

2030
FORMAT
FORMAT
FORMAT
FORMAT
FOB MAT
=ORMAT
FORMAT
1 = »,F
FORMAT
(IH
11H
( IH
(IH
(IN
(IH
(IH
1.2)
(IH
1 ,' BOOS
2050

2130
FORMAT
I ,' S
FORMAT
(IH
.S.
(IH
            ,'SHORT?')
            ,'CO YOU  WANT  A  SHORT
            I'SUPE"  SH01T7M
            ,'CC1 YOU WANT  A  SUPER SHORT
         (1H1 ,'LIQUID TREATMENT SCHEME =
             ,'AMORTIZATION RATE =',C4.2
                                        PRINTOUT? (YES OR NO)'1
                                              PRINTOUT?  (YES  OR
                                              ',151
                                              ,' AMORTIZATION  LIFETIME =•

                  ,'FRACTION  CF  CONSTRUCTION COST FINANCED  BY GOVERNMENT

                  ,'BCD5  (INTO  PRIMARY) = '.F4.0
                 (INTO  SECONDARY)  = »,F4.0)
                  ,'SUSPENDED SOLIOS (INTO PRIMARY) =  ',F5.0
                 (INTO  SECONDARY)  = '.F5.0I
             (1HOi//IX,'PROCESS NA«E',4X ,'CONSTRUCT I ON',9X , •S IZING*,11X
     1 ,'AMORTI7fcC  COST',6X,'YEAR PROCESS'/16X
     2 ,'COSTdOOO  1 )',6X,'PARAMETER',13X.MIOOO $ /TP)'
     3 , 6X,'FIRST  NEEDED'/)
2150  FORMAT (IH  t3A4,7X,F9.3,5X,p10.3,2X,A4,IOX,F9.3,9X,F6.1)
2170  FORMAT (IH  ,/lX,'TOTALS  = • , 10X.F11. 3 ,28X, <=11. 3 )
3010  FORMAT (1HO,///30X,'PERIODIC OPERATING COSTS'/)
3030  FGRM4T (IH  ,'PROCESS NAME',5X,•CPERATING IAN-HOURS•,3X
     1 , 'MAINTAINANCE  MAN-HOU"S•,8X,•MATER IAL £ SUPPLY  CCST'f7X
     ft ,'LABOR COST*
     2 ,3X,'TOTAL  CCM•/14X,2(5X,•(MAN-HOURS/TP)',5XI,14X,•(  S /TP)',15x
     3 ,'(AVER AGE)«,3X,'(1000S/TP)•/15X,212X,'AVE.• t4X,•MAX. •,4X,«MIN. •,
     42XI.6X,'£VE.',BX,'MAX.',8X,'MIN.»,2X,«(1000S/TP)'/)
3050  FORMAT (IH  ,3A4,2X,6(F6.0,2X),3(FIO.2,2X),2(F10.3,2X))
3C70  FORVAT (IH  ,/lX,'TOTALS  =',6X,6(F6.0,2X),3(FIO.2,2X),2(e10.3,2X))
4010  FT^MtT (1HO,///30X,'!)NIT  CCST DAT A'/27X,'(CENTS/1000 GALLONS)'/)
4030  FORMAT (IH  ,'PROCESS  NAME ', 3X, • A-'HRTI ZAT ION ', 3X, ' LA8CR «
     1 ,3X,'MATERIAL £  SUPPLY',3X,'TOT«L'/)
4050  FORMAT CH  ,3A4,5X,C5.2,7X,C5.2,9X,F5.2 , IOX,F5.2)
4C70  FORMAT (IH  ,/lX,'TOTALS  =•,9X,=5.2,7X,F5.2.9X,F5.2,IOX,F5.2)
5010  FORMAT (1HO.///1X,'C^STS  ne SU9TITUTFS FQ^ PHOSPHATE DETERGENTS')
5030  CORMAT (IH  .'/VcPAGE  (t/TP) = •,C10.0/1X,'MAXIMUM  (S/TP)  = •
     1 ,F 10.0/1X, 'MlfiUMUM  ($/TP)  = '.FIO.O/1X, ' AVE« AGE  (CENTS/1000 GAL)
     2 = «,F5.2)
6030  FORMAT (1HO ,///20X,'SOLID SINKS COSTS'/)
6030  CORMAT (IH  ,'TTME',5X,'SI M< ',3X,«AMOUNT SOL IDS',8X,'COST•/
     1 lX,'P=.MOn    USED       (TONS)',J1X,M$/TP)')
                                    220

-------
FOT^.N  PI
                                      INTERACTIVE DAT* CO«PO«ATI3\
6050 <=OP«ftT (1H ,I6,!7,6X,F10.2,3X,P10.2)
6070 FORMAT CM ,/?X, 'TOTALS =' ,9X, F ! 0. 2 , 3X
6090 FJRM£T (1H t/ttx,«UNIT COSTS FOR SOLID
1 GAL.) =',r!0.2)

.F10.2)
WASTE DISPOSAL (CENTS/1000

7020 FOPWAT (1H , 'TOTAL UNIT CTST (CENTS/1000 GAL) =',F5.1/)
£ ***««*?** ****** *« atttt***~«* *********
C **-ox***e*****f**
c **************** START EXECUTION
C » t*» »*»**** *3» *»
^ *****««*********«*****,: a***********
C
1000 CONTINUE
C
C IF THIS IS S5COMO P6SS THRU REPORT
C SCHEME, THFN EXECUTE LCN3 PRINTOUT
IF (IPASS .EQ. 1) GO TO 1200
DC 1150 I = 1,5
Ic (ISFLCT(I) .EQ. ISCHM) GO TC 2000
1150 CONTINUE
GO TO 9000
1200 IF (ISKIP .FO. ON) GO TO 1900
1500 ISHORT = OFF
ISUPER = CFF
ISKIP = CM
C
c ASK USER OF HE/SHE DESIRES A SHORT
1550 PRINT 1551
1552 CALL PEACIN(ALPHA)
GO TO (1553,1000,1555,1550,1556), IGO
1553 PRINT ] 554
GC TO 1552
1555 IANSW? = NO
GO TO 1557
1556 CCNTINUE
1557 CONTINUE
IF (IftMSWR .EQ. YES) GO TO 1605
IF (IANSV*R .FQ. NO) GO TO 1900
GP TO 1500
C
C . SET UP CORRECT TYPE OF PRINT OUT
1605 I SHORT = CN
C
C ASK USEP. IF HE/SHE DESIRES A SUPER
1750 PRINT 1751
1152 CALL REACIN(ALPHA)
****************************
****************
****************
****************
****************************



FOR A SELECTED











PP.INT OUT FOR ALL SCHEMES















SHORT PRINTOUT


GH TO (1753,1000,1755,1750,1756), IGOTO
1753 PRINT 1754
GO TO 1752
1755 I4NSW3 = NO
GC TO 1757
1756 CONTINUE
1757 CCNTINUF
Ic UAMSfe0 .EC. YES) GC TO 1805
ic (IANSW7 .EC. NO) GC TO 1900








                      221

-------
CILE:  c?Pr?r    FOrT^AN  Pi                           INTERACTIVE DATA  CCCPCR/TI ON


       GO  TO  15CO
C
C         SFT  UP CTRRECT  TYPE  OF P3T1TOUT
1805   ISUPFK  =  JN
1900   CCNTIN'Jt
2000   CONTINUE
C
C         PRINT  SCHEME  NAVE,  AMORTIZATION RATE, AMORTIZATION LIFETIME
       PRINT  2010,  ISCHV
       IF  (ISUPER  .EQ.  ONI   GO TO 2100
       PRINT  2020,  TPLANT(A'4PATE,1),  TPLANT(AMLIFE,I)
       PRINT  2025,  GCVFc
C         IF  SChEMF  IS  CHEMICALS TO PRIMARY PRINT 9005 AND SS
       I<=  (ISCHW .GT. 8)  GO  TO 2100
       P'UMT  2030,  ecrips,  PODIAP
       SSINS  = SSU.PS - (SSINPS*PS3MVE*ADDSSR)
       P^INT  2050,  SSINPS,  SSIN«
2100   CCNTINUF
C
C      PRINT  CCNSTPUCTION COSTS
       IF  (ISUPER  .SO.  OFF)   PRINT  2130
       TOTCON  *  0.
       TOTAMC  = 0.
       00  2900 IPSCC *  l.MAXP
       IF  (FQLIIPI IPROCI .EC.  OpF)  GO TO 2900
       TOTCON  = TOTCCN  *  CONCOS(IPSOC)
       TOTAMC  * TOTA"C  *  AMCOST(IP*OC)
       YP.CA3D  = TPFAODUPFCC)*TPSIZE  + SPOP IN( YE
       IF  JISHORT  .EC.  OFF)
     I PRINT  2150i  (TPLANT(J,IP*OC),J=1»3),  CONCOS1
     2 ,  TPLANTIEPARM, IPROC),  TPL ANT ( PA»«1X ,1 PRCCI , A«COST( IPRCC)
     3',  YRFACC
2900   CONTINUE
       IF  (ISUPER  .EG.  DFFt
     1  PRINT 2170, TOTCON,  TOTAMC
3000   CCNTINUE
C
C         PRINT PERIODIC  OPERATING  COSTS
       I"  (ISUPER  ,5C.  ON>  GO TO 3100
       PRINT 3010
       PRINT 3030
C
C         ZERO COLUMN TOTALS
3100   CCNTIMUE
       CTQPAV  = 0.
       CTOPMX  = 0.
       CTOP^N  - 0.
              = 0.
              = o.
              * o.
       CTSPAV  =0.
       CTSP«X  = 0.
       CTSPMN  = 0.
       CTLBAV = 0.
       CTAV5T  = 0.
                                     222

-------
FILE:
          FORTRAN   PI
                                                      INTERACTIVE
                                                                       CO=POPATION
      on 3900  IPS.OC  =  I.MAXP
      IF |EO'.MP< IPRCC)  ,EQ. OFF)  GO TO 3900
      OP = 0.
      UP = 0.
      QOMAX  =  -1.
      OPMIN  =  1.F10
      A* = 0.
             =  -1.
             '  I.E10
      SP = 0.
      SPMAX  =  -1.
      SPMIN  *  l.F. 10
      00
      OP
      AM
      SP
         TOTAL  UP  "AN-HDURS AND COSTS
    ?eoo
    * OP
    = AM
    = SP
      OFMAX
TP = 1,MAXTP
* AKAX1(C*HRS( IPRaC,TP),O.I
* APAXUMMH3S( IPRQC.Toj.o.l
* AfAXKTMS   (IPPOCjTP),0.I
*MAXKOPKAX,O^HPS< IPPOC.TPH
      SPMAX  *  AMAX1«SPMAX,TMS  (IP"nCfTP»l
      OP.MIN  »  AKIM (QPMIM,QMHRS( IPF 3CfTPl }
      AMMIN  =  AMJM (AMMIN, MMHR$< IPRDCtTPI )
      SPMIN  =  AMIN1(SPMIM,T««S  
-------
Flic-  3TppjT    eCc'T^AN  P)                            INTERACTIVE DATA CCOPQRATION


C         PRINT  UNIT C:STS
       IF  CISUT1  .FS. ON)  00 TT 4100
       P1SP =  «SPAVE(IPPOC)/(365.*T»SIZEI )/<=L HAVE 1*100.
       «CHTOT  =  UA^C * UL3U.  * UMSP
       CTUA^C  =  CTLA^C *  UAMC
       CTULB9  «  CTL'LPR +  ULflR
       CTUMSP  =  CTUMSP *  UMSP
       CTRT -  CTRT * ROWTOT
       IF  (ISHORT  .EC. OFF)
     1 PRINT  4050, (TPLANTUtlP'.OOtJ*! f3)» U4"C, UL3R,  U«*SPf ROWTOT
4900   CCNTIN'JE
       IF  ( ISUPER  .EC. CF«-|
     1 PRINT  4070, CTUAVC,  CTULBR, CTUMSP, CTRT
5000   CCNTINJ5
C
C         PRINT  COSTS OF  SUBTITUTES FOR PHOSPHATE  DETERGENTS
       P - 0.
       PMAX *  -1.
       P*!N »  1.F10
       DO  5500 TP  * 1,1AXTP
       P » P  «• PSUBCSJTP)
       PMAX »  S»»axi(FHAX,PSiJRCSITP»)
       PMIN «  lINHPi'INtPS'JBCStTp) )
5500   CCNTINUE
       IF  IP  .LT.  C.)  GO TO 5900
       PAVE »  P/^AXTP
       UP  * «P4VE/«?65.*TOSim )/FLWAVF)"«lOO.
       ie  (ISUPFa  .=0. CNI  fiO TO 5900
       PRINT  5010
       POINT  5030, PAVE,  PHAX, P«MN, UP
5900   CPNTIN!UC
C
6000   CONTINUE
                                    224

-------
FILE: prprsr   crF'PAN  PI                           INTER4CTIVE DATA CORPORATION


c
C        PC I NT COSTS IF SHLID SINKS
      fc CIS'jnE* . = 0. ON)  r,n T,-) 4100
      PPINT 6110
      P3INT 6030
6100  CONTI^U?
      CTSSCS = 0.
      CTSfcST * 0.
      00 6500 TP = l.MAXTP
C        USE 1. INSTEAD CP 0. PEC4USP  CF  1CUNO-OFF
      IE 
-------
MLF:  SCHOSr.
                P)
                                                INTERACTIVE DATA Cr»POR AT IQfl
       SUBFOUTINE  S
C
C
C
C
C
C
C
C
C
C
C
C
/•
C
C
C
C
C
C
C
C
C
   SCfOSF  PICKS TH" SL'IT-.F HANDLING  PROCESSES  (FOUIPMENT) /JHICH
   ««E  PCTI-:
   1. NECESSARY FOP i PARTICULAR LIQUID  TREATMENT SCHFVE
   2. CONrORM  MOST  CLCSFLY WITH THF  PRESENT  PLANT CONFIGURATION
   SCHHSF  ALSO CONSTRUCTS \ COMPLETE  LIST  OF NECESSARY
   EQUIPMENT  FOP  THIS SCHEME

COM^'C^  BLOCKS:
   PRGCNT  -  PROG^'A*' CCrjT=.nL VARIABLES
   SCHEME  -  REOUIPEO LIO'JID HANDLING  EQUIPMENT
   SLGSCM  -  REQUIRE? SLUOGC HANDLING  EQUIPMENT
   TPLANT  -  CHARACTERISTICS CF TREATMENT PLANT PROCESSES

CALLEC  BY:
   TRTMNT  -  THE MAIN CDSTING SUBROUTINE
AUTHOR:
   CAVID  A  BARNES
                        26 CF.C 72
      CJMMCN  /P^GCNT/ IGOTG,
      1  , YES, NC,  CN, 0CF
      2  , ISCH^
                             FIXED, FLOTE,  ALPHA
      EQUIVALENCE  (IA

      INTEGF-? FIXEC,  FLCTE,  ALPHA
      INTEGER YES,  CN,  CFF

      COMMON /SCHEME/ SCHEM=<25,25), CL08TY(25),  MINEFP(Z5)f  MAXSCM
     1  , ALPYPS, FCPYPS,  FCLVPS, LIMEPS, ALPYFB»  FCPYFB,  FCLMFB, LIMEFB
     2  , ALUMAB, FECLA",  NAALA3, ALA3"F, ^CASMF,  NftABMF,  ALUMTF, FECLTF
     3  , ALTFMF, FCTFMF,  ALc8iS, CCFBAS, Ll^BAS,  L2F8AS,  NONE
     4  , EQtJIP<
-------
fll.t: SCHObE    FOHTtAN  PI                            1NUPACTIYE  UA1A CfWOKAT I UN


     7  ,  PNAME  ,  AMi-ATF,  AMLIIC, f'PAP"  ,  PVAR   ,  W'JPARM, wPAtt*
     8  ,  HVAM   .  OP ARM  ,  BASE  , APVAR  ,  PAP. MX  ,  H|NRV  , MAXKV
     9  ,  KAXP

      INTEGER  RWPUMP, PKF.1RT, PRKSFT, PSl'UKP,  TKKFT't, AFFU'SN
     I  ,  OIFAIK,  FLCCCP,  StCSIT, RC1PMP,  CLFEEC,  CLRASN, 4E2PXP
     ?  ,  CRVTKK,  FL( TKN,  AS'ACIG, AFROIG,  CRYL'Et),  SL01NK, VAC^TH
     j  ,  rrNFUG,  FniNC  ,  WSP'JN^, SLOUCN.  BECPHI,  UK""?, IIRSTI
     4  ,  T(RST2,  AlU'lFSf  FtCLFS, PCIIYFS,  CC2f S  . , PCKLFS, '(FCfllC
     5  ,  PNAMfc ,  *Ma/vrfc',  A^LKf, PI'ARM  ,  PvAD   ,  W)P\R», wP&PM
     6  ,  WVAR   ,  PP/HI  ,  FLOCCT, BASE   ,  AI'VAR  ,  PAK^X

      DIMENSION
£         »***4««*t«»**»*<>*»»»*<>«t***t**<-<'*»««*»«»«*»**t««t»*»*»***»»**»*

^         (r t« «««*•< ««»»»*»    START F.XFCIITICN             »<•*»»»» •*««»»»».

£         «•»»»»«***<*•«**»*«»»**«««****»*•»**»*««*«**»«(.««»*»«**«««»«•»»
C
1000   CONTINUE
C
C         RESTORE NEGATIVE PPARMS  IF  THEY HAVE BEFN  SAVEU FROM BEFORE
       IF  (1SK .NE.  CM)   GO TO 1900
       DO  1500 IfSCC  =  l.MAXP
       TPLANT IPPARK,I'>,^UC) = SAVNEG ( I PROC )
1500   CONTINUE
1900   CONTINUE
       I  * 0
C
C         CHOOSE THICKENER, DEFAULT  IS GRAVITY THICKENER
       1-1*1
       SLGSCMtI ) -  CCV1KN
       II-  (TPL ANMPI'AsM,ri.UTKK)  .E3.  0.)  GO TO  2100
       I  »  I » 1
       SLGSCM( I ) -  FI.OTKN
2100   CONTINUE
C
C         CHOOSE DIGESTERi DEFAULT IS NONE
       1=1*1
       SLGSCMU) =  0
       IF  ( TPl ANT(PPAKM,AERDIC)  .NE. 0.)  SLGSCMU)  = AEROIG
       IF  (TPLANT( PPA-  .NE. o.)  MGSCMUJ  = CENIUG
C         AUU  SLUOGI ir.JLOING  TANK  FOR VACUUM  MLTL'R  AND  CENTRIFUGE
       IF"  ISLGSCM(|» .EU.  Of LIME  FflDING ANO  STORAGE  FOI  VACUUM  riLTf«
                                       22?

-------
CILF:  SCHPS"    cCiRTrAN   PI                            INTERACTIVE  DATA CORPORATION


       IF  (SLGSCM(I-1)  .F3.  CENF'JG)   r,0 TO 2?00
       I =  1*1
       SLGSC1II)  =  LIVE=S
       I =  1*1
       SLGSC^II)  =  FECLFS
c
C        CHOOSE  INCINERATOR ,  DEFAULT IS NONE
2200   CONTINUE
       1 =  1*1
       SLGSCVII)  =  0
       IF  «TPLANT|PPA<5Mf FHINC  I  .NE. O.I  SLGSC*(I» = FBINC
       IF  (TPLANTCPP/PM,MHINC  )  .NE. 0.)  SLCSC^U) = MHINC
C
C         CHCJOSF  W^STE  STABILIZATION POND, DEFAULT IS NONE
2300   CTNTINUE
       1 =  1*1
       SLGSCM(I)  =  0
       IF  (TPL4NT(PPAPM,WSPONC)  .MF.. 0.)  SLGSCM(I) = WSPOND
C
C        CHOOSE  SLUCGE  L6GOON,  DEFAULT IS NONE
       I =*  I *  1
       SLGSCMJ11=0
       IF  (TPLANT(P?APMtSLGQON)  .NE. 0.)  SLGSCMJI) = SLGOON
C
C         IF LICUIC TREATMENT  SCHEME IS A TERTIARY LIME SCHEMEt
C         THEN  USE  RECALCINATION
       I *  I *  1
       SLGSC^I11=0
       IF  ((ISCI-M .EO. LIFBAS)  .OR.  ( ISCH* .EQ. L2FBASI)
      1 SLGSCfMIl  =  R5CALC
C
C        CONSTRUCT CPHPLETE LIST  OF NECESSARY EQUIPMENT FOR  THIS
C         STRATEGY
C
3000   CONTINUE
C
C         INITIALIZE  WHOLE  LIST  TC 'OFF'
       00  3050  IPftCC  =  1,MAXP
       EOUIP(IPKOC) = OF*
3050   CflNTI^UE
C
C         TURN  «CN' REQUIRED PROCESSES COMVGN TO ALL  SCHEMES
                     = ON
      FOUIPJPRETRT
                     =  ON
      ECUIP«PSPJMP
      PQUIP( SECSET
      E3UIPFVE< ILIQ.ISCMM)  .Nt.  0»   ECUI P« SCHEME (IL 10, ISCHM ) |  s  o\
3100  CONTINUE
                                    228

-------
FILE: sent s?    CHPTSAN  PI                           INTERACTIVE DATA
c
C         CILL  TQUIP  WITH MECESSAS* SLUDGE  PROCESSES
      On  3200  ISLG =  Itl
      1=  I SlCSr.^l ISLT- )  .NE. O)  eCUIP(?LGSCM< ISLOI ) = CN
3200  CCNTINUE
C
C         Ic  DPACM  ic  NEGATIVE, TH=N CHANG?  TT  TC ZERO
      ISK  =  CN
      DO  35UO  IPCCC  - ltMAXP
      SftVNEGl IP^HC )  = TPLANTCPPAR^.IP^CC)
      IF  ( TPLANT (ppaqM, IPk3C ) ,1_T. 0.)   TPLANTI PPARM , IPROC ) = 0.
3500  CTNTINUF
C
C         FND OF SC9«0'JTINE SCHQSE
      3ETURN
      ENO
                                      229

-------
IL F:
                         PI
                                                     INTERACTIVE  DATA  CC°PnpATIOM
C
c
C
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
         PlHPCSf :
            S=WAGF  SCADS  IN  VALUES FOR VARIABLES rtHICH DESCRIBE  THE
            CHARACTERISTICS  OF  TH = SEWAGE.
            NOTE:  ASSURER VALUES OP VARIABLES A.RF FRO" RCF.  10.

         CO^CN  BLOCKS:
            LIQUID   -  LIQUID IMCL'JF'JT INFORMATION
            PRGCNT  - CONTAIN?  PROGRAM CONTROL VARIABLES
            SL(J3Gf   -  SLUDGE 1NCCRMATION

         CALLEC  8Y:
            SYSTEM
         AUTHOR:
            CAVIC  A
                            27 DEC 72
      CCMMON  /LI'JtIC/  ALKIPS,  PODIPS,  MLSSAR, NH3IAR, PINPS, OAVE
     1                ,   QPEAK,  SSINPS, TBQOAR

      1EAL MLSS4R,  NH3IAR
              /P"GCNT/  IGOTO,
     1 t YES, NCt  C^,  OFF
     2 , ISCHW
     3 , IDU.IA'Y, CU^MY
                                      FIXED, FLQTE, ALPHA
      EQUIVALENCE  ( IANSWF ,
      INTEGER FIXEC,  FLOTE,  ALPHA
      INTEGER YES,  CN,  CFF
             /SLUCGE/ ASD    ,  FLOTUO,  GRAVUD, HPOFT , HPOVF  ,  PSETUO
                     , PSPMVE,  VFPSLG,  VSANSM, VSARM , TScTUO
1010
1051
1054
1151
1154
Z25i
125<»
1351
1354
1551

1751
175*
ieci
I 854
1-551
     FORVATtIH
     FIRMATdH
            IH
            IH
      FOIMiTdH
           (IH
     C03MAT(IH
     Fn'^AT 
                  •NH3 C'JMC.  INTO AERiTION PROC (MG/L)1)
                  •CHGSDHrl-US  CCNC.  INTO PRIMARY SETTLER (MG/L)')
                      E= ' I
                           flVrPA^E  CJ4ILY
                  •°PFSEKT  PEAK  TI'JRNAL FLOW
                  •SSINPS=')
                  'SLS0fcNOED  SOLIDS  CO\C.  INTO PRIMLY SETTLER  (MG/L)')
                                     230

-------
FILE: $r-iAf,t   C.-"?TRAN   "I                           INTERACTIVE  D«TA  CORPORATION


1<354  ctiRN-MC.^  ,'TOTAL  CHANGE  IN  B035 iC°CSS AECATICN PROCESS  (FRACTICN

2051  FO«"AT( i(-  ,iASn=»}
2054  F^RMMUH  , 'ACTIVATE1}  SLUTGE DENSITY (FRACTION)'*

2154  ensMiTdh  j'CLCTATUIN  THICKER UNDERFLOW SLUDGE DENSITY  (FRAC)*»

2254  C0«M\T(1H  ,'GRAVITY  THICKNER 'JNOEPFLCW SLUDGE DENSITY  (FPAC)')

2354  PCSVATdH  , 'PRIMARY  SETTLER  UNTF&FLOV. SLUDGE DENSITY  (FRACI'I
2451  FORK5T(iH  ,'V'PSLO=')
2454  FOP^iTdH  ,'VCL\THE CPACTIDN FCP PRIMARY SLUDGE')

2554  FOPMAf
-------
FILf!  SCWJ'~,F   CC"T5JN  PI                          INTERACTIVE DAT* CORPORATIO',


       Gf  TO  (l?53,1000,l?55,1250,l?56),   K.OTO
1253   P-"INT  1254
       GO  TL1  1252
1255   MLSS6
1457   CCNTINUE
1550   PRINT  1551
1552   CALL ^EACIN(=LOTEI
       GO  TO  (1553,1000,1555,1550,1556),   IGOTO
1553   PRIM  1554
       GC  TO  15«2
1555   QAVE -  10.
       GO  TO  1557
1556   QAVE *  AKSHER
1557   CONfPJUE
1750   PRU'T  1751
1752   CALL REACIMFLOTEI
       GO  TO  (1753,1000,1755,175(1,1756),   IGOTO
1753   PRINT  1754
       GO  TO  1752
1755   OPEAK  «  19.
       GC  TO  1757
1756   QPPAK  =  ANShS"?
1757   CONTINUE
1850   PRIKT  1951
1852   CALL PPACINIFLOTEI
       GO  TH  (1853,1000,1855,1850,1856),   IGOTC
1853   PKIVT  1854
       GO  TO  1852
1955   S$IK?S  =  200.
       GO  TO  1957
1656   5?IK°S  =  ANShf6.
1€57   COMTIMUS
1950   »RI\T  IS51
1S5?   CALL ?-ACIN(=LOT-)
       GO  TO  (1953,1000,1955,1950,1956),   IGOT3
                                     232

-------
      S-.WAC.r   cfpTRfi.M  P1                          INTERACTIVE CAT \ CORPORATION


      o^INT 1<354
      GH TO ..S57
      T2CCA* = .85
      GO Tn 1957
1956  T30DA3 = At SnEP
l«557  CCNTINU?
2000  CCNTINUr
C        FEiD IN SLUDGE CHARACTERISTICS
2050  P'lNT 2051
2052  CALL RfADIN(FLOTE)
      GC TO (2053,?000,2055,2050,20561,  IGOTO
2053  P^INT 2054
      GO TO 2052
2055  ASD = .01
      GO TO 2057
2056  ASD = ANSWEP
2C57  CCNTINUE
2150  P^INT 2151
2152  CALL RE4CIN(rLPTE)
      GO TO (2153,2000,2155,2150,2156),  IGOTO
2153  PRINT 2U4
      GO TO 2152
2155  PLOTUD = .05
      GO TO 2157
2156  FLOTUO = ANSWER
2157  CONTINUE
2250  PRINT 2251
2252  CALL R E AC I N( f=LOT6 )
      GO TO (2253,2000,2255,2250,22561,  IGOTC
2253  PRINT 2254
      GO TO 2252
2255  GHAVUO = .08
      GO TO 2257
2256  GPAVin = ANSW?P
2257  CONTIMJE
2350  PRINT 2351
2352  CALL REACIN(PLOTE)
      GO TO (2353,2000,2355,2350,2356),  IGOTO
2353  P<*INT 2354
      GO TO 2352
2355 •PSETUO = .05
      GO TO 2357
2356  PSETUD = ANSKER
2357  CONTINUE
2450  PRINT 2451
2452  CALL 'EACIN(FLOTc)
      GO TO (2453,2000,2455,2450,2456),  IGOTO
2453  P^INT 2454
      GO TO 2452
2455  VPPSLS = .78
      GO TO ?457
2456  VFPSL3 = ANShE?
2457  CONTINUE
2550  P°.INT 2551
2552  CALL ^FACIN(FLOTE )
                                     233

-------
 = ILE:  Srw/>0f   c'_; s T * J N  PI                           INTERACTIVE DATA  CC^P^P AT I ON


       GT T! (2553.20JO,25'»5,255i),2556) ,   IGOTC
 255?  PRINT 25ft
       GC TO 255?
 2555  VSANs* = .5
       G? TC1 2557
 2556  VSAK°y = A\SUF°
 2557  CT\'TlNUr
 2650  DP INT 2651
 265?  CALL UfAUN (FL3TFJ
       GQ TO (2653,2000,2655,2650,2656),  ! GCTO
 2653  PRINT 2t54
       GO TO 2«5?
 2655  VSASM =  .5
       GO TC 2657
 2t56  VSAP* =  ANSWER
 2657  CCNTINUE
 2750  PPINT 2751
 2752  CALL FEACIN(FLCTF)
       GO TO (2753,2000,2755,2750,2756),  IGrTO
 2753  PRINT 2754
       Gfl Tn 2752
 2755  HPO^T =  8.
       GO TO 2757
 2756  HPOrr =  A'JSkFF
 2757  CCNTINUE
 2650  PSINT 2951
 2852  C41L Pt^CI^(':LOTE)
       GC TO (2853,2000,2355,2fl50,2856),  IGCT3
 285?  Phi NT ,?854
       GO TO 2852
 2655  HPDVF =  e.
       GO TO 2857
 2856  HPOVC =  ANShER
 2657  CCKTINL?
 2950  PPU'T 2S51
 2S52  CALL °EACIN(CLCTEJ
       GO TO  (2953, 2000, 2<>55, 2<550,20561,   IGOTO
 2953  P^INT 2954
       GC TO 29J?
 2S55  PSS»«VE *>  .5
       GH TO 2957
 2956  PSPWVE =
 2S57  CONTINUE
C
C        ENO 0«
       RFTl
       END
                                     234

-------
= 11!
                                                     INTERACTIVE DATA COLORATION
               £ SI2F
C
c
C
c
c
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c
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c
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r
C
 c
 c
 c
     SIZ'. COMPUTES  PPR  THfj  C'J'JRFNT  TT4E PERIOD ITP), THE

     INCfPFNCENT  SIZING PARAMETERS  FO* EACH PROCESS WITH/WITHOUT
     PHOSPHORUS PEMOVAL TPEATVFNT.
          PLCCKS:

             - INCLU=NT A\C ECCLUENT LIMITS

             - LIQUID INFLUENT  INFORMATION

             - PROGRAM CfNTftCL  VAPIAPLES
             - IN=0 ABOUT LIQUID TRP4TM?NT  SCHEMES

             - SLUDGEiLIOJlOiCHEMICAL CHARACTERISTICS
             -PPQUIPEO SLUDGE HANDLING  EQUIPMENT

             - SLUDGE INFIRMtTICN

             - THE SEWERtO POPULATION
             - SOLID SINK INFORMATICS

             - PARAMETERS OF TINE HORIZON

             - CHARACTERISTICS  OF TREATMENT  PLANT PROCESSES
   SUBROUTINES CALLED:
      TSCHME(ES> - INITIALIZES IN ORDER TO SIZE WPARM


   CALLEC PY:
      TRTMNT - THE MAIN COSTING SUBROUTINE


   AUTHORS
      DAVID ft 3ARNES   12QCT72
     IIOUID

     PRGCNT

     SCHEME

     SLCHAP
     SLGSCM

     SLUDGE

     SFHPOP
     SSINK
     TIME
       CC*!VON /lELI^T/ IELIMT(2f 20)
      1 , INF, EFC


       R5AL IELIMT
       INTEGER EFF


       COMMON /LIQUIC/ 6LKIPS, B3CIPS, MLSSAR,  NH3IAP,  PINPS,  QAVE
      1               , QPEAK, SSINPSt T9QDAP.
REAL
                    NH3UR
       COMMON /PPGCNTX IGOTO,  IANSWR,  ^IXEO,  =LOT?t ALPHA

      1 t YES, NO, CN, OFF
      ? , ISCMM

      3 , IDUMMY, DUMMY
 EQUIVALENCE ( I ANSV.O , ANSWER )


 INTEGER  Fixrc, PLCTE, ALPHA
 INTEGER  YES, OM, OFF


 COMMON /SCH?H=/ SCHE«=(25,25), ELG°TY«25),

1 . ALPYPS,  FCPYPS, FCLMPS, Ll"FPS, AL«>YFP,
2 , ALUMAB,  FECLAB, NAALAP, »H9MF,
3 , ALTF^F,  FCTFMC, ALF3i$, FCC9AS,
                                            MINE?PI25),

                                            FCPYFB,
                                            NAAH»«F,

                                            L2FBAS, NCNE
                                                               MAXSCM

                                                                   LI*EF»
                                      235

-------
f ILT:
                    PI
                                                 INTERACTIVE H
                                                                       CCSPCRATION
         E U'J I P ( 4 5 )
          FLGPTV,  EOUIP,
  INTEGER  ALPYPSi  PCPYP£, FC
 I  ,  CECLAB,  AL*?MF, FCA8VF,
 2  ,
                                       ALPYCB,  ^OPY^,  FCLM=9,  ALU"A3
                                          FECLTF,  ALT=«F,  FCTF«-|ef  ALpRAS
      C3MWCN /SEVsPOP/  FNCTYP,  S PO" I N ( 2 , 5 ) , SEWPOP(20)
     1 i YEA", SPPPi
      INTEGER YEAR,  SPOP,  FNCTYP
           N /SSINK/ TSNCST,  SWASTF(20), SOL SNK ( 2 , 1 5 I ,  SSCnST(20)
     1               i BESTSS(20),  C*P, DIST, MAXSS
      INTEGER etSTSS, CAP,  HIST
 CCMMC'IN  /SLCHAP/
     L3NVTS?  LPVPS ,  L'WSS
     PCCJ2   ,  PCECL ,  PNAAL
     OSSLGE,  CTCTAL,  OTSLGE
     TIRSLG  TLPSS ,  TLBTS
     WOPFC    WCPLIM,  WOPfJAL
     PLIMC    PYFTO ,  PYVFD
     SRFEF    WRFFF ,  SRFEP
     WR^E/i    AARATO,
     CO?D
                          ADnSSF,  4LKIAF
                                  L6VTS
                                  PNAOH
                                  TLSVS
                                  PP3LY
                                  SRALP
                                  SRCATS
                          TSETUD,  LINFTH
FCVFD , LBNVPS,  LBNVSS
LIMEPC, LMVCD  t  PALIJ"
PCLYD , DPCKL  ,  QPSLGE
SRLIMF, TLBNVS,  TLSPS
WCLBSSt WOPALM,  WCPC02
WOPPLY, WQPPCK,  WRCAT
SRALF , SRCATA,  WRALC
WP.ALP , WRFEP  i  WRALA
WRCiTSt WRALS  .  WRFE5
BCOIAP, WOTLRS
 REAL        LBNVPS,  LRNVSS, L9NVTS, LflVPS  ,  L8VSS ,  L3VTS
I t LIMEPDi  L"VFD  ,  LIVFTO

 COMMON  /SLGSCM/  SLGSCM<20)
 INTEGER  SLGSCf

 CCMMGN  XSLUCGE/  A5D   ,  FLOTUO, GPAVUtS HPOFT  ,  HPOVF ,  PSETUO
I               v  PSRMVEt  VFPSLG, VSANPM, VSAR«

 CTMMCN  /TIVE/

 INTEGER  TP
                            "AXTP,  TPSIZE. T?
      CCMMCN /TPLANT/ TPLANT(16,45)
     I f  R-IPJMP, PRETRTi P^MSET,  PSPUVP,
     2 t  VCHA = R, FLCCCP, SSCSET,  RFI.OMP,
     3 .  P62PMP, GRVTKN, FLOTKN,  AfiiDIf,,  SEROIG,
     4 ,  VACeTR, CENPiJG, HHINC  ,  CBINC
     5 ,  C£CRa2, TFPST1, 1
     6 ,  C02FS , NiALcS, F
     7 ,  PN4ME » *MRiTEt A^Lirtt  -r*"." ,
     8 ,  WVA~  , SPARS  , BASF   ,  APVA" ,
                                          R,  AE^SN,  OICAIP
                                              CLRASN,  MULPTP
                                                      SLOTNK
                                              PLOCCT
                                              HOP ARM,
                                              MINRV  .  MAXRV
 INTEGER P.WPUUP,
1 , OI=AI=, FLCCCP,
2 , GRVTKN, FLCTKN,  ANAQIG,  AP
                                       PSP'JVP, TSK^TR,
                                          CLPEEO, CL"ASN,
                                     CIG,  CRYQFO, SLDTNK, VACFTR
                                     236

-------
F ILF
                        PI
                                                     INTEPACTIVE  DATA  CO»PORATION





c
c
c
r
C
C
1000
c
c
c
c

2COO
c
c
c
c
c
c
3 t Cc\FUCt FSINC , WSPCNi), SLr,GCN, RECK61,
4 . TEPST2, ALUV^S, FFCLFS, POLYPS, CC2FS ,
5 » PNA 4E > A^PATF, A*ILIeEt °PA°M t PVAR
6 , WVAS , 6PAPM , FLnCCT, BASF , APVAR j
PEAL LBCC, PLVSS
****»*«***********«****,:,,***,**,»***,,„
**** » ** A***** ***
****»*i*****»*±4 START EXECUTION
***A ************
»=»e**T*"***x*************ft4***c,»*t<»**^R
    .7 =  70 PER CENT ocwcVAL 0<
 SSRTF =  .7*(1 ,-PSK^VE ) *SS!N°S
 LBVSS =  SSRTF*VCDSLG*QAVE«PQPR*3.33
 LBNVSS = SSPTc*(l.-vcPSLG)*QAVE*POPR*8.33
 TLBSS =  LBVSS * L3MVSS
 QTOTAL = QTCTAL + OSSLGF
 TLBNVS = TLPNVS + L3NVSS
 TLRVS =  TLBVS * L^VSS
 TLBSIG = TLBSLG » TLBSS
                                      SUSPENDED  SOLIDS  IN  FILTER
                                    237

-------
FIIF:  SIZt     CPPTFAN  PI                           INTERACTIVE DATA CORPORATION
                                        < "^3560. *6. *F.QUIP(
                                         t>VAP,Ta«FTRI*lOOO. )
207C   CCNTnU =
       Ic  (FQUIPJAFPESN) -EO. OFF)  GO  TO  2090
       FOOP = TP1CiP*RODIA3
       MLVSS = .7*VLSSA3
       VA5P = *8)
       TPLANT(HPPAR«,MJLFTR) - Q
-------
FIlc: SIZf     FCRTPfN   PI                           INTERACTIVE  DATA
                                             PV A3
      QTOT4L =    GO TO 2170
      TPLANT< WlPftRM,ANADIG) * ( TPL ANT ( PVA" , AN ADI Gl *E3U IP ( ANAOI G)
      I                         *3TQTftL*lOOO.>/7.48
      TENSS  =  TLBVS /  *EQU1«> ( VAC^TR )
      1                         /(TPLANT»PVAR,VACFTR)*HPDVF)
      CCN *    «  ITLBNVS * TL3VS ) *EQ'JI P{ "HINC )
      1                         /TPLANT(PVARfMHINC)
       TPL#NT(wr?PAOK,F3INC  ) =  ITL^NVS * TLBVS »*EOUtPJ
       Ic «EOUIP(XHINCI  .FQ.  CN .OR. EQUI PI FRI NC I ,EQ. ON)
      1   TLBVS =  0.
       TPLANTIrtOPAOw.WSPGNCI  »  0.
       TPLANT( WG3i(
-------
MLF:
                                                INTERACTIVE DATA  CORPORATION
C
c
    CHEMICAL HANDLING PrlCC?SS6S
C
c
c
c
4COO
c
c
c
c
c
c
      W30CO?  =  PCC2
      W9PFC   =  PCECL
              =  PNAAL
 W2PNOH
 WTPPCK
 WO°PLY
                PPCKL
      T PLANT) wOPAOM , =ECLFS »
      TPLANTtWOPAFK.LIfFFS)
      TPL AMT (WOPARM»°3LYFS)
      TPLANT(WCPARM,C02 FS )
      TPLANT(WO-»ARM,.MAALFS)
                         PALUM/ll.*FflUIP(ALUMFS)
                         PFCCL/2.89*EQUIP«FECLFSI
                         PUIME*EQUIP(LIMEFS)
                         r>PnLY*5CUIPSRMVE*ADDSSR)*OAVc*POPR*VFPSLG*8.33
                *(1.-VFPSLGI*SRLIM=/8.33)*QAVE*PCPR*8.33
               L3VPS * LBNVPS
                TLBNVS * LBNVPS
               TLBVS * LBVPS
                TLBSLG * TLBPS
              » TLePS/(PSETUD*(10.**6.)*8.33)
                OTOT^L + OPSLGE
             QAVF*PCPR*8.33
               PALU*
               PFECL
               PLI^E
               PpCLY
• WRALP*I?LI*'TUNPfTP)*AARATO*CON
* WRFEP*IELIMT(INFfTP)*FFRATQ*CON
* LI"EPO*CCN
* POLYO*CON
PRMSETI a C3AVE*POPR*1000.*ECUIP
-------
f ILE: sm
               FCBTFAN   PI
                                              INTERACTIVE DATA CORPORATION
                                                SnLIDS  IM FJLTF?
           ;'. = .02<5»OAvE*pr:pR
C        .7 * 70 PfB CENT REMOVAL  Oc

      LBVSS = SS3TF*VFPSLG*0*VE*P)PR*B.
      LBNV'S = ( SSC TF*( l.-VFPSlr.l+W'ALF'
     1         +SRfE?*rfRFEF*IfLIMTMNF.TP)»*9 AV6»POP<**8. 33
      TLBSS * LRVSS  *  L«NVSS
      CTPTAL - QTCTAL  *  CSSLG?
      TLBN'VS = TL6NVS  *  LBNVSS
      TLBVS » TLBVS  »  LBVSS
      TLBSLG a TLPSLG  *  TLBSS
      PALUM * PALUV  »  WRALF*IELI^T(INF,TP)*AARATO*CDN
      PFECL = PFECL  »  W?=EF*IELIMT(INctTP)*FFRATO*CON
      TPLANTIWPARP,  TRKFTR1  =  OAV E*PC1PR*43560.*6.*EQ'JIP( TRKFTR )
     1                         /(TOLANT(MVAR,TFKFTR)*1000.)
 'LSSAR
      VAEP * (TPLAMT(1.VVAR,AER9SN)/2'».)*QAVE*PO[»R
      TPLANTt wPARM,  AERBSN)  -  ( VA'P / 7.48) *lOOO.*(rQUI P< AERBSN)
      URSS = USO*10000.)/MLSSAR
      RTUPN « (l.-1.08*cnOO/1LVSS  *  I,25*VAER/(3AVE*POPR))/(URSS-1.)
      IF (RTURN .LT. 1.)  RTURN =  ?.
      LBOD = C.58*FCOO*OAVE*PnPR4-l.l6*.l25*VLVSS*.6*VAER»NH3IAR*4.6

      LBVSS
      SCON =
      L8NVSS
      TLBNVS
      TLBVS
      TLBSS
      OSSLGE
      QTOTAL
      TLBSLG
      PALUM
      PFECL
      PNAAL
      1
               (!.C8*FOOD*OAVE*P3P'*-.125*VAER*KLV$S)*8.33
              SRCATA*IELI«T( INF,T(>)*3AVE*POPR*8.33
              *  L3VSS*.3/.7 «•  (WRFEA * WRALA)*SCON
              »  TLBNVS  +  LBNVSS
               TLBVS  *  LBVSS
               L3NVSS * LBVSS
              *  TLBSS/«10.**6.)*ASD*3.33>
              -  OTCTAL  *  QSSLGE
                       *  TLBSS
                       HRALA*IELlMT(lN|::»TP)*AAR.ATa*CON
                       W«PEA*tELIMT( INF,TP»*FFRATO*CON
                       WRALA*IELIMT( INcf TP »*AARATO*CON
                       FAIRI »  (LB3D*EGUIP«DIFAIR) )/<.075*.232
                               *TPLANT(WVAR,OIFAIR)*1AAO.*1000.)
               (15CO.«'QAVE*POPP*3C9IAR*8.33)/(1440.*1000..»
       IF  (T»LANT( WPA3M,  OIFAIRI  .LT. TENSS)  TPLANT« WPARM, 0 IFAI R I-TENSS
       TPLANKWPAR*-,  »»CHAFR) »  ( LBOD*ECUI1>(MCHAPRI J/l TPLANTi WVAR .MCH4ER)
       « TLBSLG
        PALU1 *
        PFECL +
        PNAAL *
       TENSS
       TENSS  »  (QAVE*P1PR*BQDIAR*8.33I/«TPLANT(KVAR,MCHAER)*24.)
       IF  (TPLANTIWPARM, MCHAER) .LT. TENSS)  T«»LANH WPAPM ,  MCH&ER I»TENSS
 *00«>«'*EOU!P(FLOCCT)
                     SECSCT) - (1AVE*POPP*1000.*ECUIP(SECSET»)
                               /TPLANT«WVAR,SECS?T|
       TPLANTJ WPARf ,
       TPL ANT I HP ARM
TPLANT IWP4FK,
TPLANT( WPARPt
                     CL3ASNI
                               QPEAK*PQPR*TPLANTCWVAR ,CLF£EOJ*8
                               *EOUIP«CLFEED»
                                                                 33
                                     241

-------
MLf: Sia      FORTRAM   PI                           INTERACTIVE DAT* CC1PCRATIQN


     1                         *EQUIP(C13/VSM) /( 1. 440*7.41 >
      TPLANT( UPA^I* f  VIILFTrtJ  =  C
      OTOTAL  * OTOTAL  «•  OTSLGE
4C93  CCNTIMUE
      CCN =  QAVE»POPP*8.33
      PALUM  =  PALUM  +  I EL I "T ( INC , TP) *WP. ALS*£ARATO*CCN
      PFECL  '  P=£CL  *  IELI^T(lNF,TP)*W!}PES*FFftATO*CON
      PLHE  *  PLIMt  «•  LI»«tTD*CCN
40S5  CONTINUE
      IF   .EO.  Ccc»   GO TO 4097
      T PL A NT (W PARC,  TERST2J  =  ( QAVE*POPR*1000.»E/3UIP( TERST2) }
     1                         /TPLANT(WVARtTERST2)
      L8VTS  =  C.
      LBNVTS  * 0.
      TLBNVS  * TLBNVS  +  L3NVTS
      TLBVS  =  TL3VS  *  L9VTS
      TLBTS  =  LBNVTS «• LBVTS
      TLBSLG  = TLBSLG  «•  TLRTS
      OTSLGE  * QTSLGE  *  TLBTS/( TSETiJD*( 10. **6. 1*3.33 )
      QTQTAL  * OTOTAL  *  CTSLGE
4C?7  CONTINUE
C        *********************
C        SLUPGE PROCFSS?S
C        V******K***********1«*
C         IF  THERE IS AN  AIR  FLOTATION THICKENER  .THEN  IT HANDLES
C        BIOLOGICAL  AND  SECONDARY SLUCGE ONLY

      TPLANT(*PA*Kt  FLOTKNI  =  TLBSS*EQUIP(FLOTKN)
     I                         /(TPLANT
-------
FILF: s
                         Pi
                                                                 CMA CCDDr:P AT I OH
4130
4150
C
c
C
4160
4170
               TLBSLG/(r.cAVUD*8.3^*(10.-*6.)l
                                     / ( TPL ANT( WVA3 ,GR VTKN) «1000. I
TPLANT
eCNMMUe
VSRFM = 1.
IF (EQUIP(AERCIG)  .Eg.
TPLANT(WPA3C, A?»OIj)
VSREU " VSAPM
C^ NT I Nil?
IF (E3UIP(ANACIG)
TPLANKWPARK,
                          EQ.
      1
                              CFF)   SO TH 4150
                             » (TPL ANT (VWAR , AEaTIG)*EOUtP< Ac
                               *OTr)TAL*lOOO.)/7.48
                        CFF)  GO TO 4170
                       = tTPLA^TlWVAR,ANADIO)*EQUIP(AN4DIG)
                         *QTOTAL*lOOO.)/7.43
      TFNSS =  TLBVS  /  *
      Ie (TPLANT(HP£<:i,
      VSREM «  VSANRK
                  ANODIC)  .LT.  TENSS)   TPLANT
-------
     : SIZF      FCPTPAN  P!                           INTERACTIVE DATA CORPORJTI Of,


      SWASTE(TP)  =  SWCC\'/2000.*365.*TPSIZE
C         **«»»<
C         CHEMICAL  HANDLING PRCCESSES


            '(WP1RP*  CECLCS) = PFECL/2.89*ECU!P(FECLFSI
      TPL ANT( WPAKNt  LI'IF^S) = PL I ^C*60UI P( LI M?FS )
      TPLANT(WPAPft  POLYCS) = PPOLY*EOUIP(POLYCS)
      TPLANTI WPA^V,  c^2 FS» = ?co2 /i^'.o./.123/1000.*fOuiP(C02 cs>
      TPLANT(HPA7^f  PCKLFS) = PfCKL/2.27*EOUIP(PCKLFS)
      TPLANT (WPAf^^f  NAOHFSI = PNAOH*CCUI P( NAQHFS )
C
r
C         END  OF  SUBROUTINE SIZE
      RETURN
      END
                                    244

-------
FILF:
               FCFTKAN  PI
                                               INTERACTIVE C4TA COc
C
c
C
c
c
c
c
c
c
c
c
c
c
c
c
c
SUBROUTINE SPFNC


   PURHQSe:
        SP^NC COMPUTES THE SIZE  OF  TH£  STORED POPULATION OVE?  ALL
      TIKS PERIODS Oc a CTV5N CONTROL  STRATEGY.


   COMWCN PLCCKS:
      SEWPOP  - THC SEWF^^O  PTPULATICN
              - PARAMETERS OF TIMF
   CALLEC 3VS
      INTIME  - READS  IN  T I'lE  HCPIZTN OF CONTROL STRfiTEGY

   AUTHOR:
      DAVID A BARNES    061CT72
      CCMMGN  /SFWPOP/  FNCTYP,  SPOPIN(2,5), SEHP3P<20)

      1  , YEAR,  SPCP,  MAXPV


      INTEGER YrAR,  SPOP,  FNCTYP


      CCMMON  /TIKE/  NOYPSf MAXTP, TPSI2E, TP


      INTEGER TP
C
C
C
c
c
c
c

c
c
1000
 2000
 2500
 C
 C
 C
 C
 2900


 C
 C
             **** ***•***£?****:*******«******« *********** 8 ***********

   ******«=*********                                 ****************

   ****************     STAP.T  EXECUTICN             ****************

   ****************                                 ****************

   ********* **********•-*»*«:************* ***************************



   GC TC  APFPCPRIMfc TYPE OF  FUNCTION

GO TO HOOOtZOOOi 3000,4000) .   CNCTYP
            LIKEA9  WITH 5 PERCENT GROWTH

CONTINUE
SLOPE =  .05 *  SPCPINtSPCP.l)
GO  TO 2500
CONTINUE
POPDLT  =  SPCPIN(SPOP,2) - SPOP I N t SPOP, 1 1

TOELT =
-------
CILE: SPC?.C    FCftTRAN  PI                          INTEPACTIVE 04TA CORPORATION


3000  CONTINUE
      SPPATO = SPCPIN
-------
FILF: SSKCST   FORTRAN  PI                           INTERACTIVE DAT* CORPORATION


      Sl3rPIJTINE SSKCST
c
C        PURPCSE:
C           SSKCST COMPUTES  THE  COST  OF  TRANSPORTING THE SOLID WASTE
C           FRCM THr TREATMENT PUNT  TO  A SINK WITH SUFFICIENT CAPACITY.
C           THIS TS DONE  FOR  EftCH  TIME  PERIOD.
C
C        CHMMCN BLOCKS:
C           PRGCNT - PPOGRAM CONTROL  VARIABLES
C           SS1NK  - CHARACTERISTICS  OF  THS SOLI1"? SINKS
C
C        CALLED BY:
C           REMOVE - THE  MAIN P3CGRAM
C
C        AUTHOR:
C           CAVID A BARNES    120CT72
C
c        	
      COMMON  /PRGCNT/  IGOTO, UNSWP-,  FIXED, FLDTE, ALPHA
      1  , YES,  NO, CN,  Or':
      2  , ISCHf
      3  , TDUMMY, DUMMY

      EQUIVALENCE (IANSWP,ANSWER)

      INTEGER  FIXEC,  FLQTE,  ALPHA
      INTEGER  YES, ON, OFF

      COMMON  /SSINK/  TfNCST, SW4STE(20», SCLSNKJ2,15) ,  SSCOST(20)
      1              ,  BFSTSS(20), CAP, OIST, MAXSS
      INTEGER  BESTSS,  CAP,  DIST

      COMMON  /TIME/  NOYRS,  MAXTP, TPSIZE,  TP

      INTEGFK  TP

      rOMMON  /TSCST/  CNSTRC, MATRLS

      REAL MATRLS
       DIKENSICK DSINK(2,15»

 6010  FORMAT  (IN ,'***** WARNING -  ALL  SOLID  SINKS ARE COMPLETELY FILLED
      \ ')


 £         ****************                                ****************
 £         ****4****»******     START  EXECUTION             ****************
 C         ****************                                ****************
 £         ************«*A****j»*********A*********************************

 C
 1COO  CONTINUE
 C
                                      247

-------
FILF:  5SKCST   PQOTRAN   PI                           INTERACTIVE  DATA CORPORATION
C        SET CAPACITY  OF  DUHwy  SINKS  TO  ACTUAL  SINKS
      DC 1500  ISNK  = l.MAXSS
      OSINMCAP.ISNK)  =  SOLSNKCAP.ISNK)
1500  CONTINUE
C
C        COMPUTE THE COST FOR EVFRY TIME  PERIHO
      DO 5000  TP =  l.MJXTP
      DSTMIN = 9999S.
      9ESTSS(TP) =  99
      SSCCST< TPJ =  0.
C
C        SEARCH ALL SINKS TO FjKiO  t SINK  FOR  EACH  TIME  PE
-------
      STPTT.Y
                                              INTERACTIVE  DATA  CORPORATION
C
c
C
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c

c
c
c
c
c
c
c

c
c

c
c

 c
c

 c
c
SUBROUTINE ST3TGY

   PUPPCS=:
      STPTGY CALLS THE SUBROUTINES WHICH ".CAD IN VALUES FOP
      THE VARIABLES OF THE OESI&E9 CONTROL STRATEGY.
      TI-ESE VA^IA^LES AP.E IN THE CATEGORIES OF: TIME, EFFLUENT
      LIKITSt OETEFGENT PESTR ICTI DNS, AND  INDUSTRIAL CDNTPOLS.

               CALLED:
              - READS IN RESTRICTIONS PN DETERGENT  PHOSPHATES
              - READS IN RESTRICTIONS ON T»EATMENT  PLANT EFFL'JENT
              - READS IN RESTRICTIONS ON INDUSTRIAL
              - READS IN DESCRIPTION OF TIME HORI7QM
      1NDLIM

      INTIME
   CALLED BY:
      »Ef»OVE  - THS MAIN
   AUTHCP:
      OAVIC A BARNF.S   06XT72
****************
*****4**********

****************
                        START  EXECUTION
                                                  ****************

                                                  ****************

                                                  ****************
   READ IN DESCRIPTION CF TIME HORIZON

CALL INTIME


   REAO IN PHOSPHORUS EFFLUENT RESTRICTIONS

CALL
   REAO IN RESTRICTIONS ON PHOSPHATES  l\ DETERGENTS
CALL
   READ IN FESTRICTIONS CN  INDUSTRIAL  PHOSPHORUS  EFFLUENTS

CALL INDLI"


   END OF SLBPOUTINE  STRTGY

RETURN

END
                                      249

-------
                :JRTP<\N   PI
                                                     INTERACTIVE DATi CORPORATION
C
C
C
C
C
C
C
C
C
C
C
r
C
C
C
C
C
C

C
C
C
C
C
C
C

C
C

C
C

C
C
                  SYSTEM
      SYSTEM CALLS THE SUBROUTINES  WHICH  READ  IN  A  DESCRIPTION  Qf
      ThE TOTAL WASTE SYSTEM. THIS  DTSCRIPTION  CONSISTS  OF  THE
      CHARACTERISTICS OF THC COWUNITy,  THC  INFLUENT  SEWAGE,  AND
      THE TREATMENT PLANT.

   SUBROUTINES CALLED:
      CMMNTY  - hEADS IN DFSCRIPTION  OF  COMMUNITY
      SEWAGE  - BEADS IN DESCRIPTION  OF  INFLUENT  SEWAGE
      PLANT   - READS IN DESCRIPTION  OF  TREATMENT PLANT

   CALLED BY:
      REMOVE  - THE MAIN
      DAVID A 34!
-------
ILF:  TRTVNT    FO*TCAN  pi
                                                   INTERACTIVE DAT*
C
C
C
C
C
C
C
C
C
C
C
C
C
C
c
C
C
C
C
C
C
C
C
C
c
c
r
c
C
C
C
C
 C
 F
 C
              r T^TMNT
           TRT«ENT IS THE MftIN COST COMPUTING SUBROUTINE. IT FIRST
           DETERMINES WHIT ADDITIONAL (IF ANY) SLUDGE HANDLING
           EyUIFPFNT IS REQUIRED f?Y THE CCMBIMTION OF THIS TREATMcNT
           PLANT AND ELIGIBLE T«?.\TMENT SCHEMF.  THEN FOR EACH TIME
           PERIDC THE FCLLOWIN3 WILL BE COMPUTED.
           1. SIZE AND CIST CF ADDITIONAL EQUIPMENT
           2. OPERATION ANO MAINTAINENCE COSTS
           3. MATERIAL AND SUPPLY COSTS.
           NOTE: THE ABOVE COSTS ARE ONLY THOSE AT73 I BUT4SLE TO
                 PHOSPHORUS REMOVAL

               BLOCKS:
           PRGCNT - PROGRAM CONTROL VARIABLES
           SCHEHE - IMFC  iOCUT LIQUID TP.EATMNFT SCHEMES
           TPLANT - INFO. 490UT LIC3UID TREATvcNT PROCESSES
           TI«E   - PAPAIETfPS OF TIME HQRUON

        SUBROUTINES CALLFO:
           BUILD  - DETERMINES MAXIMUM SIZE  OF ADDITIONAL  EQUIPMENT
           SCHOSE - CHOOSES  SLUDGE  HANDLING  PHOC^SSIS
           SIZ6     COMPUTE  INJEPENOFM  SUING PA^AMETESS  fC\  PROCESSES
           T*Tl   - CCVPUTSS  C S M  CCS'-S
           T.^T''   - Cfp'iTrs  o i M  crsrs
           cr|r.csT - co^t?jTs  crvsT'-'ucTi IN COSTS

        CALLFCIY:
           REMOVE - THE  VAIN  PROGRAM
AUTHOR:
   CAVID A BARNES
                             23  MAR  73
     CCMMCN  /PRGCNT/  IGOTO,  IANSW? i  FlXECi FLOTE, ALPHA
     1  t  YES,  NTt  CNt  OFF
     2  ,  ISCHM
     3  t  IOUMMY,
      EQUIVALENCE  ( IANSW"
      INTEGER  FIXED,  FLOTE, ALPHA
      INTEGER  YES, CN, O^F

      C3MMCN  /SCHEME/ S CHEME( 25 , 251, ELG9TY(25),
     1 ,  ALPYPS,  FCPYPS, FCL^PS, LIMEPS, ALPYF3, !=CPYF9, PCLMFB, LIMEF6
     2 t  ALU^AB,  FECLAB, NAALAB, AURMF, FCAftMF, NAA5MF, ALUMTF, F?CLTF
     3 t  ALTFMF,  CCTFMF, ALFBAS, FCPBAS, LI^SAS, LZFBAS, NONE
     A ,  FQUIP(45)
      INTEGER ELCRTY, E'.:JI', ?
      T^Tf-j---, iL^Yrs, =rPY^s, ^CLXOS. ALPYC?, CCPYCB, FCLMFB,
     1  ,  CCCI'.6, £L.'aM^, =rA3MC, ALJMTF, FECLTF, ALTFMF, FCTFMF,
                                    251

-------
FItF:
               FORTRAN   PI
                                               INTERACTIVF CAT* CORPORATION
      REAL MIMEFP

      COMMON /TIME/ N3YRS, MAXTP, TPSIZE,  TP

      INTfcGPP TP

      COMMON /TPLANT/ TPLANT(16,45)
1
2
3
4
5
6
7
8
9
RWPUMP,
MCHAER,
RE2PMP,
VACFTR,
PECRC2,
C02FS ,
PMAME ,
WVA1 ,
MAXP
PRETRT,
FLCCCP,
CaVTKN,
CENFUG,
TERST1,
NAALFS ,
AERATE,
BPARM ,

PRMSET,
SECSET,
FLOTKN,
MHINC ,
TE*ST2,
PCKLFS,
AML I CF ,
BASE ,

PSP'JMP,
? ? 1 P M P ,
4NAOIG,
F3INC ,
4L'JMrS,
N*OHCS,
0 p A tJ w ,
APVAR ,

TO-KFTP,
CLFEEO,
A ERO I G,
W SPOND»
FECLFS,
RECALC,
PVAR ,
PARMX ,

iER3SN,
CLBASN,
ORYBED,
SLGOCN,
LIMEFS,
FLOCCT
WGP4RM,
MINRV ,

DIFAIR
MULFTR
SLDTNK
RECP31
POLYPS

WPARM
MAXRV

      INTEGER RWPUVP, PRfTRT, PR^SiET, PSPUMP,  TRKFTR,  AERBSN
     1 , DIFAIR, FLCCCP» SECSET, REIPMP,  CLFEED,  CLBASN,  RE2P1P
     2 , GRVTKN, FLOTKN, ANADIG, 4ERDIG,  DPYBED,  SLDTNK,  VACFTR
     3 , CENFUG, F8INC , WSPOND, SL500N,  RECP.B1,  RECRB2,  TERST1
     A , TERST2, ALUV.FS, FECLFS, POLYPS,  CC2FS ,  PCKLFS,  RECALC
     5 , PNAME , AMRATE, A«LIPE, pPiR"  ,  PVAR   ,  WOPARH,
     6 , WVAP  , PPARM , FLOCCT,
3351 FORfAT (1H ,'SUPRESS?')
3354 FORMAT (1H , • DO YOU WISH TO S
1 • )
3550 FORMAT (1H ,«***** WARNINS -
1 PROCESS •••,3A*,»«« = «,p10.
2 ,F10.3,« TC «,F10.3)
C ****************¥*****«***
^ ****************
C **************** START
C *****************

IPRESS THE WA^NIN'J MESSAGES? (YES/NO)

THE VALUE CF THE SIZING PARAMETER FOR
3./16X," LI?S OUTSIDE TH= RANGE •

*************************************
****************
EXECUTION ****************
****************
C *************** *********«**a* **********************************
C
1000 CCNTINUE
C



C PICK THE APPROPRIATE SLUOGE HANDLING PROCESSES
CALL SCHCSE
C


C COMPUTE, FOP EVERY TIME PERIOD, THE INDEPENDENT SIZING
C PAR4YETEF FOR EACH PSOCFSS
C REMOVAL. THEN COMPUTE THE
00 2000 TP = l.MAXTP
CALL SIZE
CALL BUILD
2000 CONTINUE
3000 C°NTINUE
, WITH AND WITHOUT PHOSPHORUS
ADDITIONAL SIZE NEEDED TO 6E BUILT.





IF (IPASS .NE. 0)
IPASS = 1
                         GO TC 3500
                                    252

-------
FILE: T'T'nT   FORTRAN   PI                           INTERACTIVE PiTA CORPORATION


C
C        «SK USE"  IF  HE/SHC  DESIRES  TO SUPSESS WARNING MESSAGES
3300  CONTINUE
3350  PRINT 3351
3352  CALL 
      IP (EQUIPUPRCC)  .EG. OFFJ  GO TO 3900
      IF (TPLANT«EPARM,IPROC) .EG. 0.)  GO TO 3900
      IF ((TPLANTIRPAOM,IPROCI .LT. TPLANT(MINRV,IPROC>  .OR.
      1  TPLANTJBPAR*,IPROC) .GT. TPLANT(MAXRV,IPRCC))  .AND.  ISUP.EQ.OFF)
      2  PRINT  3550,  (TPLANT(J .I^ROC),J=1,3), TPL^NT
-------
FILE: TtUl     FORTRAN  PI                           INTERACTIVE  DATA  CORPORATION


      SUBROUTINE TRT!
C
c        PURPOSE:
C           TRT1 COMPUTES THE OPERATING  AND  MAINTAINANCE  MAN-HOUPS
C           RECUIREC AND THE TOTAL MATERIAL  AND  SUPPLY  COSTS.
C           NHTE:  «TRT1« IS SFPAP4TE  FROM  •TPTfNT*  ONLY TO  EASE
C           COMPILATION REQUIREMENTS.
C
C           THE COSTS ARE COMPUTED COP EACH  PROCESS  WHICH IS
C           BEING  USED FOR THF  CURRENT TREATMENT SCHEME IN
C           ThF FOLLOWING MANNED:
C
C           I. COSTS WHICH DEPEND ON  THE SIZE  OF THE  PROCESS
C             A. IF p .LE. O.f  THEN COST=F(B)
C             B. IF TP .LT. TPFACD, THEN COST=0.
C             C. IF TP .GE. TPFAOOi THE  COST=FtP+8|-F
-------
          FOf-ThA-J   PI
                                                 INTEFACTIVE DATS CCf-POP flT I 3*.
 F.QUIV4LEKCF  ( Ifl NJSV'P , ANSWE" )

 INTFGE9. FIXEC,  FLCTE,  ALPHA
 INTFGEP. YES,  C".,  HFF

 COMMON /SCHEME/ SCHFMC<25,25),  UGBTY<25),  1INEFP(25), MflXSCM
1 , «LPYPS, FCPYPS,  FCLN-PS,  LI«E°S, ALPY^e,  FCPYFB,  FCLMFB, Ll"EFB
2 , ALU*AP, FECLAS,  NAALAR,  ALABMF, FCABV-,
3 , ALTFMF, FCTFMF,  ALFRAS,
4 , FguiP(^5)
                                     LlFBASt  L2FRAS,  MCNir
                                                              FECLTF
 INTEGER ELGPTY, EQUIP,  SCHEME
 INTEGER 4LPYPS, FCPY"S,  <=CIMDS,  4LPYF8, cCpYFB,  FCLMFH,
1 i PECLAB, ALABMP,  PCAB«e,  U'JVTF, C6CLTF,  ALTFMF,  FCTFMF, ALC3AS
2 , FCFPAS
      MINEFP
                 FNICTYP,
  t YEAF, SPOP, MAX^V
 INTFGtff YEAR, SPOP,  FNCTYP
COMMON /SL
1
2
3
A
5
o
7
8
q
LBNVTS,
PC02 ,
QSSLGE,
TLBSLG,
WOPFC ,
Pll^E ,
SRFEF ,
W?crA ,
C020 ,
CHAR/
L8VPS ,
PFECL ,
QTPTAL,
Ttess ,
WOPLIM,
PYFTD ,
WRFEF ,
AAF.ATO,
SRTLIM,
ADOSSF , ALKIAR ^CVFO ,
L3VSS , LBVTS
PNAAL PNAOH
OTSLGE
TL«TS
WOPNAL
PYVFO
SRFEP
CFO&TO
TSETUD
SRCAT
TLBVS
^00NOH
PPOLY
S^ALP
SRCATS
LIMETD
LIMEPC,
PCLYC ,
SRLIME,
WCLRSS,
WO^PLY,
SR4LF ,
WRALP ,
WCCATS,
BODIAR,
LBNVPS,
LMVFO ,
PPCKL ,
TLBNVS,
WOPALM,
WOCPCK,
SRCATA,
WRFFP ,
WR4LS ,
WOTLBS
L3NVSS
PALUM
OPSLGE
TLBPS
WQPC02
WRCAT

WRAL4
WRFES

 REAL       LBNVPS,  LBNVSS,  LRNVTS, L8VPS
1 t LIMr.PC, L^VFO  ,  LIMETO

 CCMMQN /TIME/ NOYKS,  M4XTP,  TPSIZ5, TP

 INTEGES TP
1
2
3

5
6
7
8
<3
                                            .  LBVSS , L3VTS
    /TPL4NT/ TPLANH16,
PWPUKP, PRETRT,  PRMSFT,
MCH4EP, FLCCCP,  SECSET,
RE2PMP, GRVTKN,
VACFTR, CENCUG,
        TEPSTl,
        NA4LFS,
        AMRATE,
        6PAR»1  ,
C02FS
PN4ME
WVAR
1HINC ,
TEPST2,
PCKLFS,
A«LIFE,
BASE  ,
                             AN40IG,
                             CPINC ,
                                 CLFEED,
                                 AESDIG,
                         AHRBSN,  DI«=AIP
                         CL3ASN,  MULFTp
                         ORY?EO,  SLOTNK
                             N40HFS
FECLFS,
"ECiLC,
                             APVAR , PAPMX
LIMEFS, POLYPS
ctOCCT
        WP4BM.
        MAXRV
                                 255

-------
FILE: T->T1
                         PI
                                                INTERACTIVE DATA CCMPORATION
     ft . T5RST2,  ALUMCSt  F5CLFS,  POLYPS,  C02FS ,  PCKLFS, RECALC
     5 t PNAME f  AMp«TE,  AMLIFEi  PPARX  ,  PVAR  ,  H3PARM, WPAP.M
     6 , WVAP  ,  POACM  ,  FtOCCT,  34SE   ,  APV&S ,  PARMX

      CCMMON /TRTCST/ QMHRS(45,?0J,  MMHRS(45,20),  TMSC<^t20), CONCOS(45)
     1               , AMCOST(AS),  TPFADJU5I

      REAL MMHRS
      INTEGER TPFACC
C
C
C
C
C
C
C
C
C
C
C
C
C
C
    OPERATION, MAITAINANCE, AND SUPPLY STATEMENT  FUNCTIONS
    FOR EACH PPOC^SS:
       1. LETTER I "F THE FUNCTION NAVE  DESIGNATES TH? KIND OF
       FUNCTICN-
           ANNUAL OPERATING MAN-HOURS
           HA^TAINANCE MAM-HOUPS
           SUPPLY COSTS (JAN 71  tJ
           ELECTRICAL COSTS (JAN  71  $)
           CHEMCAL COSTS
           TCTAL MATERIAL AND SUPPLY COSTS  (JAN  71  $)
          LETTERS 2 THRU 6 CESIGN4TE THE  PROCESS.
    RAW WASTEWATER PUMPING
 ORWPMP680*ALOGIY»**4)
 ARWPMP**2)
 ERWPMP(Y) » EXP(6.799199+.735690*ALOG
 TPRTRT(Y) * EXP(7.235657*.399935*ALOG(Y|-.224979*ALOG(Y)**2
1            ».ll0099*ALOr,(Y)**3-.01l026*ALOG(Yl**4>
    PRIMARY SETTLER
 OPRMST(V| = EXP(5.846565*.254913*ALOG{Y)*.113703*ALOG(Y)**2
1            -.010942*ALCG(YI**3»
 APRMST(Y) = EXP«5.273419*.228329*ALOG(Y|*.122646*ALOG(Y)**2
I            -.Oll672*ALOG(Y)**3)
 TPRHST(Y) » EX"(5.669881*.750799*ALCG(YlI
         PRIMARY SLUOG9
                  EXP(3
                   PULPING
                   941555*.
                   993365*.
                                               )
 APSPMPIY)
 TPSPMP
    TRICKLING FILTER
 OTRKFTIYI = EXP(4.536510-.09573l*ALCG(YI*.173718*ALOG(Y)**2
I            -.OIOU4*ALOGIY)**3)
 ATRKFT(YI = EXP(4.312739-.052122*ALOG(Y)+.
1            -.010245*ALC1G( v)»*3)
 TTPKFTJY) = EXP(5. 1059^.6*.4651 00*ALCG(Y» )
                                     256

-------
PILE: T*TI     PORTPAN  PI                          INTERACTIVE DATA CORPORATION


C        AESATION 5AMN
      OAEPRM(Y) * 0.
      AA£P9N
      ADIFAR(Y) = FXP(6.169937*.29l
                  EXP(5.9115'il-.Ol315e*ALOG( Y) *.0766*3*ftLQGC Y J**2 )
      ERIPMP(Y) « EXP(6.799199*.785690*ALOG(Y)*.037865*ALOGCY)**2
     1            -.042646*ALOG(Y)**3-.004488*ALOG
-------
FILF:  T^n      FJBTRAN  PI                           INTERACTIVE  DATA COOPQP6TIDN
      I             + .07320l*ALOr, ( YJ**3-. 006680* ALOG(
       AR2PMPJY)  = FXP(5.9115U-.OlM5fl*ALOG( Y) «-.0766
-------
                         PI
                                                INTERACTIVE DATA
3200
3230
C
c
33CO
3330
C
C
3400
 CrNTl'j'JE
 IF  {E>JIP(PRET:a> .EQ. Cc=)   30  TO 3300
 IF  (TPLAM ( PP/..-'1,P'ETRT )  .GT.  0.)   GC TO
                                                 3230
 CMHPStPRfcTKT,'"' t =
 "'•IMF SIPtfTRTiTPI =
                          IPRTP.T ( QAVEftPriPR)«TPSIZE
                          APR TKTUAV^PPPR^TP SIZE
                          TPRTKT(OAV£*POPR)*TPS!ZE
GO TO  3300
ijMHP5<
            T,TPJ
                  = 0.
                  = 0.
                  = 0.
    PRIMARY SETTLE*
 CCNTIMUE
 IP <£TIIP(PpMSET|
 Ic
 TMS  (PR^SET.TP)
 GO TO 3400
 OMHPS(PP.^SETfTP)
 f^HPSIP^^SET.TP)
 TVS  (PRMSfcT.TPI
                              CFF»   GO  TO  3400
                              )  .GT. 0.)   GO  TO 3330
                              1ST(Tf>LANT(BPAp«,P|».M$ET))*TPSIZE
                          APRMSTJTPLANT(<3PARM,PR.MSET) )*TPSIZE
                          TPRMST(TPLANT(8PARM,PPMSET)|*TPSIZE
                    0.
                    0.
                    0.
 3430
 IF (TP ,LT. TPFAP-1(f>PMSET) )   GO TO 3400
 OMH9S  -QP^MST (TPL ANT ( PPARM, PP MSET ) ) ) *TPS I ZE
                   =  (APRyST(TPLANT(PPABM.PRMSET)
                  ' WSET»  -APPMST(TPLANT( PPARM.PRHSET) ) )*TPSIZE
 THS  (PPMSET,TP)  =  (TPRMST(TPLANT(PPARM,PRMSET)
1 ^TPLANTteoA^.f , P-i. WSET) I  -TPRMST(TPLANT(PP ARM,PRESET) ))*TPSIZE

                    PUMPING
    PRIMARY SLUCGf
 COMTPIJP
 IF  (EOUIP(PSPUMP)  .EQ.  OFF)
 1=  (TPLANT(PPA*",PSPUMP)  .GT
 CMHF.S(PSPUMP,TP)
 MMHRS(PSPUMP.TP)
 T^S  
-------
FILE: T.^T:      rrcTfAN  "i                           INTERACTIVE ITATA CORPORATION
      GO  TO  3600
3^30  C^HPS( TSK^TR ,TP j  =o.
      V-tHF,S (TRKFTP , TP )  = 0.
      TMS   D(TkKFTR| I  GO  TO  3600
      OMHFS(TRKFTR,TP)  = *TPSIZE
      MMHF,S(TRKFTP,T°)  = IFAIR) ) -DO IF \a (TPL AMT( PPA«M,OI FA IR ) J »*TPS t ZE
      MMHRS  = TMCHAR(QAV=*POPR»*TPSIZE
      GC  TO  3SOO
3830  0"HPS(MrMApci,Tp)  - 0.
      MVMFS(MCI-A = R,TP|  = 0.
      TMS   (MCHAER.TPI  = 0.
      Ic  (TP  .LT.  TPFADO
-------
FILE: TST1
                FORTRAN  PI
                                                      INTERACTIVE DATA CORPQOATICKJ
3*300
3S30
C
C
4000
4030
 C
 C
 4200
      IF (F.'J'JIPJFL'KrP)  .F.Q. OFF)  ^o TO 4000
      Ic (TPLANT(PP^M,FLnCCP) .GT. 0.)  GO TO
      CMHFS(FLCCCF,TP)  = OCLCCP(T?LANT(?PSPM,FLOCCPI)*TPSIZc
      MKHFMcLr;CrP,TP 1  = AFLCCP(TPL4NT(SPAPM, FLGCCP> I*TPSIZE
      TM$   (FLOCCP,TP)  = TFLCCP«7AV=*POPP)*TPSIZE
      GO TO 40CO
                        = 0.
                    TP) = o.
            (FLCCCF.TP) = 0.
       Ic  (T?  .LT.  TPFACniFLnCCm  GO TO  4000
       OMHPS(FLOCCP.TP) = (OFLCCP(TOLANT(POAPM,FLQCCP)
      1  »TPl ANT(rPA^.M,FLOCCP) • -OFLfCP(TPLANT(PPARM, FLOCCP) ) )*TPSIZE
       l*i"HPS(cLOCCPfTP ) = ( AFLCCP* TPL ANT< PPA3M , FLOCCP I
      1  +TPLANT(f)P ARM.FLCCCO) ) - AFL CCP (TPL »NT ( PPARM, FLCCCP ) ) ) *TPS I ZE
 C
 C
 4100
    SECONDARY SFTTLF«>
CONTINUE
IF  (EQUIP(StCSFT) .Fg. OFF)
Ic  (TPLANT(PPARM,SECSET» .OT,
                                     GO  TO
                                      0.)
                4100
                GO TO
4030
CMHRS(SECSET.TP)
MMHRSJSECSET.TPJ
T1S   (SECSETiTP)
GO TO 4100
OMHPS(SECSET,TP)
»HHFS(SECSET,TP)
TMS   (SECSfcT.TP)
                          CSECST(TPL£NT(BP*R^,SECSET)>*TPSIZE
                          ASECST(TPLANT(PPA9M,SECSET)
                          TSECST(TPl4NT(opARMfSECSET)
0.
0.
0.
       IF (Tf .LT. TPFACD(SECSET))   GO TO 4100
       OMHP.S(SECSETtTP) = (OSFCST ( T^LA^T ( PPARM, SECS ET )
      1 +TPLAMT'(BPAHM,SF.CSET) J-OSECST (TPL ANT| PPARM, SECSET I ) )*TPSI ZE
       .MMHP.S(SECS£TfTP) =  (ASECST(TPLA.NT(DOARM,SECSETI
      1 +TPLANT(9PARM,SECRET) )-ASECST(TPLANTIPDA^M,SEC SET)))*TPSIZE
       TMS  (SECSET.TP) =  (TSECST(TPLANT(PPARM,SEC SET)
      1 +TPL4NT(SP*RM,SECSET)I-TSECST(TPLA\T(PPARM,SECSET)))»TPSIZE
    PECIRCULAT I ON PUMPING
 CONTINUE
 IF (EQUIPCREIPMP)  ,EQ.  OFF)
 IF (TPLANTJPPA^M.REIPMP)  .GT
 OMHRS(r I J *TPS I Z E

    CHLORINE  FEPO  SVSTE"
        Ic (EQUIP(CL»:FEO)  .F.Q. OFF)  SO TO 4300
                                       261

-------
 FRF:
                FCETPAM   PI
                                                      INTERACTIVE  DATA  CORPORATION
4430
C
C
4500
4530
C
C
       IF (TPLAM (PPMM,CLFEEC»  .GT.  0.)   r,r Tn 4230
       H = (JAVE*POF»*TPLANT( WVAP ,C LP'50 » *3 65. * fl. 33/2000.
       P = 04VE»POPR*70LAN;TM , C L9ASN ) ) *TPS I ZE
                           TCLdSN ( TPL ANT ( 5P APM.CL3ASN) ) *TPS I ZE
          VULTI-MECIA
       CONTINUE
       IF   .GT.  o.i   GO TO 4430
                          CMULFT(TPLANT(BP4RM,MULFTR))*TPSIZ5
                          AMULFT»'P)
                             ) -0?2 PMP < TPL ANT ( PP4RM , q £?PMP ) ) ) *TPS I Z E
                          («S2PMPITPLANT(PPARM,RE2PMP)
                             ) -AR2 P«P (TPL ANT ( PPAosi.R P2PMP ) |) *TPS I ZE
          GRAVITY
                                     262

-------
                         PI
                                                1NTFGACTIVF  DATA CORPORATION,
4600
4«3C
C
C
4700
C'WIS'Jr
IF JFOUIP(GRVTKN)  .E'J. OFF)  GO
Ic «TPL»NT))*TPSIZE
       MMHRS(CLCTKN,TP) = (AFLCTK(TPLANT(PP4RM,FLOTKN)
      I  +TPL4NT ( 3P»^M, FLCTKN) >  -4FLOTK (T^L ANT ( PPA^i V, CLCTKN> ) ) *T°S I Z E
       TMS  (FLnTKN,TP) = (ECLCTK(TPLANT(PPA^w,=LOTKN>
        +TPLANT(bt>AR»»,
                        J  -£FLOTK(T?L«NT(
                    +TMSIFLCTKN.TP)
                                                       LOTKN) J>»TPS IZE
C
C
A800
              CIGESTION
 CCNTINJE
 IF  ( FJUIP( AN4CIG)  .EO.
 Ic  ( TPL4NTI
                               OFF)
                               1  .f,T,
                                     GO  TO
                                      0.)
4<300
OC TO
                                                  4330
       «MHRS(
            G,TP) =  04NniG(TDHNT( 3PAPM, ANA3IG) >*TPSIZE
            G,TP
       GC
4830
           S( ANAOI C-tTP
           S(
       IF (IP .LT.  TPF
             i>.^C!CfT?
             f;T OPiSM,
                  =  0.
                  =  0.
                  =  0.
                  CD( AN'CIG) )
                                   Q 4,900
                                  T(PPA^M,
                      , ) I  -J«-;DlG(TPL.A-"lT(PP4PM,ANADIG) ))*TP5I?E
                                       263

-------
FILF": TJT!      FORTPA4   PI                            INTERACTIVE DATA CO.PORM ION
        VHPSI 4>"AUI
        + TPL AN
            (4NADIG.TP)  -  (T*NDIG ) "TPSI 2E
       M1HF-S(ASiOIG,TP>  *  A ASOIG( T°L ANT( 9P A"M, AER01G) ) *TP$ I 2?
       T'-
-------
F ILC : T
-------
FILF: T
t
,

TPKFTR,
CLFEEO
AEPDI G
WSPOND
,
,
,
FPCLFS,
RECALC
PV»R
PARMX

t
,
i

AERBSN
*
CL3ASN,
ORYBEO
SLGOCN
LIMPFS
FLOCCT
,
t
t

WOPAP.M,
MINR.V

t

OIFAIR
MULPTR
SLDTNK
RECP.31
PCLYCS

WPAF.1
MAXRV

INTEGER PWPUPF, PKETPT, P^SET, PSPU^P, TRKPTR, AFRSSN
i
2
3
tt
5
&
CIF4IR,
GRVTKIS,
CENrUGt
TF.KST2,
PNAME ,
WVAf ,
FLfCCP
*
FLOTKN,
F6INC
ALUMFS
/MPATE
6PAPM
f
t
t
,
SFCSFT ,
AN40IG,
WSP1ND,
FECLFS,
AMLIFE,
FLOCCT,
RFIPMP
AF^OIG
?
*
SLGCCN,
POLYPS
PPAP.H
3ASE
,
,
,
CLFEED

RECR6J
C02FS
PVAR
APVAR
V
,
,
t
,
t
CLBASN
SLOTNK
t
t
RECRB2,
PCKLFS
WOPARW
PABMX
,
,

RE2P1P
VACPTR
TE^STl
RECALC
W P A P. M

                                                                CONCOSC«5)
                     ,  AMCOSTU5), TPFAOD«45)
      BEAL
      INT6GES  TPFADT

      CCVMCN  /TSCST/  CNSTRC,

      REAL HATRLS
         SLUPCE DFYIN5  BED
                =  EXP( 6.3 45052-. 476730*aLOGm*. 101 319»ALOG( Y )**2 )
                =  eXP(^.290039-.098293*ALOG(Y)*.075^53*ALOG(Y>**2)
      TCRYBD(Y) =  EX3! .693 1^3*-l.O*ALOG( Y) »
         SLUDGE HCLTING TANK
      OSLTNK(Y) =  EXP(5.727345*.000762*ALGG(YI*.093701*ALOG(YI**2
     I              -.006786*4LnG(Y)**3)
                                  14662*ALCG(Y)+.071402*AL3G
-------
      TRT2
          FURTFAN  PI
                                                     INTERACTIVE  DATA CORPORATION
C
r
    OVCFTL
C
C-
C
c-
 CVCFTL(Y)
 OVCFTKY)
I
 AVACFT(Y)
 SVACFT(Y)
 CVACCT(Y)
     1
 GCNFGLm -
 OCNPGI(Y) =
 ACENFG(Y) *
 TCENFG(Y) »
1 *1000.
    MULTIPLE
 OMHINC(Y) «
1
 AMHINCm «
1
 TMHINCCY) =
    FLUIOIZFC
           IS THE FOUATI3N FOH LANDFILL
           IS THF EOUATICM FOK. INCINEPJTICN
           = EXP(6.069419-.009994*ALnG(YI*.042699*ALaG(
           = ?XP(3.714368*.a50S48*ALCG(Y)-.074615*ALOG(Y)**2
             *.005085*ALPG(Y)**3)
           = EXP(4.3061lO-.093695*ALnG(Y)*.047738*ALOG('
           = EXP«-3.113515*.71S466*ALCG(Y)1*1000.
           = Y*«FCVFO*-ECLCS*LMVFO*LI*1ECS*PYVFD*POLYCS»
             EXP«7.62;5r7-.476977*ALOGCY)*.
             EXP(7.264153-.466246*ALOG«Y)*.
                                                0715!6*ALOG(Y)**?)
                                                069552*ALQG(Y)**2)
             HEARTH INCINERATION
             EXPO. 402537*1. 21 5130*ALOG«Y|-
             + . 00977 1*ALOC.(Y)**3)
             EXP( 3. 906553*. 702471*ALOG(Y)-.
             *. 006827* ALOGfY)** 3 >
             EXP(8.51^996-.252966*ALCG(Y1#.
              BED INCINERATION
                                                .157203»ALOG«Y)**2

                                                088337*ALOG(Y)**2

                                                0*5589*ALQG(Y)**2)
    NO DATA FOP FBINC
 OFBINCm = 0.
 A=8INr(Y) - 0.
 TFBINCm » 0.
    WASTE ST/8ILIZATION PC»4D
    NO DATA FOP WSPONO
 OWSPND(Y) = 0.
 AwspNom * o.
 ThSPNDlY) » 0.
    SLUDGE LAGCCW
 OSLGGN(Y) = EXf>(6. 567594-. 971 759*ALOG( Y1*.
 ASLGCM(V) - EXP(-2.0R7392*2.395831*ALOG(Y)
1            +.017<»99*ALOG(Y)**3)
 TSLGON(Y) = EXP(-3. 134169*. 763622*ALOG( Y) )
    RECARBCNATI3N
 ORCRBKY) - 0.
 ARCRBKYI * 0.
 TPCRBHY) « 0.
    PECARBCNATION
 ORCRe2(Y) » 0.
 A«CR«2«Y) * 0.
 TRCRB2(Y> * 0.
    TERTIARY SETTLE".
 OTRSTKYJ « EXP(5. 846565*. 25431 3* ALOGI Y I *.
I            -.010942*ALOG(Y)**3I
 ATRSTl(Y) « EXP(5. 273419*. 228?29*ALOG(YJ*,
1            -.01I672*ALOG(Y)**3)
 TTRSTl(Y) » EXP(5.669m*.750799*ALOG(YH
    TERTIARY SETTLEP
 OTRST21Y) « EXP(5. 846545*. 254813*ALOG(Y)*.
1            -.010942*ALOG(Y)**3»
 ATRST2(Y> * EXP(5. 273419*. 2283?9*ALOG(YI».
I            -,011672*ALOG(YI**3)
 TTRST2(Y) « EXP{5. 669881*. 750799*ALCG(Y)I
                                                095689*ALOG{ Yl**21
                                                -.340388*ALOG(Y)**2

                                                 *  1000.
                                                l 13703*ALOG( Y) **2

                                                122646*ALOG(Y)**2



                                                U3703*ALOG(Y)**2

                                                122646*ALOG(Y)**2
                                    267

-------
    : T?T2      -C&TSi\  PI                           INTERACTIVE DiTA CORPORATION)
C        ALLT  FEtDING A NT
      AM_*-Sm  =  £X?<5. 043043- ,09721H*ALOG( V > + .0390 30*ALOO( Y»*«2)
C        LIME  FEEDING Af.D STORAGE
      AIIWFS(Y)  =  FXD<6. 060054+. 197073«ALQG( Y) )
C        FF°,C. 1C  Ct-LC.DIOE FEECING AND STORAGE
      OrECFS(Y)  =  0.
      APECPS(Y)  =  ?X?(5. 9930^3-. 0972 1 8*PLOG ( Y » + .0390 10*ALOG( Y) **?)
C        PCLYMEI-  FPFOING AND ST'JRAGE
      APLYFS(Y)  =  EX"(6.'t2692<5-.061^43*aLOr,(Y)*.033i>37*#L!3G« Y»**2I
C        CARbC\  ClOXIOF FEE01NG AND STORAGE
      QCOIFS(Y)  =  PXP(6.9005R6*.323725*ALOG( Y ) *.059093*ALOG( Y»**2
     1             -.00^<>?6*ALDG( Y)**3)
      ACOP^Sm  =  FX"(6. 169937*. 294S 53*SLOG ( Y ) +. 1 75999*UOG< Y ) **2
     1             -.040947* ALPG(Y)*»3^.003300*ALOG(Y)**4)
      TC02FS(Y)  =  EXPd. 999679*. 703339*' LOG ( Y ) *.0 102 14*ALQG( Y I ** 2 )
     1 *iooo.tcn2; -PC02
C        SODIUM  ALUMINATE FEEDING AND STORAGE
      ANALFS****

                              START EXECUTION             ******
      W  =  TLBSLG * 365. / 2000.
      WO = W3TL°S*365./2000.
C
c         SLUCCE  CRYING BEDS
5000  CCMTIMUF
      Ip  (E JUIPl C-.YPEO) .cC. CPp)  GT  Tn  5100
                                >GT> 0>,   GC  T0 5030
                    TO )  = ATO ygo ( W ) * TPS
                                     268

-------
FILE: Tu,T2      FfPTt-A^  PI                           INTERACTIVE  OA^  CORPORATION


                        = TORYbDtVO-TPSIZF
      GH TO  5100
5030  P"HPS(r>: Y^CC iT>- )  = ( DC -iYBC ( d) -OUP YBO (WO ) )*ToSt ZE


C        SLUDGE  HOLDING TANK
5100  CONTINUE
      I- (EO'JIPISLHTMO .EO.  OFF)   GO TP 5200
      Ic (T^LANT(PPfl=v,SL3TNK)  .GT.  0.)   GC TO 51 JO
      OMHRS(SLCTNK,TP)  = HSL TNK ( T^L ANT ( 9P iRM, SL ")T NK I
      MMHF S( SLPTNKtTPl  = ftSL TNK ( T°L \NT ( BP A1? Mt SLOT NK ) ) *TPS I ZE
      TVS   (SLHT'JKtTP)  = TSL TKK ( TPLA\T( PP A^M, SLOTN^I )*TpS I ZE
      GO TO  5200
5130  CMHRSlSLCT\K,TP)  = 0.

      TKS   (SUDT\K,TP)  = 0.
      IF (TP ,LT.  TPFADD(SLOTNK))   GO TT 5200
      CVHRS(SLCTNK.fp)  = (OSLTNK(TPL ANT(PPiR",SLOTMK)

      MMHPS^SLCT^:K^TP ) =  ( iSLTNXt TPLANT ( PPARM , SLDTMK )
      i  -I-TPL Ar-.Tt-ap/s^NtSi.mNK)» -ASLTNK)) *TPSI ZE
C
C         VACl'UV FILTF.*
5200  CC\TINUF
       IF  (EQUIP(V*CFT<)  .60. OFF)  GO TO 5300
       IP  (T°L£NT(PPARvi,VACFT=<) .GT. 0.)  GO  TO  5230
      CMHRSIViCFTP,TP) =  OVCFTL(W)*TPSIZE
       \c  tFQUIP(M.HINC)  .=Q.  ON .PR. E OUIP( FBINC)  .EO. CN)
      1  GMHRS)*TPSIZF
       IF  IEQUIP<^HU'CI  .C0. CN .OR.  EOUIP(F3INC)  -EQ. ON)
      I  G*HkS(VACFTR,TP)  = (CVCFTIIW)-GVCFT I (WO ) )*TPS I ZE
       MMHFS(VACFJF,TP|  =  (AV*CcT(A}-AVACCT(WO>I*TPSIZE
       T«is    (vACFTPtTP)  =  ((svACFT(w)<-cv£CFT{ w»)-« SVACFTJHOJ+CVACFTIWCI))
      1                     *TPSIZF
 C
 C         CLNT9IFUGE
 5100  CCNTINUE
       IF (FQUlPtCE'JF'JG)  .EQ.  CF~)   GO TO 5400
                                  .GT.  0.)   GO TO 5330
       IF (FQUIP(MHINCI .FQ. OK  .OR.  rOUIP(F9INC) .E3. CM)
      1 0"!HRS ( CEN'FUG.TP ) = OCNFGK W )»TPSUr
                     TO) = TCENFG(W)«TPS!ZE
       GO TO  5^00

       IF < EQUIP( PHUC ) .EO.  ON  .OR.  cQU IP ( FR INC ) .?Q.  ON)
       1 CNHRSCCfNFUG.TP) =  (CCNFGI(W)-CCN*GI(HO))*TPS!ZE
                   ;,TP) = (ACENFG(W)-ftCENFG(WO))*TPSIZE
                                       269

-------
   ?: TOT?
               FCfrTFAN
                                                     INTERACTIVE DATA
      IMS  (CENFUG.TP) *  (TCENFG(W)-TCFNFG(WOII*TPSIZE
c
c
5400






PUL T I PL E


-HEARTH







INCINERATION
CONTINUE
IF
IF

IF.OUIPIM

-------
FILE
       OT?
               F^Fnri   PI
                                                      INTERACTIVE  0*T\
C
C
8COO
8030
C
C
8100
      1=  |F;j'MP»RPC*P2»  .^0. CFFI  GO  TO  flOOO
      0'"HFS(tL A.MT( pf>4R% TfhSTl )  .C-T. 0.) 00  TO
                                                8030
      QMHfiS( TERSTliTP)  =
      MMHRSITEPSTJ .TP)  =
      IMS   ITFRST1.TP)  =
      Gfi TC 8100
      CKHPS(T£RST1,TP)  =
      T«1S  (TERST1.TP)  =
                          J1T&STI (TPLiNT( BP«0", TERSTl ) )*TPSI ZF.
                          AT* SU ( TPL ANT ( BPAR^, TE*$T 1) ) *Tf>SI Z£
                          TTBSTl(TPL4NT< 30iPMt TE3ST1) l»TPSt ZE
                          0.
                          0.
                          0.
       IP  (TP  .LT.  TPFAOD(TEOSTI) )   GO  TO 8100
       CMHPS1TERST1 ,TP)  = ( GT "-ST1 1 TPL ANT ( PP ARM , TE*ST 1 )
     1 +TPLA«JT(BPA-V, TfRSTi. j J -uT^STi (TPL ANT ( PPAR% T£RST1 ) ) ) *TPS UE
       MMHPS«TERST1,TP)  = ( iT".ST 1 { TPL ANT( PP fiR M , TER ST 1 )
     1 *TPLANT(B°Aoy,TER5Tl) ) -AT^STL (TPLANT { PPAR"t T ERST 1) ) I *TPS HE
       IMS   (TSRST1.TP)  = 
      1  «-TPHNT(B°ARM,TE.-vST?) )  -CTRST2 (TPL ANT( °P4RM, TERST2 » ) » *TPS I ZF
      MMHRS(T£RST2tTP ) = ( ;. TR ST 2 ( T PL ANT ( PP te M , TER ST2 )
              Ttopa^w.TFRSJZ) 1  -A TRST2 (TPHNT< opARM, TEPST 2 ) ) ) *TPS I ZE
            (TFRST?,TP) = ( TTRST2 ( T°L ANT ( "i>ARM , T=RST2 )
      1  +TPLANT(BPtP",TE3ST2) )  -TTR$T2 (TPL4NT ( PPA^«, T5P-ST2 ) ) » *TPS I ZE
C
C
8200
          ALUM FSECIKG ANC
       CONTINUE
       IF (EOUIP( ILU^FS)  .EO.  CF-)  GO TO  8300
       W
       WO
       OMHPS(ALU«CS,TP) = 0.
       IF «TPL ANT(PP/>OM, ALUWCS >  .CT. 0.)   GC TO  3230
       IF  (W .GT. 100.)
       TMS  (ALUMFS.TP)
       GO  TO 8300
 8230   K^HPSULUMFS.TP >
                               ( ALUMF5.TP I  =
                                       (WVAP
                                              A4L «F S ( W ) *TPS I Z E
                                              ALUKFS >*365.«TPSI
                         =  ( AA I «F S ( W I-AAL «FS ( WO ) )*Tt>SI 1*
                                      271

-------
    : TRT2      FUPTRiN   PI                           INTERACTIVE OAT4 CORPORATION
            CALUHFS.TP)  =
     I                    -WOP4L 1«T°L4NT(3VAP,ALUMrS)
C        ITMP  FEEDING  AND  STCPAGF
8300  CO*ITI,\JJF
      IF »E3UIP(LI>»EFS)  .EQ.  CFFI  GO TO 8*00
      W *  PL I "IF
      WO  wnPLIM
      Cl*HFS(L IKEFS.TP) * 0.
      IF ITPlANTIPPASf'tLIMEPS)  .GT. 0.)   GC TO 8330
      MMHPSIL IMEFS.TP) = ALIMFS(H)*TPSIZE
      TMS   JLI«EFS,TP) «= PL I M£*TPLANT (WVA* , LI MPFS 1*365.«TPSI ZE
      GO T3 8*00
8330  ^MHesa IMEFS.TP) = »*TPSIZE
      IMS   CLIMEFS.TP) * (PLIWE*TPLANT,POLYPS)
     1                   -WOPPLY*TPL6NT
-------
FILF: T»T?     FCFTRA'4   PI                           INTERACTIVE DATA CORPO^/TIT


fltBO  G"HKS(C'-2FSfTP) =  0.
      •IT< WVAR .NIAALFS » *365. *TPSI ZE
      GC TC  3ROO
8730  ^HFS(MAALFS,TP)  = < ANALFS< W)-A*»ALF$ ( KO ) »*TPS I ZE
      TMS  (NAALFStTPI  » ( PNAAL *TPL'.NT( WVAR.MAALrS)
     I                   -WOPNAL*TPHNT(PVAR,NA4LFS> ) *365.*TPSIZE
C
C        PICKLING LIQUOR FEEDlMi AND STORAGE
8800  CONTINUE
      IF CKL*TPLANT(WVAR,PCKLFS)
     1                   -WOPPCK*TPLANT(PV4R.PCKLeS))*365.*TPSIZ E
C
C        SODIUM HYOPOXIOF  FEEniNG  AND  STORAGE
C	     KO  DATA FOP  NAOHFS
esoo  CCNTIMJE
      Ie LANT(v»rPARM,RECALC)
       IF  JTf>LANTtPPA<>M,REClLC) .GT. 0.)   GC  TO  9030
       OMHF.S(PECALC, TPI = C^C ALC i W ) »TP$I ZE
       MMHRS("ECAIC,TP) « ARC4LC(W)*TPSIZE
                                     273

-------
FILE: TkT?     FCRTRAM  Pi                           INTERACTIVE DAT* CCRPOR AT I ON
      TMS  MEC^LCiTP)  =  T"CALC(W)*TPSIZE
      GO TO 9100
9030  C"HPS( ^EC&LCtTO J  =  (  C ALC ( W ) -OPC AL C < WO ) ) *T PS I Z?
      MMHDSUFCALC.TP )  =  (ARCALC<*)-AFCaLC*TPSIZE
C
C        FLOCCULATICN  B^ORF TERTIARY
9100  CONTINUE
      IF (EQ'JIP(FLQCCT)  .EQ. QFF )   GO TO 9200
      IP (TPLANT)  =  OFLCCT(TPLAMT(^PARM,FLOCCT» )*TPSI 7E
      MVHPSP4RM, FLOCCT ) ))*TPSIZE
      MMHPS(FLOCCT.TP)  =  ( AFLCCT ( TPLfNT ( PPAS M , FLOCCT )
     1 *TPLANTJ3PA^Mf FLQCCT) ) -4FLCCT (TPL ANT ( PPARM, FLCCCT I ) ) *TPS I ZE
9200  CONTINUE
C
C        CCNVERT  JAN 71  S FOR MATERIAL S SUPPLY COSTS  TO  PRESENT LOCAL  t
      DO 9900  IPPOC  =  It^AXP
      TI"S< IPFOCfTP)  =  TKS(IPRCCiTP) * MATRLS/1.122
9SOO  CCNTI^UE
C
C        END  OF SC3PO'JTIN= TRT2
      RSTUKN
      END
                                     274

-------
FILE: TSCH«=
                        PI
                                                     INTERACTIVE OAT.' CO^ORAT I ON
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
c
      SUBROUTINE


         PURPOSE:

            TSCHME INITIALIZES ALL THE DOMAIN VARIABLES  NECESSARY  TO

            SIZE VIPAPM(J) (THE INDEPENDENT SIZING  PARAMETER  WITH

            PHCSPHOSUS REMOVAL TRF4TMENT  FnR FfCH  pRQCESSni).   THIS IS

            OONE FQF A PARTICULAR CLIGI«LC TREATMENT  SCHEM?IES).


         CHMMON BLOCKS:

            LIQUID -LIQUID INFLUENT  INFORMATION

            PRGCNT - PROGRAM CCMT3PL  VARIABLES

            SLCHAR - SLUDGr,LIQUID,CHEMICAL CHARACTERISTICS
            SLUDGE - SLUDGE CHARACTER ISTICS

            TPLANT - CHARACTERISTICS  CF TREATMENT  PROCESSES


         CALLED BY:

            SIZE   - THE INDEPENDENT  PARAMETER  SIZING SUBROUTINE


         AUTHORS

            DAVID A 3ARNES   13CCT72


      COMMON /LIOUIC/ ALKIPS, BODIFS,  MLSSAR, NH3IAR, PINPS,  QAV£

     1               , QPEAK, SSINPS,  TBOOAR


      REAL MLSSAR, MH3IAR


      CCHMON /PRGCNT/ IGOTD, IANSWP,  MXEO, FLOTE,  ALPHA
     1 , YES, NO, CK, OFF

     2 , ISCHM

     3 , 10UM«Y, DUMMY


      EQUIVALENCE (IANSWR,ANShFR)


      INTEGER FIXEC, FLOTE, ALPHA

      INTEGER YES, CN, OFF


      COMMON /SCHEME/ SCHEME(25,25),  ELGBTY(25J,  MINEFPI25),  MAXSCM

     1 , 4LPYPS, FCPYPS, FCLMPS, LIMfPS,  ALPYFB,  ^CPYPB, FCLMCB,  LIMEFB

     2 • ALUMAB, PECL4B, NAALAB, ALABMF,  FCA8MC,  NAAB^F, ALU^TF,  F^CLTF

     3 , ALTFMF, FCTFMF, ALF3AS, FCF6AS,  L1F3AS,  L2F3AS, NONE
     4 , EQUIPS)


      INTEGER ELGBTY, EQUIP, SCHEME

      INTEGER ALPYPS, FCPYPS, FCL^PS,  ALPYFB, FCPYFB, FCLMFB, ALU^AB

     1 , FECUB, ALA8MF, FCAB«C, ALUMTF,  PECLTF,  ALTF"F, FCTFHF,  ALC6AS

     2 , FCF?«S

      REAL MINEFP
             /SLCH/R/
     1 , LB^VTS, L^VPS  ,
     2 , PC02  , P^eCL  ,
     3 , SSSLGE, CTCTAL,
     4 , TLBSLG, TLPSS  ,
     5 , WOPPC , WOPLIM,
     6 , PLIME , FYFTD  ,
ADOSSP
LBVSS
PNAAL
3TSLGE
TLBTS
WQPNAL
PYVFD
ALKIAP
LPVTS
PN4CH
SRCAT
TL^VS
WP°MC?H
PP'JLY
FCV^D ,
LIMEPC,
OCLYC ,
SRLIME,
WnLRSS,
W1PPLY,
SRALF ,
                                                  LBNVPS,  LBNVSS

                                                  LMVFP ,  PALU""

                                                  PPCKL ,  OPSLGE

                                                  TLBNVS.  TL^PS

                                                  WQPALM,  WO"C02

                                                  WO«»PCK,  W
-------
FILE:
                         PI
                                                 INTFPACTIVt DATA CORPORATION
7 »
9 , KRFEJ  ,  iABATC,  F.= C4TC,
9 t Cn20   ,  SRTLIU,  TScTUOi
 PEAL
CCMHHN  /SLICGF/
             L«NVPS,  L5NVSS, LRNVTS.
                                                 ,  W°.FEP ,
                                                 t  WRALS ,  WRF5S
                                                 ,  WOTLBS

                                                 ,  LBVSS ,  LBVTS
ASD   t
PSR^VE,
FLOTUD, GP.AVUOi
VFPStG, VSAN=M,
                                          HfDFT
                                                   HPDVF
                                                                PSETUO
      CCMMDN  /TPLANT/  T°LANT(16,45)
1 t
2 ,
3 ,
  »
         F'WPUMP,
                                   , TRKFTR,  AER3SN,
                            OIFAIR
                            MULFTR
                            SLOTWC
                            RECRS1
                            POLYPS
             r *\ r ' ^ ' f  '^'"Ji-'f  ^ j >" *j • i r f
             FLCCCP,  SFCSET,  REIOMO, CL^EEO,  CLBASN,
             GRVTKN,  FLOTKN,  ANAOIG, AEROIG,  DR.Y3EC,
4 , V^CFTR,  C?NF(JG,  MHIN;C ,  C3INC , WS^OMO,  SLGQtN,
5 , PGCRR2,  TEPST1,  TFPST2,  AL'J^FS, FECLFS,  LIMEFS,
6 t CQ2FS  ,  NA/IL^S,  PCKLFS,  NAOM^S, FECALC,  FLOCCT
7 t PNAME  ,  4MRATE,  A^LIFE,  PPARV , PVA"   ,  WQPAPM,  WPARM
8 f WV43   ,  flPARM  ,  B4SE  ,  APVAR , PARMX  ,  MINPV ,  MAXP-V
9 , MAXP

 INTEGcK RWPUMP, PRFTRT,  PFVSET, PSPU^P, TRKFTR,  AEPBSN
                         5T,  ^EIPMP, CLFEED,  CLBASN,  RE2PMP
                         •IG,  AEROIG, DRY3EO,  SLDTN'K,  VACFTR
  t LC^'-u^,  rair.u  ,  war.JNDf  SLGGCN, RECR61,  RECRB2.  TERST1
  , TERST2,  SLUMPS,  FECLCS,  POLYPS, CC?CS  ,  PCKLFS,  RECALC
  , PNAME  ,  4MRATE,  AMLI=E,  PPARM , PVAR   ,  WOPARM,  WPARM
  , WAR   ,  BPARM  ,  FLOCCT,  BASE  , APVAR  ,  PAOMX
                »        t  SECS5T,
     2 t G3VTKN,  FLCTKN,  A>4«DIG,
     3 t CENFUG,  F3INC  t  HSP
     4 , TERST2,  ALUMFS,
     5
     6
      INTFGER  ES
c
1000
1500
         ****************
 CONTINUE
 00 1500  IPROC =
 TPL*NT< k«VAR,
 CONTINUE
 L3NVPS = 0.
 LPNVSS = 0.
 LBNVTS = 0.
 TLBNVS = 0.
 LBVPS = 0.
 LBVSS = 0.
 LBVTS = 0.
 TLBVS = C.
 TLBPS = C.
 TLBSS = 0.
 TLBTS = 0.
 TLBSLG = 0.
                              START EXECUTION
                          = TPLAMT ( PVAR , I PRCC )
                                                     ****************
                                                     ****************
                                                           **********
                                    276

-------
FILE:
               :CRTF.n  PI
                                                    INTERACTIVE DATA COCPORATION
CPSLGP = 0.
QSSLG.= = 0.
QTSIG- = 0.
QTCT*L = 0.
ACCSS^ = 0.
ALKIAR = M.KIPS
PCVFD = 0.
LTMF00 = 0.
LMVCT = 0.
P'LU^ = 0.
PCQ2 = 0.
PC£CL = C.
PNAAL = 0.
PN40H =0.
PCLYO = 0.
PPCKL = 0.
S»CAT = o.
SPLICE = o.
WPCAT = 0.
PLIM? = 0.
PYFTD = 0,
PYVFD = 0.
PP3LY = 0.
SRALF = o.
SRCATA = 0.
SRFfc = 0.
W=IFEF = 0.
SRPEP = 0.
WPFEP = 0.
SRALP = 0.
HPALP = C.
W^ALA = 0.
WFEA = 0.
W9CATS = 0.
SRCATS = 0.
AAPATO = 0.
F=FRATn = 0.
C020 = 0.
LIMETD = 0.
S^TLIM = 0.
TSPTUD = I.
WRFES = 0.
W=IALS = 0.
VIBALF = 0.
If (ES .Eg. ALPYPS)
IF (ES .EO. FCPYPS)
IF CS ,E!3. CCLMPSJ
IP (ES .EQ. LI^=PS)
IF 
-------
FILE:
                FTRTKAN   PI
                                                     INTERACTIVE DATA CORPORATION












2100
C
f»






2130




2135
IF
IF
1^
IF
1 =
\c
1C
IF
IF
JF
IF
IF
= S .
FS .
ES .
€S .
FS .
ES .
ES .
CS .
ES .
SS .
FS .
r.s .
CONTINUE
F.Q.
EQ.
E3.
Eg.
EO.
fQ.
FO.
FQ.
E-3.
EC.
FO.
EQ.

ALUM +
HBAIP =
SRALP *
WPC/T =
SRCAT =
PSETUD =
AARATO =
CONTINJE
AOC5S* =
PCDIAR =
POLYD =
GRAVUO =
CCNTIN'JF
2.
5.7
WAL
AUBMF)
FCABMF)
NiASKF I
ALUMTF)
FfCLTF )
ALTFKF)
FCTFMP )
ALPHAS)
CCF('AS )
L1FBAS)
L?F«)AS)
NPNE )

PCLYVER


P
GO
GO
GO
GO
GC
GO
GO
r,o
GO
GO
GO
GO

TO



TO
TO
TO
TO
TO
T1
TO
T-"t
TO
TO
TCI
Tfl

PR



4300
*500
4700
4900
5100
5300
5500
5700
5900
6100
6300
6400

IMA^Y SETTLER



SPALP
.03
11.

50.
.5
.5
.05





* 30DIPS



























      IF    GO TO 2153
                              ON  .AND.  (EQUIPtANAOIG) .EO. ON
                             60.  ON  H   GO TO 2155
                              CM  .4NO.  VAR ,V4CFTR )
      GO TO 2159
                                    278

-------
Fllf:
                         PI
                                                      INTERACTIVE  DAT4  CQRPP3AT I'„•••
2157   FCVFD  =60.
       LMVFO  =  160.
       TPL *NT(h ViR
       GC  TQ  2159
2155   CCNTIN'JF.
       TPLf\T(HVAc
       Ie  (=ECLFS)  =  OFF

TPLANT (V.VAR ,V4CeTR )  = 6.
Ir
                                        200
                                    OP  TO  2740


                                    GO  TO  2740
                                   TPL ANT(WVAR,VACFTS)
                                     279

-------
FILF: TSCH->7   FCPTRAM   PI                            INTECACTIVF  DATA CORPORATION
2<5CO
C           AL'JX  *  PC'LY'-ifH TC FLOCC'JUTION BASIN  BEFORE  PRIMARY
C
      GO TO 2100
3100  CONTINJE
C           FERRIC  CHLORITE + PJLYMS3 TO FLOCC'JLAT ION  BASIN
C
      GO TO 23CO
3300  CTNTIN'Jt
C           FSRPCIS  CHLORIDE * LI^S TO FLOCCULATION BASIN
C
      GO TO 2500
3500  CCMTIN'JfE
C           LIME  TO  THE  FLOCCULATtPN PiSIN BEFORE PRIMARY
C
      GO TJ 2700
3700  CONTINUE
C           ALUM  TU  TH£  Af^ATIQrj BASIN
C
      WRALA a  2.
              =  11.
3730  CONTINJE
      ASC  *  .015
      GPAV'J9=  .07
      TPLANTUVA
-------
FILF: TSCH^c   FCPTFVl   PI                           INTERACTIVE DATA CORPORATION


      AAP«TQ = 11.
      Gn T.T 3730
4500  CPNTINiJE
C           FERRIC CHLORIDE  TO  AcRATICN BASIN » MULTI-MEOU FILTER
C
      WRFEA = 3.5
      SRCATA = 4.8
      FFR.AT3 = 2.89
      GO TO 3730
47CO  CCNTINUe
C           SOOIUK ALUMINATP TC AERATION BASIN * MULTIMEDIA FILTER
C
      WRALA * 2.
      S»CATA = 3.
      AARATO * 
-------
 FILF:  TSCM'-f   FCST=£N   Pt                           INTERACTIVE DAT4 CORPORATION


       GO TO 4930
 5700   CTNTINUF
 C            ALUM TO FUnCC'JLATIC.M  9ASIN  AFTGF  CONVENTIONAL SECONDARY
 C
       WPALS = 2.
       S?ALS = 3.6
       W^C'TS = WRALS
       S'CATS = SP.ALS
       AAS A TO = 11.
       TSETU3 = .015
 573C   CONTINUE
       GD.AVUO * .06
                  ,G°VTKNI = 10.
                  PKFTR)  .EO. OFF)  GO TO  5740
       GxAVUO = .07
       TPLANTChVAR ,GCVTKN) = 12.
 5140   CONTINUE
       IF  IEOUIPIAFRBSN)  .EO. CN .AND. (EOUIP(ANADIG)  .EO. OFF
      1 .AND. ECUIPUE^DIG) .EO. OFF))   GO  TO  5751
       IF  (EO'JIP(TRKFT  .EO. OFF
      1  .AND. EQUIPUPROIG) .EQ. CFF))   GO  TO  5753
       IF  «EOUIP(/!E*PSN)  .EQ. CN .ANC. (E OU IP( «NAOIG)  .EO. ON
      1  .OF..  EC'JIP(AeRDIG) .FQ. ON I)   GO  TO  5755
       If  
-------
      TSCHXfc-.
                        PL
                                                     INTERACTIVE DATA COPPO^ATI
6130
63CO
C
c
6400
C
C
C
«420
£430
LTMETO =  150.
If  J4LKIPS  .GT. 300.1   tntTD  =  2<10.
SBTLIM »  3000.
CC29 = 1400.*!. 2
TSETUO =  .04
CONTINUE
G"AVU9 »  .10
TPLANTCWVAR tGRVTKN)  =  20.
PFTUKN
CONTINUE
      L1CE(2-STAG-:J  TO FL1CC.  5FTER  CONVEN.  SECONDARY
                             LI^ETO  =  400.
 LIKETO  -  30C.
 IF  IALKIPS  .GT.  150)
 SRTLTM  =«  TOCO.
 C02D  *  3000.*!. 2
 TSETUO  *  .03
 Gr  TO 6130
 CONTINUE
    NO  CHEMICALS  4DDfO FCfc PHOSPHCRUS REMOVAL

 SORIAR »  .7 * 90DIPS

 TPLANT « 12.
 CONTINUE
 Ic (EOUIP(#ERBSN)  .EQ. OFF)  GO TO 6430
 GRAVUO -  .06
 TPLANT
-------
FILE: TSCH«"E   FORTRAN   PI                           INTERACTIVE  DAT4  CORPORATION


      LMVFO = 160.
      on TO
C459  CONTINUE
      TPLANTI PVAR,C^Y3EC)  =  2.3
      IF 
-------
                         SECTION IX

                  ACKNOWLEDGEMENTS
The support and assistance of the Project Officer,  Mr. Hugh Maynard
of the Office of Planning and Management,  Environmental Protection
Agency, is acknowledged with sincere thanks.  In addition,  the
assistance of Mr.  Robert  Smith, Mr. Robert Eilers, and Mr. John
Convery of the Advanced Waste Treatment Laboratory, National
Environmental Research Center, Cincinnati in providing us with a
Fortran program for sizing and costing elements of waste treatment
plants is greatly appreciated.

The authors also wish to acknowledge the support of their colleagues,
Mr.  Ronald Orner  and Dr.  Gerald Foess in helping  with the design of
the model and providing data on liquid and solids treatment and
handling schemes.
                              285

-------
                             SECTION X

                            REFERENCES
Section IV


1.    Van Fleet, G. L. , Barr,  J.R.  and Harris,  A. J., "Treatment
      and Disposal of Chemical Phosphate Sludges in Ontario," 45th
      Meeting WPCF,  Atlanta,  Georgia, October,  197Z.

2.    Personal Communication, R. Bunch,  December 12,  1972.

3.    Warren,  C.B., Malec, E.J.,  Science,  176,  272-279,  April  21,
      1972

4.    Business Week,  October  28, 1972, p. 41.

5.    1968 Inventory Municipal Waste Facilities, Environmental  Pro-
      tection Agency Publication No. OWP-1, 1971.

6.    "Metro-The  First Ten Years," Metropolitan Council of Seattle.

7.    Converse, A.O., "Optimum Number and Location of Treatment
      Plants,"  JWPCE, 44_, 8,  August 1972. August 1972

8.    Basin Management for Water Reuse,  EPA Report No.  16110EAX,
      February 1972.
Section V

1.    Ferguson, J.F.  and McCarty, P.L. , "Effects of Carbonate and
      Magnesium on Calcium Phosphate Precipitation," Environ. Sci.
      Technol.  5_,  534-40(1971).

2.    Jenkins,  D.  Ferguson, J.F.,  andMenar, A.  B. , "Chemical
      Processes for Phosphate Removal," Water Research, 5,
      369-89(1971).

3.    Cecil,  L.K. , "Evaluation of Processes Available for Removal of
      Phosphorus  from Wastewater,"  EPA,  Project No.  17010  DRF,
      Contract No. 14-12-581 (October 1971).

4.    Shindala,  A. ,  "Nitrogen and Phosphorus Removal from Waste-
      waters - Part 1",  Water and Sewage Works,  66-71 (June  1972).

5.    Minton, G.R.,  and Carlson, D. A. ,  "Combined Biological-
      Chamical Phosphorus Removal", Jour. Water Poll. Control Fed.
      44,  1736-55  (1972).
                               287

-------
 6.    Van Fleet, G.L.,  Barr, J.R. , and Harris, A.J., "Treatment
      and Disposal of Chemical Phosphate Sludges in Ontario," paper
      presented at the 45th Annual Conference of the Water Pollution
      Control Federation, Atlanta, Georgia (October 1972).

 7.    Thompson,  J.C.,  "Removal of Phosphates at  a Primary Waste-
      water Treatment Plant,"  New England Jour.  Water Poll. Control
      Fed., 6,  121-37 (1972).

 8.    Weller, L.W. and Wahbeh,  V. N. , "Design of Waste-water Treat-
      ment Plant Additions at Rochester, New York,11 paper presented
      at the 45th Annual Conference of the Water Pollution Control
      Federation, Atlanta,  Georgia (October  1972).

 9.    Process Design Manual for  Phosphorus Removal, EPA Program
      No. 17010 GNP, Contract No. 14-12-936 (October 1971).

10.    Convery,  J.J., "Treatment Techniques for Removing Phosphorus
      from Municipal Wastewaters, " EPA Water Pollution Control
      Research Series, 17010---01/70 (1970).

11.    Long, B.A., Nesbitt, J.B., and Kountz, R.R.,  "Soluble Phosphate
      Removal in the Activated Sludge Process - A Two Year Plant
      Scale Study, " presented at the 26th Annual Purdue Industrial
      Waste Conference,  Purdue  University,  LaFayette,  Indiana
      (May 1971).

12.    "Development of Phosphate  Removal Processes," Detroit Metro
      Water Department, EPA  Water Pollution Control Research Series,
      17010FAH07/70 (July 1970).                               ~~

13.    Leary,  R.D. , Ernest,  L.A. , Powell, R. S. and  Manthe, R.M. ,
      "Phosphorus Removal with  Pickle Liquor in a 115 MGD Activated
      Sludge Plant,"  Sewerage  Commission of the City of Milwaukee,
      Wisconsin,  EPA Water Quality Office,  Grant  No. IIOIOFLQ

14.    Gulp, R. L. , and Culp,  G.L., Advanced Wastewater  Treatment.
      Van Nostrand-Ruinhold New York (1971).

15.    Adrian, D. D.,  and Smith, J.E., "Dewatering Physical-Chemical
      Sludges, " presented at the Conference on Applications  of New
      Concepts  of Physical-Chemical Wastewater Treatment, sponsored
      by the International Association of Water Pollution Research and
      the American Institute of Chemical Engineers, Vanderbilt University,
      Nashville, Tennessee (September 1972).

16.    Schmid, L.A., and McKinney, R.E., "Phosphate Removal by a
      Lime-Biological Scheme." Jour. Water Poll.  Control Fed. 41,
      1259-    (1969).                                          ~~
                              288

-------
17.   Grigoropoulos, S.G.,  Vedder, R.C.,  and Max, D. W. , "Fate of
     Aluminum-Precipitated Phosphorus in Activated Sludge and
     Anaerobic Digestion," 43. 2366-82 (1971).

18.   Malhotra, S.K. ,  Parrillo, T.P. ,  and Hartenstein, A. G. ,
     "Anaerobic Digestion of Sludges Containing Iron Phosphates,"
     Jour. San. Eng.  Div. , Proc. Amer. Soc. Civil Engr. , SA5,
     629-46  (1971).

19.   Singer, P.C., "Anaerobic Control of Phosphate by Ferrous Iron,"
     Jour. Water Poll. Control Fed. . 44, 663-69 (1972).

20.   Wildi,  P. , "Operating Experience and Results Using the Simul-
     taneous Precipitation of Phosphates in Activated Sludge Plants
     for 5,000 to 30,000 Inhabitants in the Canton of Zurich,"  Water
     Research, 6_, 477-79 (1972).

21.   Shuckrow, A.J., Bonner, W. F. ,  Presecan, N. L. , and
     Kazmierczak, E.J., "A Pilot Plant Study of Physical-Chemical
     Treatment of the Raw Wastewater at the  Westerly Plant in
     Cleveland, Ohio,"  Water Research, 6, 619-26  (1972).

22.   Saduk,  S. E. , "An  Electrochemical Method for  Removal of
     Phosphate from Waste Waters," EPA Water Pollution Control
     Research Series 17010---02/70 (1970).

23.   Bell, G.R.,  Libby, Div. and Lordi, D. T. ,  "Phosphorous
     Removal Using Chemical Coagulation and a Continuous Counter-
     current Filtration  Process," EPA Water Pollution Control
     Research Series 17010 EDO 06/70 (1970).

24.    Ewing, L. ,  "Phosphate Removal  Systems for Small Activated
      Sludge Plants," a paper presented to the Pennsylvania's Water
      Pollution Control Assn. , State College,  Pennsylvania (August 1970),

25.   Levin, G.V., and  Shapiro,  Jr.,  "Metabolic Uptake of Phosphorus
      by Wastewater Organisms," Jour. Water Poll. Control Fed. ,
      37_, 800- (1965).

26.   Mulbarger,  M.C., Shifflett, O.G., Murphy, M.C.,  and  Huffman,
      D. D. ,  "A Full-Scale Evaluation of "Luxury Uptake" for
      Phosphorus Removal," presented at the  42nd Annual  Conference
      of the Water Pollution Control Fed. ,  Boston, Massachusetts
      (October 1970).

27.   Levin, G.V., Topol, G. J. , Tarnay,  A.G., and  Samworth, R. B. ,
      "Pilot Plant Tests of a Phosphate Removal Process", Jour. Water
      Poll.  Control Fed. 44,  1940-54(1972).

28.   Sherrard,  J.H., and Schroeder,  E. D. ,  "Importance of Cell
      Growth Rate and Stoichiometry to the Removal of Phosphorus from
      the Activated Sludge Process," Water Research  6, 1051-57 (1972).
                              289

-------
29.    Winkler,  B. F. ,  andThudes, G. , "Kinetics of Orthophosphate
      Removal from Aqueous Solutions by Activated Alumina, " Jour.
      Water Poll. Control Fed.  43,  474-82 (1971).

30.    Ames,  L. L. , "Evaluation of Operating Parameters of Alumina
      Columns for the Selective Removal of Phosphorus from Waste-
      waters and the Ultimate Disposal of Phosphorus as Calcium
      Phosphate," Robert A. Taft Research Center, Report No.
      TWRC-8 (March 1969).

31.    Eliassen, R. ,  and Bennett,  G. E. , "Anion Exchange and Filtration
      Techniques for  Wastwater Renovation, " Jour. Water  Poll. Control
      Fed.,  39,  R82-91 (1967).                                 ~     '

32.    Pollio, F.X. ,  and Kunin,  R. , "Tertiary Treatment of Municipal
      Sewage Effluents,"  Environ. Sci Technol. 2, 54-60 (1969).

33.    Gregory, J. ,  and Dhond, R.U. "Wasewater Treatment by Ion
      Exchange" Water Research  6, 681-694 (1972).

34.    "Investigation of a Niw Phosphate Removal Process," EPA
      Water Pollution Control Research  Series, 17010DJA 1 1/70
      Contract No.  14-12-487 (November 1970).

35.    Block,  J. ,  "Chemically Exfoliated Vermiculite for Removal of
      Phosphate from Wastewaters," EPA Water  Pollution Control
      Research Series, 17010 DHK 08/69 Contract No. 14-12-485
      (August 1969).

36.    Memoranda on "Cost of Phosphorus Removal in Conventional
      Wastewater Treatment Plants by Means of Chemical Addition,"
      from Robert Smith of  National Environmental Research Center.
      Cincinnati, Ohio, Nov. 3, 1971, May 30,  1972,  July 6, 1972,
      July  17, 1972.

37.    "Activated Sludge Processing," Union Carbide Corporation,
      EPA Report No. 17050 DNW,  February 1972.
Section VI

1.   Monograph No.  9, Environmental Reporter, 20 August 1971,

2.   Chemical Handbook  Manual of Current Indicators, Stanford
     Research Institute,  August 1971.

3.   Personal Communication, L. Cox, EPA,  11 September 1972.

4.   "News Release  of Friday, 1 May 1970", U. S. Department of
     Interior,  FWCA.
                             290

-------
5.     "Report to OECD Working Group on Detergents", Bunch,  R.  L. ,
      September 1971.

6.     "Estimating  Costs  and Manpower Requirements  for Conventional
      Waste-water Treatment Facilities, " Black and Veatch,  Inc. ,
      EPA Report  No. 17090 DAN.

7-     JBF Scientific Corporation unpublished data.
8.     "Sewage Treatment Plant Construction Cost Index, " EPA -  Office
      of Water Programs (Current Edition).

9.     "Wholesale Prices and Price Indices - Industrial Commodities, "
      U.  S.  Department of Labor (Current Edition).

10.   "COST2, " A Computer Program by Richard Eilers,  EPA -  NERC
      Cincinnati.

11.   Personal Communication, W.  C. Krumri, Proctor and Gamble,
      Cincinnati, 6 September 1972.

12.   Process Design Manual For Phosphorus Removal, EPA Report
      No. 17010 - GNP.

13.   "Cost and Performance Estimates For Tertiary Wastewater
      Treating  Processes, " Smith, R.  L. ,  McMichael, W. F. ,
      EPA,  Cincinnati, Ohio, June 1969.

14.   "Employment and Earning Statistics -  Water, Steam, and
      Sanitary Systems (SIC 494-497), " U. S.  Department of Labor.

15.   "Wastewater Treatment Plant Cost Estimating Program, "
      R. G. Eilers, R. Smith, EPA, Cincinnati,  Ohio, April 1971.
                             291

-------
                           SECTION XI
                           APPENDICES
APPENDIX A

 Liquid-Phase Treatment System Options
 For Phosphorus Removal
System Option 1:  Addition to the Primary Clarifier
A.
Process Schematic*
      Chemical
            Prelim.
         Trmt. Units
#only major treatment units are shown.   Buildings, pumps, etc.  are
 omitted for simplicity.  Also, processes incidental to P-removal,  e.g.,
 chlorine contact basins,  are not included.


B.     Attainable Effluent P:  2 mg/1 (either option)
C.
Alternative Chemical Additives
            1.
            2.
            3.
            4.
         Lime
         Alum + Polyelectrolyte

         Pickle Liquor or FeCl? &  lime

         FeCl., + Polyelectrolyte
 System Option,2;  Addition to a Flpeculation Basin Prior to Primary Clarifier
A.     Process  Schematic
       Chemical-

Rapid
Mix


Flocculator

                                  293

-------
B.     Attainable Effluent P: 2 mg/1


C.     Alternative  Chemical Additives


            1.   Lime
            2.   Alum + Polyelectrolyte
            3.   Pickle Liquor or FeCl2 & lime
            4.   FeCl., + Polyelectrolyte
System Option 3;  Chemical Addition to the Aeration Basin in Activated
                  Sludge  Treatment
A.     Process Schematics
                                         >econd.
                                         Sett.
                   Chemical
 B.      Achievable Effluent P;  2 rrig/1


 C.      Alternative Chemical Additives


            1.   Alum
            2.   FeCl3
            3.   Pickle Liquor or FeCl2 (not one of the modeled schemes)

            4.   Sodium Aluminate
                                  294

-------
System Option 4:  Chemical Addition to Trickling Filter Effluent
A.     Process Schematics
B.     Achievable Effluent P;  2 mg/1



C.     Alternative Chemical Additives


            1.   Alum

            2.   FeCl3

            3.   Pickle Liquor or FeCl? (not one of the modeled schemes)

            4.   Sodium Aluminate (not one of the modeled schemes)




 System Option 5;  Option 3  or 4 Plus Multi-Media Filtration


 A.      Process Schematics

         1.  Sub-option 5-A.
                                               Filter Aid
                             Aeration
                              Basin
Filtra-
 tion
                    Chemical"
                                  295

-------
      2.  Sub-option 5-B.
                             Chemical
B.     Achievable Effluent P;  0. 5 mg/1


C.     Alternative Chemical Additives


            1.   Alum
            2.   FeCl3
            3.   Pickle  Liquor or FeCl2 (not one of the modeled schemes)

            4.   Sodium Aluminate



System Option 6: Lime Addition to Secondary Effluent


A.     Proces s Schematics


       1.   Sub-option  6-A.  Single Stage
Secondary-
Effluent     —^
Rapid
Mix
ime


Flocculator

                                         Settler
Recar-
bonator


Filter
       2.   Sub-option 6-B.  Two Stage
Secondary-
Effluent ~~"
Rapid
Mix


Flocculator
            Lime
Filter


Recarb.


                                296

-------
B.     Achievable Effluent P
            Option 6-A Single Stage      0. 5 mg/1
            Option 6-B Two Stage        0. 1 mg/1
System Option 7;  Alum Addition to Secondary Effluent
A.     Process Schematic
Secondary 	 .
Effluent ~*~

Rapid
Mix



Flocculator


Settler ]
V /



Filter
              Chemical

B.     Achievable Effluent P:  0. 3 mg/1

C.     Alternate Chemical Additives
             1.    Alum
             2.    Fed,
                                  Z97

-------
APPENDIX B
Sludge Handling System Options
Option 1
All
Sludge

Gravity
Thickening



Anaerobic
Digestion
>


Dewatering
       Dewatering Alternatives

            1.   Drying Beds
            2.   Vacuum Filtration
            3.   Centrifugation

       Application

            Existing plant contains anaerobic
            digester, no incinerator
Option 2
All
Sludge
Gravity
Thickening


Dewatering


Incineration
       Dewatering Alternatives

            1.   Vacuum Filtration
            2.   Centrifugation
                                  298

-------
       Application
            Existing plant treats primary and secondary

            sludge in combination, has incinerator
Option 3

Primary +
Tertiary
Gravity
Sludge (If
Any)
Secondary
Sludge
imcKemng

Flotation
Thickening
i
j

Dewatering


Incineration
        Dewatering Alternatives


            1.  Vacuum Filtration

            2.  Centrifugation


        Application


            Existing plant has flotation thickener
 Option 4
All
Sludge
Gravity
Thickening


Anaerobic
Digestion


Dewatering
-
Incineration
                                  299

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       Dewatering Alternatives

           1.  Vacuum Filtration
           2.  Centrifugation

       Application

           Existing plant contains anaerobic digester,
           contains incinerator
Option 5
Tertiary
Lime
Cln^rrc.
Gravity
Thickening
— »-
Centrifuga-
tion


Calcination
»i
Slaking
       Application
           Phosphorus removal scheme selected is
           lime addition to secondary effluent
       Note
           Thickening and dewatering processes used in this option are
           independent of any similar processes used in primary and
           secondary sludge handling "upstream" in the plant.
                                300

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APPENDIX C
Design Parameters
Type of
Sludge
A. No Chemical Added
Primary
Primary- & Trickling
Filter
Primary fc Activated
B. Lime Addition Before
Primary
Primary
Primary & Trickling
Filter •
Primary & Activated
C. Fe or Al Addition Before
Primary
Primary
Primary & Trickling
Filter
Primary & Activated
D. Fe or Al Addn. to Aerator
Primary & Activated
E. Chemical Addn. to
Trickling Filter Effluent
Primary & Trickling
Filter
F. Fe or Al Addn. to
Secondary Effluent
Primary & Activated &
Tertiary
Primary & Trickling
Filter & Tertiary
G. Lime Addn. to Sec.
Effluent
Tertiary Lime Sludge
Sludge % Solids
Unthickened

4

4
3


5
5

4


2

3
1. 5

4



5



3

4


3
Thickened

8

7
6


9
8

7


5

6
4

7



8



6

7


10
Design Solids
Loading
Ib/sq ft/day

20

12
10


20
15

10


8

10
8

12



15



10

12


20
                                301

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DESIGN PARAMETERS FOR VACUUM FILTRATION





A.







B.




C.








D.




E.
.




F.









Type of
Sludge



No Chemical Added
Primary & Activated
Primary & Trickling
Filter
Digested Primary &c
Activated
Digested Primary &
Trickling Filter
Lime Addition Before
Primary
Primary & Activated
Primary &t Trickling
Filter
Fe or Al Addn Before
Primary
Primary &i Activated
Primary & Trickling
Filter
Digested Primary &t
Activated
Digested Primary &
Trickling Filter
Fe or Al Addn to
Aerator
Primary & Activated
Digested Primary &
Activated
Chemical Addn to
Trickling Filter
Primary & Trickling
Filter
Digested Primary
&t Trickling Filter
Fe or Al Add to
Secondary Effl.
Primary & Activated
Tertiary
Primary & Trickling
Filt. & Tertiary
Digested Primary &
Activated & Tert.
Digested Primary &
Trick. Filt & Tert.
Liquid & Solids
Processing Options
From Which Sludge
Is Derived


--





—

L.O. I
S. O. II, III

S. O. II, III

L.O. I
S. 0. II, III

S. O. II, III

S. O. I, IV

S. O. I, IV

L.O. II
S. O. II, III

S. O. I, IV

L.O. Ill

S. 0. II, III

S. O. I, IV
1
L.O. V

S. O. II, III

S. O. II, III

S. 0. I, IV

S. 0. I, IV
Design
Yield

(Ibs /sq
ft/hr)

4. 5 -

7

4

4.5


6

7
i

3

'5 ''

3

4


6

5



7

6



5

6

6

5
Chemica!
(Ib/Ton

i FeCL,
as FeCl3

70

40

: 70

60

' '



, •.

70
.
40
. . 'J. . ,
70-

60


70
•
70



40 |

60 ;
i

l
70
!
40

70
I
60
I
L Dose
Solids)

Lime
as CaO

< 100

160

180

160







100

160

180

160


100

180



160

160



100

160

180

160
                302

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DESIGN PARAMETERS FOR SLUDGE DRYING BEDS
Type of
Sludge
A.


B.


C.



No Chemical Added
Digested Primary &
Activated
Digested Primary &
Trickling Filter
Fe or Al Add'n Before
Primary
Primary & Activated
Digested
Primary & Trickling
Filter Digested
Fe or Al Add'n to Aerator
to Trick Filt Effl, or to
Secondary Effl
Primary &: Secondary
& Tertiary (if any)
Digested
Bed Area Requirement (sq ft/capita)
Open Beds
North

2.3
1.6


2.6
1.8



2.4
South

1. 8
1. 3


2. 0
1. 5


Covered
Beds

1.4 .
1. 1


1.6
1.3


1
i
1
2.1 1.4
                     303

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  DESIGN PARAMETERS FOR ANAEROBIC DIGESTION,  FLOTATION
       THICKENING AND MULTIPLE HEARTH INCINERATION*
Conventional Anaerobic Digestion

       Organic  Loading Factor = 40 Ib VSS/day/1000 cu ft
       Hydraulic Loading Factor =  30 days detention

High-Rate Anaerobic Digestion

       Organic  Loading Factor - 150 Ib VSS/day/1000 cu ft
       Hydraulic Loading Factor =15 days detention

Multiple  Hearth Incinerator

       Solids Loading Factor = 2 Ib/hr/sq ft hearth area

Air Flotation Thickening

       Solids Loading Factor  = 2 Ib/hr/sq ft
       Chemical Dose  =  10 Ibs Polymer/ton

*Design parameters for these  processes are assumed to be independent
 of the liquid-phase processing and sludge handling scheme selected.
                                 304      AU.S. GOVERNMENT PRINTING OFFICE. 1973 546-311/102 1-3

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           ) /Vuni/MT
                            ,S'u/-;.'<-'
                                06B
                                          SELECTED  WAVE:* R:SOUXCES ASSTRACTS
                                                INPUT TRANSACTION  FORM
     Organization
               JBF Scientific Corporation
     Title
        A Computer Model For Evaluating Local Phosphorus Removal Strategies
 10
j22j
        Donald S. Yeaple
        David A.  Barnes
        Francis A.  DiGiano
                               16
Project Designation
                                             Contract No. 68-01-0758
                               21  Nate
Citation
 mo I Descriptors (Starred first)                            ~~                  '•

	*Phosphorus, #Water Pollution Treatment, '-Evaluation, *Costs,  Local
        Governments,  Eutrophication
 25
Identifiers (Starred First)

   ^Phosphorus Removal Strategies,  Chemical Treatment,  Detergents
 27
     Abstract
        A computer model for evaluating a number of strategies for removing phosphorus
        in wastewater has been developed.  The influence on total treatment cost of
        several non-treatment strategies  such as the elimination of phosphates in deter-
        gents can be evaluated in terms of the treatment cost at local waste treatment
        plants.

        A review of phosphorus removal technology was  conducted in  order to deter-
        mine what methods should be included as  available techniques in a treatment
        strategy.  Chemical precipitation techniques were selected as being both avail-
        able and most effective at the present time and in the immediate future.

        The model reports to the user the total cost  of a selected strategy for removing
        phosphorus.   Over 21 treatment schemes with several sludge handling schemes
        can be selected and evaluated depending on local conditions.   The computer
        guides the user through a series of questions and answers  to develop a local
        profile and prediction of future conditions.
**•*•*'" Donald S.  Yeaple
                         Institution
                                    JBF Scientific Corporation
  VVR:102 (REV, JULY >»•»)
  WRilC
                       »BNO, WITH COPY OF DOCUMENT. TOl rtATEH RESOURCES SCIENTIFIC INFORMATION CENTER
                                                 U.S. DEPARTMENT OF THE INTERIOR
                                                 WASHINGTON. D. C. 20240
                                                                               6I>G. I S.7.J- 3H

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