WATER POLLUTION CONTROL RESEARCH SERIES • 12130 EZR 05/71
  Combined Treatment of Domestic
       and Industrial Wastes
        by Activated Sludge
ENVIRONMENTAL PROTECTION AGENCY • WATER QUALITY OFFICE

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             Water Pollution Control Research Series

     The Water Pollution Control Research Reports describe
the results and progress in the control and abatement of
pollution in our Nation's waters.  They provide a central
source of information on the research, development, and
demonstration activities in the Water Quality Office, in the
Environmental Protection Agency, through in-house research
and grants and contracts with Federal, State, and local agencies,
research institutions, and industrial organizations.

     Inquiries pertaining to Water Pollution Control Research
Reports should be directed to the Head, Project Reports System,
Water Quality Office, Environmental Protection Agency,
Washington, D. C. 20242.

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          Combined Treatment of Domestic
                and Industrial  Wastes
                  by Activated Sludge
                            by

                 The City of Dallas, Oregon
                          for  the

                 WATER QUALITY OFFICE
           ENVIRONMENTAL PROTECTION  AGENCY
                    Grant No.  11060  EZR
                  Project No. 12130 EZR


                        MAY  1971
For sale by the Superintendent of Documents, U.S. Government Printing Office, Washington, D.C. 20402 - Price $1.25

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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, nor does mention of trade names or
commercial products constitute endorsement or recommendation for use.

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                                    ABSTRACT
The  operation  of a completely aerobic secondary treatment facility  for  treatment  of
combined domestic  and industrial wastewater from  the City of Dallas,  Oregon, was
studied  for a period of 15 months. The system was designed for an average  daily flow  of
2.0 mgd and a BOD load of 7000 pounds per day. The results of this study indicate the
flexibility and economy of the completely aerobic system, consisting of activated sludge
with  aerobic  digestion,  for  a small  community with  proportionately  high  industrial
wastewater loads. The  effluent BOD concentration averaged 8 mg/1 and the  effluent total
suspended  solids concentration averaged 13  mg/1 for  the  15-month study period. The
biological solids yield  averaged about 0.7 pounds of solids per pound  of BOD removed
and the net accumulation of biological volatile  solids was about 0.42 pounds of volatile
solids  per  pound   of BOD  removed.  These  values were  obtained  with  a  MLSS
concentration  range of 700  to 3000 mg/1,  an average  sludge age  of 19  days and an
organic  loading range of 0.05 to 0.40 pounds of BOD per pound of MLSS per day. Total
capital cost of the system was about 66 percent of that for a  conventional activated
sludge plant and operation and maintenance  costs were only about 33 percent of those
for a  conventional system.

This  report was submitted in fulfillment of Grant No. 11060 EZR under the  partial
sponsorship of the Water Quality Office, Environmental Protection  Agency.
                                     in

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                                CONTENTS

SECTION                                                         PAGE

I                CONCLUSIONS                                     1

II                RECOMMENDATIONS                               3

III               INTRODUCTION                                    5
                     Scope                                          5
                     Background                                     6
                     Theoretical Considerations                         7

IV               TREATMENT FACILITIES                           11
                     General Description                             11
                     Design Concept                                 14
                     Design Criteria                                 14
                     Design Factors                                 15

V                DEMONSTRATION PROCEDURES                    23
                     Plant Startup                                   23
                     Operation                                     23
                     Sampling Schedule and Procedures                 23
                     Analytical Methods                             26

VI               WASTEWATER CHARACTERISTICS                  29
                     General                                       29
                     Canning Season                                 29
                     Dry Weather Non-Canning Season                  34
                     Wet Weather Non-Canning Season                  34
                     Infiltration                                    35

VII              TREATMENT PLANT PERFORMANCE                37
                     General                                       37
                     Effluent Quality and System Stability              37
                     Aerobic Digestion                               47
                     Solids Deposits                                 51
                     Velocity Profiles                                51
                     Dissolved Oxygen Profiles                        57
                     Oxygen Uptake Rates                           57
                     PVC Liner                                     57
                     Operational Considerations                       62

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                        CONTENTS  - CONTINUED

SECTION                                                        PAGE

VIII             FINANCIAL CONSIDERATIONS                         63
                    Construction Costs
                                                                   x--3
                    Operation and Maintenance Costs                     o:>
                    Total Annual Costs                                63

IX              DISCUSSION                                        65
                    Activated Sludge System                            °5
                    Aerobic Digestion                                 "°
                    Chlorine Contact                                  75

X              ACKNOWLEDGMENTS                                77

XI              REFERENCES                                       79

Xil             PUBLICATIONS                                      81

XIII            ABBREVIATIONS                                    83

XIV            APPENDIXES                                        85

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                                   FIGURES

NO.                                                                       PAGE

 1                Treatment Facilities                                          12

 2                Schematic Plan                                              13

 3                Aeration Basin, Typical Section                                18

 4                Aerobic Digester, Typical Section                              20

 5                Chlorine Contact Channel, Typical Section                      21

 6                Flow and Rainfall vs. Time                                    31

 7                Influent BOD vs. Time, Weekly Average Data                    32

 8                BOD Loading (Ib/day) vs. Time, Weekly Average Data            33

 9                Influent and Effluent BOD vs. Time, Weekly Average
                  Data                                                       38

 10                Influent and Effluent TSS vs. Time, Weekly Average
                  Data                                                       39

 11                Influent BOD and Effluent Total and Soluble BOD vs.
                  Time, Canning Season                                        43

 12                BOD Removal vs. Time, Canning Season                         44

 13                Influent BOD and Effluent Total and Soluble BOD vs.
                  Time, Dry Weather Non-Canning Season                         45

 14                Influent BOD and Effluent Total and Soluble BOD vs.
                  Time, Wet Weather Non-Canning Season                         46

 15                Effluent  Soluble BOD vs. Aeration Time                         48

 16                Organic Loading vs. Time, All Data                            49

 17                Solids Accumulation in Aeration Basin No. 1,
                  October  1970                                                52

 18                Aeration Basin Velocity Profile, Two Aerators,
                  Low Speed (one foot)                                        53
                                       vn

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                            FIGURES  -  CONTINUED

NO.                                                                          PAGE

19                Aeration Basin Velocity Profile, Two Aerators,
                  Low Speed (6 feet)                                             54

20                Aeration Basin Velocity Profile, Two Aerators,
                  Low Speed (9 feet)                                             55

21                Aeration Basin, Velocity Profiles                                56

22                Aeration Basin D. O. Profile, Two Aerators,
                  Low Speed (one foot)                                          58

23                Aeration Basin D. O. Profile, Two Aerators,
                  Low Speed (6 feet)                                            59

24                Aeration Basin D. O. Profile, Two Aerators,
                  Low Speed (9 feet)                                            60

25                Aeration Basin D. O. Profiles                                    61

26                Substrate Removal vs. Effluent Soluble BOD                     66

27                Clarifier  Hydraulic Loading vs. Effluent Suspended
                  Solids                                                         69

28                Clarifier  Solids Loading vs. Effluent Suspended
                  Solids                                                         70

29                Horsepower - Oxygen Transfer Relationships                    71

30                Composition of Waste Sludge  Solids                             73
                                     vin

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                                     TABLES





NO.                                                                   PAGE





1                 Treatment Plant Design Criteria                           14




2                 Design Factors                                          16




3                 Detailed Operation Schedule                              24




4                 Sampling and Testing Schedules                           25




5                 Influent Characteristics                                  30




6                 Effluent Characteristics                                  40




7                 Influent and Effluent Characteristics, All Data             41




8                 Total Annual Costs                                      64
                                       IX

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                                    SECTION I
                                  CONCLUSIONS
Operation  of a  completely  aerobic  wastewater treatment plant,  designed  to provide
secondary treatment of domestic and industrial wastes from the City of Dallas, Oregon,
has been studied during the period from August,  1969 through November 1970.

The following conclusions have been reached, based on the results of the study presented
in this report:

       1.  Effluent  quality was good  throughout the study  period, even during  such
          extreme conditions  as periods of flow at maximum hydraulic capacity during
          the non-canning season.

      2.  Cannery startup, operation and shutdown have had no significant effect on the
          operation of the treatment system.

      3.  The  system is  sufficiently stable to  produce  a good quality effluent  with
          aeration times varying from 4 hours to 60 hours.

      4.  The system  has adequate  flexibility and stability to withstand shock organic
          and hydraulic loads.

      5.  The wastewater characteristics during  the first year  of operation more  closely
          resembled  domestic   wastewater  as  opposed  to   industrial   wastewater
          characteristics.

      6.  Effluent BOD averaged 8 mg/1 and effluent suspended solids averaged 13 mg/1,
          for the entire study  period.

      7.  The  substrate removal  coefficient, k,  averaged  about  0.041 and  was  not
          significantly  affected by changes in the temperature range  of data encountered.

      8.  The biological sludge yield averaged about 0.7 pounds of solids per pound of
          BOD removed.

      9.  Net biological volatile solids  accumulation was about  0.42 pounds of volatile
          solids per pound of BOD removed.
                                          1 -

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10.   The biodegradable portion  of the solids wasted  to  the digester averaged about
     19 percent of the total wasted solids.

11.   Aerobic digestion  is  an effective and  economical  means  of waste activated
     sludge stabilization.

12.   The  average reduction  in  volatile solids  content  through the digester  was 5
     percent.

13.   Digested  sludge  has been stabilized to the extent  that no objectionable odors
     have evolved from  the humus storage ponds.

14.   A treatment system of this type can be constructed and operated at substantial
     savings in cost compared to a conventional activated sludge system.

15.   Total capital cost was about 66 percent of the  cost for a conventional  2 mgd
     activated sludge plant.

16.   Operation and  maintenance costs  for the first  year averaged $33  per million
     gallons treated, or about 33 percent of those for a conventional plant treating
     the  same average flow.

17.   Total annual treatment cost  averaged  $0.097  per pound of BOD removed
     (amortized capital  cost portion of annual cost based on BOD  removal capacity
     rather than actual pounds of BOD removed).

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                                   SECTION  II
                               RECOMMENDATIONS
Analysis  of the data obtained during the demonstration  period indicates  several  areas
where design modifications or further operational studies would be desirable.

DESIGN MODIFICATIONS—Only minor design modifications are recommended and are
as follows:

The  concrete  protective  pads  beneath the aerators should be larger to  prevent bottom
scour.

Measurement  of recycled  sludge  flow with  a propeller type meter is  not satisfactory
because of frequent  fouling of the propeller. A magnetic flowmeter would  be preferred.

FUTURE STUDIES—Organic loadings to the plant during this study were low, relative to
design  capacity. Analysis of some aspects of  the  treatment unit performances was very
difficult to achieve because of this. Therefore, it would be desirable to reevaluate some of
these analyses at loads closer to  the design  capacity. The extremely low solids loading
rate  and  the  low degradability of the solids wasted  to the  digester during  this  study
precluded an  accurate analysis of digester performance under a full range  of operating
conditions.  Future  studies of the  performance  of the  aerobic  digester  would  be
particularly useful.
                                          3-

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                                   SECTION  III
                                 INTRODUCTION
SCOPE

A  completely  aerobic system  designed to  provide  secondary  treatment of combined
domestic and industrial wastes  was constructed  at the City of Dallas,  Oregon,  and was
studied  during  the period from September  1969 through November 1970. This project
was financed with the aid of a  research, development and demonstration grant provided
by the Environmental Protection Agency (EPA), under grant number 11060 EZR.

The basic purpose of this program was to demonstrate the economics and efficiency of
the completely aerobic treatment method when applied  to the treatment of combined
domestic and industrial wastes from a small municipality.

The specific objectives were to:

     1.    Demonstrate, in full-scale plant  operation, the BOD and  suspended solids
          removal capabilities and stability of the completely mixed, completely aerobic
          system  treating combined domestic and industrial  waste flows from a small
          municipality.

     2.    Determine  the influence of rapidly changing industrial waste loadings resulting
          from startup and shutdown of canning operations, changes in canning product,
          and brief periods of cannery inactivity during the canning season.

     3.    Determine   the efficiency  and operating  characteristics  of  the  combined
          treatment system during the off-canning season.

     4.    Determine  the  effect of  varying  the  detention  time in the  aeration basins,
          between 12 and 48 hours, on BOD and suspended  solids removal and system
          stability.

     5.    Demonstrate  the  applicability  of  aerobic  digestion  to biological  treatment
          systems serving small  municipalities.

    6.    Study the  quantity and character  of aerobically digested sludge when varying
          the liquid and solids  detention time in the  aerobic  digester between 5 and 20
          days.
                                        -5-

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     7.    Demonstrate  the  savings  in  both  construction  and operating costs  of the
          completely  aerobic treatment method when utilizing earthen basin construction
          and floating mechanical surface aeration units for mixing and supplying  oxygen
          to the aeration basins and aerobic digester.

     8.    Demonstrate  the  use  of  polyvinyl  chloride  (PVC)  sheet  lining  in waste
          treatment plant construction.

BACKGROUND

Many small cities are  faced  with the problem of providing wastewater treatment  services
to local  industry.  Waste loads  from such industries as food  processors are  seasonal in
nature and may constitute  the major  organic load  on the wastewater treatment plant.
These small cities therefore  require  a treatment  system which will withstand these shock
loads, yet is economical enough to minimize the  financial burden on the community. The
completely aerobic system was evaluated on this basis.

The  City  of Dallas, Oregon, retained the engineering firm of Cornell, Howland, Hayes &
Merryfield to design  and supervise  the  construction  of the treatment facility  and to
exercise technical supervision over the research and  development program.

An EPA research and development  grant (No. 11060 EZR) was accepted by the City on
21 February  1968.

The  treatment  system  receives a  combination of domestic  and  commercial  wastes,
cannery  wastes, a limited quantity  of slaughterhouse  wastes  and an occasional flow of
phenolic glue waste from a plywood mill.

The  plant was designed to  meet water quality  requirements  established by  the  Oregon
State Department  of  Environmental Quality,  which state  that effluent to the receiving
stream  may  contain  not more  than 20  milligrams per liter (mg/1) each of BOD and
suspended solids. The process employed was  a completely mixed activated sludge system
with aerobic digestion of the waste solids.

A complete list of definitions of the technical terms used in this report may be found in
the WPCF Glossary  [ 1 ], and a list of abbreviations and  symbols used is contained in
Section XIII.
                                          -6-

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THEORETICAL CONSIDERATIONS

MICROBIOLOGY-The living organisms found in activated  sludge are classified  as either
plants or animals. The plants consist of bacteria and fungi  and the animals are primarily
protozoa, rotifers and nematodes.

Hawkes [2]  stated that  bacteria  are  normally  dominant as primary feeders on organic
wastes,  with  different holozoic  protozoa being  secondary  feeders, and rotifers  and
nematodes  are found  at  the  higher  levels in  the food chain.  Fungi cannot normally
compete with bacteria, but they may predominate as primary feeders if certain conditions
exist,  such   as:  low  pH,   nitrogen  deficiency,  or  low   dissolved   oxygen  [3].
High-carbohydrate wastes are also reported to stimulate fungi growth.

The  composition of the organic waste determines which bacterial genera will predominate
[2,3]. Protein wastes favor Alcaligenes, Flavobacterium, and Bacillus, while carbohydrate
waste favors Pseudomonas. A high population of free swimming bacteria will sustain free
swimming ciliata as the predominate protozoa; however, if the  food level is lowered by a
reduction in  the free  swimming bacterial population, the free swimming ciliates will yield
to stalked ciliates which require less energy.

Rotifers thrive in very stable systems  and are better indicators of stable conditions than
are the nematode worms.

METABOLISM— The  metabolic reactions  which occur within activated  sludge  can  be
divided  into  three phases:  (1) oxidation, (2) synthesis,  and (3) endogenous respiration.
These three phase reactions can be illustrated with the following general 'equations, which
have been formulated by Weston and Eckenfelder [4] :

     (1)  Organic Matter Oxidation

         CxHyOz + aO2 -* xCO2 + bH2O + Energy

                         y   z
         where a = x + — ---
     (2)  Cell Material Synthesis

         CxHyOz + NH3 + dO2 + Energy -* C5H7NO2 +eCO2 + fH2O
                                          7-

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           ,      ,    x + y   z
          where d =	5
                       4     2
                e = x  -  5
     (3)   Cell Material Oxidation

          C5H7NO2 + 5O2 — «5CO2 + 2H2O + NH3 + Energy

In the presence of enzymes, produced by living microorganisms, about one-third of the
organic matter removed is oxidized to carbon dioxide and water, to provide energy for
synthesis to cell material of the  other two-thirds of the organic matter removed  [5]. The
cell material  is also oxidized to  carbon  dioxide, water, etc., by endogenous respiration
(auto-oxidation).

KINETICS-Several authors  [6,7,8] have formulated mathematical  equations for design
and operation of  complete-mix  activated sludge plants.  Some  of these formulations are
more  easily used  for evaluation of full-sized plant operation than others. Eckenfelder's
basic equations [7,9] are of this  nature and  are presented below.

SUBSTRATE  UTILIZATION -The Michaelis-Menton relationship was used to define the
microbial  growth rate and steady state substrate removal in  a completely mixed system,
and a simplified equation for substrate removal was developed:
                       sa   sf     sr
          where Sr   = BOD removed, Ibs per day
                Sa   = influent BOD, Ibs per day
                Sf   = soluble effluent BOD, Ibs per day
                Se   = soluble effluent BOD, mg/1
                Xa   = average mixed liquor volatile suspended solids, Ib
                t    = aeration time, days
                k    = removal rate coefficient (Ib BOD/day/lb  MLVSS) per mg/1 BOD

The  equation  shows that the substrate removal is proportional to the product  of the
MLVSS and the aeration time. This equation is valid  only  for conditions in which the
actual  substrate  concentration is much less than the substrate concentration at one-half
the maximum  reaction  rate (Michaelis Constant).  A low  effluent soluble  BOD from  a

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completely mixed  system indicates  a low  substrate  concentration  since  the  effluent
soluble BOD  is the same as the soluble BOD in the aeration basin. Therefore, the above
condition is met if the effluent soluble BOD is consistently low.

SLUDGE YIELD—Excess  solids in  the  activated  sludge  system will  result from  the
non-biodegradable  suspended solids in  the influent and the biological  cells synthesized in
the system during BOD  removal,  less the quantity of cell mass synthesized which is
broken down by endogenous respiration.

McCarty and  Brodersen [10]  have presented an equation which gives the net sludge
accumulation in terms of pounds of volatile biological solids produced  per pound of BOD
removed, as follows:

                                  0.53
                         0.65  -      B
          where  A  =
                 F  =
                 E  -
                 M  =
                 b  =
                                     bM
net accumulation of volatile biological solids
BOD removed
suspended solids lost from system per day
total suspended solids in system
endogenous respiration constant
This equation shows  that the net accumulation  of solids  is dependent  on the rate  of
synthesis of biological solids, the rate of solids degradation by endogenous respiration and
the sludge age of the system.
                                       -9-

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                                   SECTION IV
                            TREATMENT FACILITIES
GENERAL DESCRIPTION

Figure 1 is an aerial photograph of the treatment system. The photograph was taken just
prior to completion of construction.

Waste flow from  the City's collection system enters the plant through a 36-inch diameter
influent sewer at the  pump  station (1). The raw waste is pumped through an 18-inch
pipeline to the headworks (2). The waste is shredded by the comminutor (3) and then
flows to the  aeration basin splitter box (4) where it is discharged to one or both aeration
basins (5). The effluent from  the aeration basin flows by gravity to the clarifier (6) where
the activated  sludge is settled.

The activated sludge to be returned to the aeration basin is removed from the clarifier by
means of six suction pipes mounted  on the revolving clarifier mechanism and flows by
gravity to the return sludge pump station located nearby (7). Two sludge pumps, sized to
return 25 to  100 percent of  the plant dry weather design  flow, lift the activated sludge
back up to the splitter box (4).

Excess,  or waste, sludge  is collected on the bottom of the clarifier by a revolving scraper
arm and pumped directly to  the aerobic digester (8) through sludge pumps located in the
control building (9).

The effluent  from the clarifier flows  by gravity  through the flow measurement box (10)
to  the chlorine contact  channel (11) and is finally discharged through the outfall (12)
into LaCreole Creek.

A sludge pump located  in the control  building transfers the  digested sludge to  one, or
both, humus  storage ponds (13) where it  is further stabilized and dried. The supernatant
from the humus ponds flows  by gravity to the plant influent line (1).

Figure 2 is  a schematic diagram  of the treatment system, showing flow  pattern and
locations of sampling points, flow metering, control valves and gates, and pumps.
                                        11

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      10
1.  RAW SEWAGE PUMP STATION
2.  HEADWORKS
3.  COMMINUTOR
4.  AERATION BASIN SPLITTER BOX
5.  AERATION BASINS (2)
6.  FINAL CLARIFIER
7.  RETURN SLUDGE PUMP STATION
8.  AEROBIC DIGESTER
9.  CONTROL BUILDING
10.  FLOW MEASUREMENT BOX
11.  CHLORINE CONTACT CHANNEL
12.  OUTFALL SEWER
13.  SLUDGE LAGOONS (2)
                                            FIGURE 1
                                     TREATMENT FACILITIES

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      HEADWORKS
c
RAW SEWAGE
INFLUENT
        LEGEND


 CONTINUOUS & AUTOMATIC
 SAMPLING POINT

 OTHER SAMPLING  POINTS

 CONTINUOUS FLOW METERING

 CONTROL VALVE OR GATE

  CONSTANT  SPEED  PUMP
                                                                                                                       TO PLANT
                                                                                                                       INFLUENT
                                                                                        EMERGENCY
                                                                                 DIGESTED  SLUDGE OVERFLOW
                                    AERATION
                                      BASIN
                                      NO  1
                                                                                                                        HUMUS POND
                                                                                                                           NO. 2
                                                                                          CONTROL BUILDING
                                                                                            PUMP ROOM
                                            DIGESTED
                                               SLUDGE
                                              D
                                                              AEROBIC
                                                              DIGESTER
                                                                          UNDIGESTED
                                                                          SLUDGE
                              AERATION
                              BASIN
                              SPLITTER BOX
                            SLUDGE RECIRC-
                            ULATION PUMPS
SLUDGE
RECIRCULATION
                                                                                                                   CHLORINE  CONTACT
                                                                                                                        CHAMBER
                                                                                                                                       7
                                                                                                                                      TREATED EFFLUENT
                                                                                                                                      TO STREAM
                             AERATION
                              BASIN
                              NO.  2
                               CLARIFIER BYPASS


                                      FIGURE   2




                                 SCHEMATIC PLAN

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DESIGN CONCEPT

The design  was based  on  the  need  to minimize the  following  shortcomings often
associated  with  conventional  activated sludge designs:  high  construction  costs; high
operating labor  costs; need  for highly trained operators; susceptibility to upset by shock
organic,  hydraulic  and  toxic  loads; and waste solids handling,  stabilization  and disposal
problems.

These shortcomings were minimized by  use of the following design concepts:

Primary  clarification and grit removal  facilities were eliminated. Grit  will  settle  in the
aeration  basins  and will be  removed  periodically  by  heavy  equipment. The  aeration
capacity  was increased to compensate for the greater organic load to the aeration basins.

Aerobic  digestion  was  employed  in place  of the  higher cost conventional anaerobic
digestion.

Earthen  basins,  with  shotcrete  sideslope linings,   were  used  in  place  of higher cost
reinforced concrete construction.

The complete-mix activated sludge  principle, designed for a conservative range of organic
loadings  and adequate hydraulic surge capacity, was employed to reduce susceptibility to
process upset. Hydraulic surge capacity was provided by the use of narrow aeration basin
outlets  which  provide   a  more  uniform  basin  effluent  flow, and  allowance  for  a
fluctuation of about one foot  in the basin water level.

The use of aerobic digestion and automatically controlled sludge  pumping simplifies waste
solids handling and  disposal  problems.

DESIGN  CRITERIA

The criteria used for final  design of the City of Dallas wastewater  treatment plant are
listed in Table 1.

                                     TABLE  1
                    TREATMENT PLANT DESIGN CRITERIA

      POPULATION
         Present                                                         5,900
         Design                                                         10,400
                                         14-

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      FLOW (MGD)
         Present Average                                                0.94
         Design Average                                                 2.00
         Design Maximum, day                                          6.00
         Peak Instantaneous                                             7.00

      BOD LOAD (LB/DAY)
         Canning Season                                               7,080
         Non-Canning Season                                           2,080
         Population Equivalent^
            Canning Season                                          41,600
            Non-Canning Season                                      12,200

      EFFLUENT REQUIREMENTS
         Maximum  BOD (mg/l)                                           20
         Maximum  S.S. (mg/l)                                            20

      Includes 5,000 Ib/day industrial BOD

      2Based on 0.17 Ib BOD/capita/day

DESIGN FACTORS

The  design factors used  for the major unit and equipment selection are listed in Table 2.
Photographs of several of the major units are included in Appendix A. Appendix B lists
the manufacturers of the major equipment items. The major treatment units are described
below.

Each aeration basin provides a volume of 1.0 million gallons. The basins were constructed
of earth with  a reinforced concrete ring wall and  shotcrete lined sideslopes.  A typical
section through the aeration basin is shown on Figure 3. Oxygen is  supplied to each  basin
by four 25-hp,  two-speed, floating mechanical  aerators. The maximum water depth is 12
feet.  The design  was based on an organic loading of 0.23 Ib BOD/lb MLVSS (26 Ib
BOD/1000 C.F.) and an aeration time of 24 hours at design BOD loading.
                                      - 15-

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                             TABLE 2
                        DESIGN  FACTORS

INFLUENT PUMPS
   Number                                                       2
   Type                                                  Centrifugal
   Capacity                                               2400 gpm
   Total  Head                                                26 feet

HEADWORKS
   Sewage Grinder
       Number                                                    1
       Size                                                  25-inch

AERATION BASINS
   Number                                                       2
   Depth                                                    12 feet
   Volume (each)                                    1.0 million gallons
   Hydraulic Capacity (each)                                  6.0 mgd
   Design Organic Loadings1                 0.23 Ib BOD/lb MLVSS/day
                                         (26 Ib BOD/1000 cu. ft./day)

AERATION EQUIPMENT
   Number of Aerators (each basin)                                  4
   Type                        2-speed, floating, mechanical surface type
   Size                                                       25-hp

CLARIFIER
   Number                                                       1
   Diameter                                                 60 feet
   Side Water Depth                                          10 feet
   Surface Overflow Rate2                              707 gal/d/sq. ft.
   Solids Loading Rate2'3                               26 Ib/d/sq. ft.
   Detention Time2                                        2.5 hours
   Sludge Removal                                Revolving suction arm

SLUDGE  RECIRCULATION
   Number of Pumps                                              2
   Type                                                1 single-speed
                                                     1 variable-speed
   Recirculation Ratio2                                    0.25 to 1.0
                                16-

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FLOW MEASUREMENT
   Plant Flow
   Recycled Sludge Flow
   Waste Sludge

CHLORINATION
   Type
   Control
                                         Prop, meter, clarifier discharge
                                            Prop, meter behind pumps
                                       Time clocks, constant pump rate
                                                  V-notch chlorinator
                                                          Plant flow
CHLORINE CONTACT
    Unit
                 r\
    Detention Timez
                                   Outfall and chlorine contact channel
                                                          1.55 hours
SLUDGE DIGESTION
   Number
   Type
   Volume
   Detention Time4
       4000 mg/l solids to digester
       8000 mg/l solids to digester
   Oxygen Supply and Mixing
   Minimum Digested Sludge Age4
       4000 mg/l solids to digester
       8000 mg/l solids to digester

DIGESTED SLUDGE DISPOSAL
   Method
   Number
   Area, each
       Total
   Supernatant Drainage
   Operation

EFFLUENT POLISHING
   Method
                o
   Detention Time^
                                                                  1
                                Aerobic flow-through without thickening
                                                      480,000 gallons

                                                            5.2 days
                                                           10.4 days
                                      30-hp floating mechanical aerator

                                                           15.2 days
                                                           20.4 days
                                                       Humus ponds
                                                                  2
                                                       67,000 sq. ft.
                                                           3.1 acres
                                                      Return to plant
                                          Dry to 3-foot depth of water
                                        Discharge to humus pond No. 1
                                                           20 hours
1At 3500 Ib. BOD/day/basin and 2200 mg/l MLSS
^At average design flow of 2.0 mgd
3At 2200 mg/l MLSS and 1.0 recirculation ratio
4At design loading
                                 17-

-------
                                                        GRAVEL BACKFILL
NOTES: BASIN SYMMETRICAL ABOUT
      CENTER LINE. CONCRETE PADS
      PLACED UNDER EACH AERATOR
                                               FIGURE 3
                                           AERATION BASIN
                                           TYPICAL SECTION

-------
The  60-foot diameter clarifier has a 10-foot sidewater depth. Recycled activated sludge is
removed by a rapid sludge withdrawal mechanism utilizing suction pipes mounted on the
scraper  arms.  Waste sludge is scraped to the center of the  unit and  removed through a
sludge hopper. The design was based on  a  hydraulic overflow rate of 707 gal/day/sq. ft.
and  a solids loading of 26 Ib/day/sq.  ft.  at a mixed liquor flow of 4.0 mgd and a mixed
liquor suspended solids (MLSS) level of 2,200 mg/1.

The  maximum capacity of the aerobic digester is 480,000 gallons. The basin is 90 feet in
diameter with a maximum water depth of  12 feet. The digester construction is similar to
that of  the  aeration basins, i.e.,  earth  basin with  a reinforced concrete ring wall and
shotcrete lined  sideslopes. Figure  4  is a  typical  section through the aerobic digester.
Oxygen is  supplied to the basin by a single-speed 30-hp floating mechanical aerator. The
design was based on a hydraulic detention time, at design loading, of 10.4 days with a
waste sludge  solids concentration of 8000 mg/1.

Chlorine contact time is provided in a  shotcrete lined channel, 450  feet in length. The
design provides a  1.55  hour  contact time at average design flow. A typical  section
through the chlorine contact  channel is shown on Figure 5.

The   control  building  houses  the  plant  motor   control  center, automatic  samplers,
laboratory, and waste sludge  pumps.
                                         19-

-------
to
O
                       NOTES: BASIN SYMMETRICAL ABOUT
                             CENTER LINE. CONCRETE PAD

                             PLACED UNDER AERATOR
                                                            FIGURE 4
                                                       AEROBIC DIGESTER

                                                        TYPICAL SECTION

-------
EARTHEN-
EMBANKMENT
GRAVEL BACKFILL-
NOTE: DISCHARGE OVER CONCRETE WEIR
                                           FIGURE 5
                                 CHLORINE CONTACT CHANNEL
                                       TYPICAL SECTION

-------
                                   SECTION V
                        DEMONSTRATION  PROCEDURES
PLANT STARTUP

Initial aeration basin startup was accomplished as described below.

Prior to  startup, the aeration basins were partially filled  with water, to test the aerator
operation. Aeration basin number 2 was seeded with  8,000  gallons  of secondary sludge
from the City's old trickling filter plant, and approximately  one cubic yard of barnyard
manure obtained from an adjacent farm. All four aerators were run  at low speed to mix
the basin contents and increase the dissolved oxygen level. Raw wastewater flow into the
basin was begun after one day of aeration and was gradually increased to  0.75 mgd over
a period of about  one week. Three days were  required to fill the basin because  of the
low initial flow. All biological solids produced were returned to the aeration basin until
the MLSS reached the desired level.

Acclimation  of  the system  was  monitored  with daily  COD determinations  on both
influent and  effluent flows and suspended solids analyses of  the aeration basin  contents.
The system was assumed to be completely acclimated after approximately four weeks of
operation when the daily COD removals leveled off above  90 percent.

Aeration basin number 1 was started after basin number 2 became acclimated. All of the
activated sludge was returned to basin number 1  for  36 hours  prior to the  addition of
any wastewater. The entire wastewater flow  was diverted to  the basin at the end of this
period.

OPERATION

The treatment system was operated continuously  from August 1969, through November
1970. Table 3 is a detailed schedule of operations during the demonstration period.

SAMPLING SCHEDULE AND PROCEDURES

Samples  were taken at various  locations throughout  the system.  These sample  point
locations are  shown on Figure 2, and are described below. All subsequent discussion of
sample points will  refer to Figure 2. Table 4 lists the sampling and testing  schedules used
throughout the demonstration period.
                                       -23-

-------
TABLE 3
DETAILED OPERATION SCHEDULE
DATE
AUGUST 1969
SEPTEMBER
OCTOBER
NOVEMBER
DEC. 1969
JAN. 1970
FEBRUARY
MARCH
APRIL
MAY
JUNE
JULY
AUGUST
SEPTEMBER
OCTOBER
NOV^Z°
CANNERY111
OPERATION
I GREEN
-j-l BEANS
jt PRUNES










„ -J

AJ
.».

L. 	 ,,
GREEN
BEANS
P
PRUNES


AERATION
BASINS USED
t



Ul
•z.
O




'
t
^
t

Ul
0

1
k








r
k
r
h



f
AVERAGE
PLANT FLOW (mgd)
START-UP & A
ACCLIMATION V
— 	 •" - - -- - - T
CM



4-
2

1
/

^

*


in
O)
d

T
t
0
CM° ^




r
k
r
AVERAGE12'
AERATION TIME (hrs.
T

S




^
LO
i
j
in
1
i
s
^
in
CM

1
J
CM
«— ^

r
i

T
k
f
I


r
i,
f
AVERAGE
MLSS<3> (mg/l)

li
8 *
* i
4
8
t

1

^
-1
o t
r- 1
O t
1

O
§
1
k
r
k
r
k
r
k



r
k
r
k
r
k
r


r
AEROBIC DIGESTER
DETENTION TIME (days)


,
§
c
.
§ ,
,
s
i
8 1
<
in
CO ^
s;
^
o
1
% J
s!
k

r
k
r
l

f
b
r
k
,




DATE
AUGUST 1969
SEPTEMBER
OCTOBER
NOVEMBER
DEC. 1969
JAN. 1970
FEBRUARY
MARCH
APRIL
MAY
JUNE
JULY
AUGUST
SEPTEMBER
OCTOBER
NOV. 1970
(1) CANNERY OPERATION BASED ON ACTUAL RECORDS FOR 1969 AND 1970 ADDITIONAL PRODUCTS MAY BE PRODUCED IN THE FUTURE.
(2) AERATION TIME WAS SET BY THE NUMBER OF AERATION BASINS IN OPERATION AND THE INFLUENT FLOW RATE.
(3) MIXED LIQUOR SUSPENDED SOLIDS.

-------
                                  TABLE 4

                      SAMPLING AND TESTING SCHEDULES
                           (NUMBER OF TESTS PER WEEK)
                    CANNING SEASON (JULY 15 TO SEPT. 30)



SAMPLE POINT
A PLANT INFLUENT
B AERATION BASIN
EFFLUENT
C WASTE ACTIVATED
SLUDGE
C AEROBIC DIGESTER
E PLANT EFFLUENT
f POLISHING POND
EFFLUENT



BOD TOTAL
3




-
3
*

Q
111
^
o
a
0
0
ca
-




-
3


SUSPENDED SOLIDS


TOTAL
3
3

3

3
3
*



VOLATILE
3
3

3

3
3



il I
SETTLEABLf
5
5



-
5





a
5
5



5
5



LU
CC
TEMPERATU
10
10



10
5





DISSOLVED
OXYGEN
5
5



5
5





COLIFORM
-




-
1




, —
NITROGEN11
1




-
1


CM
w
^)
PHOSPHORO
1




-
1





ALKALINITY
3
3



3
3





CHLORINE
RESIDUAL
-




-
5




O
MICROSCOPI
EXAM
-
1



1
-


                   NON-CANNING SEASON  (OCT. 1  TO JULY 14)



SAMPLE POINT
A PLANT INFLUENT

B AERATION BASIN
EFFLUENT
C WASTE ACTIVATED
SLUDGE
D AEROBIC DIGESTER
E PLANT EFFLUENT

F POLISHING POND
EFFLUENT



O
O
O
m
2

_

_

-
2

.

Q
II |

_I
O
to
to
Q
O
O
m


_



-
1



SUSPENDED SOLIDS


TOTAL
2

2

2

2
2

*


VOLATILE
2

2

2

2
2

_


SETTLEABLE
3

3

_

-
3

_




a
3

3

	

3
3

	


UJ
oc
TEMPERATU
5

5

	

5
5

	




DISSOLVED
OXYGEN
5

5

	

5
5

_




COLIFORM
Bi-
Weekly
—

_

-
Bi-
Weekly
_



^
NITROGEN (
Tri-
Weekly
—

	

-
Tri-
Weekly
_

CM

--J
PHOSPHOROi
Tri-
Weekly
_

	

-
Tri-
Weekly
	




ALKALINITY
2

2

	

2
2

	




I CHLORINE
RESIDUAL
_

—

	

-
5

	



0
MICROSCOPI
EXAM


1

_

1


_

(1)  TOTAL KJELDAHL, AMMONIA AND NITRATE
(2)  TOTAL AND ORTHOPHOSPHATE
*   SAMPLING FREQUENCY AS REQUIRED

-------
PLANT INFLUENT—Automatic 24-hour composite samples, proportional to plant flow,
were obtained by pumping from the headworks,  downstream of the comminutor. This
location is shown as sample point A on Figure 2. The automatic sampler, sample  pumps
and storage refrigerator are located in the control building.

AERATION BASIN EFFLUENT-These samples were obtained by manually compositing
grab samples during the daily  8-hour operating period. The location is shown  as  sample
point B.

WASTE ACTIVATED  SLUDGE-Grab samples taken at  the waste  sludge pump were
mixed  to form a composite sample during the operating period. The location is shown as
sample point C.

AEROBIC DIGESTER—Sample point D shows  the location of these samples, which were
manually mixed  to form  composites from  grab samples taken from  the digester at  the
outlet box.

PLANT EFFLUENT-Automatic 24-hour composite samples, proportional to plant flow,
were obtained by pumping from the clarifier effluent line at the  flow measurement box,
upstream from the point of chlorine injection.  The sampler and pump are located in  the
control building adjacent to those for the plant  influent. This sample location is shown as
sample point E.

POLISHING POND EFFLUENT-Samples of the  polishing pond effluent (sample point
F) were not taken on a regular schedule after acclimation of the system since, after this
period, the polishing pond was used only for effluent bypass while the chlorine contact
channel was cleaned.  The majority of the samples were grab  samples taken  at  the
entrance to the outfall pipe.

ANALYTICAL METHODS

All  analyses, with the exception  of nitrogen, phosphorous and  coliform tests, were
performed  in  the plant  laboratory. Nitrogen, phosphorous and  coliform analyses were
performed at the EPA's Pacific Northwest Water Laboratory in Corvallis, Oregon.

All plant  testing was done in accordance with the twelfth edition (1965) of  "Standard
Methods for the  Examination  of Water and Wastewater" of the American Public  Health
Association [11], with the following exceptions:

SUSPENDED SOLIDS-Suspended  solids  tests  were  performed using  Whatman No. 541
hardened ashless  filter discs instead  of asbestos mats.
                                       26-

-------
Settleable solids were measured by both the volume method and the weight method. Use
of the weight method was discontinued early  in the program because of the very  small
quantity of settleable solids encountered.

Nitrogen and phosphorous tests were performed  in accordance with the FWPCA manual
[12].

A list of laboratory equipment used for the analytical testing is included in Appendix B.
                                       -27

-------
                                 SECTION VI
                       WASTEWATER  CHARACTERISTICS
GENERAL

Influent wastewater data was separated into three different categories to obtain a more
meaningful analysis. The  three  categories are  as follows:  (1) canning season, (2)  dry
weather non-canning season, and  (3) wet weather non-canning season.

The  canning season normally extends from about 15 July through 30 September, and the
wet  weather non-canning season  from 10  December through 20 March. The dry weather
non-canning season occurs in two separate periods:  1 October through 9 December,  and
21 March through 14 July.

Table 5 lists average, maximum, minimum and standard deviation data  for the various
parameters used to evaluate the influent  wastewater characteristics. These values were
calculated from data for each category described previously. These data are discussed in
the following paragraphs.

CANNING SEASON

ALKALINITY AND pH—The  influent wastewater alkalinity during  the  canning season
varied from 68 mg/1 to 129 mg/1 with an average value of  99 mg/1, as CaCOg. The pH
varied from 6.0 to 7.4 and averaged 7.0.

TEMPERATURE AND DISSOLVED  OXYGEN (D.O.)-The  temperature ranged from 14
degrees C  to  22 degrees C  and averaged 20 degrees C.  The  minimum D.O. level was 0.3
mg/1, the maximum level was 1.7 mg/1, and the average was 0.5 mg/1.

FLOW—The wastewater flow averaged about 1.0 mgd during this period and varied from
a minimum of 0.4 mgd to a maximum of 2.4 mgd. Figure 6 shows influent flow vs. time
for the demonstration period.

BIOCHEMICAL OXYGEN DEMAND (BOD)-The influent BOD averaged 166 mg/1 (1108
Ib/day) and ranged from 59 mg/1  (497 Ib/day) to 635 mg/1 (3813 Ib/day).  Figure 7 shows
influent  BOD in mg/1 vs. time and Figure 8 shows  influent BOD in Ib/day vs. time for
the total operating period.
                                     -29-

-------
                                                                                        I    M   F   L   U   E    N    T

                                                        CANNING   SEASON    *   *   *   *
                                                                                                                                 TABLE          5

                                                                                                                                   CHARACTERIST
 FLOW   (MGO)

 bOD    (MG/L)

 BOO    (LB/D)

 TSS    (MG/L)

 TSS    (LB/D)

 VSS    (MG/L)

 VSb    (LB/D)

ALK    (MG/L)

PH

 TtMP    (OEG   C)

D.O.    (MG/L)

TKN   (MG/L)

NH3-N    (MG/LI

NO3-N    (MG/L)

T-PO4    (MG/L)

O-PO4    (MG/L)
  AVG.
  0 . 9 B

  165.8

1107.7

  1 24.3

  908.7

    62.7

  577.5

    98.5

      7.0

    19.6

      0.5

    14.4

      4  .9

      1  .0

      5.4

      3.2
   MAX.
   2.39

   635.0

3813.0

   552.0

3314.6

   232.0

2109.0

   129.0

       7.4

     22.0

       1  .7

     35.5

     11.7

       9.6

       7.2

       5.8
MIN .
0.42

  59.0

496 .a

  2fl.O

233.5

   14.0

113.2

  68.0

    6.0

  14.0

    0.3

     1 .4

    0. 1

    0.0

    3.9

    1 .3
STD.
DEV.
0.27

1  26.7

624.6

110.3

637. 1

   48.5

492.7

   14.4

     0.3

     1 .2

     0.2

   1  1 .5

     3.8

     3.0

     1 .  1

     1 .4
*   *   *    *


AVG.
1.18

   95.3

880.5

   94. 1

966.5

   76.5

798.2

   97.0

     7.2

   15.7

     1.3

   10.0

     5.7

     1 .6

     5.2

     3.6
                                                                                                                                                    DRY    HEATHER
                                                                                                                                                    NON-CANNING
                                                                                                                                                          «   *   *   *     »ET   WEATHER
                                                                                                                                                                                NON-CANNING
  MAX.
  4.97

   195.0

2353.8

  320.0

5631.1

  320.0

5261.6

  132.0

       7.6

     21.0

       6.0

     22.9

     10.0

       7.2

       7.2

       6.9
MIN.
0.60

  35.0

304.7

     8.0

  98.0

     1  .0

     8.9

  48.0

     6.6

     8.0

     0.3

     0.  1

     0.8

     0.  1

     1  .9

     1  .6
STD.
DEV.
0.55

   31.2

338. 1

   62.7

942.9

   63.8

972.2

   18.7

     0. 1

     2.3

     1  .0

     7.4

     3.2

     2.8

     1  .5

     1  .6
                                                                                                                                                                                                                     AVG.
                                                                                                                                                                                                                     3.66
                        MAX.
                        7.  1 1
    40.4           123.0

1023.9        2988.0

    65.2           310.0

1891.1      13107.9

    48.9           260.0

1429.6      10993.7

    56.8             91.0
       7. 1

     1 1  .5

       4.5

       7.7

       4.3

       1  . 1

       2.4

       1  .4
  7.5

16.0

  7. 1

13.3

  5.6

  2.3

  3.9

  2.7
MIN.
0.87

     6.0

222. 1

   12.0

458.6

     2.0

   78.9

   37.0

     6.7

     9.0

     1  .6

     0.4

     3.3

     0.2

     0.9

     0.3
  STD.
  D6V.
   1 .76

     26.2

  613.4

     59.8

2401.7

     52.2

2022.2

     12.5

       0. 1

       1 .7

       1.9

       6.5

       1.1

       1 .0

       1  .«

       1  .2

-------
      SEPT.   OCT.    NOV.    DEC.    JAN.    FEB.      MAR.   APR.    MAY    JUNE     JULY    AUG.   SEPT.    OCT.    NOV
CO
en
      SEPT.   OCT.     NOV.    DEC.    JAN
                  1969
FEB.     MAR.    APR.   MAY    JUNE    JULY    AUG.    SEPT.    OCT.     NOV.
                                   1970
           C.S.  = CANNING SEASON
       D.W.N.C.  = DRY WEATHER NON-CANNING
       W.W.N.C.  = WET WEATHER NON-CANNING
          FIGURE 6
                                            FLOW AND RAINFALL VS.  TIME

-------
   g
   to
         C.S.
                                      W.W.N.C.
                                                                  D.W.N.C.
                                                                                           C.S.
                                                                                                      D.W.N.C.
                                                                                                              W.WJM.C.
OQ
       SEPT.   OCT.    NOV.    DEC.    JAN.

                    1969
                                            FEB.    MAR.   APR.
MAY    JUNE   JULY    AUG.    SEPT.   OCT.    NOV.

      1970
                                                      FIGURE 7
                                              INFLUENT BOD  VS. TIME
                                              WEEKLY AVERAGE DATA

-------
SEPT. '  OCT.   NOV.   DEC.    JAN.   FEB.    MAR. ' APR.    MAY  '  JUNE   JULY  ' AUG.  ' SEPT. '  OCT.  ' NOV

            1969                                           1970
                                           FIGURE 8

                               BOD LOADING (LB./DAY) VS. TIME
                                    WEEKLY AVERAGE DATA

-------
TOTAL AND VOLATILE SUSPENDED SOLIDS (TSS, VSS)-The average TSS was 114
mg/1 of which 63  mg/1, or 51  percent, was VSS. The range was from a low TSS value of
28 mg/1 (14 mg/1 VSS) to  a high of 552 mg/1 (232 mg/1 VSS).

NUTRIENTS-The  BOD:nitrogen:phosphate ratio in  the influent wastewater  averaged
100:8.7:3.3.  The average  ammonia nitrogen concentration was 4.9 mg/1, and the total
phosphate concentration averaged 5.4 mg/1.

DRY WEATHER NON-CANNING SEASON

ALKALINITY AND  pH-The influent wastewater alkalinity  during the dry weather
non-canning  season varied from 48 mg/1 to 132 mg/1  and averaged 97  mg/1, as CaCX^.
The pH ranged from 6.8 to 7.6 and averaged 7.2.

TEMPERATURE AND D.O.-The average influent temperature during this period was 16
degrees C with a range from 8  degrees C to 21  degrees  C. The D.O. level ranged from 0.3
mg/1 to 6.0 mg/1 with an average of 1.3 mg/1.

FLOW-The  influent  flow varied from 0.6 mgd to  5  mgd, as shown by Figure  6, and
averaged 1.2  mgd for this period.

BOD—.The average influent BOD was 95 mg/1 with a  range from 35 mg/1 to 195 mg/1.
BOD to the  plant, in pounds per day, averaged 880 and varied from 305 Ib/day to 2550
Ib/day. These relationships are shown on Figures 7 and  8.

TSS  AND VSS-The  average TSS concentration was 94 mg/1 of which  76.5  mg/1 or 81
percent was volatile.

NUTRIENTS-The average BOD:nitrogen:phosphate ratio was 100:10:5.5.

WET WEATHER NON-CANNING SEASON

ALKALINITY AND pH-The alkalinity ranged from 37 mg/1 to 91 mg/1 and averaged 57
mg/1, as CaCO3, during the wet weather non-canning season. The pH range was from 6.7
to 7.5 and the average pH  was 7.1.

TEMPERATURE AND D.O.—The temperature of the  influent wastewater averaged 11.5
degrees C  and varied from 9 degrees C to 16 degrees C. D.O. levels ranged from 1.6 mg/1
to 7.1 mg/1 and averaged 4.5 mg/1.
                                      34-

-------
FLOW—Referring again to  Figure 6, the influent flow varied from 0.9 mgd to 7.1 mgd,
and averaged 3.7 mgd.

BOD-The average BOD during this period was 40 mg/1 (1024 Ib/day) and ranged from 6
mg/1 (222  Ib/day) to  123 mg/1  (2988 Ib/day). These relationships are also shown  on
Figures 7 and 8.

TSS  AND  VSS-TSS averaged 65 mg/1 and varied from  12  mg/1  to 310 mg/1. VSS
averaged 49 mg/1 and varied from  2 mg/1 to 260 mg/1.

NUTRIENTS—The  average  BOD:nitrogen:phosphate  ratio  during   the  wet  weather
non-canning season was 100:19:6.

INFILTRATION

The  flow data discussed above shows a wide  variation in the quantity of wastewater
received at the plant. Figure 6 shows the correlation between plant flow and rainfall data.
In general,  during the wet  weather, the peak flows are associated with rainy periods. This
phenomenon is primarily due to infiltration of  groundwater into the  sewer system. This
effect is much less  prevalent in  the  summer  and  fall before  the ground has become
saturated.
                                      -35-

-------
                                  SECTION  VII
                      TREATMENT  PLANT  PERFORMANCE
GENERAL

The plant was scheduled  for startup prior to the beginning of the 1969 canning season.
However,  due to construction  delays,  startup was not accomplished until near the peak
canning period  in  August.  Following startup,  the  plant was operated continuously
through November 1970,  including the full 1970 canning season.

EFFLUENT QUALITY AND SYSTEM STABILITY

Influent  and  effluent  wastewater  quality  parameters were monitored  throughout the
operating  period to provide a basis for analysis of the system stability and performance.
These data were analyzed in conjunction with other variables which affect the operation
of biological systems.

EFFLUENT QUALITY-Figure 9 is a  plot of weekly average influent and effluent BOD,
in mg/1, vs. time, for the entire operating period. Figure 10 is a similar plot for influent
and effluent total suspended solids data. These figures show a consistently good effluent
quality  throughout the  year,  regardless  of the  influent loading, flow, or operating
temperature encountered.

A summary of effluent data is listed in Table 6. This summary is separated into canning
season, dry weather non-canning season, and wet weather non-canning season. It  includes
average, maximum, minimum and  standard deviation values for  all effluent data  for each
period. A summary of influent and effluent average, maximum, minimum and standard
deviation data for the entire demonstration period is listed in Table 7.

During the canning season, the effluent BOD averaged 7.8 mg/1 with a maximum  value of
16 mg/1. The  average effluent TSS was  11.8 mg/1 and ranged from 1 mg/1 to 31 mg/1.

The  average  BOD and TSS values during  the  dry weather  non-canning period were,
respectively, 8.4 mg/1 and 13.9  mg/1.

The averages  during the  wet weather  non-canning season were  7.3 mg/1 BOD and 13.9
mg/1 TSS.
                                      -37-

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                       MAY    JUNE  JULY  ' AUG.   SEPT.   OCT.   NOV
SEPT.   OCT.   NOV.   DEC.    JAN.

           1969
              FIGURE 9
INFLUENT AND EFFLUENT BOD VS. TIME
       WEEKLY AVERAGE DATA

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SEPT.   OCT.   NOV.  DEC.

           1969
                         JAN.    FEB.
MAR.   APR.   MAY   JUNE  JULY   AUG.

                 1970
SEPT.   OCT.   NOV.
                                        FIGURE 10
                           INFLUENT AND EFFLUENT TSS VS. TIME
                                  WEEKLY AVERAGE DATA

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BOD (MG/L)
bOO (LB/D)
SOL BOD ( MGL )
TSS (MG/L)
TSS (LB/O)
VSS (MG/L)
VSS (LB/D)
ALK (MG/L)
PH
TEMP (DEC C)
D.O. (MG/L)
TKN (MG/L)
NH3-N (MG/L)
NQ3-N (MG/L)
T-P04 (MG/L)
0-P04 (MG/L)

* * * *
AVG.
7.76
66.6
2.4
11.6
109.4
7.6
73.7
62.8
7. 1
19.6
5.0
2.3
0.5
3.5
4.4
4.2

E F F
CANNING SEASON » *
MAX. MIN.
16.00 3.00
1 34.2
6.0
31.0
496. 7
25.0
326.0
93.0
7.5
22.0
8.6
10.5
5.6
16.4
6.7
6. 1
25.0
1 .0
1 .0
6.7
1 .0
6.7
27.0
6.5
16.0
3.2
0.2
0.0
0.4
1 .1
3.0
L u e N
* *
STD.
DEV.
2.93
2R.6
1 .4
7.8
95. 1
7.4
83.7
18.4
0.2
1 .4
1 .3
2.8
1.6
4.7
1.5
1 .0
T C H A
* * * *
AVG.
8.42
83.9
3.5
13.9
1 38.3
12.3
122.2
34. 1
7.0
17.5
6.0
3.3
0.8
5.9
5.3
4.3
RACTERIST
DRY HEATHER * *
NON-CANNING
MAX. MIN.
22.00 3.0O
224. 1
9.0
40.0
366.6
46.0
540.4
65.0
7.4
21.0
10.0
12. 3
5.0
10.2
7.8
6.4
23.5
1 .0
1 .0
8.7
1.0
6.6
7.2
6.6
7.2
3.5
1 .1
0.0
0.3
2.6
2.3
1 C S
* *
STD.
OEV.
4.05
51.8
2.9
9.2
99.2
10.2
112.5
1 1.6
0. 1
2.5
1. 1
3.2
1.5
3.2
1.5
1 . 1

* * * *
AVG.
7.32
211.2
2.6
13.9
451 .0
11.8
377.8
38.7
7.1
14.6
6.5
1 .1
0.2
5.1
2.1
1.8


WET HEATHER * •
NON— CANN ING
MAX. MIN.
20.00 2.00
835.6
5.0
68.0
1916.8
42.0
1607.7
66.0
7.4
16.0
8.9
1.6
0.6
7.0
3.4
3.2
23.5
1 .0
1 .0
16.9
1.0
1 1 .9
23.0
6.5
13.0
4.4
0.6
0.0
3.1
0.9
0.3

« *
STD.
DEV.
5. 16
195.9
1 .3
13.3
466.2
10. a
376.9
8.1
0. 1
o.a
1.0
0.3
0.2
1.7
1.4
1.3

-------
TABLE 7
INFLUENT AND E F
CHARACTERIST
-ALL DATA-
CHARACTERIST 1C AVERAGE MAXIMUM MINIMUM STANDARD
DEVIATION
FLOW (MGD) 1.84 7.11 0.42 1.54
BOD ( MG/L ) 103.9 635.0 6.0 88.9
BOD (LB/D) 983.5 3.813.0 222.1 517.0
SOL BOD (MGL)
TSS (MG/L) 96.6 552.0 8.0 82.7
TSS (LB/D) 1,178.5 13.107.9 98.0 1.444.0
VSS (MG/L) 65.3 320.0 1.0 57.7
VSS (LB/D) 912.? 10.993.7 8.9 1,301.3
ALK (MG/L) 85.8 132.0 37.0 24. «
PH 7.1 7.6 6.0 0.2
TEMP (DEG C) 15.7 22.0 8.0 3 . 
-------
CANNERY STARTUP, OPERATION AND SHUTDOWN-Figure 11 is a plot of influent
and effluent BOD and effluent soluble BOD vs. time, during the canning season.

The plant was started up during the 1969 canning season. The  peak BOD loads shown on
Figure  11 for the period from  9 September through 12 September, however, were not
attributable  to  waste from  the  cannery. During  this period, a high  concentration of
plywood  glue waste  appeared in the plant  influent. There was, however, no significant
deterioration of effluent quality as a result of these peak loads.

The peak BOD load during the  1970 canning season was significantly less than for the
1969  season, even after  eliminating the peaks associated with the  glue waste. This can
probably be attributed to a poor  crop  yield in 1970. The peak period again occurred
during  September with no significant loss in effluent quality.

There  appeared  to  be no significant effect  on  effluent quality as a result  of cannery
startup or  shutdown. This could be partially due to a gradual increase and  decrease in
processing by the cannery.

Figure  12  shows percentage of BOD  removal  during  the same period of  time. BOD
removal during the  canning season  was greater  than 90 percent most of the time. The
efficiency dropped to about 88  percent  following the 1969 cannery shutdown. However,
a  comparison  with  Figure  11 shows that  only a small increase in effluent BOD was
observed and the  reduced efficiency was principally due to the  reduction in influent BOD
concentration.

The drop in  efficiency  to about 86 percent BOD removal following cannery startup in
1970  was due only  to a  reduction  of influent BOD concentration. A further comparison
with Figure 11 shows no  change in effluent BOD concentration during this period.

NON-CANNING  SEASON  OPERATING CHARACTERISTICS-Figure  13 is  a  plot of
influent  BOD  and  effluent total  and  soluble BOD  vs.  time for the  dry weather
non-canning  season.  This  plot  shows  a wide  fluctuation in influent waste  strength,
resulting mainly  from large variations in flow. However, the effluent BOD concentration,
and particularly  the  soluble portion, maintained a uniform level throughout  the period,
indicating a stable system.

Influent BOD and effluent total  and soluble BOD data are plotted  on Figure  14 for the
wet weather  non-canning season. The influent BOD  fluctuated widely as during  the dry
weather period. Again, this is due principally to the wide variation in flow rate. Effluent
total  BOD varied to a  greater  extent  than  during the dry  weather  period. However,
                                        42

-------
-1^
OJ
                                                                                                             EFFLUENT
                                                                                                             SOLUBLE
                                                                         1970
                                                            FIGURE  11

                                 INFLUENT BOD AND  EFFLUENT TOTAL AND SOLUBLE  BOD VS. TIME
                                                         CANNING SEASON
                                           (19 JULY 1969 - 27 SEPT 1969, 24 JULY  1970 - 28 SEPT. 1970)

-------
   s
   s
  ,8
UJ
o:

Q
O
GO
               SEPT.
                  1969
                                A \
                             "OCT. N \ JULY
 AUG.
1970
SEPT.
                                                 FIGURE 12
                                 BOD REMOVAL VS. TIME - CANNING SEASON
                               (19 JULY 1969 - 27 SEPT. 1969, 24 JULY 1970 - 28 SEPT. 1970)

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OCT.
            NOV.
                   DEC. MAR.
                             APRIL
                                          MAY
                                                      JUNE
                                                                 JULY
                                                                           OCT.
      1969
1970
                                                                                  NOV.
                                        FIGURE 13


                 INFLUENT BOD AND EFFLUENT TOTAL AND SOLUBLE BOD
                     VS. TIME - ORY WEATHER  NON-CANNING SEASON
             (6 OCT.. 1960 - 7 DEC, 1969, 23 MARCH, 1970- 19 JULY 1970, 5 OCT.  1970 - 8 NOV. 1970)

-------
o
oS
GO
            DEC.

            1969
                               JAN.
FEB.
                  MAR.
                                                                                 \\
                                  NOV.
    1970
                                              FIGURE 14
                        INFLUENT BOD AND EFFLUENT TOTAL AND SOLUBLE BOD

                            VS. TIME - WET WEATHER NON-CANNING SEASON

                              (8 DEC. 1969 - 22 MARCH 1970. 9 NOV. 1970 - 31 NOV. 1970)

-------
effluent soluble  BOD was uniform throughout the period, indicating that the variation in
effluent quality was  mainly  due to solids carryover. However, these  fluctuations were
relatively minor since the effluent total BOD concentration was well below the effluent
requirement nearly all the time.

EFFECT OF VARYING DETENTION TIME-Figure 15 is a plot of effluent soluble BOD
vs.  aeration  basin detention time. A  significant  conclusion is difficult to reach from
studying this figure. All data fall within a range of values so  small that the  difference
between the  maximum  and minimum values is nearly insignificant.  The  data appear to be
quite scattered.  However,  the  scatter occurs over a very small range of soluble BOD
values.

From  this figure it  appears that there is  no significant  influence  on  BOD removal
efficiency from varying the detention time, at least in the range of loadings encountered
in this study.

ORGANIC LOADING—Figure  16  is a  plot of  organic  loading  vs.  time for the  full
operating period. In general,  the load varied between 0.05 and 0.15 Ib BOD per Ib MLSS
per day, with peak rates as high  as 0.4 Ib BOD per Ib MLSS per day.  The SVI averaged
77  for the entire period. The average sludge  age for the  demonstration period was 19.5
days.

AEROBIC DIGESTION

GENERAL—The   aerobic   digester  was   operated   continuously   throughout   the
demonstration period. Pumping times' to  and from the digester  were recorded along with
the  respective  solids  concentrations.  Several  other parameters such as pH,  D.O.,
temperature,  and alkalinity  were monitored to provide a basis  for determination  of  the
digester performance.

DIGESTER   PERFORMANCE-Solids loading  to  the digester  was much  lower than
originally anticipated. The average  loading rate over the entire period  of operation was
about 10 Ib V.S./day/lOOO cu. ft.

Digester performance was evaluated on  the basis of the  following two parameters:   (1)
reduction  in  volatile  solids content,  and  (2)  net volatile  solids destruction.  Both
parameters were calculated from average  values of the data  for the entire demonstration
period.
                                       -47-

-------
a
o
m
LU
_l
CO
               +  +
ID
_J
LL.'
U_
LU
* * *»
             •H- «•••• +M- <*•«•<*>
       •»• *     <*>     «•   *** •*>    <*>
              I
             10
               —I—
                20
    ?0         40         50
RERRTION  TIME  (HOURS)
                                                                so
                                                                  70
                                        FIGURE 15


                                  EFFLUENT SOLUBLE BOD
                                    VS. AERATION TIME

-------
                                                                                               W.W.N.C.
SEPT
       OCT.    NOV.

             1969
DEC.  "  JAN.  "   FEB. "   MAR.  ' APR
MAY   JUNE  ' JULY '  AUG.  ' SEPT.  ' OCT.  ' NOV. '

      1970
                                               FIGURE 16
                                     ORGANIC  LOADING VS. TIME
                                              ALL  DATA

-------
Reduction in volatile solids content was calculated by the following formula:
                              R:     Dv
     VS Reduction (%)  =  1 - — ^ x  -i  x  100
                              Di     RV
           where Rj   =  fraction of inert solids in raw sludge
                  Dj   =  fraction of inert solids in digested sludge
                  Dy  =  volatile fraction of digested sludge
                  RY  =  volatile fraction of raw sludge

Net reduction of volatile solids was based on the ratio of total pounds of volatile solids
removed  from the digester  to total pounds of volatile solids applied corrected for change
in volatile  solids concentration  in  the digester and quantity of volatile solids applied to
fill the digester initially.

The  average   reduction  (in  percentage  of  total)  of volatile solids  content  for  the
demonstration period was  5 percent. The net volatile  solids destruction for the same
period  (calculated in pounds) was  about  34  percent. The average digester detention time
was 69 days.  The basin temperature averaged about  12 degrees C and the pH averaged
5.1  with  an average alkalinity of 17 mg/1.

QUANTITY  AND CHARACTER  OF DIGESTED  SLUDGE-The quantity  of sludge
wasted to the humus ponds was calculated from the data recorded for pumping time  and
solids concentration  of the digested sludge. The total quantity of digested sludge wasted
to the humus ponds during  the demonstration period was about  265,000 pounds (dry
solids  basis),  or an  average of 670 Ib/day. The  average volatile solids content  of  this
sludge  was  about 63  percent.

The relative drying character of the digested sludge was observed during the early summer
of 1970, when the supernatant was drained  from the sludge in one  of the humus ponds.
Some odor was  present for a short period of time when the sludge was exposed to  the
air.  However, the odor, much like that  of  a  barnyard  although  less intense, was  not
objectionable  and disappeared with the formation of a crust on the sludge layer.

The wet sludge, which  had a maximum  depth of  about 1.5 feet,  required a period of
about  3  months to  dry completely. The maximum depth  of sludge in the pond after
drying  was about 6 inches. The sludge formed  individual clumps upon drying,  as shown
by a photograph of  the dried sludge included in  Appendix A. The relatively long period
required  for complete drying of the sludge was primarily due to inability to drain out  the
water which was trapped underneath the sludge  blanket.
                                       -50-

-------
The length  of time before removal of the solids from the humus storage  pond will be
required was estimated to  be  a minimum of three  years,  based on the quantity of solids
accumulated in one humus storage pond during the  study period.

SOLIDS DEPOSITS

Aeration basin number 1  was drained  after about  14 months of operation, to determine
the quantity of solids which had accumulated in the basin. Prior to dewatering the basin,
the biological solids were  washed out by recycling water from the polishing pond back
through  the plant,  without returning activated sludge to the aeration basin.  Pumping was
begun after reducing  the MLSS level as low as  possible. All four aerators were run while
pumping, to keep the residual MLSS in suspension.

A visual observation  of the condition of the basin  bottom  was made.  Figure  17 is a
sketch  of  aeration basin  number  1,  showing  the condition  of the  bottom,  after 14
months operation.  Appendix A contains photographs of the basin, showing bottom scour
and solids deposits.

Bottom  scour was evident around  the concrete target pads  beneath  the aerators. The
maximum depth of scour was about 15 inches.

Solids deposition was  generally light. The greatest accumulation occurred  adjacent to the
aerator  location in the northeast corner of the basin. The maximum depth of  solids in
this location was  about 1.5 feet. The solids consisted mainly of non-degradable  plastic
materials and  appeared to  contain a relatively small amount of grit. The overall  quantity
of  solids deposited was relatively insignificant. Removal of solids from  the basin should
not be required for a  period of at least five years, based on these observations.

VELOCITY PROFILES

Velocity measurements were  made in Aeration Basin  No.  1  under different  operating
conditions. Typical examples  of  velocity profiles are  shown  in  Figures  18, 19 and 20,
(plans at different depths) and  Figure 21  (section) for one set of operating conditions.
Velocity profiles for other  operating conditions are included in Appendix C.  The  numbers
shown on the  aerators indicate the operating horsepower of each unit.

Measurements were made  from  a  boat  using a Gurley No.  622 propeller-type current
meter.  These  data provide an evaluation  of the mixing  characteristics in  the  basin at
different power levels and provides an indication  of possible low velocity areas where
solids settling might occur.
                                         51

-------
LEGEND

       SOLIDS
       SCOUR
                             FIGURE 17

                SOLIDS ACCUMULATION IN AERATION
                    BASIN NO. 1 - OCTOBER  1970
                                S"1

-------
DEPTH OF READINGS:  1 FOOT
C
ROTATION OF AERATORS
IN OPERATION
VELOCITIES IN FEET PER SECOND
                         FIGURE 18


             AERATION BASIN VELOCITY PROFILE
                TWO AERATORS - LOW SPEED
                           -53

-------
DEPTH OF READINGS:  6 FEET
c
ROTATION OF AERATORS
IN OPERATION
VELOCITIES IN FEET PER SECOND
                        FIGURE  19

            AERATION BASIN VELOCITY PROFILE
               TWO AERATORS - LOW SPEED
                           - 54

-------
                          A
DEPTH OF READINGS:  9 FEET
C
ROTATION OF AERATORS
IN OPERATION
VELOCITIES IN FEET PER SECOND
                        FIGURE 20


           AERATION BASIN VELOCITY PROFILE
               TWO AERATORS - LOW SPEED
                        -55

-------
SECTION A - 2 AERATORS, LOW SPEED
SECTION B - 4 AERATORS, LOW SPEED
          FIGURE  21
       AERATION BASIN
      VELOCITY PROFILES

-------
Analysis of the profiles for the minimum operating conditions (two aerators  low speed)
shows bottom velocities in the range of 0.4 to 0.5 fps, found by Eckenfelder [7] to be a
minimum for uniform suspension  of solids.

DISSOLVED OXYGEN PROFILES

Dissolved oxygen  (D.O.) measurements were taken at different  depths in aeration basin
number  1  under different  operating  conditions.  The D.O.  readings were taken from a
boat  using a YSI  meter and  field probe. Figures 22, 23 and 24 show D.O. profiles at
different depths in the basin and Figure 25 is a D.O. profile section through the  basin.

These figures show a higher D.O.  concentration toward the  south side of the  basin.
Ammeter readings indicated a greater current draw and thus a higher horsepower output
from  the aerators  on that side of the basin.  This difference is indicated by the  operating
horsepower shown on each aerator. This  resulted in a greater transfer of oxygen to the
mixed liquor and,  therefore, higher D.O. readings.

OXYGEN UPTAKE RATES

Several oxygen uptake measurements were taken on  grab samples of aeration basin  and
aerobic digester mixed liquors. The tests were conducted by the  following procedure:  A
two-liter bottle was filled with the sample, a YSI D.O. probe was inserted and the top of
the bottle was sealed. D.O. readings were taken at regular intervals until the  oxygen  was
depleted. The sample was mixed  continuously during the test by a magnetic stirrer with
teflon stirring bar.

The oxygen uptake data was plotted  as dissolved oxygen used vs. time. These figures are
included in Appendix C.

The aeration basin oxygen  uptake rates varied from 0.155 to  1.03 mg ©2 per day per mg
MLVSS  at a temperature range  of 17.5  to  19  degrees  C.  The  aerobic digester oxygen
uptake rate averaged  about 0.012 mg 02 per day per  mg MLVSS. No detailed analysis of
the system oxygen requirements was made  because  not  enough data were  available to
establish a relationship between oxygen uptake and BOD removals.

PVC LINER

The original demonstration plan involved  the use of PVC (polyvinyl chloride) sheet liner
in the aeration basins and aerobic digester. The City subsequently elected to use  shotcrete
liners  in  these units instead of PVC, at an additional cost of about $0.25 per square foot.
However, since one of the grant  objectives  was to evaluate the  use of PVC as a lining
                                       -57-

-------
DEPTH OF READINGS: I-FOOT
C
ROTATION OF AERATORS
IN OPERATION
D.O. IN MG/L
                                FIGURE 22


                      AERATION BASIN D.O.  PROFILE
                      TWO AERATORS - LOW SPEED
                                 -58

-------
DEPTH OF READINGS:  6 FEET

   ROTATION OF AERATORS
   IN OPERATION

D.O. IN MG/L
                      FIGURE  23


            AERATION BASIN D.O. PROFILE
             TWO AERATORS - LOW SPEED
                       -59-

-------
DEPTH OF READINGS: 9 FEET
(  .ROTATION OF AERATORS
^IN OPERATION

D.O. IN MG/L

                         FIGURE 24


                AERATION BASIN D.O. PROFILE
                TWO AERATORS - LOW SPEED
                           -60-

-------
                                  n
SECTION C - 2 AERATORS, LOW SPEED
                                  n
SECTION D - 4 AERATORS, LOW SPEED
           FIGURE 25

        AERATION BASIN
          D.O. PROFILES

-------
material, several PVC strips were placed in the aeration basin, to be removed and tested
at periodic intervals. The  first specimens were removed after one year of submergence,
and the following tests were performed:  Grabes Tear Test (ASTM D1000-4) and tensile
and elongation tests (ASTM D882). The tests were performed by the General Engineering
Department of Oregon State University.

The tests showed no detrimental effect on the physical properties of the PVC material.
The complete test results are included in Appendix E.

OPERATIONAL CONSIDERATIONS

Relatively few  operating problems  were  encountered. Those affecting  plant operation
were mechanical  problems involving equipment.  These are  described in the following
paragraphs.

AERATION  EQUIPMENT-Shortly after  plant startup, a bearing failure  occurred in one
of the  mechanical aerator gearmotors. This necessitated  startup  of the other  aeration
basin. Subsequent operation resulted in  similar failures in four of  the  eight remaining
aerators. The cause  of this problem was isolated as a failure to lubricate these  bearings
during assembly of the units at the factory.

RECYCLED SLUDGE PUMP  STATION-A delay in delivery  of these pumps resulted in
use of a temporary  pumping  facility. Very little control of the sludge recirculation  rate
was possible  for a period of several weeks.

WASTE  SLUDGE  PUMPS-A  problem  with the  waste  sludge  pump  motors  was
encountered  which  limited  control  of  the  sludge wasting  rate. The  problem, which
involved  motor overheating  and shutdown, was corrected by  replacing the motors on
both pumps. The sludge wasting rate was affected for an 8-month period.

Another  problem developed  which  affected sludge wasting  rate. A leak in  the  pump
suction  line  allowed air  to  enter  the pump,  thus reducing the pump capacity. This
condition affected operation for a period  of about 2 months. The sludge pump automatic
time clock failed to operate properly on several occasions, resulting in a rapid reduction
in MLSS concentration in the  aeration basin.

AUTOMATIC  SAMPLERS—A  mechanical problem  with  the automatic sampler timing
device required manual sampling of the  influent  and effluent  flows during the first  4
months  of operation. The  sample quality suffered somewhat as a result  of  this  problem
even though  the samples were manually mixed to form composites during the operating
shift.
                                      -62-

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                                  SECTION VIII
                         FINANCIAL CONSIDERATIONS
CONSTRUCTION COSTS

The total capital cost for construction of the treatment facility, including engineering and
land costs,  was  $605,470. A detailed  cost  breakdown is included  in  Appendix  D.
Comparison  of this  total  with  a total cost of $913,000  for a  conventional activated
sludge  plant,  obtained  from  Smith's  curves  [13]  and  updated to  1968,  indicates a
substantial saving in capital costs.

OPERATION AND MAINTENANCE COSTS

The total operation and maintenance costs for the first year of operation were $32,700.
Operation and maintenance costs for the plant, after deducting costs attributable only to
the demonstration program,  were  $22,200 and  represent  the normal  yearly cost for
running the  plant. The added  costs due to the demonstration program were attributed to
additional sampling and  testing  requirements,  supervision and data analysis.  A detailed
breakdown of operation and maintenance costs is included in Appendix D.

Michel [14] reported annual operation and maintenance costs, for activated sludge plants
treating an average daily flow  of 1.0 mgd,  ranging from  about $21,000 to $70,000 with
an average  cost  of about $37,000 per year (costs updated  to  1970). The operation and
maintenance cost of $22,200 for the Dallas  plant was about 60 percent of the average.

Smith  [13]  reported average operation and maintenance costs, for activated sludge plants
treating an  average daily  flow of 1.0  mgd, of about  $100 per million gallons  treated
(costs  updated to  1970). Operation and maintenance costs  at the Dallas plant averaged
$33 per million gallons treated or about 33  percent of Smith's figure.

TOTAL ANNUAL COSTS

Table  7 lists total annual costs of the treatment  system  for the  first year of operation.
Total  annual costs include:  1) annual capital  amortization  costs (6 percent interest, 20
years), 2) annual operation and  maintenance  costs, and  3)  equipment replacement and
depreciation costs (5  percent of equipment capital cost).
                                       -63-

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                                    TABLE  8
                            TOTAL ANNUAL  COSTS

        Item                                                   Annual Cost

        Capital Cost                                               $605,470
        Amortized Capital Cost (6%-20 years)                          52,800
        Annual Operation and Maintenance Cost                       22,200
        Estimated Equipment Replacement
           and  Depreciation                                           6,800

        TOTAL ANNUAL COST                                   $81,800


On  the  basis of this total annual cost, and the total pounds of BOD removed during the
year, cost of treatment was calculated as $0.258 per pound of BOD removed.

This unit cost appears to be higher than would normally be expected. However, the plant
has  been operated far below the BOD loading capacity  and high infiltration  into the
collection system results in  a very dilute waste during wet weather periods. Therefore, the
cost per unit of BOD  is increased because of the required operation of units not related
to BOD removal.

A more realistic approach would be  to  calculate unit cost for the amortized capital cost
portion  of the  annual  cost,  based on  available BOD loading capacity rather than on BOD
removal. The unit cost, calculated on this basis, was  $0.097 per pound of BOD removed,
and  included  $0.026  per  pound of  BOD based  on debt service  and depreciation and
$0.071 per pound  of BOD removed based  on operation and maintenance costs.
                                      -64-

-------
                                   SECTION IX
                                   DISCUSSION
ACTIVATED SLUDGE SYSTEM

MICROBIOLOGY— The system  was operated  at a relatively long sludge age, which tends
to favor the higher  forms of organisms. Periodic microscopic examinations revealed  the
presence of a wide  range  of organisms, ranging  from bacteria through rotifers,  during
different periods throughout the demonstration program.

The  system appeared to  operate most efficiently  when a moderately large population of
rotifers and a large population of stalked ciliates were present in the activated sludge. The
moderate rotifer  population  indicated  that the system  was very stable,  as discussed in
Section III.

Very few  filamentous organisms  were observed, although some nitrification occurred in
the aeration basins throughout  the  period. However, the alkalinity of the wastewater was
sufficient to buffer the system, thus minimizing the conditions favorable to filamentous
growth.

The  predominant protozoa identified in the activated  sludge during the periods of most
efficient  operation  were  the  stalked  ciliates  Vorticella campanula   and   Vorticella
microstoma.

SUBSTRATE  REMOVAL-Substrate  utilization  in  the  activated  sludge  system, as
previously  discussed in Section III, is described by the  following equation:
                       kS  =
                         6
The  substrate removal  rate, k, is  equal  to the slope  of  the  first order curve passing
through the origin, on  a plot  of total pounds  of BOD removed per day per pound of
MLVSS vs.  mg/1 of effluent soluble  BOD.  Figure 26 is a  plot of substrate removal vs.
effluent soluble BOD for all data obtained during the demonstration period.

The field data plotted  on Figure 26 show considerable  scatter,  as may be expected. For
this reason,  the  curve  from the origin was  drawn through the  mean  coordinates of the
data points.
                                       -65-

-------
(/D
ZD
C/3
 EFFLUENT  SOLUBLE
               FIGURE 26

SUBSTRATE REMOVAL VS. EFFLUENT SOLUBLE BOD

-------
This figure includes data for a relatively wide range of temperatures (9  degrees C  24
degrees C).  Three  separate  curves  were plotted initially, for data of  three  different
temperature  ranges.  Substrate  removal  rate  coefficients  obtained from these  plots,
however, showed no reasonable variation  with temperature  as described in the literature
[15,  16,  17].  Therefore,   it  was  concluded   that, within  the  range  of  operation
experienced,   the   substrate  removal  coefficient  is  not  affected  significantly  by
temperature.

The average substrate removal  coefficient, k, calculated from  the  data plotted on Figure
26, was 0.041. This value agrees closely with the data for domestic wastewater presented
by  Eckenfeldef  [15], but is somewhat higher than the coefficients obtained  for potato
processing wastewater [17]  and fruit processing wastewater [16]. This indicates that the
composition of the wastewater influent to the treatment plant at Dallas is predominantly
domestic in nature.

CANNERY STARTUP, OPERATION AND SHUTDOWN-The discussion of the nature of
the influent wastewater presented  in the previous paragraph  is reflected  by the lack of
effect on plant operation of cannery startup and shutdown.

The peak  BOD loads  to  the system  occur  during the  canning  season. However, no
significant change  in  effluent quality has  resulted from these  peaks. The gradual increase
and decrease of processing load at  the  cannery tends to reduce the shock load effect of
cannery startup and shutdown.

The distance  from the cannery to the treatment plant  may have some  effect on the
strength of the canning waste. It is likely that a significant BOD reduction occurs in the
sewer between the cannery  and the treatment  plant  since the canning waste is highly
soluble and the detention time is relatively long.

The canning  waste is  also  substantially  diluted  by the  domestic wastewater and by
infiltration into the  system, resulting in a lower BOD  concentration at  the  treatment
plant.

EFFLUENT  QUALITY-The effluent  quality data presented  in Section VII give an
indication of the  flexibility and  stability  of  the  system.  The  effluent quality was
consistently good during a wide range of operating conditions. The wide variation in flow
through the plant  resulted in a large fluctuation of aeration  time. During the wet weather
flows, aeration times were as low as 3.4 hours.

The organic loading rate, in  general, varied  between 0.05 and 0.15 Ib BOD per Ib MLSS
per  day.  This range  of loading rates is  somewhat lower  than the values generally
                                       -67-

-------
considered  desirable for efficient operation of activated sludge systems. However, a check
of the effluent BOD values plotted on Figure 9 shows that an effluent of extremely good
quality was maintained at these  low loadings.  The organic  loading was  particularly low
during the  wet weather non-canning season due to  the low  influent BOD. Some control
of the  organic loading  was  accomplished  by reducing the MLSS level. However, a
minimum MLSS level of 700 mg/1 was maintained  to provide a resistance to shock loads
from  glue waste discharges and to minimize washout of  solids during peak flow periods.

Aeration basin  temperatures  varied from  9   degrees C  to  24  degrees C.  The low
temperature periods generally  coincided  with periods of low organic loadings and short
aeration  times, resulting in  conditions  highly unfavorable for  biological  treatment.
However, the stability  of the system prevented the  occurrence of a poor-quality effluent.

CLARIFIER OPERATION-Figure 27 is  a  plot of clarifier hydraulic loading vs. effluent
suspended  solids. Clarifier overflow rates  varied from about 200 gallons per  day per
square foot to  as high  as  2500  gallons per day  per square foot during  wet  weather
periods. The  scatter  of the data on this plot shows that there is very little correlation
between clarifier efficiency and hydraulic loading rate. However, efficiency of the clarifier
was good at all ranges of loading, indicating  a  reasonably stable activated sludge system.

Clarifier solids  loadings were plotted vs. effluent suspended solids on Figure 28. These
loadings ranged from a low  of about 4 pounds per  day per square foot to as much as 50
pounds  per day per square foot. Analysis of this  figure yields  the same conclusions as
discussed in the preceding paragraph for hydraulic loading.

OXYGEN  TRANSFER—Each  aerator is capable of  transferring  to  water, at standard
conditions,  a  minimum of 1180 pounds of oxygen  per day at high speed and at least 50
percent of  that amount on low speed.

Figure 29 is a  plot  of operating horsepower  vs. oxygen transfer capacity. Listed  on this
curve are  the  points  of operation possible to achieve with  the aeration equipment
available. This indicates the wide range of flexibility  of the system.

AEROBIC  DIGESTION

VOLATILE SOLIDS  REDUCTION-The  average reduction  (in  percentage) of  volatile
solids content  of the  waste sludge was  about 5 percent. The long sludge age (19 days
average) in the activated sludge  system  contributed  to  this low percentage of  volatile
reduction as indicated  by Loehr [18]. Another factor affecting the reduction in  volatile
content was the relatively low average VSS  content of the waste sludge (63 percent).
                                       -68-

-------
U-g
  10
  CJ
a
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a:g
or
a
  o
  o .

-------
o
CO
CD

_J
  a
  «
oo
Q
o
LU
a:
    NOTE:  CURVE FIT BY METHOD

         OF LEAST SQUARES
12         18         *4         30

      EFFLUENT  5-  S-  IM&/L)



               FIGURE 28
                                                                         42
                              CLARIFIER SOLIDS LOADING VS.

                               EFFLUENT SUSPENDED SOLIDS

-------
   100 T
    80 .
                                                                                                         3H, 1L
                                                                                        A  3H
                                                                                        *   (2H. 2L)
    60 .
QC
LLJ


O
Q.
LU
C/J
OC

O
I
    40  -
               "2H

               (1H.2L)
                                                   3L
                                                  (1L.1H)
                            ,AlH,3L
                              (2H, 1L)
    20 •
               MIN. OPERATING HP

               FOR MIXING
                                                                                       NOTE: L = LOW SPEED


                                                                                             H = HIGH SPEED
                    600
                                 12,000
1,800          2,400          3,000

OXYGEN TRANSFERRED (LBS./DAY)
3,600
4,200
4,800
                                                        FIGURE 29
                                  HORSEPOWER  - OXYGEN TRANSFER RELATIONSHIPS

-------
An analysis of  the  sludge wasted  to  the digester  was made, using information obtained
from  the literature and concepts discussed by Loehr [18]. Figure 30 shows the calculated
composition of  the  waste sludge solids. The solids  lost from the system per day consisted
of an average of 950  pounds pumped to the digester  and 220 pounds in the effluent, for
a total of 1170  pounds per day.

A large portion  of  the influent TSS  is carried   through   the  system  as residual,
nondegradable,  solids.  These residual solids consisted of all  the inert solids  plus  that
portion of the volatile solids  which were nondegradable.

The nondegradable influent volatile solids were assumed to constitute 40  percent of the
influent VSS, as suggested by Eckenfelder [15].

The  remainder  of the solids wasted to the digester (387  Ib/day) were biological solids.
The   biological   solids  were   also  broken  down  into  three  classifications:  inert,
nondegradable volatile, and degradable volatile. The fraction of each type depends on two
important  operating parameters: sludge age and temperature. Analysis of  data presented
by Eckenfelder  [20]  and McKinney  [3] indicates that, at 15.7 degrees C and a sludge
age of 19.5 days, biological solids will be about 77 percent volatile. Determination of the
degradable and  nondegradable portions of the biological volatile solids was based on data
presented by McCarty and Brodersen  [10]. The biological volatile solids were estimated
to be  about 60 percent degradable at a temperature of 15.7 degrees C and assuming a
19.5 day sludge  age.

This analysis shows  that there is a  maximum percentage of the total waste  solids that are
degradable  for  a particular  set  of  operating  conditions.  For the  average operating
conditions  encountered during this study, the maximum degradable  portion  of the waste
solids was calculated to be about 19 percent.

This low percentage of degradable  solids is partially due to the relatively high proportion
of influent suspended  solids  to  waste  activated sludge solids  in the  sludge wasted to the
digester.  The long sludge age of the system is also  partially responsible for  this condition,
since  the biological solids are already highly degraded before being wasted to  the digester.

The items  discussed in the preceding  paragraphs serve  to explain the low percentage of
reduction in volatile  content  through  the  digester.  The  reduction in volatile content
should increase  in the future, as digester biological solids loading increases  and the sludge
age decreases.

DETENTION  TIME—The  minimum  digester  detention time occurring  during  the
demonstration period  was about 35 days. A  plot  of VSS content of the digested sludge
vs.  digester detention  time  showed highly  scattered data with no reasonable  trends.
                                        -72-

-------
               INERT
  RESIDUAL
  INFLUENT
   SOLIDS
             VOLATILE
          NONDEGRADABLE
BIOLOGICAL
  SOLIDS
                        DEGRADABLE
             VOLATILE
                      NONDEGRADABLE
                             \
               INERT
                i
                 *£.<$>.•$
                   ;*',  *'.^V
TOTAL SOLIDS WASTED/DAY (AVG.)
                                                          260  LBS./DAY
                                     303  LBS./DAY
                                                         179  LBS./DAY
                                                         118  LBS./DAY
                                                         90  LBS./DAY
                                                         950  LBS./DAY
                               FIGURE 30
                 COMPOSITION OF WASTE SLUDGE SOLIDS
                                   73-

-------
Lawton and Norman [19] have shown that very  little volatile solids reduction occurs at
detention times greater than about 15 days. Since the minimum detention time recorded
during this study period was 35 days, all the data lay in the range of low activity. Thus,
the  data  scatter  is  a  result  of  variations in testing  rather than  differences in  VSS
reduction.

SLUDGE YIELD-The  following  equation, giving the  net  accumulation of volatile
biological solids per pound of BOD removed, was presented in Section III:
                     A              	
                    T ' °'65 -  i  +  E
                                       bM

In  this  equation,  the  constant,  0.65,  represents  the sludge yield  coefficient,  a,  for
domestic  sewage and the constant, 0.53,  is the yield coefficient based on synthesis of
degradable biological  solids  only. The term E/M is equal to the reciprocal of the  sludge
age, Ts.

The net  accumulation of  volatile biological  solids per pound  of BOD  removed  was
calculated  from  field data  as 0.425  Ib  VSS  per  Ib  BOD removed.  The  equation  was
modified  as follows,  to enable the determination  of  the sludge yield  coefficient, a,  for
this system:

        The constant 0.65 was replaced by the constant a.

        The constant 0.53  was replaced by the constant 0.6a, which represents
        the degradable fraction  of the volatile bioligical  solids as established
        previously in  this Section.

        The term E/M was replaced by l/Tg.

These modifications resulted in the  following expression for  a:

                               A/F
                         "      06
                     a = 1    	
This equation yields an "a" value of 0.70 for a sludge age of 19.5 days and a "b" equal
to 0.1,  which is in relatively close  agreement with McCarty and Brodersen's  a  value of
0.65 for domestic sewage.
                                        -74-

-------
CHLORINE CONTACT

The  effluent total coliform count averaged about 41 per 100 ml with a maximum of 230
and  a minimum  of 2. A chlorine  residual  of about 1.0 ppm was  maintained in the
effluent nearly all the time.

Studies  were conducted, using Rhodamine B dye and a  fluorometer, to determine the
actual detention  time in the chlorine  contact channel.  These tests  indicated  that the
actual detention time was about 83  percent of the theoretical detention time, based on
the time of peak  dye concentration. The efficiency could likely be increased substantially
by the  addition of an inlet  baffling system.  However, the coliform data has been well
within the required standards, indicating that  the channel  has provided effective contact
time.
                                       -75

-------
                                  SECTION X
                             ACKNOWLEDGMENTS
This project was supported in part  by Environmental Protection Agency Research and
Development Grant No.  11060 EZR. Appreciation is expressed to the administration and
staff  of  the City  of Dallas,  Oregon, the EPA Pacific Northwest Water Laboratory
personnel, and Cornell, Rowland, Hayes & Merryfield staff members for their cooperation
and assistance during this study.
                                       77-

-------
                             SECTION  XI
                             REFERENCES
 1.   "Glossary:  Water  and  Wastewater  Control  Engineering,"  APHA,  ASCE,
     AWWA, WPCF, (1969).

 2.   Hawkes, H.A., Ecology of Waste Water Treatment, Pergamon Press, New York,
     N.Y. (1963).

 3.   McKinney,  R.E., Microbiology for Sanitary Engineers, McGraw-Hill Book Co.,
     New York, N.Y. (1962).

 4.   Weston, R.F., and Eckenfelder, W.W., "Application of Biological Treatment to
     Industrial Wastes, I. Kinetics and Equilibria of Oxidative Treatment." Sewage
     and Industrial Wastes, 27, 802 (1955).

 5.   McKinney,  R.E., "Biological Design of Waste Treatment Plants." Presented at
     Kansas City Section of ASCE Seminar, Kansas City, Mo. (1961).

 6.   McKinney,  R.E., "Mathematics of Complete Mixing  Activated Sludge." Jour.
     San. Engr. Div., Proc. Amer.  Soc. Civil Engr., 88,  SA3, 87 (May 1962).

 7.   Eckenfelder, W.W., "Comparative  Biological Waste Treatment Design." Jour.
     San. Engr. Div., Proc. Amer. Soc. Civil Engr., 93, SA6, 157 (December 1967).

 8.   Lawrence, A.W.,  and  McCarty, P.L., "Unified Basis  for Biological Treatment
     Design and  Operation." Jour. San. Engr. Div., Proc. Amer. Soc. Civil Engr., 96,
     SA3, 757 (June  1970).

 9.   Eckenfelder, W.W.,  "A Theory  of Activated  Sludge  Design  for  Sewage."
     Proceedings of Seminar at the University of Michigan,  72 (February 1966).

10.   McCarty,  P.L.,   and   Brodersen,  C.F., "A Theory   of Extended  Aeration
     Activated Sludge.", Jour. Water Poll. Control Fed., 34, 1095 (1962).

11.   Standard  Methods  For  the Examination  of Water  and Wastewater, APHA,
     AWWA, WPCF, New York, N.Y. (1965).
                                  79-

-------
12.  FWPCA Methods For  Chemical  Analysis of Water and  Wastes. Federal Water
    Pollution Control Federation (1969).

13.  Smith,  R., "Cost of Conventional and  Advanced Treatment  of Wastewater."
    Jour. Water Poll. Control Fed., 40, 1546 (1968).

14.  Michel, R.L., "Costs and Manpower For Municipal Wastewater Treatment Plant
    Operation  and Maintenance,  1965-68," Jour.  Water  Poll.  Control Fed.,  42,
     1883 (1970).

15.  Eckenfelder,   W.W.,   "Volume   1  -  Manual   of  Treatment   Processes."
    Environmental Science  Services Corp. (1968).

16.  Snokist Growers, Inc.,  "Aerobic Treatment of Fruit Processing Wastes." Report
    No. DAST-8, U.S. Dept. of Interior, Fed. Water Quality Admin. (1969).

17.  French,  The  R.T.  Company,  "Aerobic  Secondary  Treatment  of Potato
    Processing  Wastes."  Environmental  Protection Agency,  Water Quality  Office
   ~ (1971).

18.  Loehr,  R.C.,  "Aerobic  Digestion:  Factors  Affecting  Design."  Water  and
    Sewage Works, R170 (1969).

19.  Lawton, G.W., and Norman, J.D.,  "Aerobic Sludge Digestion Studies."  Jour.
    Water Poll. Control Fed., 36, 495 (1964).

20.  Eckenfelder, W.W.,  and Ford, D.L., "Laboratory and Design  Procedures For
    Wastewater Treatment  Processes." The Center For Research in Water Resources
    at the University of Texas at Austin; Austin, Texas (1968).
                                   80

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                                 SECTION XII
                                 PUBLICATIONS
Graham, J.L. and Filbert, J.W., "Combined Treatment of Domestic and Industrial Wastes
By Activated Sludge." Proceedings, First National Symposium on Food Processing Wastes,
Sponsored By:  FWQA Pacific Northwest  Water Laboratory;  USDA Western Regional
Research Laboratory; National  Canners Association; and  Northwest Food  Processors
Association,  Portland, Oregon (1970).

Graham, J.L. and Filbert, J.W., "An Unconventional Approach,"   The  American   City,
October 1970.
                                      -81 -

-------
                           SECTION  XIII
                          ABBREVIATIONS
mg/1                                               Milligrams per liter
BOD                                      Biochemical Oxygen demand
MLSS                                     Mixed liquor suspended solids
MLVSS                             Mixed liquor volatile suspended solids
mgd                                           Million gallons per day
TSS                                            Total suspended solids
VSS                                          Volatile suspended solids
SVI                                              Sludge volume index
D.O.                                                 Dissolved oxygen
O2                                                         Oxygen
Ts                                                        Sludge age
                               -83-

-------
                   SECTION XIV
                   APPENDIXES
NO.                                            PAGE

A       Photographs                               87
B       Process and Laboratory Equipment             95
C       Velocity and Dissolved Oxygen Data           99
D       Costs                                    115
E       Results of PVC Tests                       119
                       -85

-------
 APPENDIX A



PHOTOGRAPHS
    -87-

-------
00
OC
                                                       FIGURE A-1

                                               CLARIFIER & CONTROL BUILDING

-------
   FIGURE A-2




AERATION BASINS

-------
   FIGURE A-3




AEROBIC DIGESTER

-------
FIGURE A-4

-------
                 FIGURE A-5
 SOLIDS DEPOSITS - AERATION BASIN NO. 1, N. SIDE
                FIGURE A-6
SOLIDS DEPOSITS AND SCOUR-AERATION BASIN NO. 1
                  -92-

-------
      FIGURE A-7




  DRIED HUMUS (2'x3' AREA)
      FIGURE A-8
AERATION BASIN NO. 1
        -93-

-------
            APPENDIX B



PROCESS AND LABORATORY EQUIPMENT
               -95-

-------
                           PROCESS EQUIPMENT
EQUIPMENT

Comminutor
Sludge Recirculation Pumps
Raw Waste Pumps

Aerators
Clarifier

Chlorination Equipment

Flowmeters
Flowrecorder
Sampler

Waste Sludge Pumps

Sample Pumps
Chlorinator Water Supply
Nonpotable Water Pumps

Air Compressor
MODEL

25A
6FNJD-15
6FNC-15

Model 25
Model 30

RSR Type

V-800 Chlorinator

Propeller Type

260-B

T4A3B

FS-22
PACO 1070-1
PACO 1270-5
MANUFACTURER
Worthington Corp.
Eimco Corp.


Dorr-Oliver, Inc.

Wallace & Tiernan

Hersey-Sparling Meter Co.



Gorman-Rupp Co.

Robbins and Meyers
Moyno Pump Division

Pacific Pumping Co.


Bell & Gossett Products
                                   -96-

-------
                        LABORATORY  EQUIPMENT
EQUIPMENT

Furnace

Drying Oven

Magnetic Stirrer

pH Meter

Demineralizer

D. 0. Meter

Balance
TYPE

Thermolyne Type 1400

Precision Scientific

VW & R Magnistir

Photovolt

Barnstead Bantam

YSI  Model 54

Voland &  Sons
Model 220D
RANGE

0-1400°C

0-140°C
0- 10gal/hr.

0 - 20 ppm

0 - 200 g
                                   -97

-------
             APPENDIX C



VELOCITY AND DISSOLVED OXYGEN DATA
                -99-

-------
DEPTH OF READINGS  1  FOOT

   ROTATION OF AERATORS
   IN OPERATION
VELOCITIES IN FEET PER SECOND
                      FIGURE C-1

          AERATION BASIN VELOCITY PROFILE
             FOUR  AERATORS - LOW SPEED
                         I 00-

-------
DEPTH OF READINGS:  6 FEET
c
ROTATION OF AERATORS
IN OPERATION
VELOCITIES IN FEET PER SECOND
                       FIGURE C-2


          AERATION BASIN VELOCITY PROFILE
             FOUR AERATORS - LOW SPEED
                         101

-------
DEPTH OF READINGS:  9 FEET
c
ROTATION OF AERATORS
IN OPERATION
VELOCITIES IN FEET PER SECOND
                       FIGURE  C-3


          AERATION  BASIN VELOCITY PROFILE
             FOUR AERATORS - LOW SPEED
                          - 102

-------
DEPTH OF READINGS:  1 FOOT
c
ROTATION OF AERATORS
IN OPERATION
D.O. IN MG/L
                       FIGURE C-4

             AERATION BASIN D.O. PROFILE
             FOUR AERATORS - LOW SPEED
                         -I 03-

-------
DEPTH OF READINGS:  6 FEET
c
ROTATION OF AERATORS
IN OPERATION
D.O. IN MG/L
                         FIGURE  C-5

               AERATION BASIN D.O. PROFILE
               FOUR AERATORS - LOW SPEED
                          -104-

-------
DEPTH OF READINGS: 9 FEET
r>
ROTATION OF AERATORS
   IN OPERATION

D.O. IN MG/L
                         FIGURE C-6

               AERATION BASIN D.O. PROFILE
               FOUR AERATORS - LOW SPEED
                             105

-------
   6-
Q
01
CO
X
o
Q
LU
uj  2.
Q
                                                  do

                                                  dt
                                        5.6mg/l/HR.


                          D.O. UPTAKE =  0.013 mg Oj/mg VSS/d
      DATE:


      TIME:


      TEMP.:
   20




OCT.  16, 1970


10:00 A.M.
40            60

TIME  (MINUTES)


  TSS =  15,000 mg/l


  VSS =  10,000
                                                             80
                                                                           100
                                FIGURE  C-7


                       DISSOLVED  OXYGEN DATA

                                DIGESTER
                                   - 106 -

-------
   6-
   4-
D
LU
to
=>
X
o

Q
LU
uj  2-
Q
                                                  do

                                                  dt~
                                       = 4.5 mg/l/HR.
                                          D.O. UPTAKE   0.011 mg 02/mg VSS/d
     DATE:


     TIME:


     TEMP.:
    20





OCT. 16, 1970


1:15 P.M.
40            60

 TIME (MINUTES)



   TSS =  15,000  mg/l


   VSS =  10,000  mg/l
                                                             80
                                                                           100
                                FIGURE C-8


                      DISSOLVED OXYGEN  DATA

                                DIGESTER
                                       !07

-------
Q
LU
in
LU
13  4-


X
o
_

8
H;  2-
D
                              do
                              -r- =  7.5 mg/l/HR.
                              dt
                                     D.O. UPTAKE    1.03 mg 02/mg VSS/d
                 20
                 40            60

                 TIME (MINUTES)
                                                         80
                                                                       100
     DATE:



     TIME:



     TEMP:
OCT. 14, 1970



11:30 AM
TSS


VSS
630 mg/l


175 mg/l
                              FIGURE C-9



                      OXYGEN UPTAKE DATA

                          AERATION BASIN
                                 - 108-

-------
O
LU
C/3
=>
X
o
Q
   6-
   4-
   2 -
                                              do
                                ——  =  5.5 mg/l/HR.


                          D.O. UPTAKE  =  0.155 mg02/mg VSS/d
     DATE:

     TIME:

     TEMP.:
    20




OCT. 15, 1970

9:30 A.M.
40            60
TIME (MINUTES)


  TSS  =  1360 mg/l

  VSS    850  mg/l
                                                           80
                                                                         100
                                 FIGURE  C-10


                        DISSOLVED OXYGEN DATA
                            AERATION BASIN
                                     109-

-------
   6-
   4-
Q
LU
to


z
LU
d

X
o

Q
LU
O
C/J
OT  2-

Q
                                              —   6.55  mg/l/HR.
                                              at
                                      D.O. UPTAKE   0.16mg02/mg VSS/d
                 20
                               40
                                              I
                                             60
                                                           80
                                                                        100
                                TIME (MINUTES)
     DATE:


     TIME:


     TEMP.
             OCT. 15, 1970


             11:00 A.M.
TSS    1240 mg/l


VSS    990
                                FIGURE  C-11



                       DISSOLVED OXYGEN DATA

                            AERATION BASIN
                                     MO-

-------
   6-
   4_
Q
LJJ
CO
X
o
Q
LLJ
O
to
55  2.
Q
                                                do
                                  dt  - 6.70  mg/l/HR.


                          D.O. UPTAKE    0.28 mg 02/mg VSS/d
      DATE:


      TIME:
    20





OCT. 15, 1970


1:45 P.M.
                                40            60
                                TIME  (MINUTES)
TSS    850  mg/l


VSS =  570  mg/l
                                                            80
                                       100
      TEMP.:   17.5 C
                                 FIGURE C-12


                        DISSOLVED OXYGEN DATA

                             AERATION BASIN

-------
  6-
Q
01
in
01
13  4-


X
o

Q
LLJ
o

!>•
                                        --= 5.69 mg/l/HR.
                                         dt


                                  D.O. UPTAKE   0.21 mg Oj/mg VSS/d
                20
                            40          60

                            TIME (MINUTES)
                                                                 100
DATE:
TIME:
TEMP:
OCT. 14, 1970
4:00 P.M.
19°C
TSS
VSS

= 860 mg/l
660 mg/l

                            FIGURE C-13


                    DISSOLVED OXYGEN DATA

                        AERATION BASIN

-------
   8-1
_J  6-
Q
LLJ
   4-
X
o
Q
I.
                                              do
                                             	 = 6.45 mg/l/HR.
                                              dt

                                      D.O. UPTAKE = 0.76 mg 02/mg VSS/d
                  20
                                40           60

                                 TIME (MINUTES)
                                                           80
                                                                        100
      DATE:


      TIME:


      TEMP.:
               OCT. 14, 1970


               1:30 P.M.
TSS  680 mg/l


VSS= 205 mg/l
                             FIGURE C-14



                       OXYGEN UPTAKE DATA

                          AERATION BASIN
                                    H3-

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APPENDIX D



   COSTS
   - 115

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                                 TABLE  D-1
                        CITY OF  DALLAS, OREGON
                   WATER  POLLUTION CONTROL PLANT
                           CONSTRUCTION  COSTS

ITEM                                                            TOTAL COST

Temporary Facilities                                                    $ 12,000
Bond and Insurance                                                       8,000
Move-In and Site Preparation                                              20,000
Cleanup and Finish Grading                                                2,000
Earthwork                                                               7,000
Headworks                                                               4,000
Aeration Basin Splitter Box                                                3,500
Aeration Basins                                                          83,000
Clarifier and Sludge Recirculation Pump Station                              40,600
Aerobic Digester                                                         19,600
Flow Measurement Box                                                      600
Chlorine Contact Channel                                                 12,500
Humus Ponds                                                             8,000
Control Building                                                         23,000
Maintenance and Storage Building                                           1,500
A.C. Road and Parking                                                     7,250
Gravel Road and Parking                                                   2,000
Concrete Walks and Curbs                                                  1,800
Fencing                                                                 7,000
Painting                                                                 6,000
Outside Piping and Plumbing                                              30,500
Sewage Shredder                                                         10,000
Aeration Equipment                                                      81,000
Clarifier Mechanism                                                      17,500
Sludge Recirculation Pumps                                                9,500
Self Priming Sludge Pumps                                                 2,150
Flow Measurement Equipment                                              4,000
Chlorination Equipment                                                    6,100
Miscellaneous Pumps and Sampler                                           2,000
Hoisting Equipment                                                       2,500
Laboratory Equipment and Furnishings                                       3,000
Electrical                                                               21,000
Raw Sewage Pump Station                                                73,000
                                      116

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                           TABLE D-1 -  Continued

ITEM                                                            TOTAL COST

Plans and Specifications                                                $ 31,480
Test Borings                                                               400
Supervision and Inspection of Construction                                  20,910
Administrative, Legal and Fiscal Costs                                        1,080
Land                                                                   20,000

     TOTAL                                                          $605,470
                                       117-

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                                 TABLE D-2
                    DEMONSTRATION, OPERATION AND
                           MAINTENANCE  COSTS
                                OPERATION AND           DEMONSTRATION
          ITEM               MAINTENANCE COSTS             COSTS

Labor                               $11,460.87
Electrical Power                         6,395.72
Chemicals                              2,153.39
Maintenance                              956.99
Miscellaneous (Supplies, etc.)              1,225.26
Post Construction Studies
  and Reports                                                   $ 8,319.91
Legal and Fiscal Costs                                                506.45
Administrative Costs                                                1,679.19

      TOTALS                      $22,192.23                 $10,505.55


Total Cost   First  Year  Demonstration   $32,697.78

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     APPENDIX E



RESULTS OF PVC TESTS
       -119-

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 OREGON  STATE UNIVERSITY                           CORVALUS. OREGON

 SCHOOL OF ENGINEERING                                      Reply to: DEPARTMENT OF
                                                         GENERAL ENGINEERING

 December 8,  1970
Mr. Robert  Burm,  Staff  Engineer
National Waste Treatment  Research  Program
Pacific Northwest Water  Laboratory
200 S.W. 35th St.
Corvallis,  Oregon  97330
Dear Mr. Burm:

     Following are my  interpretations of the  test  results  on  the  PVC
liner.   I have assumed  that  the used material  (A) was  the  same  as  the
20 mi 1 new material  (B)  initially.

     There is evidently  some  loss  in material over  the one year use
as a sewage pond  liner.  The  chemical action, however, is  apparently
not detrimental to the properties.  All measured properties show  an
increase in resistance  to  load:  approximotely  10%  increase in  tensile
strength and secant modulus  and about 20%  increase  in  tear resistance.
The percent elongation at  break shows about a 20%  increase, also.  The
Change in all these factors  can be conveniently expressed  as  a  signi-
ficant increase in toughness .

     The one other significant result is related to the standard
deviations.  The  standard  deviations of both  the new samples  are
essentially the same while those of the used  sample are approximately
50% to 200?o larger than  those of the new samples.  As could have  been
foreseen, this indicates that the effect of the chemical environment
Is quite variable even though the trend in change  is as indicated  in
the previous paragraph.

     One would expect to approach   optimum use time after which  the
properties as measured  in  these tests would begin to decrease and  at
some later time come back  to  the original  values and thence decrease
further.  The determination of the regression time to original  values
is important as it may be  anywhere from relatively short to quite  long.
Ultimately, the material may  fail  as a result of extreme thinning  (with
the occurance of  holes) before decreased strength values leading  to
fai 1 ure occur .

     If you should require any further assistance, please  feel  free to
cal 1  upon me .
                             Yours truly,
                             David A. Bucy
                             Associate Prof.

                                   120-

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       .// ^H     I
CORVALLIS. OREGON 97331                            gj
December 1, 1970
OREGON STATE UNIVERSITY

DEPARTMENT OF
METALLURGICAL ENGINEERING
Mr. Robert Burm, Staff Engineer
National Waste Treatment Research Program
Pacific Northwest Water Laboratory
200 S.W. 35th St.
Corvallis, Oregon  97330


Dear Mr. Burm:

Enclosed are the results of the tests you requested on  the  three samples of
plastic liner.  Also included is a detailed procedure  followed during testing.

As discussed by telephone on October 20, 1970,  the results  of these tests are
mutually comparable and should be comparable to further tests conducted
following the outlined procedure.  The tear test results  are not necessarily
comparable to tests conducted following ASTM D1004 because  of the  lack of a
.-!t*a for cutting the samples.  Other than the lack of a  die, the tests were
conducted following ASTM D882 and ASTM D100*».

If you should require any further assistance,  please feel free to  call upon me.


                                 Yours truly,
                                 David A.  Bucy
                                 Associate Professor
DAB:jaw
                                     - 121 -

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                            SUMMARY OF TESTS
Gage Length  (Tensile)


Nominal Width, in.


Nominal Thickness,  in.


Break Factor, Ib/in.

            S


Tensile Strength, psl .

            S


% Elongation at Break

            S
Secant Modulus of Elasticity,
  AL = 3 in., psi
Tear Load, Ib

            S
A
5
1
0.0195
40.5
2.2
2090
no
238
31
1760
55
7.88
0.7**
B
5
1
0.0209
40.2
1.1
1920
48
195
9-7
1600
38
6.51
0.41
C
5
0.5
0.0299
64.5
1.4
2170
43
304
10
1290
35
9.15
0.66
A - used 20 mi 1   PVC

B - new 20 mi 1  PVC

C - new 30 mi 1  PVC

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                 PLASTIC SHEETING TEST REPORT
FOR:  Mr. Robert Burn, Pacific Northwest Water Laboratory
 BY:  David A. Bucy, P.E., State of Oregon^Department of
      Metallurgical Engineering, Oregon State University
Procedures for Testing Plastic Sheeting
      Tensile Properties Test
      ASTM D882  (copy appended) was followed.  Report
      proper includes all pertinent information.
      Tear Resistance Test
      ASTM D100A  (.copy appended) was followed except for
      the die described under paragraph 3-(e).   Samples
      were cut through a mimeographed copy of the shape
      attached to the material using a razor blade.
      Particular attention was paid to the 90°  notch to
      ensure no over cut occurred.
                                123-

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                  TENSILE PROPERTIES OF THIN PLASTIC SHEETING
1.  Material
    Three lots of material were supplied by Robert Burm, Pacific Northwest
    Water Laboratory and will be designated A,B, and C as follows:

    A.  Used plastic liner. Apparently, from cutting, density,  and burn
        test, it is polyvinyl chloride (PVC).   Assumed to be isotropic in
        plane of sheet."  Six strips approximately 3 inches by  20 inches.

    B.  New sheet approximately 13 inches by 32 inches.   Marked "20 mil
        thickness, PVC" by R. Burm.   Thought to be identical  with A but
        unused.   Cutting, density, and burn test results same as A (PVC).

    C.  New sheet approximately 17 inches by 29 inches.   Thicker than A
        and B.  Cutting, density,  and burn test results  same  as A and B
        (PVC).  Assumed to be isotropic in plane of sheet."
2.  Preparation of Test Specimens
    Test specimens were cut with a razor blade moved  along  a  straight edge
    guide.   Specimen edges were inspected microscopically  to  detect  nicks
    or tears.
3.   Specimen Dimensions (Nominal)
    Material           Thickness             Width.             Length

       A              0.0195 in.            1.0  in.             7.0  tn.
       B              0.0209 in.            1.0  in.  .           7.0  in.
       C              0.0299 in.            £3  in/1^        7.0  in.
    *  All  sample pieces  are too small  to identify  original  roll  transverse
       and  longitudinal  directions.
                                        124-

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 Tensile Properties of Thin Plastic Sheeting Cont.
 Page Two

 A.   Number of specimens
     Six specimens of each material were tested.

 5.   Strain rate - 0.1 in./in./min. was used in  order  to  meet  requirement  for
     Modulus of Elasticity measurement.


 6,   Initial grip separation - 5 inches.


 7.   Crosshead soeed - 0.5 in./min.
 9.  Gr?p s - rubber faced approximately 1  inch  x 1  inch  square as supplied by
     Instron.
TO.   Test method - A


11.   Conditioning
       Temperature - 70°F
       Relative Humidity -


12.   Anomalous behavior - Tear in one specimen,
                                          125-

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      Accession Number
                                 Subject Field & Group
                                      05D
                                                SELECTED WATER RESOURCES ABSTRACTS
                                                        INPUT TRANSACTION  FORM
      Organization
         Dallas,  Oregon,  City  of
      Title
         Combined Treatment  of  Domestic and  Industrial Wastes
         By  Activated  Sludqe
  10
Authors)
         Dallas,  Oregon,
         City  of
                                    16
                                        Project Designation
                                           Grant ftp. -~.L213ffiBZR  (11060 EZR)
                                          21
                                              Note
  22
      Citation
      Descriptors (Starred First)

         *Waste  treatment,  *Aerobic  treatment,  Industrial wastes,
          Activated  Sludae,  Domestic Wastes
  25
      Identifiers (Starred First)
         *Food  processing wastes,  Aerobic  digestion, Treatment  costs.
  27
      Abstract
The operation of a completely aerobic secondary treatment facility for treatment of combined domestic and industrial wastevvater
from the City of Dallas, Oregon, was studied for a period of 15 months. The system was designed for an average daily flow of 2.0
mgd and a BOD load of 7000 pounds per day. The results of this study indicate the flexibility and economy of the completely
aerobic system,  consisting of activated  sludge with  aerobic digestion, for a small community with proportionately high industrial
wastewater loads. The effluent BOD concentration averaged 8 mg/1 and the effluent total suspended solids concentration averaged 13
mg/1 for the 15-month study period. The biological solids yield averaged about 0.7 pounds of solids per pound of BOD removed and
the net accumulation of biological  volatile solids was about 0.42 pounds of volatile solids per pound of BOD removed. These values
were obtained with a MLSS concentration range of 700 to 3000 mg/1, an average sludge age of 19 days and an organic loading range
of 0.05 to 0.40  pounds of BOD per pound of MLSS per day. Total capital cost  of the system was about 66 percent of that for a
conventional activated sludge plant and operation and maintenance costs were only about 33 percent of those for a conventional
system.

This report was  submitted  in fulfillment of Grant No.  11060  EZR under the  partial  sponsorship of the Water  Quality Office,
Environmental Protection Agency.
 Abstractor
           John L. Graham
                             Institution
                             Cornell,  Rowland,  riayes &  Merryfield,  Corvallis,  Ore
   WR:102  (REV. JULY <969)
   WRSI C
                                               SEND TO: WATER RESOURCES SCIENTIFIC INFORMATION C EN
                                                       U.S. DEPARTMENT OF THE INTERIOR
                                                       WASHINGTON. D. C. 20240
                                                                                         * CPO: 1563-359-33?

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