-------
              Table 9.   DYNAMIC  TOXICITY  TEST B —
                        MATERIAL BALANCE  ON COPPER
                        (BASIS 24 HOURS)
                  Copper ,
                    mg

Copper In         10,044

Copper Out

Overflow, liquid   2,253

Overflow, bacteria   956

Wasted, Bacteria   1,043

Total Out          4,252

In-Out             5,792
Copper
Accumulation

In Liquid

In Bacteria

Total
Accumulation
                    Copper.
                      mg
  848

5*048


5,896
                              134

-------
to


£ 4000
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          Figure  55.
Dynamic toxicity test B,
copper accumulation in
aeration basin mixed liquor
0  3000
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 •  2000
                               Copper in Bacteria
03
s  1000
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-------
miniplant, about 5800 mg of copper were accumulated In
the bacteria, resulting in an increase of copper concen-
tration from 656 to more than 4000 mg of copper per Kg
of dry bacteria.  The copper uptake rate by the bacteria
was very rapid during the first eight hours, reaching a
level of 3000 mg per Kg of dry bacteria.  A plot of the
rate of copper uptake versus the amount of copper adsorbed
by the bacteria (Figure 56) indicates a second order
reaction.  This shows that the reaction with copper was
controlled by the amount of respiratory enzyme available,
which was large at the start of the test, showing no
reduction in activity, then, at a point where most of the
enzyme sites were complexed with copper, sharply decreased
in activity.
                          136
-------
      Figure 56.
   Reaction order kinetics of copper
   adsorption on glycol-salt bacteria
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                        SECTION IX
  EFFLUENT QUALITY MONITORING AND INSTRUMENTS EVALUATION

An Ionics Model 225 Total Oxygen Demand (TOD) Analyzer and
a multiple stream selector were used to monitor the feed
to the activated sludge miniplant and the effluent before
and after chemical flocculation.

A schematic of the monitoring system is shown in Figure 57-
The five-stream selector was equipped with a four-stream
manifold for the three streams to be monitored and for a
standard solution used to calibrate the instrument response
once a day.  The feed stream was diluated 1:3 with distilled
water using a cassette peristaltic pump.  Gravity flow of the
effluent samples to the instrument resulted in plugging the
sample valves.  Filters were added in the sample lines and
pumping at a rate of 20 ml/min was necessary to maintain
the sample flow to the instrument.  The instrument was
calibrated daily with a 700 mg/1 TOD standard solution and
the gain adjusted for a 70-percent full-scale response.
The response that included the diluted feed and the effluent
samples concentrations was linear in the range of 100 to
700 mg/1.  The linear range of the calibration curve was
checked once a week.

The Total Oxygen Demand Analyzer and the Total Carbon
Analyzer, used for the control of nutrients addition and
F/M control, were quantitatively evaluated for their per-
formance during the periods of monitoring both fresh water
and salt water streams (8 to 10 percent NaCl).
                             138
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                               139
-------
PERFORMANCE OP THE TOTAL OXYGEN DEMAND ANALYZER
The instrument was operated in the laboratory for several
months before being installed in the miniplant.  The
precision of measurement of standard solutions was ±4 per-
cent in the linear range of 0 to 500 mg/1 TOD.  The rotary
sampling valve required frequent adjustments to prevent
leakage around the injection port and the drive gears for
the motor turning the valve failed early during the second
month of operation.  The gears were replaced under warranty
by the manufacturer at a cost of four hours labor and four
days downtime.

The instrument and the multiple stream selector were installed
in the miniplant and operated on fresh water samples for a
period of four months and on salt water samples for one month.
During the second week of operation, the printed circuit
card in the stream selector, containing a stepping switch,
failed and was replaced under warranty, resulting in three
days downtime and four hours labor.  This was followed by
several problems with the instrument, a failure of a control
card (two days of downtime), a failure of a power relay in
the combustion heater circuit (two days downtime), and a
failure of the balancing motor of the recorder (four days
downtime).  Numerous, short-duration downtimes occurred
for cleaning the rotary sample valve and adjusting its 0-ring
injection seal.  The oxygen sensor required adjustment of
electrolyte level (that affects sensitivity) as frequently
as twice a week and was disassembled for electrode cleaning
once a month.

A precision chart and a record of the time out of control,
downtime, and hours of maintenance labor were kept during
the continuous operation of the instrument.  A sample of
the precision control chart is shown in Figure 58 and a summary
                             140
-------
         Figure  58.
Precision control
TOD analysis
chart	
       Range - 45-65% Scale
       * = 0.05 0 =  0.05
        Full Scale = 1034 mg/1  TOD
        S  = 1.90% Scale
CM
-o
   -50
                  23456
               Day of Duplicate Sample, M
-------
of the performance of the instrument is given in Table 10
for the fresh water and salt water sampling.  The last month
of operation on salt water (8 to 10 percent NaCl) samples
proved to be very difficult.  The combustion tube was coated
with a salt glaze and carbon precipitated in the lines
between the tube and the oxygen sensor, plugging the sample
passage in less than four days of operation.  The combustion
tube was then slowly cooled to prevent its rupture and
replaced every four days.

PERFORMANCE OF THE TOTAL CARBON ANALYZER
The instrument was operated in the laboratory for a period
of three months, without incident.  The precision of measure-
ment of standard solutions was ±1 percent of the range of 0
to 300 mg/1 organic carbon.

Operated on the miniplant feed stream was once interrupted
by the failure of a heater element around the combustion
tube that was replaced under warranty.  For the purpose of
monitoring the total carbon of a homogenized sample from the
aeration basin, several controls were added to the analyzer.
The added controls included a sampling switching circuit, a
memory control, and a signal retransmission circuit.  Oper-
ation of the analyzer on the homogenized bacterial samples
caused frequent plugging of the injection valve until the
sample handling system was improved to include a backwashing
with the continuous feed sample.  Replacement of the injec-
tion tube below the slide valve with one of larger bore
resulted in significant loss of sensitivity.

A sample of the precision control chart is shown in Figure 59,
and a summary of the instrument performance is given in
Table 11 for the fresh water and salt water operation.
During the four months operation on fresh water sampling one
                             142
-------
Table 10.  PERFORMANCE OF THE TOTAL OXYGEN DEMAND ANALYZER
           (Ionics Model  225-Serial No.  357)
                              Fresh Water
                              4-mon. Per.
             Salt Water
             1-mon. Per,
Time in Control, %
Time Out of Control, %
Down Time, %
Maintenance Labor, hrs
62.5
35.4
 4.1
95
52.6
41.6
 5.8
20
                            143
-------
         Figure 59.  Precision control chart	
                     TC analysis
         Range - 44-55% Scale  Full Scale  = 690  mg/1  TC
         <* = 0.05  6 = 0.05    Sd = ±  3.67% Scale
CM
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1X1
  - 50-
  -100-
      0   1
23456789  10  11
  Day  of  Duplicate  Sample,  M
                          144
-------
   Table 11.   PERFORMANCE  OF  THE  TOTAL  CARBON  ANALYZER
              (Ionics  Model  1212-Serial  No.  1196-12)
                              Fresh Water
                              4-mon. Per.
            Salt Water
            1-mon. Per,
Time In Control, %

Time Out of Control, %

Down Time, %


Maintenance Labor, hrs.
82.2

14.3

 3.5


60
97.5

 2.0

 0.5
                           145
-------
Incident resulted in most of the downtime and 50 hours of
maintenance labor.  The loss of sensitivity and the mal-
functioning of the automatic zero electronic unit attached
to the infrared detector resulted in a need to overhaul
many parts of the instrument, including the infrared unit
adjustment to restore its optical balance.  Satisfactory
operation was restored only after replacement of the com-
bustion tube.  Apparently, the catalyst inside the tube had
fallen below the high temperature region and was the main
cause of the erratic results.

Operation on the high salt (8 to 10 percent NaCl) sampled
at 18-minute intervals was excellent for a period of three
weeks followed by a slow loss of sensitivity to the end of
the one-month operation.  This was due to accumulation of
salt within the combustion tube.

The slide injection valve was smoothed by grinding twice
during the one-year operation of the instrument.  Electrical
maintenance was limited to replacement of one wire in the
infrared unit, while the recorder and associated signal
conditioning circuitry required no maintenance during the
entire operating period.

Comparing the performance of the two analyzers, it was con-
cluded that;

1.  The slide injection valve of the TCA was more reproducible
    and required less maintenance to prevent leaking than
    the rotary valve of the TOD analyzer.

2.  The infrared unit of the TCA was far more accurate and
    precise than the oxygen sensor of the TOD analyzer.
                             146
-------
3-   The Hastelloy combustion tube of the TCA was  not sub-
    ject to thermal fracture as was  the  case with the
    quartz combustion tube of the TOD analyzer.

4.   Samples containing salt were difficult  for both analyzers
    to handle.   Somewhat better service  was expected with
    the TCA.
                             147
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                         SECTION X
               PROCESS DESIGN CONSIDERATIONS

The development of on-line control systems for the activated
sludge treatment process opens up many possibilities for
flexible and innovative process design.

The two most important automatic control systems that
could be incorporated in new plant designs are the biological
inhibition detection (BID) system and the F/M control system.
This is especially true for the design of facilities for the
treatment of combined domestic and industrial wastes, where
variations in the loading and the chemical composition of the
waste stream may be very large.  A typical domestic waste
may have daily variations in BOD from 10 to 250 percent of
the average value and flow rates may vary from 50 to 150
percent (Andrews, 1971).  When combined with the possibility
of slugs (or continuous flow) of industrial wastes where a
toxin to the activated sludge biota may be present, the need
for an inhibition detection system and an F/M control system
becomes readily apparent.

Figure 60 illustrates a conceptual design of an activated
sludge treatment system using these controls,

Equalization of the feed is very helpful for F/M control
and is a necessary part of the plant design.  Equalization
dampens fluctuations in the organic content, in flow, in pH
and in order physical-chemical characteristics of the feed
to the aerated basin.

As illustrated in Figure 60, the equalization tank is also
part of the feed-forward inhibition detection control system.
Equalization provides a time delay, together with dilution
of a possibly toxic feed during the biological activity
analysis period.
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A toxic feed would ordinarily be diverted to a holding basin
by the BID control system.  After determination of the chem-
ical nature of the toxin it could either be bled back into
the system or treated by other means.   Pre-treatment could
include chelation of toxic metals and  sorption of toxic
organics.

The F/M control system would include measurement of
flow and measurement of soluble organic concentration.  The
control system includes an aerated waste stabilization tank
which supplies additional microorganism recycle in periods
of high loading.  The stabilization tank may be located as
shown in Figure 60 or it may be located in the sludge re-
cycle line.  A pilot study would be useful in determining
which site is more adequate in terms of microorganism viability
and the effect on bio-flocculation in  the aeration basin.
For equal-sized stabilization tanks, a tank in the recycle
line would give the shorter hydraulic  residence time, which
would indicate a higher biota viability.  Having the tank
located in the waste line would produce a more stabilized
sludge, possibly aiding in bio-flocculation.

If the post-treatment step of chemical flocculation is used,
another alternative in F/M control is  possible.  If the sludge
from the floe-settler is viable, it may be used as the source
of additional recycle in periods of high loadings.  It has
also been shown that both the treatment efficiency and the
compactability of bulking sludge are improved significantly
with the addition of aluminum hydroxide to the mixed liquor
(Hsu and Pipes, 1973).
                             150
-------
Two possible sources of the feed sample to be used for
F/M control are shown in Figure 60.   The location used
for the experimental work in this study was in the feed
line to the aeration basin (see Section V).  Sampling from
this location allowed easy proportional control.

If the feed sample for F/M control is taken before the
equalization tank, F/M control will be more anticipatory
in nature with very short F/M response times.  The control
system could then include a mini-computer which would be
programmed to calculate the hydraulic effect that the equal-
ization tank will have on the feed flow and composition and
would affect F/M control on this anticipatory basis.  Hence,
extra sludge recycle could begin before the higher loadings
affect the aerated biomass.

Another available control system that needs to be incorporated.
into the plant design is an aeration-basin oxygenation sys-
tem.  Besides optimizing oxygen allocations, the system should
assure that proper agitation and micro-turbulence occurs so
that the various mass transfer processes can be optimized
(Kalinske, 1971).  The supply of oxygen to the stabilization
tank would also be controlled.

Nutrients and pH control would be provided for those processes
requiring them.  Tertiary treatment is necessary for
colloidal and suspended solids removal from the effluent.
Turbidity control would be provided for designs that employ
flocculation as the tertiary treatment.

OPTIMUM DESIGN OF AN AUTOMATED ACTIVATED SLUDGE PLANT
The design of the aeration basin volume needed for a specified
treatment efficiency is greatly affected by the incorporation
of the F/M control system.
                             151
-------
The choice of a steady-state model and the determination of
the kinetic coefficients and other parameters pertinent to
the chosen model are necessary in determining the aeration
basin volume.  A continuous pilot system is recommended for
determining this data.

The steady-state model may then be used to calculate the
required volume of the aeration basin as a function of other
design variables.  For examples a computer program using
the Monod model steady-state calculations (completely mixed
reactor) is presented in Appendix D and some of the design
relationships for the fresh water, propylene glycol system
are illustrated in Figure 61.  The sludge compaction data
(SVI) and the assumed recycle sudge concentration (Xr) are
obtained from the pilot study.  The treatment must be at an
F/M within acceptable SVI limits.  The aeration basin volume
(the hydraulic residence time multiplied by the influent flow
rate) is then a function of the recycle ratio.

The steady-state program also predicts the concentration of
microorganisms in the aeration basin and the cell production
rate, which at steady state is set equal to the wastage rate.

The aerated basin design should include evaluation of a
transient-state model of the system to determine the effects
that the suspected operational variations in loading will
have on the process.  The transient model permits optimum
design of the F/M control system, both in terms of control
action and stabilization tank volume.  System response times
can be determined to evaluate the adequacy of a given design.

The design  should incorporate mixing and dispersion parameters
obtained from actual equipment in order to insure that the
residence time distribution in the constructed system will be
                            152
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                          153
-------
the same as was assumed for the designed system (Irvine,
et al., 1973).  This may entail further transient-state
modeling to consider the possibility of a combination of
two or more biological reactors.

The final design of the aeration basin volume is dependent
on an economic evaluation of the alternative systems.  Items
to be considered include the reactor capital cost,  recycle
pumping costs, aeration and mixing costs, and control systems
costs.  The F/M ratio control costs include the stabilization
tank capital and the cost of aeration.  Benefits of stabiliza-
tion, such as decreased sludge handling costs because of
sludge digestion, must be taken into account.  The  benefits
of increased process removals must also be weighed.

It is clear that the availability of developed control systems
and of sufficiently accurate predictive modules will enable
more efficient, more economic, and more controllable activated
sludge systems to be built and to be operated at more closely
regulated effluent limits.  Sophisticated plants will require
more sophisticated operation.

Future plant designs will have to incorporate the best avail-
able technology.  Future plant operation will have  to reflect
the increased level of technology.  Both design and operation
depend upon the availability of sensors and the instrumenta-
tion necessary to use the sensed data to control the processes,
-------
                        SECTION XI

                        REFERENCES


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Andrews, John F.  1971.  Kinetic Models of Biological Waste
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American Public Health Association.   1971.  Standard Methods
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Arthur, R. M.  1964.  An Automated BOD Respirometer.  Purdue
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Banerji, S. K., B. D. Bracken, and B. M. Garg.  1968.  Effect
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-------
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-------
Ottengraf, S. P. P., and K. Rietema.  1969.  The Influence of
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                             158
-------
Stack, V. T., Jr.  1957.   Toxicity of Alpha, Beta-Unsaturated
Carbonyl Compounds to Microorganisms.  Ind. and Eng. Chem.
49:913-917.

Storer, F. F., and A. F.  Gaudy, Jr.  1969-  Computational
Analysis of Transient Response to Quantitative Shock Loadings
of Heterogeneous Populations in Continuous Culture.  Eng. Sci.
and Tech. 3(2) :143-149.

Stumm, Werner, and James  J. Morgan.  1962.  Chemical Aspects of
Coagulation.  JAWWA 5*1:971.

Stumm, Werner, and Charles R. D'Melia.  1968.  Stoichiometry
of Coagulation.   JAWWA 60:514.

Tenney, Mark W., and Werner Stumm.  1965.  Chemical Flocculation
of Microorganisms in Biological Waste Treatment.  JWPCF 10:1370-
1387.

Tool, H. R.  1967.  Manometric Measurement of the Biochemical
Oxygen Demand.  Water Sew. Works J. 114:211-218.

Tracy, Kenneth D., and Thomas Keinath.  1973.  Dynamic Model
for Thickening of Activated Sludge.  Presented at the 74th
National Meeting AIChE in New Orleans, Lousiana, March 11-15.

Wellens, V. H.,  and R. Zahn.  1971.  Untersuchungen iiber die
Toxizitatsbestimmung van Abwassern und Absasserinhaltstoffen
nach der Dehydrogenasen-aktivitat (TTC-method) Chemiker-
Zeitung 95:472-478.

Zeitoun, M. A.,^W. F. Mcllhenny, C. A. Roorda, J. C. Williams,
R. W. Murray, and W. D. Spears.  1971.  Treatment of Waste
Water from the Production of Polyhydric Organics.  U.S. Environ-
mental Protection Agency, Water Quality Office, Water Pollution
Cont. Res. Series 12020.
                             159
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                       SECTION XII
                   LIST OF INVENTIONS

The following inventions are disclosed herein to the United
States Government.

1.   Biological Inhibitor Detector
The invention concerns the design and automation of a measure-
ment cycle to detect the presence of toxic or inhibitory mater-
ials in waste water fed to a biological process.  The measure-
ment cycle is based on measuring the dissolved oxygen in a
controlled biological reactor as a standard sample, a waste
water feed sample, and another standard sample are consecu-
tively added to the reactor.  A toxicity index or activity
ratio is calculated by comparing the oxygen uptake of the two
standard samples before and after the bacteria sample has been
exposed to the test sample.  The invented measurement cycle is
automated for repetitive monitoring of streams fed to a bio-
logical exidation process and can be used as a feed-forward
control to divert a toxic feed before the loss or inhibition
of the acclimated biomass.

2.  Sampling System for a Homogenizable Solid-Liquid Mixture
Solid-liquid mixtures, such as an acclimated bacteria in an
activated sludge aeration tank containing 2000 to 4000 mg/1
suspended solids, are diluted as necessary and homogenized
with a high-speed mixer.  The homogenized sample then enters
a stand pipe to be de-aerated, then flows by gravity to the
sample injection valve of a monitoring instrument, and into
the second leg of the U-shaped stand pipe.  This flow flushes
the sample valve, and upon injection of the homogenized sample
all of the solenoid valves on the U-shaped stand pipe are
de-energized to drain the excess sample.  This restores the
flow of a cobinuous sample of a clear waste water, e.g.
the feed through the system, thus cleaning the lines from
any residual from the batch sample.
                           160
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                        SECTION XIII
                          GLOSSARY

ABBREVIATIONS
COD     chemical oxygen demand
DO      dissolved oxygen
JCU     Jackson candle turbidity units
MLTC    mixed liquor total carbon
MLVSS   mixed liquor volatile suspended solids
N:C     nitrogen to carbon ratio
SVI     sludge volume index
TC      total carbon
TCp     total carbon of the feed
TC]y[     total carbon of the mixed liquor
TCA     total carbon analyzer
TOD     total oxygen demand
TODr    total oxygen demand removed
VSS     volatile suspended solids

MATHEMATICAL SYMBOLS
A       waste calibration constant in equation 10
B       waste calibration constant in equation 10
C       concentration of DO in a bacteria sample, mass/volume
Cs      saturation DO concentration in a bacteria sample,
        mass/volume
E       percent efficiency of substrate removal, 100 (S0-Si)/
        So
F       food concentration, mass/volume
F/M     food to microorganisms ratio or loading
(F/M)r  F/M "removed" or (S0-Si)/Xavg
k       substrate utilization kinetic constant—maximum
        rate of substrate utilization per unit weight of
        microorganisms, time"1
                              161
-------
kr      combined substrate biodegradation rate constant,
        volume/mas s • time
        microorganism decay coefficient, time"1
Ke      endogenous reaction rate constant , time"1
KLa     oxygen mass transfer coefficient,  time"1
Ks      half velocity coefficient, equal to the substrate
        concentration when the specific substrate utiliza-
        tion equals (1/2 )k, mass/volume
M       microorganism concentration, mass/volume
n       bio-settler efficiency, percent
Q       influent waste flow rate,  volume/time
R       recycle sludge flow rate,  volume/time
rr      oxygen uptake rate by microorganisms, mass/volume* time
S0      feed soluble organic substrate concentration,
        mass/volume
Si      soluble organic substrate  concentration in aeration
        basin, mass/volume
T       total bio-settler underflow rate,  volume/time
t       time
V       aeration basin volume
W       waste sludge flow rate, volume/time
Wmax    maximum waste flow rate, volume/time
X       concentration of microorganisms in aeration basin,
        mass/volume
Xavg    average microorganism concentration in aeration basin
        over a chosen time interval, mass/volume
Xe      effluent microorganism concentration, mass/volume
Xr      recycle microorganism concentration, mass/volume
X       growth yield kinetic coefficient,  mass microorganisms
        produced per mass of substrate utilized
Y       growth yield kinetic coefficient,  mass microorganisms
        produced per mass of substrate utilized
                             162
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                             SECTION XIV

                             APPENDICES


Appendix                                                    Page


A     Operation and Maintenance Manuals                     165

B     Calculations of Plant Performance                     175

C     Transient State Activated Sludge Computer
      Simulation                                            190

D     Steady-State Activated Sludge Computer Model          196
                                 163
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                         APPENDIX A
              OPERATION AND MAINTENANCE MANUALS

The automated activated sludge miniplant is operated
unattended but the instrumentation and control systems re-
quire certain routine maintenance and trouble shooting
practices that are detailed in this appendix.  The operational
procedures include some sampling collection and laboratory
analyses to check the control systems and assess the overall
performance of the process.

The details of the control systems applied to the operation
of the aeration basin are shown in Figure 12.  The automatic
shutdown system is detailed in Figure 62.  Operation and
maintenance of these systems are described under the approp-
riate subsection of this appendix.

START-UP PROCEDURE
The influent flow to the equalization tank was started a
day or two before plant start-up depending on the volume
and residence time in the equalization tank.   The stepwise
start-up procedurewas as follows:

1.  Prepare the required concentration of chemicals and fill
    the alum, caustic, acid, and nutrients tanks.  Turn the
    pov/er on to heat the furnaces of the total carbon and
    total oxygen demand analyzers.

2.  Add enough sludge to the aeration basin to obtain the
    desired mixed liquor suspended solids (MLSS) concentra-
    tion when the basin is full.  The source  of the sludge
    could be from the sludge recycle of a sewage treatment
    plant or a batch-acclimated culture previously prepared
-------
 2.   Adjusting the  set points  for  the  alum  and  caustic  flow
     rates
 3.   Checking the liquid level of  the  alum  and  caustic  tanks

 The surface scatter turbidimeter  required  infrequent replace-
 ment of the electrical fuse,  the  lamp,  and the meter relay
 lamp.

 The Total Oxygen Demand Analyzer, monitoring the  TOD in  the
 feed and effluents required the following  routine maintenance:

 1.   Changing filters to sampling  system once a week
 2.   Checking rubber tubing in the peristaltic  pumps
 3.   Checking leaks or plugging in sampling lines
 4.   Checking the rotary sampling  valve  for leaks  or plugging
 5.   Checking the stream  selector for proper operation sequence
 6.   Adjusting the  nitrogen flow and electrolyte level  in
     the oxygen detector of the instrument
 7-   Adjusting the  level in the instrument  scrubber, the
     detector current, and the automatic zero of the recorder
     for proper range of the signal
 8.   Replacing the  scrubbing and detector cell  solutions  once
     a week
 9-   Adjusting sample valve 0-ring clearance as necessary
10.   Replacing furnace tube with freshly prepared  catalyst
     at intervals found necessary  by the operation
11.   Changing the nitrogen cylinder when empty
12.   Replacing burned out light bulbs
                                165
-------
in drums by a fill-and-draw procedure.  Open the air
supply valve and adjust the air rotaraeters to the re-
quired flow so as to maintain 2 to 3 mg/1 dissolved
oxygen in the aeration basin.  A yellow springs oxygen
meter is used to measure the DO in the aeration basin.

When the head in the equalization tank is enough to
prime the feed-recycle pump, open all valves in the
recycle loop.  Turn the pH control on bypass and press
the start switch.  When recycle has started, set the pH
at the control point midway between the upper and lower
shutdown limits.  Slowly close the ball valve on the
pump suction until five inches of mercury vacuum is
shown on the gauge.   Open the acid valve and turn the
pH controller to automatic to start the acid flow.
Observe the rotameter to check the acid flow and when
the pH, as recorded, is in control, turn the pH bypass
off.

Start the feed to the aeration basin by turning the
set point on the pneumatic proportional controller at
the panel.  This controller is calibrated for maximum
flow of one gpm and is usually started at 0.5 gpm
depending on the concentrations of the influent and
MLSS in the aeration basin.

Check the temperature of the influent in the feed line as
it enters the aeration basin.  Control the temperature by
turning on one or several of the electrical heaters around
the feed line or diverting the feed through the cooling
tower to maintain the temperature required for the test
being conducted.
                        167
-------
As the overflow from the aeration basin fills about half
of the biosettler, start the sludge recycle pump.
The variable drive on the pump is adjusted to the desired
recycle flow rate.  The rate is checked at the inlet
to the aeration basin using a stopwatch and a one-liter
graduated cylinder.

Observe the biosettler as it overflows to the flocculator
and the last settling tank.  Control the overflow weirs
in the two settling tanks and remove the air trapped in
the lines to obtain a smooth gravity flow through the
flocculator and the last settling tank.  The total over-
flow from the biosettler is directed through the Hach
Surface Scattering Turbidimeter to the flocculator.

Put the Total Carbon Analyzer in service by turning on
the recorder switch, the timer switch, and the stream
selector switch.  Keep the stream selector switch on
Stream I (the feed) for a one cycle, then observe the
instrument and the sampling system operation through a
complete cycle.  The sampling system includes Stream II
(the bacteria sample) that is diluted, homogenized, and
pumped through to the instrument slide valve.

Check the nutrient pump for proper operation and flow.
The required flow rate of the nutrients  to obtain the
right ratio of organic carbon in the feed to the
nitrogen and phosphorus  in the nutrient solution  is
controlled by two variables.  One is the speed of the
nutrients pump that is adjusted manually.  The other is
the fraction of a  (30 seconds) cycle that the pump is
on.  This is automatically controlled by the feed total
carbon signal from the analyzer.
                          168
-------
10. Operate the plant with total recycle and no sludge waste,
    bypassing the F/M control system,  till the required
    steady-state concentration of MLVSS is reached.   Adjust
    the controller, at the panel, that receives the  F/M
    signal from the total carbon analyzer  to obtain the
    required flow rate of sludge waste.  This signal operates
    a three-way solenoid valve on the  sludge recycle line
    and opens it to the waste line for a fraction of a 60-
    second cycle.  The sludge waste flow rate is measured
    in a graduated cylinder at the wasted sludge drum.  The
    maximum flow of wasted sludge is controlled by a limit
    switch that should be set so the sludge wasted during
    a 24-hour period would not exceed  a precalculated
    maximum value.  This limit  switch guards against a
    washout of the bacteria in the event that the F/M
    control system fails.

11. Put the Hach Surface Scatter Turbidimeter in service by
    switching it on  and setting the range to record the
    turbidity of the biosettler overflow.  Open the  manual
    valves on the alum and caustic tanks, and start  the
    flocculator stirrer.  The flow of  the alum solution is
    controlled at the panel by adjusting the set point
    depending on the optimum dosage found by experiment.  The
    flow of the caustic  solution is controlled by setting
    the pH control system at the predetermined optimum pH
    (about 6.5).

12. Calibrate the Total Oxygen Demand  Analyzer using standard
    solutions setting the instrument zero at 5-0 on  the
    sensitivity dial.  Put the stream  selector in service by
    starting the sampling pumps and adjusting the stream
                             169
-------
    selector switches 1, 2, and 3.   Check the flow of all
    samples and the signals en the  recorder through one
    complete cycle.  Readjust the sensitivity of the instru-
    ment to obtain a feed TOD signal around 75 percent of
    chart.

PLANT OPERATION, SAMPLING, AND ANALYSES
The operation of the automated miniplant was limited to
daily and weekly routine checks of  the control systems.
The extent  of sampling and analyses depended on the experi-
mental design and the data required.  The objective of the
fresh water and salt water glycol feed tests was to evaluate
the control systems.  Accordingly,  data collection was limited
to those data necessary for this evaluation.

The influent pH-controller had a limit switch on high and
low pH that closed the feed valve to the aeration basin if
the pH got  out of control and opened it when the pH control
was regained.  The control points were set at 5.5 and 9.0
with the set point at an intermediate value of 7.8-  The
pH electrodes were checked with buffer solutions as frequently
as needed.   A twice weekly check was found to be sufficient.

The nutrient control system was checked by running daily
analysis of ammonia in the final effluent from the plant.
The dial setting on the nutrient pump was then readjusted
to minimize the residual ammonia in the effluent.  A daily
check of the amount of nutrients used was made by reading
the calibrated sight glass on the nutrients tank, where
each 3 mm was equal to one liter of solution.  Using a
nutrient solution of 1 percent ammonia and 0.1 percent phos-
phoric acid, normal operation of the plant consumed one tank
of 55 gallons every two weeks of operation.
                             170
-------
The food to microorganisms (F/M) control system required
daily attention and service.   The wasted sludge, collected
in a 55 gallon drum, was measured and samples for analysis
every 24 hours of operation.   The sludge recycle rate was
measured manually every day to check the performance of
the recycle pump and to verify the recycle and waste sludge
flow rates.  The sampling system to the total carbon analyzer
was cleaned daily to prevent  any solids accumulation in the
lines that could result in irregular analyses or even plug-
ging of the sample flow.

The flocculation control system required very little
attention.  If the turbidity  readings were recorded, the
24-hour results were obtained; otherwise, the indicator of
the instrument should be read and entered in the data book
daily.

The Total Oxygen Demand Analyzer, monitoring the feed and
effluents, had no controls that affected plant operation.
Calibration curves for this instrument and the Total Carbon
Analyzer were run once a week.  Daily, one standard was run
to check of the two instruments, and the span control was
reset if necessary.

Laboratory analyses were made daily as follows:

1.  Feed grab sample:  propylene glycol by VPC
2.  Aeration basin mixed liquor:  sludge volume index (SVI),
    Mixed liquor suspended solids (MLSS), and volatile
    suspended solids (MLVSS)
3.  Biosettler overflow composite:  MLSS, MLVSS, TOC,
    and ammonia
                             171
-------
4.  Final settler overflow composite:   MLSS,  MLVSS,  and
    TOC
5.  Sludge waste:  MLSS and MLVSS

A plant data sheet was posted daily showing the data
recorded by the instruments and the results of the labora-
tory analyses.

MAINTENANCE OF  INSTRUMENTS AND CONTROLS
The instruments used for control and monitoring the  oper-
ating parameters of the activated sludge miniplant required
strict routine  maintenance for good operation.  Sample
preparation and pretreatment was emphasized to minimize
downtime for non-routine maintenance.   Regular routine
maintenance practices for recorders and support equipment
are not covered in this text.

The influent pH-control system required the following routine
and non-routine maintenance:

1.  Inspecting and cleaning the pH-electrodes (once  a week)
2.  Calibration against high and low pH-buffer solutions
    (once a week)
3.  Checking the acid line and rotameter for any leaks (daily)
4.  Replacing defective electrodes (when necessary)
5.  Cleaning acid flow rotameter (once a month)

The Total Carbon Analyzer (Ionics Model 1212) used to
measure the TC in the feed and mixed liquor of the aeration
basin required daily checking of the sampling system besides
the following routine maintenance:
                             172
-------
1.  Checking the liquid level of the liquid gas separator
2.  Checking the gas flov; to the infrared analyzer
3.  Adjusting wattmeter for correct operating wattage
    (185 watts)
4.  Inspecting reaction chamber for oven heat
5.  Checking the sample slide valve for leaks
6.  Adjusting zero on the infrared analyzer
7.  Back-flushing of sample flow to analyzer (once every
    two days)
8.  Calibrating with one or two standards (daily)
9.  Running all of the calibration curve (once a week)
10. Replacing nitrogen cylinder when empty
11. Replacing distilled water for water rinse (once a week)

In cases of out-of-control instrument response the main
defective parts to check are:

1.  Sample injection valve - which may have to be dis-
    assembled, cleaned, and reground to prevent leaking.

2.  Reaction tube - which may have to be removed, and the
    catalyst and the injection tube cleaned.

3.  Infrared detector - which may require removal and clean-
    ing of the sample cell.

The flocculatlon control system, comprising the turbidimeter
and the alum and caustic addition, required very little
special maintenance:

1.  Draining the turbidimeter once a day to clean the solids
    accumulated at the surface.
                             173
-------
                         APPENDIX B

              CALCULATIONS OP PLANT PERFORMANCE

A computer program was developed to facilitate routine
data handling and to calculate parameters which describe
the miniplant performance.  The program was written in
Fortran IV language and a Xerox Sigma 5 batch time-sharing
monitor was used.

A sample data input form (#12) and the resulting computer
printout displaying the summary of plant performance are
presented.  The logic of the program is also given (#13 and
Definitions of symbols in the program can easily be related to
the data input sheet and the corresponding READ statements
and to the output printout and the corresponding WRITE state-
ments.  Material balances and parameters calculated have been
described in the literature (Zeitoun, et. al., 1971).
-------
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-------
                    TABLE  13.   COMPUTER PROGRAM FOR
                   CALCULATIONS OF PLANT PERFORMANCE
  1.000   1070  FORMAT<2X,*ECHO CHECK  ON  INPUT DATA'/)
  2.000  " 990  FORMAT<65X,'PAGE 3* //26X, • **SYSTEMS PERFORMANCE**'///
  3.000      Cl IX, 'LOADING ',14X,' REMOVAL' /,28X, 'THRU CLARIFIER* ,9X,
  4.000      C'THRU FLOCCULATOR' )
  5.000 _ 989   FQRMAT< 7X, » LBS/DAY  LBS/DAY    LBS/DAY  LBS/DAY',
  STOOU      C~»~~Wr  CFS7T5SY   DBS /DAY  %W*1           ~"
  7.000    988  FORMAT ( 1 5X, • /LBMLVSS' , 1 2X, • /LBMLVSS* , 16X, • /LBMLVSS' /1X,
  8TOOO      C»TC^73X7l^.273X7F5.3T5XTfT727^X7F5T3y2XyFSVl71X7F7.27
  9.000      CF5.3,2X,F5.1 >
  10.000   ~987  FORMAT* 30X, 'CARBON BALANCE1 /28X, 'ON AERATION I BASIN'/
  i 1.000      C16X, 'CARBON IN    CARBON  OUT  CARBON TO C02*>
~ T2 .uou — sus — FTjRMsrrnrxTTnra^yiJffY --- -LBSTDHY ------ CBSTTFAY— wr^Ti 7x7
  13.000      CF7.2,5X,F7.2,4X,F7.2,2X,F4.1/)
  14.000    985^ FORMAT(1X/,27X,' AERATOR PERFORMANCE' /34X7' AND* A
  15.000      C22Xj 'AERATION BASIN OXYGEN BALANCE' //I IX, • 02 SUPPLIED*,
  16.000      C8X,'02 TRANSFERED       EFFICIENCY' / 11X,'CFM    LB/HR»T"~"
  17.000      C7X,'KLA  CS*  LB/HR           %')   _ _      _
"~T8VODa    9aT4""FORMATT9X7F5".27T
  19.000    983  FORMAT<9X, '02 CONSUMED' ,25X, ' 02 CONSUMED'/
  20.000      C2X, 'BASED ON CARBON BALANCE         BASED ON 02=',
  21.000      C'A(L3S TOD REM/DAY) +3(VSS) ' 2X, • LBS/DAY   LBS/LB TC ' ,
  22.000      C'  REM', I 5X, • LBS/DAY     LBS/LB TC"REM'")
  23.000    982  FORMAT(2X,F5.2,9X,F5.2)
                                           * F ST
 25.000    949  FORMAT(6X,'FLOW   LBS/HR' ,4X,F8. 1 , 1 9X,F8 . 1 /1^2X,
 26.000       C'Gf9M',10X,F6.2,21X,F6.2)
 27.000    948  FORMAT<6X,'PH',18X,F4.1,23X,F4.1/6X, «TOC    PPM',
 23.000       C10X,F5. 1/22X,F5. 1/1 2X,' LBS/DAY' 5X,F6. 1,21 X,F6.1)
 29.000    946 FORMAT<65X,'PAGE  2' //23X, ' EQUILIZATION BASIN CONTENTS'//
 30YIKKJ - C^OX7^TE^P^Y5X7~'i:raTJTiy~I^^
 31.000       C4X,'DEG C ', 1 OX, ' GALLONS' , 1 OX, 'HRS ')
 32.000    945 FORMAT< 12X,F4.1,4X,F5.179X,F7.1,10X,F5.1//>
 33.000    899 FORMAT <29X,'PH  CONTROL SYSTEM* //4X, • EQUILI ZATION  BAS',
 34.000       C« IN' Y5X, 'AERATION BASIN INFLUENT     HCL ADDITION'/
 35,000       C12X,'PH', 13X,'HIGH PH   LOW PH  AVG PH ' ,9X, 'ML/MIN' /
 3Gr. 0 00       rrOX77^TT7r4X7F^VlV6X7F^VT7^X7F^VrV9^7F^71 775          ~~
 37.000    848 FORMATC26X, 'NUTRIENT ADDITION SYSTEM' //, IX,
 33.000       C 'FLOW FROM         CARBON' ,9X, • NUTRIENT ' ,14X, 'RATIOS' /
 39.000       C1X,'EQUILIZATION    FROM EQUILZ .', 3X, 'FLOW    COMPOSITION
 40.000       C'N'/1X,'    LB/HR'J9X,'LB/HR',6X,'LB/HR',3X,*%NH3»,4X,
 4^1 . 000 _ C_' %P',5X, 'C:N*,9X,* C t P* /3X,F7.2,5X, F8 . 3 ,6X,F5«3,2 X , F 5j^2^
 42"70(JG       C~3X,F4.2,2X,' 100": ',F4. l,4X7"*TOO: *,F47T77)
 43.000    8^5 FORMAT<23X,'F/M CONTROL SYSTEM* //2X, 'WASTE FROM EQUIL',
 44.000       C'IZATION    AERATION BASIN    RECYCLE  SLUDGE
 45.000       C/7X,' CONCENTRATION          MLVSS    TC


                                    176
-------
     Table 13 (continued)  .  COMPUTER PROGRAM FOR CALCULATIONS OP
                            PLANT  PEEFORMANCE -     -          -
 46.000      C'FLOW    MLVSS     FLOW'/3X,'GPM   PPM PG   PPM TC•,
 47.000      C'        PPM     PPM        GPM    PPM',6X,'GPM*/2X,
 48.000      CF4.2,3X,F6.1,4X,F5.1,6X,F6. 1 ,2X,F6.i /4X,F4 72*2X.F6'.Ij
 49.000      CF4.2/)
 50.000844"FORMAT<22X,'FOOD/MICROORGANISM RATIO (LOADING)'/~
 51.000      CIX,'FEED PG/',6X,•FEED TC/',6X,'LBS TC/DAY/»,5X,
 52.000      C »LBS TC/DAY/LB MLVSS»/rX7'AER~MLVSS•,5X,'AER TC*78X,
 53.000      C'LBS MLVSS',4X,'BASED ON MLVSS=»TC BUGS( 1 1 3/60) */1X,F4. 2,
"54TOaO	CTOX,F4.2,10X,F4.2,16X,F4.2//J
 55.000   795 FORMAT<26X,'AERATION BASIN CONTENTS'//1X,'TEMP  PH*,6X,

 57.000      C' AGE*/1X,*DEG C*,10X,*LBS*,6X,'GALLS    PPM    LBS',
 5870OO	CT»	PPM     LHS      DAYS1^~~
 59.000   794 |.-QRMATC1X,F5.1,1X,F4.1,3X,F8.1,2X,F7.I,2X,F6.I,
 £* /\"*"rtrt rt "" * **" "-1""™ ~^ f~f v1 J' i? £ ' yy"""«9l'r f«i^IA^r3»A^ OA > r O • c* ^
 61.000  _193_ F/jRMAT_( l x* ^x *x*f RECYCL?_   _   ^^RPf _J?_ME BASE^_ °J1* *	
 627660C9X,'SLUDGE   TC REM RATE  TOD R.R.'/2X>'RATIO      IN',      ^
 63.000   	C'FLUENT     INFLUENT* RECYCLED	VOLUME   CONSTANT  __C^_*_  __
 64.000      C' ONSTANT*~)                                                   E
 65.000   792 FORMAT<4X,*%',9X,'HRS»,14X,'HRS',9X,'INDEX*,6X,*1/MRS*,
67.000    791  FORMAT<_IX>F5. 1 *6X,F5. 2, 1 2X,
68.1000^       C//)
69.000    745 FORMAT <30X,» SETTLER DATA'//
70VOOO       C20X, TOVERFLOW» , IOX, » INFLOW
71.000       C • RATE ' , IPX* 'HOLDUP  T I ME
                                             .2>9X>F5.
                                                BOTTOMS
                                                            SLUDGE~r722X
                                            RATE • *6Xj,* DEPTH * / 1 5X,
 T2TTJOD
 73.000
 75.000
 76 .000
 77.000
          695 FORMATUX,•BIO-SETTLER',5X,F6.1,5X,F4.2,5X,F6.2,9X,F4.2,

             CF4.2,6X,F5.1///)
          696 FORMATT25X, »FLOCCULATI ON CONTROT. "SYSTEM* /7T7X7
             C'CAUSTIC     PH         ALUM',I OX,'OVERFLOW*/18X,
 78.UOO      C"'USUAaE*,I4X,fUSUAGE*,«X,i TURBIDITY*/I 9X7
 79.000      C'LB/HR',1 OX,•LB/HR',2X,•ML/MIN* *8X,•JCU*/I8X,F6.4,4X,
 80.000CF4.1,rX,F6«4,F6.1,9X/F4.17)
 81.000 	697_FORMAT<_1 IX,'FLOCCULATOR INFLUENT     FLOC-SETTLER OVER',
 82.000      C'FLOW      %  REMOVED•/18X7* LB/DAY* ,20X,* LB/DAY'76X7*TC»7"~
 83.000      C11X,F5.3,21X,F5.3,14X,F5.1/6X,*TOD*,10X,F5.3,21X,F5.3,
85.000
86.000
87.000
88.000
89 .00
             Cl4X,F5.1/>                                       ~
          645 FORMAT C1X,^/,27X, 'MICROORGANISM BAJLANCE ' /29X,
             C'ON AERATION BASIN' /)
          644 FORMATCIX, 'AVERAGE', 14X, 'VOLATILE SOLIDS FORMEp*,,
             C12X, 'RATIOS' /2X,IMLVSS',7X,» IN  BASIN  WASTAGE*,
             C   CLAR  QVERF LW   TOTAL     LBS  VSS/DAY/' /I X, 'PPM
90.000
91 •000^
92.000"
93*000_
947660"
95.000
               __             __                                 ____
             C ' S • , 3X, ' LBS/DAY' , 3X, • LBS/DAY' , 5X, • LBS/DAY ' ,4X, *LBS>DAY« ,
              3X,'MLVSS  TOC REM* )
          643 FORMAT
-------
      Table 13 (continued).  COMPUTER  PROGRAM FOR CALCULATIONS OF
                            PLANT  PERFORMANCE
   96.000   300 FORMAT < 65X7* PAGE" 1V/7T5X,
   97.000      C'GLYCOL WASTE TREATMENT MINIPLANT A-1656'///
   98.000      C14X, 'SUMMARY OF PLANT*,
   99.000      C'  PERFORMANCE FOR », 12, IX, 12, IX, I2///25X, • STREAM' ,
  100.000      C*  CHARACTERISTICS'/)
  lOi.QOO   299 FORMAT (13X, 'WASTE TO BASIN ___ 81 0_-SETTLE_R RECYCLE __ WASTE
  102.000      C ' -SETTLER' /14X, 'BASIN   EFFLUENT  OVERFLOW     SLU ' ,
  103.000      C'DGE   SLUDGE OVERFLOW'/)
  104.000   298 FORMAT (IX, 'FLOW  LB/HR • ,F7. 1 , IX, F8. 1 , 1X,F8, I ,2X,FJ3 . 1 ,
  105.000       C1X,F7.1,2X,F8.1)
  106.000   297 FORMAT(9X,'GPM    ',F5.2,3X>F6.2,3X,F6.2,4X,F6.2,2X,
  107.000       CF6.2,4X,F6.2)
  108.000   296 FORMAT UX, ' TC      PPM    • j LF5 . !_*_! 3X,F5 .1
  T697000~ 295"FOWMAtC6X,iLB/DAY •,F8.2,
  110.000   294  FORMAT < IX, 'REMOVAL  % • ,22X,F5. 1 ,23X,F5. 1 )
  IT 1 . 0<30~   293  FORMAT < 1 X, • TOD     PPM  '/F 7.1 * 1 2X, F6 . 1 , 22X, F6 . I )
  112.000   292  FORMAT <6X,'LB/DAY * ,F8.2> 1 OX,F8 .2,20X,F8.2)
  113.000   290  FORMAT<1X,'PH'.,13X,F4.1.»42X,F4.1)
  114.000   291  FORMAT C IX ^ '.REMOVAL  X ' ,22X,F5. 1 j.23X>F5 . U
  11 5.000   289  FORMAT < : 1 X> • TEMP  DEG C V, 3X, F5 . 1 ,4X,F5 . lV~4X* F5 • I * 23X,
  U6.000 _   CF5.D  __^        _  _            ___
  1 17.000   288  FORMAT < 1X/'PG',6X> 'PPM' >3X,F5. i74X,F5. U4X,F5. 1 *23X>
  118.000 __ ^P"5*1^  _______________            __
  TT9700Cr~~2~g7  F>JRMAT( 1 X, «~MLSS    PPM' > \ IX, F6. I ,3X,Fr6TT73X,F7. 1,TX,
         ____           __^
  121 .000    286  FORMAT<6X, 'LB/DAY' , 1 2X,F6.2, 3X,F6.2,3X,F7.2, iX,F7.2,
2  122.000      C3X,F6.1)
  123.000    285  FORMATOX,'MLVS    PPM' , 11X,F6. I ,3X,F6 . 1 , 3X,F7. 1 , IX,
  124.000      CF7.1,4X,F6.1)
  125.000    284  FORMATC6X,'LB/DAY',12X,F6.2,3X,F6.2,3X,F7.2,IX,F7.2,3X,
  126^000	CF6. \2	   			
  127.000    283  FORMATCIX,'RES     MRS',4X,F5.2,4X,F5.2,4X,F5.2,23X,
  128.000      CF5.2)                          		        _____
  1297000    282  FORMAT<1X,'NACL     %•,5X,F4.1)
  130.000    281  FORMAT<1X,'NAOH     %',5X,F5.2)
  131.000    278~TORMAT(IX,'ALUM  LB/HR' , SIX, F5. 3)
  132.000    277  FORMATC1X, 'BASE  LB/HR' , SIX, F5^j3)
  133.1300    276  FORMAT
                                   178
-------
     Table  13 (continued).   COMPUTER PROGRAM FOR CALCULATIONS  OF
                            PLANT PERFORMANCE
 143.000   494 FORMATX6F)
 144.00^   44J3 FORMATOrF)              		
 145.000   447 FORMAT POND  FROM POND*)
 146.000	446^ FORh!ATUX,«TOD',2X,F7.2,3X,F5.3,5X.sF7.2,3X,F5.3,2X,F5.1,
 147.000      C3X,F5.2,4XVF5.3,2X,F5.1///)
 148.000   442 FORMATOX,' SLUDGE AQEt * >F6.2> 'MRS. '/) 	
 149.000       READ<1,502>MTH,IDAY,
 1 50.000       READ< 1 >500)HEWFLV>yOLCP.»DENSj ,TOC1 *OH1 *CHL1 ,PH1 *TCP2	
 T5UOOO       REXDCPWFLW.» TINBAS*TOC2,DENS2, PJi2^HA8H,PHABL>TAB,
 TSTTOTOO"CSMETEH
 154.000       READC1,497)VOLAB,SS4,VSS4^PDVSS4>TOC^>DENS4,PHAB
 T55.000	READ(l,496>TOC5>SS5,VSS5,DENS5>SLDEPii,SLDEPF>TCL*PH5
 156.000       READ<1,495)FALUM,FNAOH,PHFL*TURBT2,TOC7,DENS7.,SS7,VSS71,
 1577000
 158.000       READ
 188.000       ABVFLW=CPVFLW+CSVFLW
 190.000       RX=RR/100.0  __


                                   179
-------
    Table 13 (continued ).
                           COMPUTER PROGRAM FOR CALCULATIONS OP
                           PLANT  PERFORMANCE
 191.000
 192.000^
 193.000
 194.000
 195.000
 196.000
T97.00O
 198.000
 I99TUOO"
 200.000
 2017000
 202.000
                      	            (1.0+RX)
               TOCFI=ABWFLW*TOCI*24.O/1.OE6
               CODI = (COD2-KRX*COD4))/( 1 .0+RX)
               CODFI=ABWFLW*CODI*24.071.OE6
               WSS6=
               V5STB= CW55TB* F • OE6 57 CABWFl.W*Z4VO )
               CVFLWa
204.000
205VOOTJ
206 . 000
2077000
2 08.000
                                       . OE6
               WVSS4=(CWFLW*VSS4*24.0)/1 .OE6
               RSTAB=< VOT-AB/ < ABVFLW*60 . 0 >T
               RSTABS»< VOLAB/ < CPVFLW*60 . 0 ) )
               WTAB=WLAB^*8 . 34*DENS4~762.~5
               S S A B a(WTAB*S S4)/l . OE6
 210.000
 211.606 C
 212.000
 213.000
 214. OOP
~2 1 5701TO
               AIRFLW=j/6^J  _  ____ ___ ___________
 2 27.000     "~~RSTC=50 . / < CVFLW*60T)
 228.000_      TOCRC=TOCF2-TOCF5                           __
 229.000       TOCPRC=(TOCRC/TOCF2)*100.0
 230.000       BOTFLV^CSVFjLW+CVSLUG
 235.000 C     FLOCCULATOR
 232 .pj)0_j; __ CHANGE ML/MIN TO LB/HR USING ALUM DENSITY 4Q.»OOOMG/LITER
 233.000       FALUMW"=FALUM
 234.000 ________ FALUM=FALyM*60.*40./(454.*1000. ) ____________ ________________      __
 235.000       TEWFLW=»FWFLW
 236.000 _____ TEVFLWa'TEWFLWjtt62.5/<8.34*DENS7*60.0)         ______
 237.000  ~ ~ ~  toCFT=(fEWFLW*TOC7*24. )7l.OE6
 238.000       WSS7=(TEWFLW*SS7*24.0)/1 .OE6
                                   180
-------
    Table  13 (continued).   COMPUTER PROGRAM FOR CALCULATIONS  OP
    	~    PLANT PERFORMANCE
 239.000       WSS7=*/1 . OE6
 240.000 	    FVSLUQ=(FWSLUG*62.5)/<8.34*DENS8*60.>
 241.000       FOVFLW3/1.0E6
 249.000       CWVSS»WSVSS6+WVSS5
 250.000       DWVSS»
 251.000       AVWVSSs/1.0E6
 252.000^       SLDAGE=AVWVSS/(WVSS5+WSVSS6)
 253.000       TOC2L=TOCF2/AVWVSS
 254^000 ____ RTOCCa
 258.000       RSLUG 1 =DWVSS/AVWVSS
 259.00"0       RSLUG2=DWSS7*1 00.~ ~
278.000	REMVTDaC 500)HEVFLW,VOLCP*DENS1,TOC1*OH1,CHL1*PH1,TCP2
283.00CT       WRITEX: 3^4991 SV3/PERNH37PERPHO>FO^01THCLFLWyTUR8TI
284.000       WRITE(3,498)CPVFLW,TINBAS>TOC2,DENS2>PH2>PHABH>PHABL*
                                   181
-------
    Table  13 (continued).
                           COMPUTER PROGRAM FOR  CALCULATIONS OF
                           PLANT PERFORMANCE
 285.000
 286.000
             CTA8,SMETER
              V/RITE<3*497WOLAB*SS4,VSS4,PDVSS4,TOC4,DENS4,,PHAB
 288.000
 289.000
 290.000
~29iVOOO
 292.000
              WRITEC 3*^195 >FALUMW,FNAOH,PHFL*TURBT2>TOC7*DENS7,SS7,
             CVSS7,TFL~
              VRITE< 3 , 494) SCSVFL, SCVSLU, SS6^VSS6,DENS6> WFLV
              WRIT EC 3T4W>COD2^'J^
              CALL PA6E<3>
293.000
294.000
               WRITE<3,300)MTH,1DAY^IYR
               WRITEC3,299>
 295.000
 296.000
 297.000
 298.000
              WRITE<3,298)CPWFLW,ABWFLW,FWFLV,CSWFLW,CWSLUG,TEWFLW
              WRlfE(3*296)tOC2,tOC5,tOC7
              WRITE<3,295)TQCF2*TOCF5jTOCF7
 300.000
 302.000
 303.000
 304.000
~3 057000
 306.000
 307.000
 308.000
"3097OOO
 310.000
              WRITE<3*293)COD2>COD4,COD6       ___
              WRITEr3,292)CODF2VCODF4,CODF6          ~"~
              WRITE<3^291 )CODPRC,CODPRF
              WRITEDENS2,D£NS4,DENS5,D£NS6>DENS67DEN57
              WRITE<3>290)PH2,PHFL
 31 1 .OOO
 312.000
 314.000
 31T. 000
 316.000
 317. ODD"
 318.000
 31 9. 000
 320.000
 3 21. 000
 322.000
 323.000
 324.000
 325.~000
 326.000
 327.000
 328.000
 329. OOO
 330.000
              WRITE< 3*289 )TINBAS>TAB,TCL*TFL
              WRITEC3,288)PG2*PGAB,PG47PG6
              WRITE(3>287)SS4,SS5,SS6,SS6,SS7
              WRITET3T256)^S54; WSS57V5S6TW 55^6^557
              WRITE<3*285)VSS4>VSS5>VSS6,VSS6,VSS7
              WRlTEr37^84)WV554,WVS55*WVS567W5VS
              WRITEC3,283)RSTABS>RSTAB,RSTC*RSTF           ___
              WRITE<37282)CHL1
              WRITE<3*28l>OHl
              WRir£(3V278)FALUM
              WRITE<3,277)FNAOH _          _
              flH rTET3T276~TSinpr
              WRITE(3,275)SV3
              WRITE<3*745)
              yRITE<3,695>COVFLW,FWLW,RSTC,BOTFLV,SLDEPB,FOVFLW,
             CTEVFLWjrTlSTF^                    "~"    ~
              CALL PAGE<3)
              WRITEO,^^
             _WRITE<3J,945^
              WRITE (3, 795 >
              WRITE (3,794) TAB ^PHAB,WTAB,VOLAB,SS4,SSAB>VSS4,VSSAB,
             CSLDAGE
              WRITE<3,793)
              WRITEC3,792)                    ~~
              WRITEC3,791)RRJRSTABS,RSTAB,SVI4,RTOC,RCOD
                                  182
-------
      Table  13  (continued) .   COMPUTER PROGRAM FOR CALCULATIONS OP
                            PLANT PERFORMANCE

 331.000       WRITEC3,987>
 332.000       WRITE(3^986>CIN,COUT,DELTAC,PCC02
 333.000WRITEC37985)
 334.000	VRITE(3,984)AIRFLV
 335. OODWRTT£T37913r3>~
 336.000       WRITEC3*982)RATE02*R02TOC   	
 337.000       WRITE<3>645~)
 338.000       WRITE<3,644)
 339.000       WRI TEC 3*643 >AVVSS,AVWVSS,ABVSS,WSVSS6,WSS5,DWVSS,
 340.000 _ CRSLUG1*RSLU62
"341.000       CALL PAGE<3>
 342.000       WRITE(3,990)          _    _
               WRITET3>959~)         "
 344.000       WRITE(3^988^TOCF2>TOC2L*TOCRC>RTOCC>TOCPRC*TOCRF,RTOCF>
 346.000       WRITE<3,446>CODF2,COD2L>CODRC,RCODC,CODPRC,CODRF,RCODF,
 348.000 _   WRITERS, 899 )PH I, PHABH,PHABLjLPH2*HCLFLW
 349. 000"     "~WRITE< 3,848yCPWFLW,tOCF2H*PDNOT*PERNH37PERPHO, CN,CP
 350.000       WRITE<3,845 >CPVFLW,PG2,TOC2*VS^^TOC4^,CSVFLW^VSS6
 351.000       WRITE<3V844)RPGVS4yFDARTC,TOC2L,TOC2LC :~"
 352. 000 _ WR I TE ( 3,696)FNAOH
-------
  Table  14.   SUMMARY  OF PLANT PERFORMANCE	
              June  18,  1973
              Glycol Waste Treatment MIniplant
              A-1656

            STREAM CHARACTERISTICS
WASTE TO BASIN   BIO-SETTLER
 RECYCLE  WASTE  FLOC-SETTLER
""SLUDGE	SUJETGEr WERFLTW	
FLOW LB/HR
GPM
TC PPM
LB/DAY
REMOVAL X
TOD PPM 1
LB/DAY
REMOVAL %
DENS LB/FT3
PH
TURB JCU
TEMP DEG C
PG PPM
MLSS PPM
LB/DAY
MLVS PPM
LB/DAY
RES HRS
NACL Z
NAOH 2
ALUM LB/HR
BASE LB/HR
SVI
SV MLS-30MINS
249.9
.50
473.0
2.84
511.0
9.06
62.4
6.5
30.0
680.0

8.33
.0
.00


370.0
.74



62.4
30.0
.0
2188.0
19.43
2044.0
i^7T5~~
5.63


146.3
320.0
240.8 120.1 9.1
.48 .24 .02
41.0
.24
91.6
93.0
.54
94.1
62.4 62.4 62.4
30.0
.0
.0
15.0 5889.0 5889.0
.09 16.98 1.29
13.0 5818.0 5818.0
.08 16.77 1.27
1.13



24078
.48
19.0
.11
96.1
85.0
.49
94.6
62.4
6.5
2.0
.0
.0
.0
.0
.0
.0
1.73

.062
.000

                  SETTLER DATA


BIO-SETTLER
FLOC-SETTLER
OVERFLOW
RATE
GAL/FT2/DAY
1 13.8
1 13.8

GPM
.48
.48
INFLOW
HOLDUP TIME
DAYS
1.13
1.73
BOTTOMS
RATE
GPM
.26
.00
SLUDGE
DEPTH
INCHES
14.0
30.5
                     184
-------
     Table  14 (continued).   SUMMARY OP PLANT  PERFORMANCE	June 18,  1973
                        EQUILIZATION BASIN CONTENTS
             PH
             6.5
             TEMP      LIQUID INVENTORY HOLDUP TIME
            DEC  CGALLONS           MRS
                .0           2580.0            86.0
 TEMP
 DEC C
  307TT
PH~
                           AERAT1ON BAS1N CONTEMTS
 AERATED" LIQUID
 LBS      GALLS
_2UHJ_7
                                     MLSS
                                   PPM    LBS
                                      ~.U2tT5
MLVSS
                                                   LBS
            SLUDGE AGE
                DAYS
 RECYCLE
""RATIO
    %
~~4~8~.~l
      ^lOLDUP
    TNFLUENT
      HRS
     8.33
                           BASED ON      ___ SLUDGE
                         INFLUENT+RECYCLE   VOLUME
                                MRS      __ INDE.X_
                               5.63         146.3
7C REM_RATE_
 CONSTANT
  I . 264
             TOD R.R.
            "CTlNSTANT
             1/HRS	
            T7830
                               CARBON BALANCE
                          	ON AERATION BASIN	
                CARBON  IN"   CARBON OUT  CARBON TO C02
                 LBS/DAY      LBS/DAY    LBS/DAY   %WT
                                  ^^        r^   ^T-^



                            AERATOR PERFORMANCE
                                   mD-                            .       .

                      AERATION BASIN OXYGEN BALANCE	

           02 SUPPLIED         02 TRANSFERED        EFFICIENCY
           ^...^   LB/HR        KtA- - CS*~ LB/HR           %


         02 CONSUMED                          02  CONSUMED
  BATS ED ON~CSnRBOW~BArffNCE	BASED ON~Tj2=A(LBb TOU HKM/UAY>-fB< VSS;	
 LBS/DAY   LBS/LB TC REM                LBS/DAY     LBS/LB TC	
   5.672.18                    """


   	MICROORGANISM BALANCE	
                             "OFTAElWriON BA^IN

 AVERAGE              VOLATTLE~~SOLTDS" FORMED             RATIOB
  MLVSS       IN BASIN  WASTAGE  CLAR OVERFLW    TOTAL    LBS VSS/DAY/
-DPM    tB^   LBS7DAY   LBS/DAY     LBS7DAY~   LBS/DAY"   MLVSS TOC~REM
 1910.0 4.0    .56      1.27         .08         1.91      .48   .73
                                   185
-------
    Table 14 (continued)
                          SUMMARY  OP  PLANT  PERFORMANCE-—June 18, 1973

                          **SYSTEMS PERFORMANCE**
TC
TOD
      LBS/DAY  LBS/DAY
              /LBMLVSS
        2.84     .714
        9.06   2.279
                             "REMOVAL
                         THRU CLARIFIER
                        LBS/DAY   LBS/DAY  %WT
                                 /LBMLVSS
                          2.60     .654    91.6
                          8.52    2.144    94.1
                      THRU FLOCCULATOR
                     LBS/DAY   LBS/DAY  *WT
                               /LBMLVSS
                     ~ 2.73.68696.1
                       8.57     2.156   94.6
   EfiUILIZATION BASIN
  	PH       ~
          6.5
                             PH  CONTROL SYSTEM
                          AERATION  BASIN INFLUENT
                          HTefl"PH~   Lw~pir~~svsrnp!
                             7.1        6.1     6.5
                                                     HCL ADDITION
                                                    	HU7MTNT-
                                                             .0
                         NUTRIENT  ADDITION SYSTEM
FLOW FROM
EQUILJZATION
   LB/HR
   249.90
               CARBON     "    NUTRIENT
             FROM EQUILZ.   FLOW    COMPOSITION	
               LB/HR      LB/HR    %NH3    %P     C:N
                 .118      1.576     .53    .07  100: 5.8
                                                       RATIOS
                                                                C:P
                                                               100:   .9
 WASTE FROM EQ U I L I ZAT ION
GPM
.50
        PPM PG
         680.0
                  PPM  TC
                   473.0
AERATION BASIN
 MLVSS	TC	
  PPM"     PPM
 2044.0   836.0
RECYCLE SLUDGE
 FLOW   MLVSS_
  GPM"   PPM
  .24  5818.0
                                                                 WASTAGE"
GPM
 .02
FEED PG/
AER MLVSS
 .36
                     FOOD/MICROORGANISM RATIO (LOADING)               	
              FEED  TC/LBS TC/DAY/     LBS TC/DAY/LB MLVSS
              ASR TC         LBS MLVSS   _?ASEiD ON MLVSS=TC J3UGS( U ^/6jD>
                ."57            .71                  .87
                         FLOCCULATION CONTROL SYSTEM
CAUSTIC
USUAGE
LB/HR
.0000
PH

6.5
FLOCCULATOR INFLUENT
LB/DAY
TC .237
TOD .537

ALUM
USUAGE
LB/HR ML/MIN
.0624 11.3
OVERFLOW
TURBIDITY
JCU
2.0
FLOC-SETTLER OVERFLOW % REMOVED
LB/DAY
.1 10
.491
8.6
                                 186
-------
The intput data needed for the execution of this program
are:
CARD NO. 1
V       -
Q       -
SPEED   -
SFEED2  -

RECY    -
W       -
XR      -
KSUBS   -
YIELD   -

KENDOG  -
           aeration basin volume (gallons)
           influent feed flow rate (gpm)
           initial influent feed concentration, (mg/1 TOD)
           influent feed concentration after step change
           (mg/1 TOD)
           recycle flow rate (ml/min)
           waste flow rate (ml/min)
           return sludge concentration (mg/1 MLVSS)
           half velocity coefficient (mg/1 TOD)
           growth yield coefficient (Ib VSS formed/lb TOD
           removed)
           microorganism decay coefficient (day-x)
CARD NO. 2
XSTEP   -  time at which feed concentration is changed
           (hours)
XF      -  time at which simulation ends (hours)
H       -  stepsize (hours)
INT     -  frequency of data output desired (real-time data
           output every H*INT hours)

CARD NO. 3
Y(l)    -  initial substrate concentration in aeration basin
           (mg/1 TOD)
Y(2)    -  initial microorganism concentration in aeration
           basin (mg/1 MLVSS)
CARD NO.
FACTOD  -
FACVSS  -
           conversion factor (mg TC/mg TOD)
           conversion factor (mg TC/mg MLVSS)
                              18?
-------
CARD NO. 5
LOPT    -  simulation option:    enter 0 for no F/M control
           enter 1 for F/M control
AA      -  constant for waste  calibration (see Equation. 10)
BB      -  constant for waste  calibration (see Equation 10)
WMAX    -  maximum waste flow  rate allowable,  (ml/mln)

Mini-plant kinetic data was obtained in terms  of MLVSS  and
TOD.  Since the F/M control action was in terms of total
carbon, it was necessary to have conversion factors FACTOD
and FACVSS.  The theoretical FACTOD conversion factor for
propylene glycol is 0.28.  However, the number entered  into
this program should be the actual conversion factor based on
the operation of the TC and TOC instruments.  Similarly,
FACVSS should be the conversion factor from MLVSS to MLTC
using values from on-line total carbon analysis (FACVSS is
theoretically equal to 0.53 for cellular formula CSH702N.)

The program and a sample printout are given in Tables 15 and
16, respectively.
                              188
-------
                         APPENDIX C
                 TRANSIENT STATE ACTIVATED
                 SLUDGE COMPUTER SIMULATION
A computer program was developed in order to predict
transient changes in microorganism concentration, P/M
and aeration basin substrate concentration to step changes
in loading.  The program logic uses the Monod type kinetic
equations which are incorporated into the unsteady-state
material balance equations (Equations 8 and 9).  The
P/M control is included in the program logic.

The computer program consists of the main program SIMUL,
the logical function RKG, and the subroutine PXY.

The main program includes all the input (READ) and output
(WRITE) statements.  It also includes a calculation of
the initial steady-state microorganisms concentration (XSTST)
and the initial aeration basin substrate concentration (SONE)
by using Monod kinetics.  When inputting plant data, this
calculation shows how close the process is to the theoretical
steady state.  The equations used are discussed in the litera-
ture (Lawrence and McCarty, 1970).

The material balance differential equations are solved in
logical function RKG by using a fourth-order Runge-Kutta
method with Gill's coefficients (Gill, 1951).  The actual
derivative evaluations are done in subroutine PXY.  Function
RKG also includes the P/M control logic.  Counter ICNT in
function RKG permits transfer to the main program for data
output.
                              189
-------
               TABLE 15.  TRANSIENT-STATE ACTIVATED SLUDGE,
                         COMPUTER PROGRAM
1.000 C
2.00O~C
3.000 C
4.OOO
5.000
6.000
7.000
8.000
9.000
10.000
11.000
12.000
13.000
14.000
15.000
16.000
17.000
18.OOO
19.000
20.000
21.000
22.000
23.000
24.OOO
25.000
26.000
27.000
28.000
29.000
30.000
31.000
32.000
33.000
34.000
35.000
36.UUU
37.000
38.000
39.000
PROGRAM SIMUL
TRANSIENT STATE ACTIVATED SLUDGE SIMULATION
DIMENSION Y(2),F(2)
REAL K,KSUBS, KENDOG
COMMON V, 6, SFEED,R,XR,K,KSUBS, YIELD, KENDOG, COMPAC
5 FORMAT(HF)
6 FORMAT<25X,'F/M CONTROL TEST SIMULATION'//)
7 FORMAT <22X,' BLANK SIMULATION - NO F/M CONTROL'//)
LOGICAL RKG,LOGRKG
8 FORMAT(27X, 'KINETIC MODEL CONSTANTS' /14X, 'K,l /DAY',
1' KSUBS,MG/L TOD YIELD KENDOG, I /DAY'/
2l5X,F4.1,7X,F6.1,llX,F4.2,5X,F5.3//)
9 FORMAT( IX, 'INPUT VALUES* V6X, 'AERATION BASIN VOLUME',
1' =', Ell. 4,' GALLONSV6X,' INFLUENT FLOW RATE = ',
2E11.4,' GPM'/6X, 'BIO-SETTLER UNDERFLOW »',E11.4,
3' ML/MIN' /6X, 'INITIAL RECYCLE FLOW a',Ell.4,
4' ML/MIN (RECYCLE RATIO =»' ,F6. 3, ')' //4X, * INITIAL *,
5'CONDITIONSt'/6X, 'AERATION BACTERIA =',F8.1,
6« MG/L MLVSS (*,F7.1,» MG/L TO '/6X7* SLUDGE BACTERIA',
7' =',F8.1,» MG/L MLVSS C,F7.1,' MG/L TO'/
86X,'BIO-SETL OVERFLOW TOD =',F8.l,' MG/L TOD (AER*,
9'ATION SUBSTRATE CONG) '/6X, • INFLUENT WASTE CONC. =»',
1FS.1,' ML/L TOD C,F6.l,' MG/L TO'//
16X,' SLUDGE COMPACTION RATIO =',F5.2,' MG/L SLUDGE PER'
2,' MG/L BACTERIA' /6X,'TC CONVERSION FACTOR = *,
3F5.2,' TC/MLVSS'/6X,'TC CONVERSION FACTOR »',F5.2,
4' FEED TC/FEED TOD' //6X, • INITIAL F/M LOADING »',
5F5.3,' TC/TC'///' INITIAL STEADY STATE VALUES AS CAL',
6*CULAT£D BY THE KlNETtC MODELt »/lX, 'MIXED LtGUoR SUB»,
7'STRATE CONCENTRATIONt',F6.l,' MG/L TOD OR',F7.1,
8' MG/L TC'/IX, 'MIXED LIQUOR BACTERIA CONCENTRATION* ',
9F7.1,' MG/L VSS OR',F7.1, ' MG/L TC'////6X, 'TIME AT',
" 1* WHICH LOADING IS CHANGED J *,F8.1, • HOURS »/6X,
2'NEW (T»',F4.1,') INFLUENT WASTE CONC«',F8.1,
3» MG/L tOD <*,F5.G,' MG/L TO'//)
10 FORMAT(4G)
15 FORMAT (2F)
16 FORMAT (20X,« ACTIVATED SLUDGE TRANSIENT SIMULATION'//)
 41.000
 42.000
 43.000
Tl4.OOO-
 45.000
 46.000
 47.000
 rrTORMArc2F>
 18 FORMAT(4G)
 19 FOHMAT<*TlM£   BACTERiA,MU/L.  i>UH5»l hATE  MlXt.U
   1'LIQ F/M  RECYCLE  WASTE    WSUM'/'HOURS  M',
  2rLV5S   TC     TOD,  MG/t   MG/L TC  TC/TC^T
  3'   ML/MIN  ML/MIN  GM VSS')
"20 FORMAT(F5. 1 ,F8. 1 ,F7TrnxVT8TT73X,Fffi 1,
   1F8.3,1X,F7.1,F8.1,1X,F7.1)
                                 190
-------
     Table  15  (continued).   TRANSIENT-STATE ACTIVATED SLUDGE
                           COMPUTER PROGRAM
  49.000
 -507000
  51.000
  52.000
  53.000
  b4.0UU C
  55.000
READV,Q,SFEED,SFEED2,RECY>W,XR,K>KSUBS,YIELD*KENDOG
READTITTO T) X5TE*, 'XFTK. INT
READCU15>YU>,Y<2)
READ<1.»18>LOPT.,AA,BB<»WMAX
  56.OOO
  57.000
  bS.UUO
  59.000
  60T001T
  61 .000
  527000"
  63.000
 -54700IT
  65.000
RsRECY/	
  7T).000       SONE»-1.)
~T^700D       XSTSTa < Yl ELD* C 5FEW-3WE5 vriiETA5">7"
	73.000      1 «1.+KENDOG*THETAC)*THETA)	    	
^T47000       SOTjETC>SONE*F~ACtOD
  75.000       XSTSTC=XSTST*FACVSS   	      	
-"757000       ^TCB^?r2T*FACVS"S
  77.000  	TCF=SFEED*FACTQD      	
  78.000XRTC=XR*FSCV53
  79.000 C	         		
  807000WRITE<3*T6)
  81.000       IF~
  85.000    26 K=K*24.               	
~B 67000       KENDOiG=kENDOG*24 .
  87.000	WRITE<3,8)K*KSUBS*Y1ELD,KENDOG
  88.000K=K/24.
  89.000	KENDOG»KENDQG/24.	         	
"90.000       9^5760^  ~    ~~  ~~   ~                        ~
  9J^±000	WRITE<3*9)V,Q*T,RECY,Rj,YC2)*TCB*XR,XRTC*YCl >_,SFEED*TCF»
  92.000     lCOI^ACVFACVSSVFACTOO«FMLOAb'
 J93.000	2XSTEP,XSTEP, SFEED2,FEED2C
  94.000       Q=Q*60.
  95.000       WRITE<3,19>
                                 191
-------
      Table 15 Continued).
TRANSIENT-STATE ACTIVATED SLUDGE,
COMPUTER PROGRAM
  96.000"    30 CONTINUE                      "                    "	
  97.000	    LOGRKG=RKG(N*X,XSTEP>SFE^D*SFEED2,Y,XF>H,INT>
  98.000      fTCB*FACVSS,FACTOD*FMLOAD7LOPt7AA7BB*W7RECYiWSUM*tHETA*t7
  99.000	    2WMAX,R,VJ,XR,TCMIX>
 100.000       WRITE<3*20)X,Y<2y,TCB,Y
 101.000	IF(.NOT.LOGRKG)GO TO  30
 10270015       STTjP
 103^,000	END^
 104.000 C            "               ~
 105.000 C	
 r06.000       LOGICAL FUNCTION
 107>000	ITCB;>FACySS,FACTO
 103.000      2WMAX.,R,V.,XR,TCMIX>
 109.000	REAL K(2)_                    _     	
 110.000       DIMENSION a<2),Y(2)\»FC2~)                   ~~
 11 1.000	DATA AI , A2» A3 *A4, AS* A6/V29 2893218813A5,0 .5^ 5 7864 376269O,
 112.000      10.12132034355964*1.70710678118655,3.41421356237310,
 113.000	14.12132034355964/	
 114.000       DATA 1CNT/0/
 115.000 j;   _ FUNCTION RKG SOLVES A SYSTEM OF N SIMULTANEOUS FJRST
 116.000 C     ORDER ORDINARY DIFFERENTIAL" EQUATIONS USING THE FOURTH
 117.000 C	   ORDER RUN6£-KUTTA_ METHOD J^ITH GILL^S COEFFJ[CIE^NTS.	
 118.000    40 CONTINUE
 1 1 9 .000	^F ( X.GE.XSTEP) SFEEDaSFEED2	^___	
nr2TJ".F>
 1_2UOOO	DO 50 I = 1>N	  	   	   	
 122.000       KtI>=F(I)*H
 1 23.000	Y( I ) =YUy*K( I ) * . 5     	     	
 124.000    50 Q(I)=iK(I)
 125.000 C
 126.000       X=X+.5*H
 127.000	CALL FXYCXjYjFV)	
 128.000       DO 51 I = UN
 129.000       K>
 137.000    52 Q=A5*K	
 T38TOOO C
 139.000       X=X+.5*H
 140 VOO'CT       CALlTFXYrXTYVF )
 141.000       DO 53 I=1>N
 1427^00       RCTy^FTIT*ff
 143.000    53 Y(I)=.YCI)*KCl)/6.-Q(I)/3.
                                     192
-------
     Table  15 (continued).
               TRANSIENT-STATE ACTIVATED  SLUDGE,
               COMPUTER PROGRAM
 145.000  C
 146.000
 147.000
   DO F/M CONTROL  OF  RECYCLE AND WASTE IF OPTION LOPT»1
   TCB=YT2)*FACVS5
   TCF=SFEED*FACTOD
 149.000
 TbU.OOO
 151.000
 1527000
 153.000
   FMLOAD=TCF/TCMIX
   IFCLOPT.NE.15GO  TO  56
   W=BB-AA*FMLOAD
   IFQ,SFEED,R*XR,K,KSUBS, YIELD, KENDOG*COMPAC
                       <1 ) )-K*Y< 1 )*YC2)/ * ( R*XR- (1 . +R > *Y ( 2 )T+YiELD*K* YTl )"*YC 2 >
  1/
-------
            Table 16.  ACTIVATED  SLUDGE  TRANSIENT SIMULATION
                      F/M  CONTROL TEST SIMULATION
                5.0
                      KINETIC  MODEL CONSTANTS
                  ~KSUBS*Md7L  TOD	TTEtD	KKNDOGiT/DAT"
                      117.0             .21      .060
 TNPUT~VALUE5:
      AERATION BASIN VOLUME
      INFLUENT FLOW RATE
 _ BIO-SETTLER UNDERFLOW
      INITIAL RE^YCLE^FLOW
    I N I T I AU~C OND I T I ON Si
      AERATION BACTERIA
                          .2500E 03 GALLONS
                          .6000E 00 GPM
                          .7850E 03 ML/MIN
                          .7000E  03 ML/MIN (RECYCLE RATIO =*  .301)
                                                736.4 MG/L TO
      BIO-SETL OVERFLOW TOD
      INFLUENT" W A STE^CONC.
 1938.0  MG/L  MLVSS  (
"75TO.O  MG/L  MLVSS  T
  116.0  MG/L  TOD (AERATION SUBSTRATE CONG)
 1556.0  ML/L  TOD ( 404.6MG/L TO"
SLUDGE COMPACTION  RATIO
TC CONVERSION FACTOR
TC~C~
                                3.88 MG/L SLUDGE  PER MG/L"BACTERIA
                                 '3J? IC/MLVSS	
                                 -~   ~"^~   TOD
      INITIAL F/M LOADING = .528 TC/TC
INITIAL STEADY STATE VALUES AS CALCULATED BY THE  KINETIC  MODEL:	
 MIXED LIQUOR SUBSTRATE" CONCENTRATIONi  116.7 MG/L TOD   OR   30.3 MG/L TC
 MIXED LIQUOR BACTERIA CONCENTRATION: 1992.0 MG/L VSS   OR  757.0 MG/L TC
      TIME AT WHICH LOADING IS CHANGED:
                                       9.0 HOURS
      NEW 
-------
                         APPENDIX D
         STEADY-STATE ACTIVATED SLUDGE COMPUTER MODEL

A computer program was developed to determine the minimum
volume of aeration basin required under steady-state conditions
for a specified treatment efficiency.  Several treatment ef-
ficiencies may be specified and the results tabulated according
to recycle ratio and recycle sludge concentration.  The basis
for the calculations is the Monod kinetic model.  A good dis-
cussion of the development of the model equations is presented
by Lawrence and McCartly, 1970.

The input data needed for the execution of this program are:

CARD NO. 1

Q      -  influent feed flow rate (gpm)
SPEED  -  influent feed concentration (mg/1 TOD)
K      -  substrate utilization coefficient (day""1)
KSUBS  -  half velocity coefficient (mg/1 TOD)
YIELD  -  growth yield coefficient (1 Ib VSS formed/lb TOD
           removed)
KENDOG -  microorganism decay coefficient (day ~ )

CARD NO. 2
NI     -  number of efficiencies specified
NJ     -  number of sludge concentrations specified
NL     -  number of recycle ratios specified

CARD NO. 3
EFF(I) -  efficiency of substrate removal (S0-Si)/S0.
          I = 1, NI
                             195
-------
CARD NO. 4

XR(J)   -  recycle sludge concentration (mg/1 MLVSS)
           J = 1, NJ
CARD NO. 5

R(L)    -  volumetric recycle ratio.  L = 1, ML


The computer program and a sample printout are given

in  Tables 17 and  18 respectively.
                              196
-------
        Table 17.   STEADY STATE ACTIVATED SLUDGE COMPUTER PROGRAM
   1 .000 C
   2.00O~C~
   3.000 C
   4 .OHO
   5.000
         c
    PROGRAM BACT
    MONOD~ MODEL" STEADY- ST ATET C ALCULAT I ON S
    REAL K,KSUBS,KENDOG
   7.000
   8TOTJO
   9.000
T070O0
  11.000
 10 FORMAT <6F)
"T5~FJJRMATC///iaX, 'STEADY  STATE
   123X, 'KINETIC MODEL CONSTANTS* /I 2X, «K, i /DAY
            TTECD
                                                   KSUBS,*,
   3F4.2,7X,F5.3/)
  12.000
  J3._000
  _.___. ^

  15.000
 20 FORMAT ( 10X7^1 NFLUENT^FLOW, GPM     lNFLUENTWA5TEf,
   I' CONCENTRATION,  MG/L T^D'/I SX^Fl 0^2,20X^8. 1/)
 25» FORMATT3I)
  17.000
  18.0015
  19.000
  20.000^
  21 .000
  22.00(
  23.000
  24.000
  25.000
  26TOOTT"
  27.000
 __                        		
 35~FORMATCTX77TX, 'CASE1 7l3*^ • r/8X7liEFFICIENCY^~OF*T
   I* WASTE REMOVAL  =* jrFS.U'X    C*^ F5 >l>* MG/L EFFLUENT •»
   2~*TOD>'/8X, • RECYCLE KLUDGE CONCENTRATION  ='*
	 3F6.0,* MG/L MLVSSf//5X> •REQUIREMENTTS TO  MEET THE DESIRE
   4 «ED REMOVAL: *78X,•BIOLOGICAL MASSV~XV =  V»E1674,
   5' LBS.VSX, «F/M  LOADING J^H^Ji''^-^^  LB  TOD/*,
   6'LBHL^S^-DAY'/SX^'F/M "REMOVAL RATIO =»,F67S7*
   7'LB MLVSS-DAY«/3X,'SLUDGE AGE REQUIRED =',F5.2,» DA',
   B^YSVHX,'WA~5HOUT  SLTTDUS AGE =1
  29.000
  y o.ooo
  31.000
                                       f DAYS
 9'  W =',£!
> FORMAT OX
 1'RECYCLE
 2' AEEATIT/N   TIYDRAUL 1C r 725G"' RAri7T~    FLO W7GPM   *
 3'  FLOW,  GPM      MLVSS,MG/L   VOL, GAL.  RET*N,*,
RECYCLE
                           WASTE SLUDGE
                                            BACTERIA
 33.)00
  35.000
 40 FORMAT<1X,F5.2,4X,E10.4,3X,E10.4,6X,F6.0,3X,E10.4,
~ T3X,F6.2)
 45 FORMATC 1X///20X, f *************#*5Me**********#**»/)
^48 FORMAT ( //// • CASE f ,1 3, •    RECYCLE SLUDGE "CONCENTRAT I ON * ,
   !•  =«,F6.0//>
36.000 C
37.000
38.000
39.000
40.000
41.000
42.000 C
43.000
44.000
45.000
READC 1,10) Q,SFEED,K, KSUBS, YIELD,KENDOG
READC1,25) NI,NJ,NL
R£AD<1,30) 
-------
    Table 17 (continued).
                          STEADY-STATE ACTIVATED SLUDGE
                          COMPUTER PROGRAM
  46.000
  47.000
~~4~87TFOO~
  49.000
  5~OiOOQT"
  51.000
  527000"
  53.000
           47 CONTINUE
              R=D
               1 = 1    	
           ~5ZT M*M+1
           51  SAER»SFEED-SFEED*EFF(I)/100.
  54.UUU
  55.000
 56.000
 57.000
~5BT001T
 59.000
 60~70~OlF
 JJI-OOO
 62.000
 63.000
 64.000
 65.000
n&6TOTTO"
 67.000
 68YOOO
 69.000
 TO". 000
 71.000
-72.UOO
 73.000
 74.00(
 75.000
 76.OOO
_77_»000
"T8VOTKT
 79j.OOO^
"80700"0"
 81.000
 82.000
 83^000
~B470~00"
 85.000
 86 ."000
    AERVOL»< 1440 . *Q*THETAC* ( 1 . +RC L> »/
    IFCL.NE.l)
    IFFMREM*THETAC>
~ 1AGE«1N>WMAX
 55 WRITE<3J36>
 36" WRTTET3"^40)«CO*RECY(L),t^AERX:,AER\70L7HRT
               ~1 ¥ ( L .nCETNLTUOTTT ^5T~
               L=l
               J=J+I
               IF45)
               GO  TO 50
               GO  TO 47
           140 WRITE<3*48)M,XRCJ)
               GO  TO 55
           150
               "END
                                   198
-------
             Table 18.   STEADY-STATE ACTIVATED SLUDGE MODEL
                       KINETIC MODEL CONSTANTS
            K,T/DAYKSUBS7MG/L   YIELD   KENDOG,1/DAY"
             5.0         117.0      .21        .060
          INFLUENT FLOW,  GPM
    INFLUENT WASTE CONCENTRATION*  MG/L TOD
                    rscr
CASE   1.
        EFFICIENCY OF  WASTE REMOVAL =
        RECYCLE SLUDGE CONCENTRATION
         80.OX   (400.0 MG/L  EFFLUENT TOD)
         * 5000. MG/L MLVS~S
    REQUIREMENTS TO MEET THE DESIRED REMOVAL*
       BIOLOGICAL MASS,  XV »  .2542E 01 LBS.
       F/M LOADING  RATIO
       F/M REMOVAL  RATIO
4 . 84 LB TOD/LB MLVSS— DAY
3.87 LB TOD/LB MLVSS -DAY
        5LUDGEAGEREQUIRED
        WASHOUT  SLUDGE AGE =
 1.07 DAYS  (MAX W »  .3855E-01  GPM)
RECYCLE
RATIO
.10
.20
.30
.40
.50
RECYCLE
FLOW, GPM
.5000E-01
.1000E 00
. 1500E 00
.2000E 00
.2500E 00
WASTE SLUDGE
FLOW, GPM
•3112E-01
•31 12E-01
.31 12E-01
.31 12E-01
.3112E-01
BACTERIA AERATION
MLVSS,MG/L VOL, GAL.
737. .4038E 03
1093. .2725E 03
1393. .2137E 03
1651. .1804E 03
1874. . 1589E 03
HYDRAULIC
HETW* TSSYS"
.56
.38
.30
.25
.22
IASE  2    RECYCLE SLUDGE CONCENTRATION = 7500.
RECYCLE
RATIO
.10
.20
.30
.40
.50
RECYCLE
FLOW, GPM
.5000E-01
.1000E 00
.1500E 00
.2000E 00
.2500E 00
WASTE SLUDGE
FLOW, GPM
.2075E-01
.2075E-01
.2075E-01
.2075E-01
.2075E-01
BACTERIA AERATION
MLVSS,MG/L VOL, GAL.
965. .3087E 03
1509. .1973E 03
1970. .1512E 03
2365. .1259E 03
2707. .UOOE 03
HYDRAULIC
RET*N, DAYS
.43
.27
.21
.17
.15
                                   199
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    Table  18 (continued).   STEADY-STATE ACTIVATED SLUDGE MODEL
CASE  "3V
       EFFICIENCY OF WASTE REMOVAL
       RECYCLE SLUDGE CONCENTRATION
                                       <200.0  MG/L EFFLUENT TOD)
                                5000. MG/L "MLVSS"
    REQUrREHEFTS~^rrn«EET THE "DE SI RED~~REMOVAL~i
        BIOLOGICAL MASS* XV a  .3507E  01  LBS.
        FVM LOADrNG RATIO =
                      3.51  LB Tt
F/M REMOVAL RATIO  =  3.15  LB TOD/LB M^SJ5-DAY	

WASHOUT SLUDGE  AGE »  1.07 DAYS  (MAX W  •  .5318E-O1 GPM)
RECYCLE
RATIO
.10
.20
.30
.40
.50
RECYCLE
.5000E-01
. TOOOE 00
.1500E 00
.2000E 00
•2500E 00
WASTE SLUDGE
TLOW, GPM ~
.3438E-01
.3438E-01
.3438E-01
.3438E-01
.3438E-01
BACTERIA
MLV5S,MG7L
767.
I12CT.
1418.
1674.
1896.
AERATION
VOL, GAL.
•5356E 03
.3669E 03
.2897E 03
.2454E 03
.2167E 03
HYDRAULIC
RET*N, D~AT5~
.74
.51
.40
.34
.30

RECYCLE
"RATTTl
    10
    RECYCLE
   •5000E-01
WASTE SLUDGE
 LW7~GPM
 .2292E-01
 BACTERIA   AERATION
MLVSS7MG7L" VOUT^GAL
   994.     .4132E  03
HYDRAULIC
RET*NTr DAYS
   .57
,2U
.30
,^»TJ
.50
.10UUE 00
.1500E 00
.2000E DO
.2500E 00
.yyyyE-oi
.2292E-01
" ~.2292ET-01
.2292E-01
Ib36.
1995.
"-- 12388.
2729.
.2674E 03
.2059E 03
.1720E 03"
•1505E 03
.37
.29
.24
.21
                                  200
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                             TECHNICAL REPORT DATA
                       (I'li-ase read Ittaruclioim on the reverse before completing)
 I Ml I'tlll I NO.

  EPA-660/2-75-021
e> fesffrtff*?z ^K •? rtf. 1
                           KEY WORDS AND DOCUMENT ANALYSIS
               DESCRIPTORS
Waste  Water Treatment
Industrial Waste Treatment
Petrochemical Waste Treatment
Pilot  Treatment Facility
                                       b. IDENTIFIERS/OPEN ENDED TERMS  C.  COS AT I Field/Group
                                        Activated Sludge
                                        Automation  and
                                          Control Systems
                                        Biological  Activity
                                          Monitor
                                        Nutrients Addition
                                        Sludge Recycle Con'
                                                              Cont.
                                                              rol
          N STATfcMENT

  Release Unlimited
                                     19. SECURITY CLASS (This Report)
21. NO. OF PAGES
    200
                                       20. SECURITY CLASS (Thispage)
                                                              22. PRICE
CPA form 2220-1 (»-73)
                         ft U 5 GOVERNMENT PRINTING OFFICE 1975-698-908 /3 REGION 10
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