&vi " s/11
I&6e^3
^ IN STORAGE
0)oU")y
670273027 PROPERTY OF
e:-:v!Row«ntai protectiob agcnei
ROTATING BIOLOGICAL DISK WASTEWATER ttBRARY REGION x
1209 SIXTH AVENUE
TREATMENT PROCESS - PILOT PLANT EVALUATION
J t J n ( 1 y 11
by
Department of Environmental Sciences
Rutgers University
New Brunswick, N. J. 08903
for the
RESEARCH AND DEVELOPMENT OFFICE
ENVIRONMENTAL PROTECTION AGENCY
Project #17010 EBM
August 1972
U.S. EPA LIBRARY REGION 10 MATERIALS
~ ~
RXD
~ 34
b34
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EPA Review Notice
This report has been reviewed by the Research
and Development Office, EPA, 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.
ii
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ABSTRACT
The results of operating a 10,000 to 20,000 gal per day
staged rotating disk pilot plant have been presented for
three modes of operation, namely, (1) the slimes in all
stages exposed to ambient atmospheres, (2) the slimes in
stage 1 exposed to an atmosphere enriched with oxygen, and
(3) the slimes in stages 1 and 3 of a 3-stage operation
exposed to atmospheres enriched with oxygen0 It was found
that in the first mode of operation about 30 minutes of
contact with the slimes was sufficient to remove 90% of
the B0OoDo 5 while during the second mode of operation,. 18
minutes accomplished the same rate of removal of B.O0P.5.
In the third mode of operation, not only was 90% of the
Bo0oDo5 removed during 18 minutes of contact with the slimes
but a substantial portion of the nitrogenous demand was
satisfied„
This report was submitted in fulfillment of Project No.
17010 EBM under the Sponsorship of the Office of Research
and Development, EPA„
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CONTENTS
Section Pftg.L
I Conclusions 1
II Recommendations 3
III Introduction 5
IV Description of Pilot Installation 9
V Operating Results - Biological Section 13
VI Operating Results of Treatment 51
Subsequent to 10 Stage Unito
VII Activated Carbon Adsorption p 61
t
VIII Special Studies 67
IX Studies under High Flow Rate 87
X The Biota of the Growths on
the Rotating Disks 105
XI Mathematical Steady State Model
Application for Removal of Organic
Matter 117
XII Design Considerations 133
XIII Acknowledgements 143
XIV References 145
XV Publications 147
XVI Appendices 149
v
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FIGURES
PAGE
le COMPARATIVE PROFILES OF B.O.D.5 FOR OPERA-
TION PHASES 1 AND 2 17
2. COMPARATIVE PROFILES OF C.O.Do FOR OPERATION
PHASES 1 AND 2 22
3 o COMPARATIVE PROFILES OF T.O.C. FOR OPERATION
PHASES 2 AND 3 26
40 COMPARATIVE PROFILES OF D.T.O.C. FOR OPERATION
PHASES 2 AND 3 27
5. COMPARATIVE PROFILES OF S.O.Co FOR OPERATION
PHASES 2 AND 3 28
60 COMPARATIVE PROFILES OF NITRATE PRODUCED 34
7, REMOVAL OF B.O.D.5 FROM MODIFIED AERATION
EFFLUENT 49
80 FINAL SETTLING TANK 52
9C EFFECT OF CULTURAL AGE ON REMOVAL OF B.O.D.g
STAGES 1 TO 6 70
10o EFFECT OF CULTURAL AGE ON REMOVAL OF B0O.D.5 78
llo EFFECT OF TIME OF CONTACT ON REMOVAL OF B.O.D.5
STAGES 1 TO 6 81
12o EFFECT OF TIME OF CONTACT ON REMOVAL OF B.O.D.g
STAGES 1 TO 6 83
13. CARCHESIUM SP. FILAMENTS BEGGIATOA STAGE 4 107
14. BEGGIATOA STAGE 4 108
15. VORTICELIjA SP. DlFFLUGIA CONSTRICTA STAGE 7 109
vi
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PAGE
16. TYPICAL ROTIFER STAGE 10 HO
17. AMOEBA STAGE 11 EDGE 111
18. HORMIDIUM KLEBSII STAGE 11 SIDE J12
19. DIFFLIJGIA CONSTRICTA SMALL SPECIMENS
DIFFLUGIA SP. HORMIDIUM KLEBSII NITZSCHIA SP.
CILIATES STAGE 11 EDGE 113
20. DIATOMS NITZSCHIA IGNORATA NITZSCHIA SP.
STAGE 11 114
21. NEMATODE IN EGG HORMIDIUM KLEBSII
NITZSCHIA SP. STAGE 11 SIDE 115
22. BETWEEN ILLUMINATED UNITS "BLACK ALGAE"
ARCELLA SP. IN TANGLE OF OSCILLATORIA FILAMENTS 116
vii
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TABLES
Noc Page
lo Profile of Monthly Average of BoO.Dojj Phase 1 14
2e Profile of Bo0oD.5 Phase 2 16
30 Range of B00oDO5 Values for periods of opera-
tion with Normal and with Enriched Atmosphere
Operation 18
4. Profile of Monthly Average of C.0„Do 20
5o Profile of Co0oD. 21
6. Profile of Monthly Averages of Total Organic
Carbon (T.0cCo) and dissolved total organic
carbon (DoTo0.Co) 24
70 Profile of Monthly Averages of Total Organic
Carbon (T.0oCo) and dissolved Total Organic
Carbon (DoT000C0) 25
80 Profile of Suspended Solids 30
90 Three Stage Treatment Results 31
10. Profile of N02/N03-N 33
llo Profiles of NH3-N 36
12o Profiles of Albuminoid and Ammoniacal-N 37
13o Profile of HCO3 Alkalinity and NO3-N 39
14o CO2 Acidity 40
15. Orthophosphates as PO4 43
16,, Comparative Effect of Adding Lime to the
Influent from Algal Unit 44
vii i
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46
48
53
55
59
62
64
65
68
71
72
73
74
Comparative Effects of Adding Lime to the
Influent to Pilot Plant the Effluent from
the Algal Unit
Profile of Organic Removal Treating
Modified Aeration Effluent Concentrations
Removal of Total Organic Carbon by Final
Settling Tank Equipped with Submerged
Plastic Surfaces
Concentrations of Inorganic-N passing through
final settling Tank
Performance of 5 Stage Algal Unit after
Modification
Profile of Total Organic Carbon from Algal
Unit through Activated Carbon Adsorption
Activated Carbon Adsorption B.0oD.tj - Mg/1
Activated Carbon Adsorption NH3*/N03 - Mg/1
Comparison of Suspended Solids Removal
Microstraining vs. Quiescent Settling
Effect of cultural Age on Rate of B,0„De^
and T.O.Co Removal Stage 1 - 65% O2 in
Atmosphere
Relation of Grouped Values of Stage 1
Effluent B0O0D05 to Influent Bo00Da5
Effect of Cultural Age on Rate ofl Bo00DOg
and T.O#C0 Removal - Stage 2
Effect of Cultural Age on T.0eCo and B000D.5
Removal - Stage 3
ix
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NpB Fags.
30o Effect of Cultural Age on T.0oCo and B.0oDO5
Removal Stage 40 75
310 Effect of Cultural Age on Bo0.DO5 Removal and
To0oC0 Removal Stage 5 76
32« Effect of Cultural Age on B#0«D„5 Removal and
T00#C0 Removal Stage 6 77
33. Effect of Time of Contact on Removal of B000D05 82
34, Effect of Time of Contact on Nitrate Concentration 85
35« Average Operating Data November 1970 for Flow Rates
of 705 and 1707 gpm 88
36. Average Operating Data Period Nov0 29 to Dec. 22,
1970 at 12 gpnu 90
37o Average Operating Data January 1971 Using Sludge
Recyclingo 92
38. Average Operating Data February 1971 with and
Without Recirculation of Nitrate Treated Slimes 96
39o Average Operating Data March 1971 without
Recirculation of Nitrate Treated Slimes at
14 gpm 98
40o Monthly Average Performance of Algal Unit -
December 1970 through March 1971 100
41o Monthly Average Performance of Activated Carbon
Adsorption Dec0 1970 through March 1971 102
x
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SECTION I
CONCLUSIONS
The number of stages used for the removal of carbonaceous
matter should be not less than 2 nor more than 4„ One
stage following carbonaceous removal is adequate for nitri-
fication.
Immersion of the disks should be slightly less than one half
the disk diameter,.
Disks should be rotated at a peripheral velocity not less
than 05 ft/sec« because of lowering excessively the capacity
for oxygenation and because of increasing the immersion time«
The peripheral velocity should not be more than 1 ft/sec.
because energy consumption increases as the third to fourth
power of the velocity0
The performance of a rotating disk unit is not sensitive to
the direction of rotation.
There should be a clear spacing between clean disk surfaces
of 3/4 inch for carbonaceous removalo For nitrification
such surfaces could be reduced to as low as 1/8 inch.
The area of disk surface required for 90% B0O0D.5 removal
from normal domestic wastewater varies between 300,000 and
600,000 sqc ft0 per M.G0D0 of treatment depending upon the
number of stages used and the magnitude of the diurnal
variation in flow rate and strength,.
The area of disk surface required for nitrification is
3600 sq„ ft. per lb. of ammonia N. to be oxidized daily,
over the temperature range of 58° to 78° F„ Provision
should be made to provide for oxidizing the ammonia at
the rate applied during high flow conditions or, alterna-
tively, dampen the flow variation prior to application to
the disk treatment»
When using oxygen enriched atmospheres, 200,000 sq. ft0 of
rotating disk surface is required per M.G0D0 treated to
remove 90% of the BcO„D0 "s from normal domestic wastewater,.
Since nitrifiers are sensitive to high dissolved oxygen and
1
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necessitate dealing with the adverse effects of predation
associated with nitrification when using enriched atmospheres
it was not possible to determine the areal requirement for
disk surface area within the limitations of the study period.
Nitrification when exposed to ambient atmospheres proceed 3d
at a rate of 2e2 mg/1 per stage or 22 mg/1 per hour of
contact with the slimes. Under the specific operating
condition prevalent in the third mode of operation, described
above, nitrification proceeded at a rate of 76 mg/1 per hour
of contacto
A portion of the effluents from ambient and oxygen enrich-
ment operation was subjected to treatment using partially
submerged, illuminated disks for the purpose of extracting
nutrients from the stream by their synthesis into attached
algal cellso The effluents from algal production unit was
subjected to adsorption of residual organics on packed beds
of granular activated carbon. The total leakage of organics
through the system was le4 mg/1, all soluble, for all three
modes of operation, while the practical carbon exhaustion
rate was in the range of 15 to 20 mg/1©
During the latter part of the investigation the rate of
application of settled wastewater was almost doubled in
order to assess the response of the 10 stage biological
unit to stresso The first two stages of treatment were
operated in parallel using oxygen enriched atmospheres to
overcome the oxygen deficiency in the upper stageso Under
this condition of stress, the ten stages of treatment,
affording a total of 33 minutes detention time, was able to
remove about 90% of the B0O.D05 and effect a small amount of
nitrification in the tenth stage0 Sludge was recirculated
from the subsequent settling tank until the mixed liquor
reached 2000 mg/1, but there was no evidence of improved
performanceo
2
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SECTION II
RECOMMENDATIONS
An important and immediate consideration with regard to
utilization of rotating disk systems in the U.S. is the
capital costs associated with such installations,, The
capital costs involved in the application of the rotating
disk process to the removal of organics from wastewater is
basically dependent upon (1) the amount of disk surface
and drive equipment required, and (2) the volume of tankage
required. Accordingly studies should be conducted to
determine the optimum concentration of disk surface in the
reactors with due consideration to minimizing the number
of stages in order to minimize capital costs <> The operating
costs involved in the application of the rotating disk
process to the removal of organics from wastewater is
basically dependent upon power consumption, for applying
the necessary torque. That the rotational velocity can
be decreased in a downstream direction is evident, but the
magnitude of such decreases has not been defined,,
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SECTION III
INTRODUCTION
Aerobic biological slimes, which attach and grow on contact
media have been used for removal ana oxidation of contami-
nants in wastewater for almost a century. Although the means
of providing a contacting pattern between the attached slimes
and the wastewater and of supplying oxygen to the organisms
in the slimes has differed widely, yet, when facilities are
available, satisfactory treatment efficiencies are attainable.
Thousands of trickling filter plants throughout the wor^d
depend on the activity of attached biological slimes for
their effectiveness in removing pollutants from wastewater.
This form of treatment involves raising the wastewater to
a level sufficient for distributing it uniformily over a bed
of contact media upon which the slimes develop. The waste-
water passes through orifices in a rotating mechanism and
flows downwardly contacting the slimes which have the cap-
acity of bio-extracting contaminants for their nutrition.
Such periodic dosing allows the slimes to be exposed to the
atmosphere for oxygen adsorption. By this procedure, the
wastewater is brought into intimate but rather short contact
period with the slimes, while the adsorption of oxygen di-
rectly from the atmosphere into the slimes is an effective
means of securing oxygen adequate for the respirational needs
of the organisms.
Another method of treating wastewater is by the contact
aeration process which employs totally submerged vertical
contact surfaces placed transversly across a long aeration
tank upon which surfaces biological slimes develop, receiving
for their nutrition the pollutants in the wastewater and for
their respiration the oxygen dissolved in the wastewater.
This process has not gained acceptance mainly for the reason
that the mechanism of supplying oxygen by diffused air to
the slimes has been inadequate, especially at the beginning
of the treatment process.
In an overall sense the trickling filter and the contact aera-
tion processes represent the outside limits of the time of
contact and oxygen supply considerations. Even though the
trickling filter process utilizes a contacting pattern that
enables the slimes to receive their oxygen directly from the
5
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atmosphere, it cannot develop the full potential of ef-
ficiency because of the relatively large voids between the
widely spaced contacting surfaces and the short contact
periodo The contact aeration process which provides for
taking full advantage of time of contact by submerging all
slime surfaces, is of limited efficiency because of the
necessity of having to supply dissolved oxygen through ii.-
jection of compressed air below the water surface. Both
processes are plagued with problems arising from the
inaccessible surfaces across which slime bridge even though
the surfaces are placed quite far apart.
In order to be able to satisfy the oxygen demand of th^
slimes, increase the surface concentration per unit volume
of tank and make the slimes accessible for operational
control, the rotating disk form of treatment has been devised.
In this process the slimes are moved rather than the waste-
water, so that they alternately contact the atmosphere to
absorb oxygen directly and immersed in the wastewater to
enable the pollutants in the wastewater to be extracted„ When
the disks are immersed about halfway, the voids between the
disks are filled with wastewater thus providing an ap-
preciable contact period between one half of the slimes and
the wastewater while the other half of the slimes are
receiving oxygen from the atmosphere„ Rotation reverses
these conditions more frequently than once a minute,, Rota-
tional velocity and direction as well as the proportion of
disk surface immersed can be varied to provide operational
control with respect to slime thickness especially when the
concentration of slime surfaces have been substantially
increased over that in conventional processes„ The rotating
disk process thus affords opportunity to treat wastewater in
a manner to accelerate the biochemical reaction rates through
providing a contacting pattern so that the oxygen demands of
the slimes can be met in a manner to afford adequate contact
time between the wastewater and the slimes. Additionally
the exposure of the slime surfaces serves to make them ac-
cessible for operational control of slime thickness and so
affords the opportunity to increase the concentration of
slime surface per unit volume of reactor,,
SCOPE AND PURPOSE
A pilot plant to evaluate the capacity of partially submerged
rotating disks to treat domestic wastewater was operated at
the 90 M.G0Do Jamaica Pollution Control Plant in New York
City* For the purpose of the study, a 10,000 to 20,000 gallon
6
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per day portion of the settled wastewater from the main plant
was conducted uniformly to the pilot plant0 Since the main
plant served a resident population of some 600,000 and a
relatively small industrial load, it is believed that the
results obtained under a variety of controlled conditions
are completely reproducible when treating any domestic \ aste-
watero It might be pointed out that two atypical factors aid
exist in the character of the load to the pilot plant in that
(1) the flow from the Kennedy Airport,, which handles more
than 500,000 operations per year with the attendant wastewater
problems was tributary to the main plant and (2) the waste-
water contained 350 Mg/01 of chlorides0 originating from
seawater, which entered through tide gates0
The basic objectives of the pilot plant study were as follows:
1« Removal of organic matter.
2« Oxidation of ammoniac
3, Synthesis of Nitrogen and Phosphorus into attached algal
cellso
4, Develop process design criteria*
7
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SECTION IV
DESCRIPTION OF PILOT INSTALLATION
The pilot plant was located in a closed 3 car garage of the
Jamaica Pollution Control Plant. The plant employed about 1
hour of primary settling followed bj aeration and final
settling to treat tha wastewater from some 600,000 inhabitants
in the connected drainage area. The raw wastewater contained
160 Mg/1 of suspended solids and 150 Mg/1 B.O.D. while the
primary effluent contained about 120 Mg/1 of suspended solids
and 120 Mg/1 of B.O.D.^.
The flow to be treated by the pilot plant was taken from the
common primary effluent channel of the main plant. This was
done by means of a submersible pump which rested on the floor
of the channel about 10 feet below the water surface. The
pump lifted about 150 gpm of primary effluent to a 5 ft.
diameter tank which was continuously overflowing, leaving a
constant level water surface. This furnished the head to
supply a substantially constant flow of 11 gpm to the pilot
plant through a 200 ft. long 1 1/2 inch diameter rubber hose.
A valve on the line served to control the flow when less than
11 gpm was treated.
The pilot plant was divided into a 10 stage treatment section,
a settling tank and a 6 stage algal producing section. Each
stage of the treatment section was composed of 48 - 3 ft.
diameter, 1/16 inch thick aluminum disks mounted on 15/32
inch centers on a horizontal shaft. The disks were keyed
into the shaft and were separated alternately by 6 and then
by 7 one ft. diameter, 1/16 inch thick aluminum spacers which
served to restrain the large thin disks into alignment at
their peripheries. On either side of the disk assembly the
shaft extended and rested on self-aligning sealed bearings.
The disk assembly with the shaft horizontal was placed into a
half-formed cylindrical tank so that about 45% of the disk
diameter was submerged in the wastewater which passed through
the tank perpendicular to the shaft and thus parallel to the
disks. The contour of the "one-half" cylindrical tank con-
taining the wastewater was such that a space of about 1/2
inch was provided between the periphery of the disks and the
tank surface. A drain was provided at the base of each of
the tanks.
9
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The flow entered the pilot plant for treatment through a
splitter box having four triangular notched weirs capable of
dividing the flow in the desired proportions so as it could
be fed all to the first stage or step fed to any of the
combinations of the first and subsequent three stages via
hoses provided for that purpose.
The torque necessary to rotate the shafts was supplied by
hydraulic motors installed at one end of each shaft which were
impelled by the flow of oil at 100 lbs/sq. inch pressure from
a single electrically driven gear pump. Provision was made
to change the direction and velocity of rotation of each of
the shafts.
A drawing entitled "Layout of the Biological Section of Pilot
Plant" enclosed in the Appendix shows the details of the
construction and the sloped placement of the 10 stages to
avoid any inter-mixing between stages. Also included in the
appendix is a drawing entitled "Tank Assembly" which describes
the structure of the tank holding the wastewater being treated.
Measurement showed the capacity of each tank, that is each
stage, was 45 gallons when the disks were devoid of slime.
A rubber gear pump was used to lift a 3.5 gpm portion of the
effluent from stage 10 to an improvised rectangular settling
tank. This tank was not equipped with a sludge collection
mechanism but had a hoppered bottom. The settling tank pro-
vided 1.5 hours of fluid detention time at 3.5 gpm for the
separation of the biological solids generated by the 10 stage
treatment section prior to entering the subsequent algal pro-
duction section.
The overflow from the settling tank was conducted to a
distribution tank capable of dividing the flow by use of
triangular notched weirs into as many as six portions for feed
to the six stage algal production section. Any combination
of feed to the first stage with subsequent stages via step
feed hoses was thus made possible.
Each of the six stages of the algal production section was
equipped with varying numbers of overhead Growlux fluorescent
lamps and 3 foot diameter aluminum disks. The disks were of
triangular shape and of variable angle intended to optimize
the growth economics of attached algae from the standpoints
of surfaces concentration and light utilization. The first
10
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stage "had 12 disks, the second, 10; the third, 8? the fourth,
6? the fifth, 4? and the sixth, 2. The six disk assemblies,
submerged to about 45% of their diameter, were forcibly
rotated for alternate exposure to the light and immersion in
the fluid by a hydraulic motor at the end of each shaft.
These motors were impelled by the flow of oil under pressure
from separate gear pump driven by an electric motor for the
algal section. The tanks in which the disk assemblies wei.e
placed were otherwise identical in construction to the pre-
viously described tanks used in the 10 stage treatment unit.
For further details as to the construction of the algal section
refer to the drawing entitled "Layout of Algae Section of Pilot
Plant" which has been included in the appendix.
Enrichment of the atmosphere over the specific stages of treat-
ment was accomplished by enclosing that portion of the disk
assembly above the water surface with 1/2 inch thick trans-
parent plexiglass placed in a box-like form to form a sealed
hood. The joints between the plastic sheets were fastened by
screws, and duct tape was used for sealing purposes. Oxygen
was fed to the hood from a cylinder, the gas first passing
through a rotometer, having a range of .5 to 2 liters per
minute. A manometer, capable of measuring gas pressure be-
tween 0 to 1 inch of water, was connected to the hood. The
hood was found, by smoke testing, to contain small leaks which,
in conjunction with a pressure of less than 1/8 inch of water
under the hood, were able to pass to the outside atmosphere
the nitrogen evolved from the wastewater and the COj generated
through respiration of the slimes.
The carbon adsorption system consisted of six packed bed
columns 5 ft. 10 inches long and 3 inches in diameter. About
27 lbs of virgin granular carbon (WV-G 12 X40 mesh) was used
in the six columns. This quanity of activated carbon filled
the columns to a level that afforded a bed expansion of about
50% during the backwashing operation. The pressure across
the six columns, operated in series, at first was found to
increase at a rate of about 4 lbs. in 24 hours. A daily back-
wash schedule was practiced. A mixed media filter using coal,
sand and garnet was interposed before the carbon columns and
the pressure rise rate was lowered to less than 1 lb/sq inch
in 24 hours.
Samples of the influent to the pilot plant and of the effluents
from each of the stages were taken during the afternoon between
11
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3 and 6 P.M. The samples were prepared for analysis by
raicrostraining through a 2 inch diameter 35 micron "hand"
microstrainer.
Samples were analysed according to Standard Methods.
Allylthiourea was used to suppress nitrification in the B.O.D.
tests for those stages manifesting nitrification.
The foregoing description pertains to the basic equipment arid
when indicated/ changes or additions made during the course
of the work will be described at that time.
12
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SECTION V
OPERATING RESULTS - BIOLOGICAL SECTION
ORGANIC REMOVAL IN TERMS OF B.O.D.5
The removal of organics from the ;~:imary tank effluent of the
main plant by the 10 stage rotating disk unit, treating \
constant flow of 7.5 gpmt was conducted in two phases: (1)
the slimes on the disks of all stages rotated through normal
atmospheres and (2) the slimes in specific stages rotated
through atmospheres enriched with oxygen. The profile of
fl.O.D.^ values during the period of July to November 1969,
which is designated Phase 1, is shown in Teble 1. This table
presents the average values for the influent to the pilot
plant and the effluents from the 10 stages of treatment.
These data indicate that while the average monthly B.O.D.- of
the influent to the pilot plant varied from 84 to 173 mg/I,
the effluent from stage 10 was in the range of 6 to 14 mg/l.
These data were ootained while the disk assemblies were rotated
so as to oppose the flow of wastewater through the tanks and
at rotational velocities of 6 to 10 R.P.M.
All during the period of Phase 1 the dissolved oxygen con-
centrations in the effluents from Stage 1 and 2 were low,
being in the range 0 to 1 mg/l. The dissolved oxygen in the
effluent from Stage 3 was generally 1.5 mg/l and the corres-
ponding values for Stages 4 to 10 was in the range of 3 to
6 mg/l. It was evident that the slimes in the first two stages
of treatment, under the particular load conditions, were not
being fully satisfied with respect to oxygen supply. The
amount of such deficit was not apparent and there was not
available an effective and reasonably economic mechanism for
supplying such oxygen. Finally in July 1970 it was decided
to construct a hood over Stage 1 and to enrich the enclosed
atmosphere with oxygen gas. In this manner the slimes could
be exposed directly to atmospheres enriched with oxygen and
the effect on the process, particularly in the upper stages
of treatment, could be determined. During this operation,
designated as Phase 2, the rate of flow treated was essentially
the same as in Phase 1. Moreover the wastewater temperatures
were in the same range, that is 62° to 78 F. The direction
and speed of rotation of the disks wae maintained during both
phases of operation. Fundamental changes were made to the
equipment at the beginning of Phase 2. When the hood was
constructed over Stage 1/ the effective number of disks was
13
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TABLE 1
PROFILE OF MONTHLY AVERAGE
PHASE 1
MO.
Inf 1 ..
1
2
3
4
July -
•69 84
44
34
25
14
Aug.
112
69
48
37
23
Sept.
127
91
63
49
31
Oct.
139
--
—
57
40
Nov.
173
112
82
51
38
AVER.
127
80
57
44
29
% REM.
63
45
35
23
OF B.O.D.5 Mg/1
__5 6 7 8 9 10
10 6 6 8 6 6
16 15 11 9 9 7
23 23 16 13 11 10
23 18 17 16 14 14
31 21 19 16 9 9
21 17 14 12 10 9
17 13 11 9 & 7
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increased from 48 to 60, while in Stage 2 the number was
increased from 48 to 71. The data obtained during the Phase
2 operation is given in Table 2 as the monthly averages of
the B.O.D.5 determinations for the influent to the pilot plant
and for the effluents from Stages 1 to 6. Referring to the
averages, it can be seen that Stage 1 effected a substantial
reduction of B.O.D.5 during the 6 ir.inutes of contact of the*
wastewater with the slimes in that stage. Thereafter the rate
of B.0.D.5 removal was considerably less.
To represent the comparative performances of the pilot plant
during the two phases of operation the average results pre-
sented in Tables 1 and 2 were plotted on semilog scale in
Figure 1. It can be seen that the profile of B.O.D.g during
Phase 1 indicates that the rate of removal is first order with
respect to concentration. There was a definite decrease in
the rate of removal of B.O.D.5 below 13 mg/1. As to the pro-
file of B.O.D.g for Phase 2, it is noteworthy that there was
a rapid decrease in the B.O.D.5 remaining across Stage 1,
followed by a decrease in rate for Stages 2 and 3 but assuming
a direction quite parallel to that for Stage 1. There
followed a definite decrease in the rate of removal of B.O.D.,.
below 16 mg/1. It might be interesting to point out that in
Phase 2 the same work relative to B.O.D.^ removal was ac-
complished by 2 stages less than needed in Phase 1. This
acceleration was the result of utilizing a hood over Stage 1
containing an atmosphere enriched with oxygen to the extent
of 50% to 70% of the gases present (by an oxygen gas flow of
1.4 to 1.7 liters/minute) and increasing the effective number
of disks from 48 to 60. Based on the fact that the raw waste-
water was entering the main plant with 150 mg/1 of B.O.D.^,
the operating data taken during the period of Phase 2 indicates
that about 90% removal B.O.D.5 was effected by 3 stages of
treatment comprising a total theoretical detention time of 18
minutes (measured when the disks were devoid of slime). The
actual contact time was somewhat less, depending on the loss
of liquid volume due to the volume occupied by the slimes.
In order to throw light on the stability of the process with
respect to the B.O.D.^ remaining after the various stages of
treatment under both operating conditions, the daily maximum,
minimum and average values for the pilot plant influent and
the stage effluents are presented in Table 3. Inspection of
the 34 profiles determined during Phase 1 operation showed
the B.O.D.g of the influent was in the range of 79 to 210/mg/l
15
-------
TABLE 2
PROFILE OF MONTHLY AVERAGE OF B.O.D.5 Mg/1
PHASE 2
Stage No.
Month
Infl.
1
2
3
4
5
6
August 1970
125
46
25
18
16
17
16
October
84
32
22
16
14
12
11
November
94
27
23
15
13
11
10
AVERAGE 101 33 23 16 14 13 12
% REMAIN 33 23 16 14 13 12
-------
100
90
80
70
60
x
50
x
40
UJ
LEGEND
X Phase I data-See Table I
0 Phase 2data-See Table2
FIG I-COMPARATIVE PROFILES OF BODb for
OPERATION PHASES I and 2
123456789 10 II
i i i i ii i T T ' r i
STAGE NUMBER
17
-------
TABLE 3
RANGE OF B.O.D.5 VALUES FOR PERIODS OF OPERATION WITH NORMAL
AND WiyH ENRICHED ATMOSPHERE (1)
OPERATION PHASE 1 & 2
B. 0 - D. ^
in Mg/1
Normal
Atmosphere (2)
Phase 1
Enriched
Atmosphere
(3) Pha
Max.
Min.
Avg.
Max.
Min.
Avg.
Influent
210-
79
124
255
60
101
Stage 1
139
39
82
105
20
35
2
102
31
59
54
11
23
3
74
27
44
36
5
16
4
48
15
28
23
7
14
5
39
8
19
23
6
13
6
36
8
17
23
5
12
7
26
7
14
*
*
*
8
22
5
12
*
*
*
9
21
5
9
*
*
*
10
19
4
9
*
*
*
(1) Enriched atmosphere on Stage 1 only.
(2) 34 profiles during July to November 1969.
(3) 55 profiles during August/ October, November 1970.
*B.0.D.cj not determined on dov.-nstreara stages.
-------
while the B000D«5 of the effluent of Stage 6 varied from a
maximum of 36 mg/1 to a minimum of 8 mg/l0 During the Phase
2 operation with oxygen enriched atmosphere over Stage 1 the
influent varied from 60 to 255 mg/l while the values for
Stage 6 were between 23 and 5 mg/r In general it would
appear that the B0O.D.5 of the downstream stage eff luen-L ¦.
was confined to a range of one half to twice the average, thus
defining the relative stability of the process„
ORGANIC REMOVAL IN TERMS OF C.O.D.
The performance of the 10 stage treatment section vas evalu-
ated during Phase 1 as to the effect on C.0oD0 The data
obtained is expressed in the form of monthly averages in
Table 40 The average influent Co00D0 concentration was 304
mg/1 which was reduced to the level of 66 mg/1 after Stage
10, leaving 22% of the influent C.O0D0 in that effluento
The data obtained relative to C.00D0 concentrations during
Phase 2 is presented in the form of monthly averages in
Table 5. Sequential treatment by 4 stages reduced the
average C«,0#D«, of 245 mg/1 to 67 mg/l0
In order to evaluate the individual and comparative per-
formances of the treatment with respect to C000D# for the
Phases 1 and 2, especially in upper stages, r.he average data
from Tables 4 and 5 has been plotted on semi-log scale in
Figure 2. The profile of C0O.D0 for Phase 1 shows an initial
rapid removal across Stage 1 and then a concentration de-
pendent removal rate between Stage3 2 and 5„ Although the
rate of removal of C00oDo decreases thereafter yet signifi-
cant reductions were still accomplished by Stages 6 and 100
As to the profile of C.O.D, during the Phase 2 operation,
an increased rate of removal took place across Stage 1,
with its oxygen enriched atmosphere, then the profile as-
sumed a direction about parallel to that in Phase 1„ In an
overall sense, the operation during Phase 2 was able to
remove the same percentage of C.0oD. using only 4 stages as
was attained with 7 stages during Phase lo
ORGANIC REMOVAL IN TERMS OF TOTAL ORGANIC CARBON
Data was not obtained relative to the poncentration of total
carbonaceous matter during the Phase 1 operation0 However
such data was secured for the influent to the pilot plant and
for the effluents from the various stages during the operating
period March to June 1970o This period is designated as Phase
30 All stages of treatment were exposed tc normal atmosphere
19
-------
TABLE 4
PROFILE OF MONTHLY AVERAGE OF C.O.D. Mg/1
PHASE 1
Mo.
Inf 1.
1
2
3
4
Stage
5
NO.
6
7
8
9
10
July 1969
251
135
99
90
63
50
50
46
38
49
42
Aug.
288
201
166
144
122
108
103
90
88
76
68
Sept.
316
249
179
170
146
125
126
111
99
100
89
Oct.
295
*
*
163
129
105
91
86
82
73
66
Nov.
371
249
210
192
126
114
100
78
92
80
65
AVER.
304
208
164
152
117
100
94
82
80
76
66
% REM.
69
54
50
39
33
31
27
26
25
22
*Step
feed to stages 1 and 2, samples taken in error and so not repeated.
-------
TABLE 5
PROFILE OF MONTHLY AVERAGES OF C.O.D. Mg/1
PHASE 2
Stage No.
Month
Infl.
1
2
3
4
August 1970
238
138
84
73
-
October
232
127
101
75
63
November
266
129
96
78
72
AVERAGE
245
130
94
75
67
% REMAIN
53
38
31
27
21
-------
100
90
80
LEGEND
X Phase I data-See Table 4
0 Phase 2 data-See Table 5
70
60
50
g4°-
3*
i
a
o
o
30-
RG 2-COMPARATIVE PROFILES OF C.O.D. for
OPERATION PHASES I and 2
STAGE NUMBER
22
-------
during this period of operation. Accordingly a comparison of
total organic carbon profiles between operating Phases 2 and
3 was made possible. The flow treated during Phases 2 and 3
was held at 7.5 gpm. The temperature of the wastewater during
Phase 3 ranged between 58° and 72°F. compared to a slightly
higher range of 62° to 78°F. for the Phase 2 operation.
The data obtained relative to Total Organic Carbon (T.O.C.)
and Dissolved Total Organic Carbon (D.T.O.C.) has been pre-
sented in Table 6 in the form of monthly averages for the
influent to the pilot plant and the effluents from the stages.
The difference between the T.O.C. and the D.T.O.C., or the
suspended organic carbon (S.O.C.), has been included in the
averages for the Phase 3 operation.
For comparative purposes the T.O.C. data for the Phase 2
operation has been presented in Table 7.
In order to show the shape and direction of these profiles
through the 10 stage treatment section, the profiles of the
averages percentage of T.O.C. for the Phase 2 and 3 operations
has been plotted on semi-log scale in Figure 3. It can be
seen that the Phase 3 profile follows a straight line through
Stages 1 to 5 then the rate decreased quite markedly. During
the Phase 2 operation, when the slimes in Stage 1 were exposed
to atmospheres enriched with oxygen, there was a significant
increase in the rate of removal across that stage. Thereafter
a break in the curve can be noted at Stage 2. At Stage 5 the
two profiles join and assume the same general position and
direction to stage 10.
To shed light on the nature of the acceleration of Stage 1,
Figures 4 and 5 were plotted, which show, respectively, the
comparative profiles of D.T.O.C. and S.O.C. As to the D.T.O.C
profile in Figure 4, it can be seen that the curve for Phase
3 follows a straight line to Stage 5 and thereafter proceeds
at a decreased rate to Stage 10. From inspection of the curve
for Phase 2, it can be seen that a rapid increase in the rate
of removal of dissolved organics was accomplished by Stage 1
when the slimes in that stage were exposed to an atmosphere
enriched with oxygen. Between Stages £ and 3, the curve almost
parallels the profile for Phase 3 and thereafter decreases to
a rate parallel to that Phase 2.
Relative to Figure 5, which illustrates the profiles of S.O.C.
23
-------
TABLE 6
PROFILE OF MONTHLY AVERAGES OF TOTAL ORGANIC CARBON (T.O.C.J
AND
DISSOLVED
TOTAL
ORGANIC
CARSON
(D.T.O
.C.)
Mg/1
PHASE
3
Stage
NO.
Mo.
Infl.
1
2
3
4
5
6
7
8
9
10
Mar. TOC
85
67
51
35
26
21
18
14
15
13
13
DTOC
38
31
27
21
18
15
14
14
14
12
11
Apr. TOG
91
60
46
37
33
18
19
13
14
13
12
DTOC
35
27
18
18
19
15
17
14
12
11
11
May TOC
95
65
50
34
28
20
18
16
13
13
11
nmr-
39
28
23
19
18
15
13
11
1?
10
10
U A -
Jun TOC
94*
50*
44*
38
29
14
17
16
12
12
10
DTOC
30*
23*
17*
17
15
12
12
13
11
11
10
AVER. TOC
90
64
49
36
29
18
18
15
14
13
12
DTOC
37
29
23
19
18
14
14
13
12
11
11
SOC
53
35
26
17
11
4
4
2
2
2
2
% REM TOC
71
54
40
32
20
20
17
15
14
13
DTOC
78
66
54
52
40
40
37
34
31
31
SOC
66
45
30
20
7
7
4
4
4
4
•Plow
split between. stares 1 and 2, valves omitted from average.
-------
TABLE 7
PROFILE OF MONTHLY AVERAGES OF TOTAL ORGANIC CARBON (TOC)
AND DISSOLVED TOTAL ORGANIC CARBON (DTOC) Mg/1
PHASE 2
Month
Inf 1.
1
2
3
Stage No.
4
5
6
7
August TOC
64
31
20
18
15
13
12
11
DTOC
24
16
13
12
12
11
10
11
October TOC
78
38
29
21
18
17
16
14
DTOC
37
21
18
15
14
13
13
11
November TOC
82
41
29
26
20
17
15
14
DTOC
41
18
17
15
15
14
12
12
AVERAGE TOC
75
37
26
22
18
16
14
13
DTOC
34
18
16
14
14
13
12
12
SOC
41
19
10
8
4
3
2
1
% REMAIN TOC
49
35
29
24
21
19
17
DTOC
53
47
41
41
38
35
35
SOC
46
24
20
10
n
5
2
-------
lOOj
90
80
60
X
50
40
X
3$ 20
X
x
LEGEND
X Phase 3 data-See Table 6
0 Phase 2 data-See Table 7
FIG 3-COMPARATIVE PROFILES OF T.O.G for
OPERATION PHASES 2 and 3
STAGE NUMBER
26
-------
100
90
80
70
60
z 50
30
LEGEND
X Phase 3 data-See Tabic 6
0 Phase 2 data-See Table i
FIG 4 - COMPARATIVE PROFILES OF D.T.O.C. for
OPERATION PHASES 2 and 3
STAGE NUMBER
27
-------
\
LEGEND
X Phase 3 data-See Table 6
G Phase 2 data-See Table 7
FIG 5-COMPARATIVE PROFILES
OF S.O.C. for
OPERATION PHASES 2 and 3
4
__L
6
JL
7
1
10 11
STAGE NUMBER
28
-------
for operating Phases 2 and 3, it can be seen that the removal
of suspended organic carbon during Phase 3 was concentration
dependent at least until 96% had been removed. The compara-
tive profile for operation Phase 2, when Stage 1 was enclosed
in an atmosphere with oxygen, shows that an increase in the
rate of removing suspended matter was experienced across Stage
1 and 2. However, between Stages 3 and 7 the curve assumes
a straight line parellel to the profile of Phase 3. It can
thus be seen from Figures 4 and 5 that the acceleration in
removal of organics across Stage 1 was mainly the result of
the increased rate of removal of dissolved organics.
ORGANIC REMOVAL IN TERMS OF SUSPENDED SOLIDS
During the Phase 1 operation samples of the influent to the
pilot plant and the effluents from Stages 1 to 10 were analyzed
for suspended solids. The data obtained is shown in Table 8.
The average monthly influent to the pilot plant ranged from
35 to 132 mg/l while the effluent from Stage 10 varied from
5 to 13 mg/l. Based on the raw wastewater to the main plant
which contained 160 mg/l of suspended solids, an average re-
moval of 90% was attained between the fifth and sixth stages
of treatment.
USING THREE STAGES
Since it was observed that enrichment of the atmosphere over
Stage 1 had accelerated the removal of organics, it was decided
to test whether the enrichment of an additional stage would
provide further acceleration to the process. Accordingly, a
hood was placed over Stage 7, which had been equipped with
71 disks. The flow of wastewater being treated was bypassed
from the effluent of Stage 2 to the influent of Stage 7. Thus
Stage 7 became Stage 3 during the month of September 1970
v/hich shall be designated as operation Phase 4. For this
operation which used only 3 stages, tankage oxygen was fed to
Stage 3 at a rate of .8 to 1.2 liters/min which raised the
percentage of oxygen in the gasses'mder the hood to the range
of 35 to 40%. Stage 2 was open to the atmosphere while the
hood of Stage 1 contained an atmosphere enriched with oxygen
to the range of 50 to 70%. The effective number of disks on
Stage 1 was 60 and on State 2 - 71. The results obtained
during this three stage operation, with hoods on Stages 1 and
3 are compared with the former operation when only Stage 1
was equipped with a hood, in Table 9. This Table includes the
values of the B.O.D.^, T.O.C., D.T.O.C., C.O.D. and N03~N for
the influent, and the effluents from Stages 1, 2 and 3 for
29
-------
TABLE 8
PROFILE OF SUSPENDED SOLIDS - Mg/1
MONTHLY AVERAGES
Stage No.
Mo,
Inf 1.
1
2
4
5
6
7
8
9
10
July 1969
85
39
30
29
19
14
9
8
6
7
5
August
102
61
50
35
21
16
12
12
10
10
9
Sep terrier
105
73
65
45
37
23
20
15
14
15
11
October
109
—
--
63
46
25
21
20
16
15
13
November
132
89
58
56
23
16
13
12
13
11
10
AVERAGE
107
66
51
44
29
19
15
13
12
12
10
% REMAIN
61
48
41
27
18
14
12
11
11
9
-------
TABLE 9
THREE STAGE TREATMENT RESULTS
PHASE 2 PHASE 4
Oxygen Enrichment on Stage 1 Oxygen Enrichment on Stages 1 &2
Pilot
Infl.
1
Stage No.
2
3
Pilot
Infl.
1
Stage No.
2
3
B.O. D.
101
33
23
16
96
27
14
10
T.O.C.
74
37
26
22
70
30
17
13
D.T.O.Co
34
18
16
14
40
19
12
11
C.O.D.
245
131
94
75
253
101
82
50
NO -N
0
0
0
0
0
0
.4
7
-------
operation Phases 2 and 4, when flow conditions and wastewater
temperatures were essentially the same0 An improved quality
of effluent, measured in terms of B.00D05# T.0oCo, DoTo0oCo
and C0O.D0# was produced as a result of enriching the atmos-
phere over the third stage. In Phr ~2 4 no+ only hart the
removal of carbonaceous matter improved with respect to a-1
parameters, but 706 mg/1 of nitrates were produced0 Thus
about 18 minutes of contact with the slimes in Stages 1, 2
and 3 during the Phase 4 operation was sufficient to carry
the oxidation process through the carbonaceous zone and well
into the nitrogenous zoneD
NITRIFICATION
The nitrite and nitrate concentrations through the 10 stages
of treatment are shown in Table 10 as monthly and phase
averages for operating Phases 1„ 2, 3 and 4 when 705 gpm of
primary tank effluent from the main plant was being treated.
An exception to that procedure was made during December 1969
and January 1970 previously designated as Phase 5 when a 7»5
gpm constant flow portion of the modified aeration effluent
rather than primary tank effluent from the main plant was
treated to test the upgrading capacity of the pilot plante
The modified aeration effluent contained an average of 57
mg/1 of BoOoDog.
The data obtained shows that nitrification started at Stage 5
during Phase 1, and 3 when all stages were exposed to normal
atmosphereso During those periods the effluents from sub-
sequent stages contained a rather constant 1 to 2 mg/1 of
nitrites while the concentration of nitrates increased down-
streamo During the Phase 2 operation, when Stage 1 was en-
riched with oxygen, nitrification had started between Stages
3 and 4 and had reached a concentration at Stage 7 which had
only been reached previously between Stages 9 and 10o During
the Phase 4 operation when Stages 1 and 3 were enriched with
oxygen a nitrate concentration of 706 mg/1 was contained in
the effluent from Stage 3„ This concentration of nitrates
had not been reached during the Phase 2 operation until some-
where between Stages 6 and 70
The profiles of the average nitrate concentration for the
various phases has been plotted in Figure 60 The profiles
for operating Phases 1, 3 and 4 are substantially parallel
and linearo The five stages 6, 7, 8, 9 and 10 produced 10
mg/1 of nitrates in addition to 105 mg/1 of nitrites0 It is
32
-------
TABLE 10
PROFILE OF MONTHLY AVERAGES
no2/no3 -'N
Mg/1
Stage No.
Mo. Inf. 1 2_ 3 4
5 6
7
8
9
10
Aug„ 69
.4/.2 1.5/. 7
1.6/2.9
1.7/4 ,7+
1.7/6.8+
1.6/8.1+
Sept. 69
.8/.4 1.2/1.2
1.6/3.0
1.5/5.7
1.2/8.1
1.3/10.3
Oct. 69
.6/.3 1.3/.8
1.4/2 .7
1.4/5.2
1.6/6.2
1.4/8.1
Nov. 69
L.0/.5 1.4/.8
1.3/3.0
1.2/5.6
1.3/8.2
1.0/9.7
AVERAGE AUG. TO NOV. 69
PHASE 1
.7/.4 1.4/. 9
1.5/2.9
1.5/5.3+
1.5/7.1+
1.5/9.0+
Dec. 63 (2nd half)
1.0/.8 1.0/2.8
1.1/5.1
1.1/6.6
1 . 2/10 . 8
1.1/12 .0
Jan„ 70
1.2/2.3
1.3/4.9
1. 5/5 .14"
2.0/5.9
2.2/7.8
AVERAGE 2nd HALF DEC. 69
AND JAN. 70
1.0/.8 1.1/2.5
1.2/5.0
1.3/5.9+
1.6/8.4
1.7/9.9
1 Iirvil'Ij ->
May 70
-/ - 6 - /1_. 7
-/3 .0
-/5.3
00
\
l
-/10.3
June 70
-/I. 8
-/5.2
-./6 .6
-/10.2
-/ll.3
AVERAGE MAY & JUNE 70
PHASE 3
-/.6 -/1.8
-/4.1
-/6.0
-/9 .0
~/10.8
Aug. 70* -/.5 -/2.1
-/4 . 8 -/8.5
~/14 .
3
Oct. 70* -/- 5
-/I•9 ~/4 .1
-/7 . 2
Nov. 70* -/I.5
-/2.9 -/5.7
-/7.0
AVERAGE AUG.,OCT.,NQV.70
PHASE 2
Seot. 70*' -/ 04 ~/7.6
PHAS E 4
Note: *Oxygen er.ric>..v.=r.t ever st
?.ce 1,
*"Ox,"cen er.ricr~£-r.t cv = r st:
= 2 3.
-------
10
8
D>
2
i
•z.
i
to
O
z
4
LEGEND
X Operation phase I
G "5
Q " "3
A " "2
- "4
FIG 6-COMPARATIVE PROFILES of NITRATE PRODUCED
N0TES=(l) All data shown obtained with flow of 7.5 gpm. (constant)
(2)During pho93 5 trooting modified ooration efflufint B0Ds»57mg/l
(3) During phaso 2, stoga 7 equipped with 71 disks
(4) During operation phase 4, stage 7 equipped with 71 disks
(5)Operation phases described under removal of organics
1
6
i
8
10
STAGE NUMBER
34
-------
interesting to riote that Curing the Phase 5 operation in t'..u
winter months when wastewater temperatures were in the
of 5S° to 62°F0.. nitrification proceeded at only a slightly
lower rate compared to the other periods when temperatures
v/ers considerably higher«
During the Phase 2 operation it car. be seen from Figure 6
that whan Stage 1 was equipped with a hood enclosing an
atmosphere enriched with cxyren, nitrification v;as shifted
about two stages upstream from that in Phase 1 and procooucc.
at the same rate0 It can also be noted from an inspection
of Figure 7 that the Stage 7 value fails considerably above
the curveo This was the result of having increased the
number of disks in Stage 7 by about 48%0
During the Phase 4 operation,, when both Stages 1 and 3 were
equipped with hoods enclosing atmospheres enriched with
oxygen not only were the nitrifiers active further upstream,
but the rate of nitrate production was markedly increasedt
The curve shows that 7C2 mg/i wars produced in Stage 3 which
had a detention time of 6 minutes0 This was at a rate of
702 mg/i per hour of contact with the 900 sq» ft» of nitrify-
ing slimes on the disks of Stage 3 (formerly Stage 7)c
The data relating to the concentration of ammonia nitrogen
for the influent and effluents from Stages 1 to 10 during
the Phase 1 and 5 operations is shown in Table 110 It can
be seen that an average of about 13 mg/1 of NH->-N entered
the pilot plante which value increased to 15 mg/1 during
the first stage of treatmentc That concentration remained
until the 3rd or 4th Stage and thereafter decreased after
St^ge 10 to a level of Gc7 mg/1 during Phase 1 and to 4o4
mg/1 during Phase 5 operation,. These decreases are in
general agreement quantitatively with the total of the
nitrite and nitrate production values0
During the operation Phases 2, 3 and 4, the determinations
for total oxidizable nitrogen included the albuminoid nitrogen
as well as the ammonia nitrogen0 These monthly values are
presented in Table 120 It can be seen on a monthly average
basis that 22 to 25 mg/1 of such oxidizable nitrogen entered
the pilot planto That concentration was reduced to 14 mg/1
at the end of Stage 10 during the Phase 3 operation0 During
the Phase 2 operation the concentration was reduced to 8 mg/1
leaving Stage 7 during August* v/hile during October and
35
-------
TABLE .11
PROFILES OF WO'sTHI-Y AV
Ko« Inf 1. 1 2 3 4 _
12.3 12.6
13.4 12.3
16.5 3G.f?
14.1 14.7
14 . 1 14.1
2nd Half
Dec, 69 12.5 14.2 14.7 13.9 13.S 14.3
Jan. 70 12.1 16.6 16.2 16.3 15.3 13. S
AVER, (2) 12.3 15.4 15.5 15.1 14. G 14.1
(1) Phase 1 operation described under removal of o
(2) Only operation?.! exception to treating prin&rv
v.'e?.thfer period \;hen rr-.od if led f.&rctior. r-rf: uer.t
5£;° to 62° F., B. 0. D. rj of 57 ir.g/1 v:&s treated .
Aug c
Sept.
Oct B
Nov K
69 13 . 8
13 . 1
14 . 6
11.6
13 .5
13. 9
16 . 1
16. 1
14.8
13.7
13.7
15.8
15.6
14 . 7
12.9
13.8
17.3
15 .6
14 .9
GE? :¦:?/!
6 7_
12.5 9.8
12.0 10.4
15.7 14.2
13.7 13.0
13.5 11.9
11.4 10.1
10.6 9.5
11.0 5.8
8___ __ 9 10 _
7.2 4.6 3.3
8.0 5.8 5.2
12.8 10.9 9.8
11.7 9.7 8.4
9_._9 _ _ 7 . 6.7
8.2 6.5
7.5 4.9 4.4
7.9 5.7 4.4
nxos .
fluent v.'ap
dur incr
n cold
-------
TABLE
: 12
PROF
1LFS
OF ALBU'
MINOID AND AM'
¦SON IAC-AL
NITROGEN
MON
T'HLY AVF
_r.\ge:s
¦
Mo .
I n £ 1.
1
2
3
4
5
6
7
8
9
10
Kay 7 0
23
22
22
23
23
24
22
21
3 S
16
14
June
23
23
23
23
25
2 5
2 3
IS
1G
J 5
14
AVER , (.1)
23
23
23
23
24
25
23
20
17
16
j 4
Aug.
22
20
21
21
18
16
12
8
--
Oct.
25
25
26
27
24
23
21
18
- -
Nov.
2 4
23
24
23
22
21
18
17
--
--
AVER.(2)
24
23
24
24
21
20
17
14
_..
_.
1970
Sept, (3)
24
23
24
18
(1) May and June, 7.5 g.p.m. primary effluent treated temperature, of
v:astev:ater 65° to 70° F.
(2) Phase 2 operation with oxygen enrichment over stage 1. Flov:
treated 7.5 g.p.m.
(3) Dur ing Sept. 3 9 7 0, f 1 ov; 7.5 g.p. ih .
-------
November, 18 and 17 mg/l remained in the effluent from Stage
7. During Phase 5 operation in September 1970 the concentra-
tion of oxidizable nitrogen reached a level of 18 mg/l at
Stage 3 which concentration had not been attained until having
passed through Stage 7 in October and November.
BICARBONATE ALKALINITY
The reduction of alkalinity resulting from the process of
nitrification has been established. Accordingly, it seems
appropriate, at this time, to present profile data, relating
to alkalinity concentrations, taken concurrently with that
of nitrification so as to be able to evaluate the ratios of
alkalinity reduction to nitrate production during the in-
vestigation .
The alkalinity profiles taken have been averaged for the
individual months included in operating Phases 2 and 3 and
are shown in Table 13. The production of nitrates (from
Table 10) for the various stages of treatment is represented
below the corresponding decreases of alkalinity. Also shown
are the calculated ratios of alkalinity reduced per unit of
nitrates produced. Since the nitrite concentrations were
found during the Phase 1 operation to lie in the range of
.7 to 1.5 mg/l, irrespective of the nitrate levels, they
were not determined during the subsequent phases of opera-
tionc It can be seen from the data in Table 14 in con-
junction with Table 10 that:
Month Stage No. Alk./NO^ Ratio
May'70 Stage 10 79/10.3 =7.8 mg/l of alk. red./mg NO3 prod
June'70 " " 89/11/3 =7.9
Aug '70 " 7 97/14.3 = 6.8
Sept'70 " 3 47/7.6 =6.2
Oct '70 " 7 56/7.2 = 7.8
Nov '70 " 7 56/7.0 =8.0
Average = 7.4
Only the ratios for the downstream stages were calculated for
the reason that the omission of nitrites would exert the last
influence on those values. When considering the fact that the
nitrites were about 1 mg/l, thus constituting about 10% of
the sum of the nitrites and nitrates, it can be seen that the
average value would be reduced from 7.4 to 6.7 mg/l of bicar-
bonate alkalinity reduced per mg/l of nitrogen oxidized.
38
-------
TABLE 13
PROFILE OF HCO3 ALKALINITY AND NITRATE NITROGEN Mg/l
Month Inf1 .
1
2
3
4
5
6
7
8
9
10
May 1970 217
Alkalinity red„ mg/1
Nitrates produced mg/l
208
207
213
215
209
6
1.6
204
11
1.7
178
37
3.0
161
54
5.3
142
73
7.8
136
79
10 .3
June 1970 212
Alkalinity red. mg/1
NO3 pv.- -ced mg/1
213
216
214
224
221
203
18
1.8
173
48
5.2
158
63
6 . 6
146
75
10.2
132
89
11.3
August 1970 200
Alkalinity red. mg/1
NO3 produced ma/1
200
200
194
6
.5
170
24
2.1
147
47
4.8
127
67
8.5
97
97
14.3
—
:
-
September 1970 217
Alkalinity red. mg/1
NO3 produced mg/1
205
206
11
.4
170
47
7.6
October 1970 2 28
Alkalinity red. mg/1
NO3 produced mg/1
223
228
229
219
10
.5
215
14
1.9
192
37
4.1
173
56
7.2
November 1970 213
Alkalinity red. mg/l
NO3 produced mg/l
209
210
208
2
194
16
1.5
2.9
165
45
5.7
151
59
7.0
-------
TABLE 14
C02 ACIDITY Mg/1 - MONTHLY AVERAGES
Stage No.
Month
Infl.
1
2
3
4
5
6
7
8
9
10
fey
1970
32
26
23
21
21
18
18
17
19
20
18
June
1970
29
23
21
19
17
17
10
17
—
—
13
Aug.
1970
26
39d)
17
15
15
15
15
14
--
Sep!"
"* 970
23
49(1)
22
46(2>
—
Octj
i. >¦ / 0
32
49 (D
36
27
25
21
22
32
Nov.
1970
40
55
38
29
28
27
32(2)
(1) Stage 1 equipped with hood August 1970, September 1970/ October 1970 and
November 1970.
(2) Hood on stage 3 during September 1970 and stage 7 during October and
November 1970.
-------
Referring again to Tabic 13, it should be pointed out that
the nuiaber of disks on Stare 7 were increased from 48 to 71
or. May 13, 1970 and by June the nitrifying cultures had bo-
come established and the rate of nitrate production increasec?.
Starting at the end of August 1970 a hood enclosing an at-
mosphere enriched with oxygen was placed over Stage 7. The
data represented in Table 13 for Stage 7 was obtained during
October and November 1970 while the percentage- of oxygen in
the atmosphere over Stage 7 varied between 40 and 60% of tu.;
atmosphere.
C02 ACIDITY
Profile data relating to CO2 acidity was taken for the period
May to November 1970 {excepting July 1970) and is shown in
Table 14. During May and June 197 0 there was a decrease of
6 mg/1 across Stage 1 and a further drop of about 2 mg/1 through
Stage 2. Thereafter a slow further decrease took place of about
5 mg/1 while passing through Stages 3 to 7.
During Phase 4 (months of August, October and November 1970)
when Stage 1 was enriched with oxygen, the concentration of
C02 increased by 13 mg/1, 17 mg/1 and 15 mg/1 respectively for
those months. Passage through Stage 2 removed 22 mg/l, 13 mg/1
and 17 mg/1 respectively during the same months. The increase:?
in C0>2 concentration across Stage 7 during October and November
1970, was concurrent with a hood being used over that stage which
enclosed an atmosphere enriched with oxygen.
During Phase 4 (September 1970) the CO2 acidity increased from
23 to 49 mg/1 passing through Stage 1, was lowered to 22 by
Stage 2 and then increased to 46 as a result of treatment in
Stage 3 which was equipped with a hood and oxygen enriched
atmosphere.
pH VALUE
The pH value of the influent to the pilot plant was generally
7.2 Z 0.3 during the Phase 1 (July to November 1969) operation
as can be ceen from the data compiled in Appendix Table 1. The
pH of the wastewater being treated increased to 7.4 .2 while
passing through the first five stages of treatment. While pas-
sing through Stages 6 to 10 the pH value of the wastewater being
treated was lowered slightly by about .2 to .4.
During the Phase2(August, October, November 1970) operation the
pH value or the influent being 7.3 ± .2 was depressed by about
.2 to .4 while passing through Stage 1 which was equipped with a
hood enclosing an atmosphere enriched with oxygen. It can be
noted that while passing through Stage 2 the pH increased again
by about the name amount as the drop across Stage 1.
41
-------
During the Phase 4 (September 1970) operation, the pH de-
creased from 704 to 7„0 during passage through Stage 1 was
restored to 704 through Stage 2 and then again dropped to
609 passing through Stage 3o
ORTHO PI'OSO PHATES
During the Pha3e 1 operation profiles of the orthophosophate
concentration passing through the ten stages of operation
indicated a decrease of 1 to 3 mg/l0 expressed as P0^o When
Stage 1 was equipped with a hood enclosing an atmosphere
enriched with oxygen, profiles of orthophosphates were made
and the data is presented in Table 15 for the months or the
Phase 2 operation and the month of September 19700 This
data shows that for the Phase 2 operation, there was an
initial decrease of some 2 to 3 mg/1 across Stage 1 followed
by a slow decrease in concentration0 The monthly average
removal was 4 to 7 mg/l of PO^ through the 7 stages of
treatmento
When operating with hoods over both Stages 1 and 3 during
September 1970, there was no significant increase in the
removal of orthophosphates across the third stage relative
to that found during Phase 20
LIME TREATMENT FOR PHOSPHATE REMOVAL
It had been observed for some time that the downstream
stages, that is 6 to 10, were capable of oxidizing a large
fraction of the ammoniac Providing additional stages or
increasing the surface concentration in the subject stages
would make possible the complete oxidation of ammonia0
It was shown by an analysis of the data obtained during
this investigation that the alkalinity was reduced by aboat
7 mg/1 for each mg/1 of ammonia oxidized0 Generally the
alkalinity of the influent was 200 mg/1 and the effluent
from the algal unit contained about 65 mg/l0 Accordingly^
such reduction in alkalinity makes possible influencing
the pH upwardly using only a fraction of the conventional
lime dosage, A test was run on the effects of varying the
lime dosages on the pH of the influent to the pilot plant
and the effluent from the algal unito The data is presented
in Table 16c This data shows that to reach a pH of llo0
only about 20% of the lime dosage would be requiredo
42
-------
TABLE 15
ORTHOPHOSPHATES Mg/1
MONTHLY AVERAGES AS PC>4
Mo n th
Infl.
1
2
3
4
5
6
7 8
Aug. 19 7 0
16 .8
15.0(1)
14 .1
13.8
11 .3
12.1
13.5
12.9
Sept. 1970
21.0
17.6(1>
16.3
15.7
(1)
Oct. 1970
22.6
19.5(1>
20.9
17 .9
16 .5
-
17.0
15.4*"
Nov. 1970
20.8
17.2
17.2
14 .2
14.1
X4.2'1'
Note: (1) Hood over stage
-------
TABLE 16
COMPARATIVE EFFECT OF ADDING LIME TO THE INFLUENT TO A
PILOT PLANT AND TO THE EFFLUENT FROM ALGAL UNIT
Dose Mg/1
as Ca(OH)2
Infl.
PH
Dose Mg/1
as Ca(OH)2
Effluent
Algal Unit pH
50
8.7
15
8.8
100
9.6
33
10.5
200
CO
»
o
1—1
65
11.9
300
11.7
100
12.8
400
12.9
135
13.4
44
-------
A follow up comparative test was made to evaluate the in-
fluence of lime dosage on both the pH ana the orthophosphate
concentration in the supernatant liquor after treatment* A
sample of the influent to the pilot plant and of the ef-
fluent from the algal unit were treated with lime0 The data
obtained is shown in Table 17<> The data sh'X/s that only
about 33/6 of the lime was required atcer the alkalinity h&.1
been largely destroyed by nitrificationc It can also be seen
from the table that about 100 mg/1 of lime lowered the
phosphate level to 1 mg/1 as opposed to 250 mg/1 of lime
being required to accomplish the same reduction when treating
the influento However it should be pointed out that the
sludge produced v/hen treating the effluent from the alg.-rl
unit was diffuse and resisted compaction much more than the
sludge formed when treating the influento
TREATMENT OF jy/JDXFIED AERATION EFFLUENT
REMOVAL OF ORGANICS
From the beginning of the pilot plant operation through
Phases 1, 2, 3, and 4 only data pertaining to the treatment
of primary tank effluent was obtained0 In order to gain
information as to the capacity of the pilot plant to upgrade
the performance of an intermediate treatment process, the
effluent from the final settling tank of the modified
aeration process of the main plant was conducted to the
pilot plant for treatment starting 12/18/69& During this
operation the flow of wastewater v/as maintained at 7e5 gpm,
all 10 stages were exposed to normal atmosphere,* the disks
in Stages 1 to 5 were rotated at 10 RoP0M„# the disks in
6 to 10 vrore rotated at 6 R0P0M0 All rotation opposed the
flow of wastewater during this operation which has been
designated Phase 5« The samples of the effluents from the
various stages were prepared for analysis by hand micro-
ctraining (35 micron) from 12/18/69 to 1/14/70 end by
quiescent settling for 20 minutes from 1/15/70 to 2/9/70,,
Accordingly it was intended to secure data relative to the
effect of microstraining versus short period settling on
the profiles of residual organics0
After it was shown that the first 5 stages of treatment had
removed the no0oD,5 to a resistance level, subsequent deter-
minations were limited to the effluents from those stages°
In or. cf.Cort to take a closer look at the mechanism of B.0„DO5
45
-------
TABLE 17
COMPARATIVE EFFECTS OF ADDING LIME TO THE INFLUENT
TO PILOT PLANT THE EFFLUENT FROM THE ALGAL UNIT
Dose Lime
Influent
Algal
Unit
as Ca(OH)2
pH
P04 Mg/1
PH
P04 Mg/1
0
7.2
10.9
7.7
14.9
50
8.7
10.9
9.7
3.4
100
9.2
7.5
10.4
1.1
150
9.6
2.5
11.0
1.0
200
9.9
1.8
11.2
0.4
250
10.4
1.1
11.2
0.5
300
10.7
0.8
11.3
0.3
46
-------
removal during the initial stages of treatment* B.O0D05
determinations were made on the filtrate from #40 YJhatman
paper of samples taken from the pilot influent and the ef-
fluents from Stages 1 to 3,
The data relating to suspended solids B.0oD,5 and Co0oDo
were obtained for the periods (1) when the effluents from
the stages were microstrained and (2) when the effluents
were settled for 20 minutes, has been presented in Table 180
The modified effluent contained about 65 mg/1 of suspended
solids, 57 mg/1 of B.O.D05 and about 150 mg/1 of Co0«Do
In order to see the shape and direction of the profiles,
the B.0oDo5 data has been plotted on semi-log scale in
figure 7, During both periods, an initial drop in Bo0rDo5
was effected during the 6 minute contact with the slimes on
the dinks of Stage lu It can be noted that an accelerated
removal of BoO.Do^ took place during the second period when
passing through Stages 3 and 4« Dense populations of stalked
ciliatcs were found to have colonized the slimes on those
stages during the second period0 This biased the data in
favor of plain settling over microstraining0 It was observers
that the solids generated on the disks settled rather rapid.lyff
which would be corroborated by the data secured on the ef-
fluents after only 20 minute settling.
The filtrate B0O.D05 data has been superimposed on Figure 70
A large proportion of the filtrate B0O0D.5 was removed across
Stage 10 Thereafter the rate of removal of filtrate Bo0oDCtj
decreased until it was lowered to 10 mg/1 at Stage 3o It
can be seen from the data relating to the second period that
the difference between the total Bo0oD8^, 57 mg/1, of the
influent and the filtrate B00oDO5, 26 mg/1, was due to the
suspended solids in the modified aeration effluent being
treatedo Apparently the rate of removal of filtrate Ba0oD„5
was somewhat faster than the rate of removal of suspended
BoOaD„5 by Stage lc
Referring to Figure 1f it can be seen that about 1.8 stages
of treatment reduced the Bo0.Do^ to 30 mg/1 which would be
equivalent to a 80% removal of the B„00D0^ of the raw waste-
water «, About twice the number of stages of treatment were
required to reduce the Ec0oDO5 to 15 mg/1 representing a
removal of 90%o
47
-------
TABLE 18
PROFILE OF ORGANIC REMOVAL TREATING MODIFIED AERATION
EFFLUENT CONCENTRATIONS IN Mg/1
PHASE 5 OPERATION
Infl.
1
2
3
4
Stage
5
No.
6
7
8
9
10
12/18/69 to 1/14/70
Suspended Solids 65
46
36
30
24
20
17
17
15
12
14
B.OcD.j 57
35
26
23
17
14
10
9
8
8
8
C.O.D. 141
114
96
94
81
80
73
66
62
60
57
1/15/70 to 2/9/70
Suspended Solids 71
47
39
26
20
14
B.0.D.5 57
37
29
18
12
11
B.O.D.^ Filtrate 26
15
12
10
C.O„D. 157
120
101
87
75
68
-------
LEGEND
X B0D5 12/ki/69 fo 1/14/70
0 BODs 1/15/70 to 2/9/70
0 RLTRATE BODs 1/15/70 to
2/9/70
FIG 7-REMOVAL OF BODs from
MOOTED AERATION EFFLUENT
P
X x
u.
SI
2
i
3
i
6
_t_
8
STAGE DUMBER
49
-------
Referring to Table 18<, the C«00D,, of the modified aeration
c£f3.uent of some 150 mg/1 vtt.s reduced to a resistance level
of about 60 mg/1 during treatment by 10 stages during the
first period and almost the same level after only 5 stages
of treatment during the second period0 The effectiveness
of treatment improved as the composition of the slimes
adjusted 'o the treatment of the modified aeration effluent^
while the temperature was decreasing from about 62°F0 in the
first period to 58°F» in the second period.
50
-------
SECTION VI
OPERATING RESULTS OP TREATMENT SUBSEQUENT TO 10 STAGE UNIT
FINAL SETTLING TANK
The method of choice to separate the suspended solids from
the Stage 10 effluent was by microstrainincr rather than by
settling for the reason that the rotating disk process
utilizing fixed slimes does not require the recycling of
such solids. However, to serve the purpose of physically
removing a large fraction of such solids an improvised
settling tank was placed in service following the 10 stage
unit. During the course of the operation from July 1969
through March 1970 the tank afforded about 1.5 hours of
settling (above Hopper) for the 3.5 gpm portion of the
effluent from Stage 10. The remaining 4 gpm portion of the
effluent from Stage 10 was conducted to waste.
It was felt that the tank unit volume treatment efficiency
could and should be improved. Accordingly, submerged sur-
faces were inserted into the tank upon which biological forms
could attach themselves and utilize a portion of the re-
sidual nutrients in the flow for their metabolism. Thus
during the end of March 1970 fifteen 1/8 inch thick plastic
vanes, each measuring 5.7 ft. X 2.5 ft., were inserted into
the tank below the water surface. This furnished 430 sq. ft.
of surface upon which the biological forms could develop.
About 4 to 6 mg/1 of dissolved oxygen was contained in the
influent to the settling tank which might serve their res-
pirational needs. A nitrate reserve was available for res-
piration in the event that dissolved oxygen was exhausted.
A diagram showing the dimensions of the settling tank and
the placement of the plastic vanes is shown in Figure 8.
Horizontal plastic pipes having 1/8 inch diameter orifices
on 4 inch centers were placed above the vanes to serve the
purpose of causing the flow to pass vertically and uniformily
upward over the tank area and so distribute the nutrients
to the slimes.
From April 1970 to November 1970 data was taken relative to
the concentrations of T.O.C. and D.T.O.C. for the influent
and effluent from the above described settling tank. From
the data shown in Table 19, it can be seen that during
passage of the flow through the tank the concentration of
T.O.C. was reduced from an average of 12 to 9 mg/l and that
the D.T.O.C. was similarly reduced from 10 to 8 mg/1.
Although only 2 mg/1 of D.T.O.C. was removed, yet, it was
51
-------
ELAN
SDE ELEVATION
BAFFLE
EFFL./
PTASZ lO^i
overflow
to clgoJ unit
30"
V
to drcin
FROMT ELEVATION
fiFT=L. frn> J
IMKf
vano
l/g" to c'rc.n
G- 1/2" plastic pipes orifice! with
1/8" dt'cmcfer holes on 13" catfcrs
along upper portion
HG C-FiWAL SETTLING TANK
52
-------
TABLE 19
REMOVAL OF TOTAL ORGANIC CARBON Ug/1)
BY FINAL SETTLING TANK EQUIPPED WITH SUBMERGED PLASTIC SURFACES
Final Settling Tank
Month Infl. Effl. Removal
1970
April TOC
12
10
2
DTOC
11
8
3
May TOC
11
11
0
DTOC
10
9
1
June TOC
10
8
2
DTOC
10
9
1
X
July TOC
9
7
2
DTOC
8
6
2
August TOC
12
9
3
DTOC
10
8
2
September TOC
13
10
3
DTOC
11
9
2
October TOC
14
9
5
DTOC
11
8
->
November TOC
12
9
3
DTOC
10
8
2
AVERAGE TOC
12
9
3
DTOC
10
8
2
Note: (a) Flow through final settling tank 3.5 g.p.m.
taken from stage 10, April 1970 to Aug. 9, 1970
taken from stage 7, Aug. 10, 197 0 to Sept. 4, 1970
taken from stage 3, Sept. 4, 1970 to Sept. 13, 1970
taken from stage 7, Sept. 18, 1970 to Oct. 28, 1970
taken from stage 10, Oct. 28, 1970 through
November 13, 1970
-------
substantial in that it constituted 25% of the organic load
to bo imposed on subsequent treatment by adsorption on acti-
vated carbon.
It was found with the beginning of the summer of 1970, that
although the bottom sludge was removed by drain each day
excessive gassing took place in the sludge deposits, whic
accumulated because of lack of sludge removal mechanism.
A 1/4 inch layer over the tank surface of buoyed sludge was
removed each morning by hand scraping. In an attempt to
alleviate the problem a 3.5 gpm portion of the effluent fron
Stage 7 was transferred to the settling tank rather than from
Ftage 10. This v/as done to suppress what appeared to b^
donitrification at the bottom of the settler. This new pro-
cedure was partially effective in suppressing the dentitri-
fication during the warmer period when wastewater temperatures
exceed 63CF. A mechanism capable of providing continuous
sludge removal would have been required to fully overcome
the problem.
INORGANIC NITROGEN
The data pertaining to the performance of the final settling
tank equipped with 430 sq. ft. of submerged vanes is shown
in Table 20. A total of about 25 mg/1 of albuminoid, ammonia
and nitrate nitrogen entered the tank and about 20 mg/1 was
contained in the effluent. The average monthly decrease
ranged from .7 mg/.l in July to 6.6 mg/1 in October 1970. The
ammonia nitrogen concentration decreased while the nitrate
nitrogen concentration was relatively unaffected.
ALGAL UFIT
The effluent from the final settling tank was conducted to
the 6 stage algal unit (algal Stages 11 to 16) which has been
describe:: previously. The objective of the use of this unit
-.••as to remove nutrients from the wastewater, mainly by algal
activity. The alternate exposure of the attached algae to
the overhead light source and then their immersion in the
".¦.•ar.tewa.ter would provide the environment necessary for their
growth and maintenar.ee. Such growths would be harvested from
a particular stage by first bypassing the flow around the
"tage, draining the contents, then removing the attached algae
by scraping. It would be feasible in this manner to remove
the wet growths and gain the advantage of rapid subsequent
regrowth, An alternate method of harvesting would be to dry
the algae in place under the influence of the lights and
54
-------
TABLE 20
CONCENTRATIONS OP INORGANIC NITROGEN PASSING THROUGH
FINAL SETTLING TANK Mg/1
Influent Effluent Decrease in
Month NH3-N N03~N Total NH3ON N03~N Total Total N
May 1970
13 . 6
10 .3
23 .9
11.0
9.2
20 . 2
3 .7
June
13.9
11.4
25.3
9.6
12 .1
21.7
3.6
July
4 .2
16 .3
20 . 5
5.0
14.8
19 .8
0.7
Aug„
6.0
15.6
21.6
3.3
14 .6
17 .9
3.7
Sept.
15.9
8.4
24 .3
12 .2
8.1
20 .3
4.0
Oct.
18.0
7.9
25.9
11.0
8.3
19 .3
6 .6
Nov.
10.5
10.8
21.3
5.5
9.5
15.0
6.3
(a) Pilot plant shut down from 6/14/70 to 7/8/70 due to gasoline explosion
in main plant.
(b) Final tank received effluent from stage 10 from May 1970 through 3/10/70,
8/10/70 to 9/4/70 from stage 7, from 9/4/70 to 9/18/70 from stage 3,
from 9/18/70 to 10/28/70 from stage 7 and thereafter from stage 10
throuah November 1970.
-------
remove them in a dry form.
As experience was gained in the operation of the unit it be-
came evident that the much desired green filaments were pro-
pagating only along the outer rims of the disks where the
light intensity was about 300 ft. candles. Thin attachr ?nts
of diatoms developed towards the interior of the disk in zones
where the light intensity exceeded 50 ft. candles. The light
hoods were lowered until the grow lux lamps were within an
inch of the rim of the disks and, as a consequence, the green
filaments grew inwardly for a distance of 3 to 6 inches from
the rims. Concurrent with these changes, the side of one of
the end disks on the first stage was illuminated with J
incandescent spotlights situated about 6 inches from the sur-
face being illuminated. Three concentrations of light, each
about 4 inches in diameter, were impinging on the side of the
rotating disk at an intensity of about 2000 f.c. The light
so pulsed by the disk rotation over small areas of surface
was sufficient to grow 1/8 inch diameter strands of green
filaments (woven by the disk rotation) in about 10 days.
The experiences during the first few months pointed out the
fact that dense growths of attached algae could be produced
when adequate light dosages of illumination were rendered.
It became evident that light intensities in the range of 1000
to 2000 f.c., applied directly to the exposed algal cells,
were necessary to produce reasonably accelerated growth rates.
During this initial period from July 1969 to December 1969 the
algal unit did considerable work with respect to other para-
meters. During the 72 minutes of contact with the wastewater
passing through the six stages it removed in total from the
final settling tank effluent (a) 4 mg/1 of suspended solids
(b) 4 mg/1 of B.0.D.5 (c) 10 mg/1 of C.O.D. and it increased
the concentration of nitrates by 4.7 mg/1.
Since the growth rates were relatively slow, considerable time
was spent in an attempt to evaluate the relative effects ex-
erted by nutrition, light intensity, light quality and disk
rotational velocity. The original unit was equipped with 2 ft
long low intensity grow lux fluorescent lamps. These lamps
produce an emission which places emphasis on the blue and red
portions of the spectrum, however the intensity was quite
insufficient being only 300 f.c. near their surface. To test
the effect of increasing the light intensity, the end disks
56
-------
of Stage 11 were illuminated with two 48 inch long Very High
Output Cool-White flourescent lamps# which produced 1000 f0c0
about 3 inches from their surface. Profuse filamentous
growths covered the disk surface in 10 days and grew outward
to a thickness of about 1/8 inch in 3 weeks0 Accordingly
another experiment was set up using the blended light fr >ir
one daylight very high output and one natural semi-soft white
very high output flourescent lamp which have emissions high
in the blue and red ranges of the spectrum,, After 2 weeks the
growth of filamentous algae entered the log phase
and a very substantial mass developed during the ensuing 7
dayso On the 21st day the stage was bypassed, then drained
and 500 ml of 4„2% dry algal solids were scraped from x.he
7 sq0 fto of surface on the end disk being investigated0 A
sticky brown material with some attached green filaments
remained on the disk surface after the harvest» Normal
flow was restored. One week later the new growth was
harvested in the same manner and the volume found to be
1000 ml having 4.88% solids# which indicated that the algal
production was 48 grams in 7 days over 7 sq. ft„ of surface>
Apparently the algae had entered the log growth phase im-
mediately after harvesting,. From this data the algal
production rate was as high as 11 grains per sq. meter per
day® On the basis of this experience it was decided to
modify the algal unit by replacing the triangular hollow
disks with flat plastic disks and constructing means for
placing the flourescent lamps down and in between the
rotating disks# above the water surface0
The application for continuing that part of the investigation
pertaining to the growth of attached algae was not approved
after the 1969 experience described above. However, it was
decided to gain some information by improvising modifications
to the lighting facilities. Nov* York City plant operating
personnel undertook the job. The triangular disks were re-
placed with 1/4 inch thick plexiglass on 3 inch centers.
Stages 11 to 15 were equipped with a total of 38 disks. Stage
16 was used as a settling tank (12 minutes detention) to
capture some of the sloughed off algae, prior to mixed media
filtration. New light hoods were constructed which facili-
tated the placement of 2 high output fluorescent lamps be-
tween each of the plastic disks and 2 such lamps at each end.
The 36 inch long lamps were positioned horizontally between
the disks and such that their centerlines were 7 inches and
9 1/2 inches above the centerline of the shaft,, The side of
57
-------
the lamps were only about 3/4 inch from the surfaces of the
disks being illuminated.
This work was completed by September 1970 and the data for
that month and for October and November 1970 is presented in
Table 21. The five algal stages, affording about 50. minuter
of retention time with the 38-3 ft. diameter disks, effected
the removal of 7 mg/1 of NH3-N while forming 3 mg/1 of NO^ -N.
The average alkalinity decrease from 123 to 95 mg/.l would
indicate the formation of 4 mg/1 of NO^-N and the measured
.increase was 3 mg/1. The CC>2 acidity decreased from 32 to
11 mg/1 notwithstanding the fact that considerable CO^ was
released by nitrifying reactions involving the destruction of
alkalinity. The concentration of phosphates remained rela-
tively unchanged.
It was observed that a considerable amount of algae sloughed
off the disk surface which made it difficult to evaluate the
overall algae production. According to the data presented
in Table 21 there was a decrease of 4 mg/1 of albuminoid and
ammonia nitrogen over and above the 3 mg/1 of nitrates formed,
which was probably synthesized into algal cells.
58
-------
TABLE 21
PERFORMANCE OF 5 STAGE ALGAL UNIT AFTER MODIFICATION IN Mg/1
Month
T
.O.C.
D.T
.O.C.
NH
*
3
NO
*
3
ALK
CO
2
PO
4
In
Out
l'n
Out
In
Out
In
Out
In
Out
In
Ou t
In
Out
Sept, 70
10
8
9
7
15
7
6
8
129
109
45
] 0
12
12
Oct,
9
8
8
8
11
4
7
11
147
101
30
13
14
15
Nov.
9
6
7
7
6
1
9
12
94
74
20
10
13
14
AVER.
9
7
8
7
11
4
7
10
123
95
32
11
13
14
(a) Flow 3.5 g.p.m.
(b) 38 plastic disks in 5 stages 6th stage used to settle sloughed ofi. algae
(13 minutes detention) mixed media filtration
*measured by total of albuminoid and ammonia nitrogen
-------
SECTION VII
ACTIVATED CARBON ADSORPTION
Carbon adsorption was practiced on pilot scale starting on
1/27/70. The pilot unit comprised 6 dowrnow pacVed bed
columi.s operated in series to remove residual organics con-
tained in the effluent from the algal unit. The columns were
subjected to a loading rate of 5 gpm per sq. ft.
During the initial operation it was found that the pump pre s-
sure increased at a rate of about 4 lbs. in 24 hours, mainly
due to the formation at the surface of column #1 of a 1/4 inch
thick "wafer" which was composed mainly of algae. On 3/11/70
a pilot mixed media filter 3 inches in diameter was installed
in the flow between algal Stage 16 and carbon column #1.
Since this filter was 3 inches diameter as were the carbon
columns, the hydraulic loading rate was the same. As a result
of the use of the mixed media filter the rate of pressure in-
crease was lowered to about 1 lb. per day. However daily
backwashing was continued thereafter on columns 1 to 3 and
every other day for columns 4 to 6 to keep pressures low.
From the beginning of the run until the mixed media filter was
installed the total dissolved organic carbon applied to column
was about 8 mg/1. After the filter was installed that con-
centration was lowered to 6 mg/1.
All the operating data obtained relative to activated carbon
adsorption over the period March to November 1970, when the
10 stage unit was treating 7.5 gpm, is presented in Table 22.
It was especially desirable to obtain data after the wastewater
had been subjected to sequential biological treatment using
partially submerged rotating (.''isks. As can be seen in Table
22, the results at any stage of treatment varied only slightly.
The load on the carbon columns was almost completely dissolved
and it would appear that a removal of 1 mg/1 was affected by
each of the columns 1 through 4. The rate of removal decreased
markedly when the T.O.C. was lowered to 2 mg/1.
PROFILES OF B.O.D.g THROUGH CARBON ADSORPTION
For the purpose of identifying the nature of the unadsorbed
organic carbon moving through the activated carbon columns,
profiles of B.O.D.^ concentration in the effluents from the
columns was determined. The data for 6 profiles is given in
61
-------
TABLE 22
PROFILE OF TOTAL ORGANIC CARBON Mg/1
FROM ALGAL UNIT THROUGH ACTIVATED CARBON ADSORPTION
Algal
Column No.
Month
16
MMF
1
2
3
4
5
6
1970
March
TOC
9
8
6
4
2.1
1.8
1-4
1.4
DTOC
9
6
5
3
1.8
1.4
1.2
1.1
April
TOC
7
6
5
4
3
1.7
1.4
1.1
DTOC
7
6
5
4
3
1.9
1.2
1.3
May
TOC
7
6
5
•3
2
2
1.5
1.3
DTOC
7
6
5
3
2
2
1.6
1.5
June
TOC
8
5
5
3
3
2
1.5
1.2
DTOC
7
6
6
4
4
3
2.0
1.3
July
TOC
6
5
4
4
3
2
1.6
1.4
DTOC
6
5
4
3
3
2
2.0
1.4
Aug.
TOC
8
6
6
4
3
2
1.6
i • o
DTOC
7
6
4
4
3
2
1.6
1.4
Sept.
TOC
8
6
5
4
J
1.9
1.3
1.4
DTOC
7
6
5
4
3
2
1.4
1.4
Oct.
TOC
3
3
5
4
3
3
l.S
DTOC
3
7
5
4
o
3
n
i. - 3
Nov,
TOC
3
5
4
4
3
2
2
i .1
DTOC
7
5
4
3
3
2
1.6
1.1
AVERAGE TOC
DTOC
6
6
5
5
4
4
2.9
3.0
2.1
2.2
1.7
1.7
1.3
1.4
Notes: (1) Carbon adsorption started on 1/27/70 - not
operating 6/14 to 7/2/7 0 due to main plant shut-
down resulting from gasoline explosion in screen
chamber
(2) Column $0 renewed. -June 1970 and Nov. 1970
(?¦'¦ Culy data 7/1-v to 7/3.1/70
'4) Mixed media filter 3 inch diameter and carbon
columns 3" diameter, pressure overflow, series
operation loc.c.s'J. at 5 g.p.m. per sq. ft.
(5) From March throv.gh Aug. 1970 the algal unit was
undergoing modification to lighting and disk
configurations
62
-------
Tcble 23. It can be seen that there was substantial removal
of biodegradable organic carbon across column #1 as the average
concentration was lowered from 4.7 to 1.2 mg/1. Thereafter
the concentration of B.0.D.5 in the effluents from columns 2
to 6 remained essentially constant at about 1 mg/1.
FATE OF NITROGEN THRU ACTIVATED CARBON ADSCOPTION
The data accumulated relative to the concentrations of ox^d-
izable nitrogen and of nitrates passing through the carbon
columns is shown in Table 24. This data demonstrates that
curing the six month period from May to November there vas
•nbout a 1 rag/1 loss in ammonia nitrogen and a similar loss
in nitrate nitrogen. The dissolved oxygen in the liquor
pr.ssing through carbon adsorption was generally lowered fror
the range of 4 to 6 mg/1 in the influent to 1 mg/1 in the
affluent from column v6. As such the operation was substant-
ially aerobic. It should also be noted that the effluent from
carbon #6 contained only 0 to 3 mg/1 of oxidizable nitrogen
coring 0.11 months except September. That month only 3 stages
•."pre used to treat the wastewater prior to final settling
which accounts for the higher ammonia concentration remaining
in the influent to activated carbon adsorption.
63
-------
TABLE 23
ACTIVATED CARBON ADSORPTION
3.0.D.5 - Mg/1
Date
MMF
1
2
3
4
5
6
S/4/70
1.1
0.5
1.0
1.1
0.4
1.3
0.8
3/12/70
1.0
1.6
1.4
1.1
1.0
0.9
1.0
8/19/70
4
1.0
0.7
0.6
.9
1.0
0.7
8/25/70
4
1.2
1.0
1.1
1.5
1.2
0.9
3/26/70
5
1.4
1.0
1.1
1.6
1.0
1.0
8/27/70
4
1.2
1.4
1.0
0.9
0.8
0.7
AVERAGE 4.7 1.2 1.1 1.0 1.0 1.0 0.9
64
-------
TABLE 24
ACTIVATED CARBON ADSORPTION
NH3*/N03 ~ Mg/1
Algal
16
MMF
1
Carbon Column
2 3
No .
4
5
6
£ ^
-J »-< i
°
4.5/16.3
4.0/15.8
3.6/15.0
3.7/15 . 4
3.1/13 .4
3.1/14.0
2.7/13.9
2.5/12.8
June
.1.9/15.2
1.5/17.3
1.4/16.4
1.1/15 . 5
0.9/15.2
0.8/14 .9
0.5/1?.3
0.5/15.5
July
1.3/14 .9
0 .8/16.3
0.6/15.3
0.4/15.0
0.3/13.6
0.3/14.0
0.2/13.5
0 .1/11.8
Aug.
1.6/14.9
1.3/15.8
1.0/13.9
0.8/11. 5
0.6/14.1
0.4/11.1
0.1/9.2
0.3/13 . 2
Sept.
7.3/8.3
6.4/9.8
6.4/9.4
-
6.2/9.0
-
-
6.4/5.2
Oct.
4.4/10 .7
3.3/11.4
3.9/11.4
-
-
-
-
2.9/9.7
NoVo
0.7/12.1
0/13.6
0.2/12.9
—
—
—
-
0 .2/10.6
*Total of Albuminoid and Ammonia N.
(a) During September only 3 stages of treatment were used in biological unit-
-------
SECTION VIII
SPECIAL STUDIES
COMPARISON OP SETTLING VS. MICROSTRAINING
During the month of December 1970 analyses were made of - de-
pended solids concentrations in samples of settled versus micro-
strained effluents from selected stages of treatment# The
effluents from Stages 1# 2, 4, 5, 7 and 10 were settled
quiescently for one hour in a liter cylinder and suspended
solids determinations were made on the supernatant liquor»
To establish comparative efficiency, the effluents frori the
same stages were passed through a 35 micron hand micro-
strainer and the suspended solids concentrations were deter-
mined on the filtrate. The data obtained is presented in
Table 25o It shows that the suspended solids passing a
microstrainer were less than contained in the supernatant
liquor after one hour Bettling0 The improvement measured
from about 32 to 39% less suspended solids in the micro-
strained effluents than in those that had been settled» It
can be noted too that the percentage of efficiency of micro-
straining over settling increased in the downstream stages.
As to the effect of such differences in suspended solids con-
centrations on BoOoD.5, it should be remembered that these
sloughed off solids, having had considerable residence time
on the disk surfaces, would exert only a fraction of demand
of raw solids for oxygen,. Calculation based on operating
data indicates that the biochemical oxygen demand of such
sloughed off solids would approximate 03 to 04 mg/1 of
Bc0oDOij per mg/1 of suspended solidso
EFFECT OF CULTURAL AGE ON RATE OF REMOVAL OF B.O.D.5
PHASE 1
A major departure from past practice in the use of rotating
disks to treat wastewater has been the periodic harvesting of
the slimeso During the Phase 1 operation, it was found that
anaerobiosis had developed after about 4 days in the lower
layers of the slimes on Stage lo That time increased progres-
sively to about 2 weeks at Stage 5n A program was carried out
to control the cultural age of the slimes and limit their
thicknesso The slimes were harvested by washing with city
water usually at the following frequencies: Stages 1 to 3
every 4 to 6 days. Stage 4 to 6 every 6 to 14 days0 Since the
bulk of the carbonaceous matter was removed in the first 6
67
-------
TABLE 25
COMPARISON OF SUSPENDED SOLIDS REMO" AL IN Mg/1
MICROSTRAINING (35 MICRON) VS. 1 HR. QUIESCENT SETTLING
Date
Inf1. *
1
2
4
5
7
10
12/2/70 Micro.
1 hr.
settling
124
43
62
52
68
30
39
25
34
23
31
15
21
12/3/70 Micro.
1 hr.
settling
98
54
68
58
66
32
40
30
36
20
28
9
17
12/13/70 Micro.
1 hr.
settling
86
36
43
38
44
30
39
25
32
15
24
8
15
AVEPAGE Micro.
1 hr.
settling
103
46
59
49
59
31
39
27
34
19
28
11
18
DIFFERENCE
-
13
10
8
7
9
7
5 IMPROVEMENT
BY MICRO. OVER
i HR. SETTLING
22
17
21
21
32
O o
J
Note: values of suspended solids are those received
by the pilot plant and the samples were neither
settled or nicrostrained before analysis.
-------
stages* only the slimes in those stages were periodically
removed# None of the slimes were observed to grow in
thickness more than about 105 nun« An additional reason for
harvesting the slimes appeared during the course of the
investigation in that sphaerotilus began to become visible
on the third day after washing off the disks ir. the upper
three ptages of treatments The large frictional surface
provided by the filamentous growth when submerged caused the
velocity of rotation of the shaft to be reducedc Consider-
ably more torque would have been needed to maintain normal
rotational velocity when the slimes were laden with such
filamentso Stages 6 to 10 carried out the bulk of the
nitrifying function and the slimes in those stages remained
very thin, that is less than „5 mm, and were not removed,,
The data obtained after the harvesting operations
performed during Phase 1 was grouped and averaged as to the
percentage of removal effected by the slimes in Stages 1
to 6 according to the days elapsed after the cleaning opera-
tion which represented the cultural age0 These values of the
percentage of removal of BoOoDog with respect to the cultural
ages for Stages 1 to 6 during Phase 1 operation have been
plotted in Figure 9„ It can be noted that the curves take
form and direction to indicate the first approximate optimum
cultural age for each of the stages of treatment. The
magnitude of the optimum efficiency of B00oD05 removal de-
creased from stage 1 to 3 and the growth time to attain such
optimum increased0 A marked increase in the optimum per-
centage of Bo0oDo5 removal by Stage 4 over Stage 3 that is
from 30% to 50% can be noted to have taken place. In that
connection microscopic examinations revealed that large
populations of stalked ciliates colonized the surfaces of the
disks comprising Stage 4. The curve for Stage 5 indicates a
lower optimum than Stage 4 and a longer period to attain that
optimum,, The curve for Stage 6 can be noted particularly for
the fact that the slime regrowth after harvesting underwent a
lag phase of about 5 days. Moreover this curve can also be
distinguished from all others in that it did not assume a
cyclical form, which wa3 a consequence of slime slough off
in the upper 5 stages»
PHASE 2
The effect of cultural age on the rate of removal of B0O.D„5
was evaluated during the Phase 2 operation0 The data obtained
has been tabulated for Stages 1 to 6 in Tables 26 to 32„ Only
the data gained for Stages 1 and 2 was representable in graph
form in Figure 100 The data for Stages 3 to 6, which involved
69
-------
LEGEM)
0 STAGE NUMBER
EFFECT OF CULTURAL AGE on
OF BODu
STAGES i TO 6
-------
TABLE 26
EFFECT OF CULTURAL AGE ON RAmE OF
B.O.D.g AND T.O.C. REMOVAL
STAGE 1 - 65% 0^ in Atmosphere
Elapsed
days from
10/12/70
Inf 1.
B .0. D . ^
Mg/1
Effl.
B . 0. D. ^
Mg/1
3.O.D.5
Removed
Mg/1
B.O-D-tr
Removed
a
*0
1
31
45
36
44
2
118
39
79
67
3
95
36
59
62
4
-
-
-
5
60
20
40
67
6
75
32
43
57
7
63
31
32
51
o
83
33
50
60
0
110
41
69
63
10
55
23
35
60
i *;
78
24
34
69
12
52
23
39
63
13
69
27
42
61
11
34
32
52
62
15
-
-
-
-
16
S3
4C
43
52
"} *7
-v. ,
M
3(5
58
62
71
-------
TABLE 27
RELATION OF GROUPED VALUES OF STAGS 1
EFFLUENT TO INFLUENT B.O.D.g Mg/1
Infl. B.OaD.c51 - 60 61 - 70 71 - 30 81 - 90 91 - 100 101 - 110 111 - 120
• - - ¦— —— —ii. .. ¦ .. i .
14 31 30 37 29 41 45
20 23 28 45 38 38 39
23 27 30 33 36 41
32 32 29
24 40 36
23 36
Average Effl.
B.OaDo 5 19 27 29 35 34 37 42
% Remaining 35 42 39 41 36 35 37
3«O.Da 5
% Removed 65 58 61 59 64 65 63
B.O.D,
The data comprising this Table v,'?,s taken from general operating data obtained
in October 1970.
-------
TABLE 23
EFFECT OF CULTURAL AGE ON RATE OF
B.O
.d.5 and t.o.c. removal
STAGE 2
Elapsed
days from
10/15/70
Infl.
B . 0 . D . r
Mg/1
Effl. B.O.D.5
B.O.D.5 Removed
Mg/1 Mg/1
B . O . ^ . 5
Removed
O,
'O
1
27
15 12
44
2
20
11 9
45
3
32
23 9
45
4
31
26 5
16
5
33
23 12
36
6
41
31 10
24
7
23
15 8
35
8
24
13 11
46
3
23
12 11
48
10
27
15 12
44
11
32
26 6
19
12
-
-
-
13
4 0
30 10
25
14
36
24 6
17
7 °
-------
TAELE 2?
EFFECT OF CULTURAL AGE ON T.O.C. AND
b.o.d.5 removal
STAGE
3
Elapsed
days from
10/22/70
Infl.
B. 0. D. g
Mg/1
Effl.
B.O.D.c
Mg/1
B.O.D.c
Removed
Mg/1
B.O.T.-
Remo\,
%
1
13
15
-2
-15
2
12
10
2
17
0
u
15
15
0
0
4
26
15
11
42
5
-
-
-
-
6
30
24
6
20
7
n
24
16
8
33
O
9
22
13
9
41
74
-------
TABLE 30
EFFECT OF CULTURAL AGE ON T.O.C. AND
B.O.D.5 REMOVAL
STAGE 4
Elapsed
days from
10/10/70
Inf 1.
B.O.D.
Mg/1
Effl.
B. 0 . D. 5
Mg/1
B . 0 . D ,,t
Remove*
Mg/1
B.O.D.^
Removea
1
—
—
—
3
30
18
12
40
4
19
15
4
21
5
C
13
15
-2
-15
O
7
7
7
0
0
8
16
13
3
19
9
13
15
-2
-15
10
14
12
2
14
11
15
14
1
7
12
11
i:
1
9
13
15
10
5
33
14
10
9
1
10
15
15
16
-1
-7
16
15
16
-1
-7
17
-
-
-
-
18
24
16
8
33
19
16
17
-1
-7
20
-
-
-
-
21
13
11
2
15
Note: Samples not taken 10/11/70 and 10/12/70, as the
oxygen feed to Stage 1 was shut off by a prankster
and the slimes in the upstream stages became
anaerobic.
75
-------
ys
/_§_
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
17
13
TABLE 31
EFFECT OF CULTURAL AGE ON B.O.D.5 ^^OVAL
aND T.O.C. REMOVAL
STAGE 5
Infl. Effl. B.O.D.5 B.O.D.5
_ f ,
&
B.O.D.5 B.O.D.5 Removed Remcved
Mg/1 Mg/1 Mg/1
13 10 3 23
13 11 2 15
18 22 -4
15 13 2 13
15 11 2 13
7' 6 1 14
13 11 2 15
15 15 0 0
12 13 -1
14 16 -2
10 9 1 10
10 11 -1 -
9 3 1 11
16 12 4 25
16 14 2 13
-------
ys
Zi
1
2
3
4
5
6
7
8
9
10
11
12
13
14
15
16
17
18
19
20
TABLE 32
EFFECT OF CULTURAL AGE ON B.O.D.5 REMOVAL
AND T.O.C. REMOVAL
STAGE 6
Infl. Effl. B.O.D.5 B.O.D.5
B.O.D.5 B.O.D.5 Removed Removed
Mg/1 Mg/1 Mg/1
%
14 14 0 0
12 12 0 0
10 10 0 0
11 8 3 27
10 9 1 10
11 10 1 9
22 20 2 9
13 13 0 0
11 12 -1
6 5 1 17
11 10 1 9
15 14 1 6
13 11 2 15
16 14 2 13
9 10-1
11 9 2 18
3 7 1 13
77
-------
iYjQTE3 Stage I eq^ppsd with hood j
enclosing atmosphere enriched j
with oxygen s
Stage _ opsn to ciniospfters [
60~
f
a* i
STAGE l^x
O^-0
v .,/~x
RG 10-EFFECT OF CV'-TL^AL AGE on
fT^ rr^\;r> • r>r- r-jpip. -
At_:.j _< V.-\;_ '.rft
5
10
( f
J L
j
CULTJHAL A,3E DAYS
73
-------
removing B.O.D.^ after a large fraction had been removed was
highly variable and did not follow a pattern.
The curve for Stage 1, equipped with a hood enclosing an
atmosphere enriched with oxygen and 60 effective disks, in-
dicates a rapid growth took place during tve first day after
cleanirg so that 36% of the B.O.D.^ was removed. On the
second day the removal rate had increased to a maximum of 67%
and thereafter a decreased removal rate accured on about the
fourth day. On the 5th, 8th and 11th days the removal rate
again peaked. The variation between the maximum and the mini-
mum was in the range of 51% to 69%. In order to determine
the effect of the concentration of influent B.O.D. on the
rate of B.O.D.,. removal by Stage 1, with its oxygen enriched
atmosphere, B.O.D. data over 28 days of operation of the
influent and effluent was grouped and is shown in Table 27.
It can be seen from the data that between the limits of 50
and 120 mg/1 the average removal rate varied only between the
limits of 58% and 65%.
The curve delineating the performance of Stage 2, wherein the
slimes were exposed to normal atmosphere, and the influent
wastewater received 10 to 15 mg/l of dissolved oxygen from
Stage 1, is also shown in Figure 10. It can be seen that the
performance of this stage was such that a rapid growth took
place after the first day when the B.O.D. removal rate was
found to be 44%. An optimum removal rate of 45% was attained
after 2 to 3 days followed by a marked decrease to 24% on the
6th day. A secondary optimum rate of removal of B.O.D.,. was
reached 9 days after harvesting. It is evident from Figure 10
that the cyclical changes in the removal rate by this stage
were much greater than those that took place in Stage 1.
EFFECT OF TIME OF CONTACT ON REMOVAL OF B.O.D.5
In an effort to evaluate the influence of the time of contact
of the wastewater with the slimes on the removal of B.O.D.^
grab samples w
-------
period during continuous flow. Samples were taken over r.:^v';
2 minute period from the drain of each tank of Stage.?. .1 to
6.. sixteen minutes after the bypassing operation and ag"w.n
•ivtcr on additional detention period of 16 irinutes. These
time intervals were chosen because the overall detention time
for Stages 1 through 6 approximated 32 minutes when coe.si.f--~
i.ng the actual fluid vcIv-m.cs in each of thj stages. 7b. i^
procedure v;?.s repeated on a number of days and a general
pattern of results was obtained. Typical of these res v. Its -f
the B.O.D.- concentrations of microstrained samples is pre-
sentee on semi-log scale i.e. Figure 11, which shows the pre:"i 1 e
during normal continuous flow and the profiles after 16 r.-~ ."3
minutes of additional contact between the wastewater ard e
--limes. The B.O.D,5 had been reduced after 16 minutes of
contact by the vertical difference between the profiles,
addition;?.J. 16 rr.ir.utes of contact exerted no effect on the
P-.O-D.j. concentration, as the 16 minute and 32 minute prof i 1^
wore practically coincident. The 3.0.D,. of the wastewater of
some 130 mg/1 had been reduced progressively to 19 m.g/1 r
Stage 6 when the flov; was continuous thorough the 6 stage-
treatment. During the additional catch-like contact time. the
slices in Stage 1 to 3 were incapable of reducing the r?-.0.~/.^
below about 42 mg/1 even after 33 minutes of additional cor.-'
tact. Apparently, the nature of the slimes in Stages 4 t~ ^
was the responsible faeter i 1 reducing the B.O.D.5 below
¦-:2 mg/1 level.
~.t was decided to repeat this procedure, the only modifisat*w~
being that of reducing the batch-like contact tires bet'-"-"-
th° elir-s and the trapped wastewater to about 1 and 2 add-
itional detention periods of 6 minutes each. It required
•-'co'.r.t a 7 minute tine span tc take the samples for each e*.•-*.
.3 at." was secured during 3 separate days end the average re-
su'1 '• a-^ shown in Table 33. The profiles of B.O.D.,. ' 1)
'"urine continuous flew, (2) after about 6 minutes of"additional
contact time and (3) ~""tcr about 6 minutes more of c^tact
been eiotted c-n semi — loc see 1 e in Figure 17.
cvr'-^s t-'ke the s^—e form. and direction on those in Fig-'r~ " * .
7. t "¦•euld appear from the curves that batch contact time w"1"
-.ore wTt1 ve * n lower" ns tb*"1 e.O-P. tbnn fJow i*ire ¦' r c~"
^ "" 5 " "" "
1 to 3, however, after cr.e additional batch !¦ deten"-'
time im all stages ef treatment, slimes in Stages 1, 2 and 3
wore, usable to reduce the B.0.P.r below the level of about
t*/1 after one or two additional contact periods.
CO
-------
I
I
L
L
LEGEMD
X PROFILE-During Flow
0 PROFILE- IRminutes of
additional coniaci-IMo Fto
~ PROFILE-32 minutes of
additional contact-No F!c%"
¦o
a
®K)d-
so:
801-
-r/V
f vy;
X
•¦vy-
V-" j
':-C~
TTO'-
20-
yv
J 0"
~
0
G
0
X
B0D5 Of TANK CONTENTS
f/DUFim FLOW
3QD5 offer
iS am? 32 rrurites of
additional contec?
FiG ii-EFFECT OF TIME OF CONTACT on
REMOVAL OF 3005
STAGES 5 to 6
2
i
- '
3
i
*
!i Jsl®
81
-------
TABLE 33
EFFECT OF TIME OF CONTACT ON REMOVAL
OF B.0.D.g
Operation Inf 1. 1 2 3 4 5 6
Continuous flow 139 84 ^ 71 59 44 34 24
After 6 min.
addl. contact 44 43 42 30 24 17
After 12 min.
addl. contact
(cumulative) 42 42 36 32 22 18
Note: (1) Samples improperly taken.
-------
I
40?
—r>.
?0r
!G!-
QL.
LJ
LEGEND
X PROFILE-Durag Flow
0 PROFILE-6 minutes of
additional contact-Wo Ftow
~ PROFILE-12 minutes of
additional contact-No Flow
5 KX)~
OPj-
w> 0*1
A
©,
~ /'
B0D5 after 6 m'jvjtas
.additional contact
BO D5 after 12minutes
Gddltior.c! contact
B0.D5 of TANK CONTENTS 1
DURiWG FLOW !
FiG 12-EFFECT OF TIME OF CONTACT on
REMOVAL OF BODs
STAGES ! to 6
c:
0
1
1
1
f:
STAGE NUMBER
83
-------
The slimes in Stages 4, 5 and 6 were able during the first
6 minuter, of additional contact to reduce the B.O.D.,- by
about the came degree v.'hcn flowing through each of thos e
stages o.s had been accomplished» coincidentally or not, duri~-~
p. .similar batch contact period in the preceding stage,
EFFECT OF TIME OF CONTACT ON NITRATE PRODUCTION
To obtain data comparing the effect of flow-through tirre
vcr.iu'i batch-contact time on the production of nitrates tV*
same by-pass procedure was used as described previously for
finding the influence of contact time on 3.0.D.^ removal,
",'n this case the performance of Stages 7 to 10 was evaluate-5
rather than 1 to 6. The data obtained is presented in Tab?e
34. Lit can be seen that for the first run the nitrate con-
centration during flow increased from 2 to 9.6 mg/1 as a
.-result of the oxidation of amr.onia by Stages 8, 9 and 10.
*?.'?>o average increase in nitrates by those stages was "7.5 ncr/1.
Since the detention time in the three stages was 13 minuter.,
"-fto average production of nitrates v.fas .42 mg/1 per minute
of contact. It can be seen from, the Table that during bntc>.
contact of 32 minutes the average production of nitrates T.-v,.~
.40 mg/1. There was no difference between flow-through a.r.d
batch-contact with respect to nitrate production.
The average data obtained during three similar profiles tc!'.on
curing flow and after 6 to 12 minutes of additional batch,
contact. is also shown in Table 34. It can be seen that
during time spent passing through Stages 8, 9 and 10 the
nitrate concentration was increased from 5,4 to 11.9 rr.g/I.
This increase was at a rate of 6,5/18 = .36 mg/1 of nitrate-
re:: mirvtc of contact. The generation of nitrates duri.no
the additional contact periods is also shown in the Table
and it can be seen that an average of .48 mg/1 of nitrates
Produced per minutes of contact. These data would
indicate an increase in the rate of nitrate production by
batch c-^ntrot over flow-through contact which was not corro-
borated by the first set of data. Differences would see;"
p.areinal if at all.
cv
-------
TABLE 34
EFFECT OF TIME OF CONTACT ON NITRATE CONCENTRATION N03 Mg/i
TEMPERATURE OF WASTEWATE7 62°
Stage No.
8 9
10
Avg.
During flow - 1st run
After addl. 16 min.
After addl. 3 2 min.
(cumulative)
2.0 5.6 8.2 9.6
10.2 11.8 15.4
19.2 20.8 22.2
Total production during
addl. contact
Production per min. of
addl. contact
13.6 12.6 12.6
.43
.39
.39 .40
During flow
After addl. 6 min.
After addl. 12 min.
(cumulative)
5.4 8.7 10.8 11.9
11.4 12.4 13.1
15.0 17.3 16.4
Total production during
addl. contact
Production per min. of
addl. contact
6.3 6.5
.52
4.5
.54 .37 .48
r> p-
OJ
-------
SECTION tX
STUDIES UNDER HIGH FLOW RATE
INTRODUCTION
Using the foregoing experiences as a background, it was
desired to obtain information relative to the capacity of
the pilot plant to cope with increased loading rates. The
work was started in November 1970. In the interest of
having to expedite the studies, the load on the pilot plant
was increased only to a range wherein the 10 stage unit
was capable of accomplishing a 90% removal of carbonaceous
matter. It was intended to eliminate, as the work progres-
sed, those factors that appeared to restrain the pilot from
being able to handle higher loading rates. As such the
load on the pilot plant could be raised further to the
highest rate consistent with removing at least 90% of the
carbonaceous matter within the 10 stages of treatment.
Accordingly to prepare for load stress the capacity of the
influent system was increased so the flow of primary tank
effluent from the main plant could be maintained at rates
up to 22 gpm. It was known that the upper stages of treat-
ment were rate limited because of oxygen insufficiency and
so stage 2, in addition to stage 1, was modified to the
extent that the number of disks was increased to 71 replac-
ing the former 48. Moreover, a sealed plastic hood, capable
of containing atmospheres enriched with oxygen, v/as con-
structed over Stage 2, Piping changes were made so as to
facilitate feeding, in parallel, the primary tank effluent
to Stages 1 and 2. The hood over Stage 7, formerly used
to contain oxygen enriched atmospheres over that stage was
transferred to Stage 10 and at the same time the number of
disks in Stage 10 was increased from 48 to 71. This was
done in order to provide the maxinmm dissolved oxygen in
the wastewater prior to admitting the treated wastewater
to the final settling tank for solids separation.
OPERATING RESULTS
At first the flow rate to the pilot plant was raised from
7.5 gpm to 17.7 gpm and the average data obtained for those
two modes of operation for Nov. 1970 in shown in Table 35.
87
-------
TABLE 35
co
CO
t
3 qvzh:
vi'ISG
dat?, :
fclOVEMS
ER 19"
0? 7
Ji ;i.«D
17,7
•i:c ru
WASTE
7;
-------
.bo seen fro v. that table the1 the BOD5 at the 7.5 go-
•oto had boon reduced to 20 tv/I. between Stages 2 md
3 while during the period of higher flow rate 10 stages
vorc required to obtain the same effluent quality. The
effluent from the final settling -tankf which receiver] s
3. f> gp;n •ocrtion of t.he effluent from Stage 10 developed
•.earl'.ed turbidity under this hi oh flow condition. Biolo-
gical growths were found to have bridged the 1 1/2 inch
spacing between the submerged plastic vanes in the fine!
settling tank after just a couple, of days, which condition
v.'orr.cr.-T1 with time. During the first part of November
when the flow rate was 7.5 gpm, nitrifying organisms were
active to the extent that 10 rag/1 of nitrates were being
produced in Stages 5 to 10. During the period of high
s'lov-* rate the nitrification process had been forced down-
r.'.r . The nitrate concentration leaving Stage 10 had
h'-en reduced to only 1.f ma/1 after a week and was cor.tin-
n'ng to decrease.
Tn the 1:1 yht of these findings the flow rate was reduced
to an average of 12 gpm near the end of November 1070 and
thi s loading rate continued through December 22, 1970.
This operation was carried out with the flow divided
;ue 7.1 v* between Stages 1 and 2 which were eeuinped with
C'O to 71 disks respect?'.voly .and both were operated with
orvcen enriched a t ito ? uh ere & (3ta.no j. , 50?^- to 70?' of oi-ryeer.
St-: go 7 - 50% and leaking) . The flow, after passing
through Stages 1 end ? ia parallel, passed through Stages
3 to .i n. ser:- as. Stag;- 10 was scuipocd wi.th a hood
"""el".'":' r/: an a.t r.icsuhere enrichrvd with O/cyoen to the extent
•j f hoi * of the total wa.sos nresont. The number of
«n Stng~ 3 wee 4S, Stage * - 43, Stage 5 - 43, Stage
^ - 7", Stage 7 - 73 , Qt^gr. 8 - 71, Stage 9 - AS, St.-g~
• 0 -¦»' r- ^ »% p'V-i Qrl V PTTl'T 3T Jm O
"*>, :°7C with re spec t to t.o.c. , D.T.O.C. and
¦: .C. \ , "•••: eir.ab.1 r nitrogen, nitrates, or thopho nphatc s
-.p,T ..¦... sa 11' a 1 i n ty are shown in Table 35o It 'V^
r.. rr~- ~-'-i this leble that the ^ 0 stages of treatment
¦ ¦' vr" ."'ll"' to reduce the T.0 . C . f roTT. 94 nr;/.!_ i n the ? n r V;.';-' '
'¦ o -r '"¦']/~ at Stage 10. An * avirago of 4.a rng/l of nitrate'
1 -rrr' pr ••¦",',r;ed ws.ile treating 12 gnrn. On the basis of 43
ga'.loof flu: d in stage {"'.secured when the disks
warn td of si its; the theoretical detention period in
¦•I1. 1 .•"'.a•¦as wou.V" have lveen 37,5 TTvlnuues. Tbo ?,ctv."'!
89
-------
JO
Ayr-7
-------
time of contact was somewhat less depending on slime
thickness.
EFFECTS OF SLUDGE RECIRCULATION
In pursuit of making such changes as mighw increase the
capacity of the 10 stage unit to treat effectively more
flow, a 6 ft. diameter settling tank with means for
continuous sludge collection was installed. A torque
flow (Wernco) pump, driven by an electric motor through
a vari-drive arrangement, was placed in service. This
pump was capable of transferring all the effluent (less
the waste to drain) from Stage 10 to the new settler.
This arrangement made possible a recycling of the sloughed-
off biological growths for the purpose of evaluating the
effect of suspended cultures on treatment efficiency.
At this time it was believed that 14 gpm of flow might be
a satisfactory load level t.o place on the 10 stages of
treatment along with the recirculation of 2.0 gpm of
sludge from the settler. Accordingly, data was obtained
for this method of operation starting with December 23,
1970 and continuing through January 1971. Normally about
8% of the flow leaving Stage 10 was wasted to the drain
and the suspended solids in the stage 10 effluent rose
to the range of 400 to 800 mg/l. The dissolved oxygen
in the wastewater passing through the stages was in the
range of 2 to 8 mg/l. On January 21, 1970, after not
wasting sludge for a few days, the suspended solids con-
centration rose to 2400 mg/l, at which solids level the
dissolved oxygen fell to the general range of 1 - 2 mg/l.
The profiles of the concentrations of T.O.C. and D.T.O.C.,
C.O.D., albuminoid and ammonia nitrogen, nitrates,
phosphates and bicarbonate alkalinity obtained during the
month of January 1970, when the average wastewater temper-
ature was 57°F., is presented in Table 37, It can be seen
from the averages that little removal of the D.T.O.C. was
accomplished by stages 3 to 9. (Stage 1 and 2 were
operated in parallel.). The effluent from Stage 10 con-
tained an appreciable amount of suspended organic carbon
that is 6 mg/l. The effluent was turbid. During this
mode of operation, when recirculating solids, nitrifica-
tion had been forced downstream to the extent that the
effluent from Stage 10 contained only u to 1.6 mg/l of
nitrates, which level was confirmed by the reduction in
91
-------
vj3
to
TABLE 37
AVERAGE OPERATING DATA. J.^SU.VRY 19 71
USING SLUDGE RECYCLING
VALUES IN Mg/1
WASTEWATER TEMPERATURE 59CF FLOV7RAT3 14 gpm
STAGE NO. *
PARAMETER I NFL. .1 2 3 4 5 6 7 8 9 10 F.S.T.
T.O.C. 78 42 47 39 35 32 29 24 21 21 19 22
D.T.O.C. 35 17 20 20 17 20 17 16 15 15 13 12
C.O.D. 284 155 164 139 122
ALB. -r A^i-'ON.N 29 27 27 28 - 28 28 27 29 :>c 28 24
NITRATE 0 0 0 0 0 0 0 0 0.4 .7 0.3
P04 (Ortho) 23 18 20 18 20 - 18 20 15 18
BICARB. ALK. 229 221 221 221 - 223 - 216 - 217 214 199
*FINAL SETTLING TASK
-------
alkalinity of about 10 mg/.l in the downstream ptagos.
It is interesting to note that on January 21, 1971
refer to dailv data ir*. .T'eondiv"' '.•'hen the recirculating
culture had been rai sed to a level of 2400 mg/1 of rus-
oond~d solids, the ccn.co:ifcrstier.s of D.T.O. J. vero about
the same as the monthly average. Suspended organic
carbon increased from an average of 6 mg/l to 9 nrr/l in
the effluents from stages 9 .-»od 10 after micro straining
".¦."hen operating at th: r high suspended solids level.
during this recycling procedure .i.t became apparent that
no significant advantage '-"as gained in the removal of
c-"1 rbonaceous ^ntfer, Micro see v,,i c examination of the re-'
eve led sludge solids revealed that, they were peptized to
the extent of being discrete sma 1.1 particles. It was
else noted that the sloughed—off solids that were bcine
reeye"1 ed contained areas of blackish discoloration probably
due to the production of sulphides in the lower layers
of the s1. imes. Stages 1 end 2, which were operated in
earallcl and coch equipped with a hood enclosing an at-
mosphere enriched with oxygen, showed significant bridging
by the slices across the 1/4 inch spacing between the disks
after about 9 da vs. When this condition was reached the
stages weie bypassed and the direction of rotation was
reversed for about 5 m: nutes. E>y this means much of the
slime" were detached and conducted to drain. Examination
of the sleughod—off solids from the 2 stage" indicated
"inaeroh';c activity had been taking place in the lower
layers of the slimes r.otwithstanding the exposure of the
sii!-/•>«- to -stmosoberes enriched with oxygen.
The slimes on Stages 3 to 6 were found to develop a
largely blackish oppearan.ee after a few days and to have
grayish aerobic skin, about 1/2 mm thick at the surface.
Although, the cumulative removal of these 4 stages was
en.lv .->v>ou.t 16 mg/1 of T.O.C. and .1.5 mg/.l of D.T.O.C.
the siu~° growth rate was sufficiently rapid to be able
b"i'7"e the ?¦/.?• ; peh s"''acire between the disks at 9
'V,y intervals. The stag^- wo.ro bypassed and the dish
r.r»v- n v,'^'.',hTr.r) £¦! rn^nu'i'cs to
separate the excessive growths from the surfaces. In
v. Ian!: practice th^se solids would be conducted to the
nf lu.e^t ef the primary settling t-^nhs. It v/as also
93
-------
observed that between Stages 7 and 9, the slime growth
rate was very slow and the thickness did not exceed 1 mm.
This made possible reducing the clear spacing between
the disks to about 1/4 inch without fear of bridging.
Since Stage 10 was equipped with a hood enclosing an
atmosphere enriched with oxygen, the slime thickness was
never more than 1/2 mm at any time, and it might have
been possible to operate with as little as 1/8 inch
spacing between the disks with due consideration for
some loss of contact time under that condition of operation.
In the light of the foregoing findings it was decided
to take the following steps in an attempt to improve the
quality of the effluent leaving Stage 10.
(a) Increase number of disks on Stage 4 to 71
and construct hood over that stage for enriching the
atmosphere with oxygen.
(b) Add sodium nitrates to the influent to the
pilot plant in order to prevent anaerobiasis in the lower
layers of the slimes with consequent organic acid and
sulfide formation.
(c) On February 17, 1971 the disks on Stage
9 were restacked with 71 to replace the former 48.
Sodium nitrate was added to the influent to the pilot
plant at about 4 mg/l as N., but due to difficulties
with the chemical feed pump the additions were quite
erratic. In any event, after operating for the first
two weeks of February 1971 without recirculation and
with modifications (a) and (b) cited above in force,
inspection of the slimes on Stages 3, 5, and 6 indicated
that much of the black discoloration in the lower layers
had virtually disappeared after only a few days. The
slimes in Stage 4 grew slowly and reached a thickness of
only 1/2 mm. after 2 weeks of such operation.
EFFECT OF RECIRCULATING NITRATE TREATED SLIMES
At this time it was felt that the new slimes, supplied
with nitrate oxygen in the lower layers might be recir-
culated in an attempt to improve the performance of the
10 stage plant.
94
-------
Accordingly on February 15, 1071 the recirculation of
sloughed off solids was again started, this time with a
culture presumably capable of utilising dissolved oxygen
for its metabolic processes in removing organic carbon
from the wastewater. The wasting rate was set so as to
accumulate about 300 to 500 mg/1 of suspended solids
Passing through the .10 stages of treatment. This solids
concentration did not stress the dissolved oxygen level.
The average data obtained has .been compiled in Table 4.
The concentrations of T.O.C. in the influent to the pilot
plant v/ere 64 and 87 mg/1 respectively for the periods
without and with recirculation while the concentration
i." the effluents from Stage 10 were essentially the same
at 17 mg/l. The concentrations of dissolved total organic
carbon were 29 and 32 for the influent and 12 and 13 for
the effluents for the two periods of operation. It would
appear that some improvement was accomplished in the
percentage removal of total organic carbon. However'that
improvement v;ar> not achieved in the dissolved fraction as
con be seen from the data presented. Therefore the in-
creased rate of removal, if significant, was confined to
the suspended organic carbon.
T.t can be seen from Table 38 that the albuminoid and am-
ron.ia nitrogen was relatively unaffected in that it entered
the pilot plant at about 23 mg/1 and left Stage 10 at 26
"¦g/l. The bicarbonate alkalinity decreased to about 20 r.g/1
across Stage 1, for some unexplained reason, and thereafter
was \:r.ir.fluonced by the treatment through Stage 1C-. This
aenfir-s that nitrification was not taking place in the
downstream stages. The orthophosphato concentration in the
wastewater entering the pilot plant was 19 mg/1 and 25 mg/1
respectively for the two periods and left Stage 10 at
'.7 r.r/1 and 20 mg/1.
0P7J'j\'.l'J0S REPEAT USING NITRATE - TREATED SLIMES WITHOUT
'v'CYCJjIKG
^•eeaur-e the foregoing data indicated that by recycling
nitrate treated slimes an improvement in operating results
"light ho possible, at least with respect to the suspended
organic "¦",rbor. fraction, it was decided to gain addition.*'!
•';."vL-a re".ovnnt to the performance without recirculation,
Accordingly, during the month of March 1971 the addition
of ro-"'"e '.-odiuf. nitrate wes continued at a rate of about
mg/1 a-
o .T,
-------
T:\BL
i\VMR«G2 0
;vriNG
DATA
L'.UARY
19 71
TRSy/.i.'2'D
'3 L-IM
ES VJ1
'EMPi
SRATUR
SJDF
L 0:1
ItriFI
: t
G
. ?. M,
1
2
3
T.O.C.
14
64
34
40
30
".¦litii
14
87
62
CO
47
D, i'.O.C.
Without
14
29
21
19
19
With
14
32
25
•n
22
C.O,D,
Without
14
197
112
111
121
With
14
294
.155
164
139
AL3»+- Arrm.N
Without
14
24
-
-
2.5
with
14
25
-
-
25
HCO3 ALK
V;i thout
14
239
219
223
With
14
247
221
—
228
^04(Ortho)
14
19
18
-
17
Without
With
14
25
22
—
21
*FINAL SETTLING TANK
38
JITH AND WITHOUT RECIRCULATION 05' NITRATE
/ASTEV.'ATKR 57° F, VALUES IM Mq/l
'Jf
4 5 6 7 8 9 10 i-'.S.T
23
39
18
19
27
31
16
18
22
29
17
17
19
25
16
15
20
22
15
14
20
22
14
J. 5
17
17
12
13
13
13
11
9
93
122
25
27
28
23
26
26
26
25
224
230
17
228 - - 224
222 - 232 - 239
215
222
17
216
215
18
20
20
18
-------
The avrarc data. obtained v:ith rerpect to Ml. parar?.etcr<-
ir riven in Table- 35. Comparisen ?/ this performance, ret
uoirtg rcci reflation, with the previous performance, uring
"^circulation, during the end of February reveal.'; no
significant advantage was gainen by the recirculation of
nitrate treated slime relative to the concentrations of
T.O.r. end D.T.O.C. leaving Stages ? and 10. The data
indicate?; that the oxidi/.oble nitroqen was reduced from
t?~o 23 ng/l level in the influent to 2.6 mg/1 leaving
Stage 10. Thin low level of nitrification was corroborated
by the drop in all;.?.Unity of about 20 m.g/1 effected while
passing through the downstream stages. Apparently the
treatment was sufficiently effective to bring the nitrifiers
b.-sr>. upstream at least to the 9th and 10th stages when not
employing recirculation.
o
J >
-------
vD
CO
NITRAT
nn£>/C
PARAMETER INFL.
12 3
T.O.C. 79 52 53 43
•D.T.O.C. 35 21 20 21
C.O.D. 303 167 172 178
AL3.+
Air^on. -N 28 - - 28
N03-JS 1 2 3 2
HC03 ALK. 242 232 - 235
P04{Ortho) 25 17 - 17
* FINAL SETTLING TANK
1 P.
3.2<
STAGE S?0.
5 6 7 8
2? 21 21 19
1 2
... o
10
16
*
F.S.
12
28
17
13 2 7
237 243 232 236 240 221 216
17 17
16
17
2 3
5
2C0
16
-------
TREATMENT SUBSEQUENT TO FINAL SETTLING TANK
A ALGAL UNIT
Towards the end of 1970 the first five stages of the six
stage algal unit had been equipped with 3 ft. diameter -
.1/4 inch thick plexiglass disks. The total number of
disks in the five stages was 38 and the spacing between
disks was about 3 inches. Inserted between each pair of
disks wsre two, horizontally placed, 3 ft. long hiqh-
output fluorescent lamps their centerliries located about
9 inches and 12 inches above the centerline of the shaft.
The end disks on the shafts were also illuminated. The
face of the lamps was about 3/4 inches from the face of
the rotating disks. The disks were rotated in the range
of velocity between 2 and 4 R.P.M. The sixth stage of
the alqnl unit was used to separate that portion of the
algae generated which had sloughed off the disks. Thi.s
was done to prepare the wastewater for subsequent treat-
ment.
The volume of fluid in each of the stages was 45 gallons and
the flow passing sequentially through the 6 stages varried
between 3 and 4 gallons per minute and so averaged 3.5 gpm.
Because the algal phase of the work was not approved for
this period of operation emphasis was placed on the as-
sessing the performance of the prior 10 stage unit which was
heing subjected to stress. However, the modified algal
unit described above was allowed to operate and data was
obtained relative to the overall performance with respect
to organic carbon, inorganic carbon, nitrogen and phosphorous.
That data has been averaged for the four months involved and
is presented in Table 40.
It can be seen from the table that the algal unit removed
both suspended and dissolved organic carbon. In fact
during January 1970 when the suspended organic carbon load
was higher, that is, (22 - 12) 10 mg/1, 90% was removed.
Removal of the dissolved organic carbon varied between 1
and 2 mg/1.
99
-------
TABLE 40
MONTHLY AVERAGE PERFORMANCE OF ALGAL UNIT - Dec. 1970 - MAR. 1971
Conditions: Flow 3.5 gpm - 5 Stages having a total of 38 - 3* diam plastic
disks 6th Stage used as settler.—Temperature 57° to 62° F.
2 - High output Flourescent lamps between each pair disks.
Disk rotational velocity 2-4 R.P.M.
PARAMETER FINAL SETTLING TANK ALGAL 16th STAGE REDUCTION
Mg/1 Mg/1 Mg/l
Dec.
Jan 0
Feb.
Mar.
Dec.
J an.
Feb.
Mar.
Dec.
Jan.
Feb.
Mar
70
71
71
71
70
71
71
71
70
71
71
71
T.O.C.
13
22
13
12
10
13
10
9
3
9
3
3
D.T.O.C.
10
12
10
10
8
11
9
9
2
1
1
1
BICARB. ALK.
160
209
216
201
111
183
172
136
49
26
44
65
C02 ACIDITY
29
30
36
25
19
23
27
17
10
7
9
8
ALB. +
Pjtunon. N .
-
-
25
23
-
16
9
-
-
9
13
NITRATE N.
2.5
0.3
4.4
5.5
7 „ 6
2.4
8.7
llo 2
5.1
2.4
4.3
5.7
ORTHO-PO4
20.5
18.1
18.0
16.0
23.2
19.5
20.3
16.7
-2.7
-1.4
-2.3
-0.7
-------
The concentrations of inorganic carbon in the form of
bicarbonates and CO^ acidity were markedly reduced. The
first concentration'being reduced in the range of 26 to
65 mg/l and the second between 7 and 10 mg/l. The bicar-
bonate alkalinity reduction was greater than the nitrates
produced, that is on the stoichiometric basis of 7 mg/1
bicarbonate alkalinity destroyed per mg/l of nitrates
produced. Either some of the bicarbonate alkalinity
was synthesized into algal cells or else more nitrates were
produced than indicated and a portion of the nitrates
synthesized.
The CC>2 acidity entering the algal unit was reduced and
:i n addition the COo of respiration resulting from the
oxidation of the organic carbon and the CC>2 produced as a
result of the oxidation of ammonia did not accumulate
which suggests that this carbon loss was due to algal
synthesis. Total nitrogen, measured only by the sum of
the ammonia and nitrate nitrogen, entering the algal unit
during the months of February and March was 29.4 and 28.5
mg/1 which was reduced by 5.7 mg/1 and 8.3 mg/1 during
passage through the algal unit.
The average monthly ortho phosphate concentrations entering
the algal unit varied between 16 and 20.5 mg/1 and the con-
centrations leaving the unit increased by .7 to 2.7 mg/l.
Algae were being produced, some of which adhered to the disks,
and some sloughed off which were removed every two days from
the bottom drain of each stage. The generation of algae on
some of the disks was scraped off at 2 - 7 days intervals.
It was found to have 3 to 5% total solids which was mainly
algal cells. The rate of dry weight production of algae
that adhered to the disk surfaces varied from 4 to 8 grams
r\ J
per M'/day. The overall algae production, which involved
the sloughed off algae, was not measured.
CARBON ADSORPTION
A .25 gpm portion of the effluent from the 16th stage (used
as settling tank) of the algal unit was subjected to mixed
media filtration followed by passing it through the six
carbon columns. The data obtained during the months of
December 1970 through March 1971 are presented in Table 7.
101
-------
TABLE 41
MONTHLY AVERAGE PERFORMANCE OF ACTIVATED CARBON ADSORPTION
DECEMBER 19 70 THROUGH MARCH 1971*
FLOW .25 GPM THROUGH MIXED MEDIA FILTRATION AND CARBON ADSORPTION
VALUES IN Mg/1
PARAMETER MONTH
ALGAL
16th STAGE
MIXED
MEDIA
FILTER
CARBON COL. NO.
3 4 5
•
u
•
o
•
Dec.
8.0
8.0
5.8
5.0
4.1
3.4
2.3
2.3
Jan.
12.7
13„0
10.6
9.0
6.8
6.1
5.5
5.0
F-b.
10.3
8.1
7.3
60 1
5.1
4.3
4.6
3.3
Mar.
8.6
8.4
7 o 3
5.4
5.9
4.2
3.6
3.1
D.T.O.C.
Dec.
6.8
6.8
4.8
4.3
3.9
3.8
3.1
2.4
Jan.
11.7
10.7
9.2
7.8
6.0
4.9
5.4
4.5
Feb.
9.1
6.5
5.8
5.9
3.9
4.1
4.3
3.1
Mar.
8.5
7.4
6.2
5.3
4.3
3.9
3.6
2.9
ALB. &
AMMON. N.
Dec.
-
-
-
-
-
-
-
-
Jan.
-
-
-
-
-
-
—
—
Feb.
15.6
15. 6
-
-
-
-
-
13.1
Mar.
10.3
10.3
—
-
-
—
-
8.1
Page 1 of 2
-------
41 £Con-inuec3)
MONTHLY AVERAGE PEp_PORLAN'CE OF ACTIVATE!1 CARBON ADSORPTION
DECEMBER 19 7 0 THROUGH .K.ARCH 1971*
FLOW .25 GPM THROUGH MIXED .MEDIA FILTRATION AND CARBON AE5CRPTION
VALUES IN Mg/1
PARAMETER MONTH ALGAL MIXED CARBON COL. NO.
16th STAGE MEDIA 1 2 3 4 5 6
FILTER
M
2 NITRATE N. tec. 9.4 11.5 11.2 - - - - 11.4
Jan. 2.1 2.1 1.6 - - - -
Feb. 8.7 9.6 8.8 - - - - 7.2
Mar. 11.2 12.1 12.1 - 9.8
* DURING THIS PERIOD THE 10 STAGS UNIT WAS BEING SUBJECTED
TO HIGHER FLOW RATES.
Page 2 of 2
-------
The concentrations of T.O.C. and D.T.O.C. entering the
carbon columns was about 8 and 7 mg/1 respectively except
for January when the corresponding values was 13 and 10.7
mg/1- The concentrations of T.O.C. and D.T.O.C. were
reduced almost linearly while passing sequentially through
the activated carbon adsorbers until reaching the level of
about 3 mg/l leaving carbon column No. 6, except for January,
when the corresponding values were 5.0 and 4.5 mg/1.
The table also includes data relating to the oxidizible
nitrogen in the form of albuminoid plus ammonia nitrogen
which parameter showed a decrease of about 2 mg/l across
the carbon columns for thr months of February and March
1971. During those same months the concentration of
nitrates was lowered by about 2 mg/1 across the carbon
columns.
104
-------
SECTION X
THE BIOTA OF THE GROWTHS ON THE ROTATING DISKS
Frequent microscopic observations were made of the growths
on the rotating disks during the entire experimental period.
The type of sequential treatment provided an opportunity
to observe the succession of biological populations with
progressive purification under a given regime of treatment,
not readily feasible with other methods of biological
treatment. On the basis of these frequent samplings the
following general observations can be made:
(a) The dominant microscopic population on the first
and second stages of the 10 stage unit, designed for the
removal of organic material and oxidation of ammonia nitro-
gen consisted of zoogleal and of filamentous bacterial
growths during the period when the disks were exposed to
normal atmosphere.
(b) As the growths on these first several stages
became thicker, the material next to the disks became
black and a white growth appeared on the surface exposed
to air which was identified as Beggiotoa.
(c) The diversity and abundance, of the protozoan
population increased progressively on the subsequent stages
of treatment. They consisted of free swimming ciliates
followed by increasing numbers of attached ciliates, roti-
fers and nematodes in succeeding stages. At times the
entire microscopic field would be covered by a lawn of
vorticella in one or the other intermediate downstream
stages.
(d) The exposure of the growth on stage 1 to en-
riched oxygen atmosphere eliminated the filamentous
bacterial growth and most strikingly moved the microscopic
animal populations referred to under item (c) upstream
to stage 1.
(e) The growths on the illuminated rotating disks
consisted primarily of diatoms and on t-he periphery of
the disks of filamentous green algae.
105
-------
In order to obtain a permanent record and a positive
identification of the microscopic life of the growths
on the disks the services of Dr. Olson, Professor of
Environmental Biclogy of the University of Minnesota
was called upon. He made a visit to the project on
December 11-12, 1969, made in situ microscopic examina-
tions and collected a series of samples from successive
stages for detailed identification and preparation of
photo micrographs in Minneapolis. His report is included
in the appendix. Of the 72 photomicrographs he has sub-
mitted 10 black and white reproductions are included in
present report as representative of the types of organisms
found. It is of interest to excerpt the following state-
ment from his report: "The overall impression, as one
view? the Rutgers rotating disc experimental waste treat-
ment unit is that the biological life which has developed
closely parallels that seen in r> small heavily polluted
creek or brook when the organic wastes added have a point
source and there is one sewer outlet. By microscopic
examination one can follow the improvement of the water
step by step as successive groups of organisms "work over"
the material".
An additional record of the biological life was made by
the private resources of the project director and the
consultant by the professional production of a motion
picture of the biota on the rotating disks. The film
vividly portrays the abundance, diversity, the activity
and the morphological details of the biological popula-
tion of the successive stages of treatment.
106
-------
FIG. 13 CARCHESIUM SP. FILAMENTS BEGGIATOA
107
-------
FIG. 14 BEGGIATOA STAGE 4
108
-------
FIG. 15 VORTICELLA SP. DIFFLUGIA CONSTRICTA
STAGE 7
109
-------
r
FIG. 16
TYPICAL ROTIFER STAGE 10
110
-------
FIG. 17 AMOEBA STAGE 11 EDGE
111
-------
PIG. 18 HORMIDIUM KLEBSII STAGE 11 SIDE
112
-------
FIG. 19 DIFFLUGIA CONSTRICTA SMALL SPECIMENS
DIFFLUGIA SP. HORMIDIUM KLEBSII
NITZSCHIA SP. CILIATES
STAGE 11 EDGE
113
-------
FIG 20 DIATOMS NITZSCHIA IGNORATA
NITZSCHIA SP.
STAGE 11
114
-------
FIG. 21 NEMATODE IN EGG
HORMIDIUM KLEBSII
NITZSCHIA SP
STAGE 11
115
-------
PIG. 22 BETWEEN ILLUMINATED UNITS
"BLACK ALGAE"
ARCELIA SP. IN TANGLE OF
OSCILIATORIA FILAMENTS
STAGE 11
116
-------
SECTION XI
MATHEMATICAL steady state model application for
REMOVAL OF ORGANIC MATTER
The modelling of the removal of carbonaceous matter from
wastewater by partially submerged rotating disks was
recognized as being an extremely complex problem. Since
Dr„ John Andrews, Professor and Head of Environmental
Systems Engineering, Clemson University has made extensive
studies of fixed film reactors* a joint effort between
Rutgers University and Clemson University was undertaken
in an attempt to resolve this problem. Accordingly, Dr»
Andrews assigned a Ph0D. candidate, Mr0 Colin Grieves# to
utilize pilot plant data obtained by Rutgers University
in conjunction with data obtained by use of a bench scale
rotating disk unit at Clemson University for the purpose
of deriving a mathematical model# The following sections,
incorporating th3 rationale and derivation of a steady state
mathematical model were extracted from the doctoral thesis
by Dr. Colin Grieves entitled "Dynamic and Steady State
Models for the Rotating Biological Disc Reactor," August,
1972c
Development of a Steady State Model for a Rotating Disc
System
A set of steady state equations for the system can be
obtained by setting the time derivatives in the dynamic
equations equal to zero. However, this would result in
equations which could only be solved by computer techniques0
By taking a slightly different point of view of the rotating
disc system, steady state equations can be more readily
developedo The?e equations can then be solved simultaneously
to produce one equation relating substrate influent concentra-
tion and flow rate with substrate effluent concentration«
System parameters in the equation will be rpm, depth of
submergence, and disc area0 Reference will be made to Figure
111-6 throughout the course of this derivation«,
Consider positions 0 around the disc. From the point of
view of an observer stationed at some position M on the disc,
a stream of liquid appears to be flowing at a rate Ff past
117
-------
RPM
00
Bulk
y * / Ff
/ r.i * «
Cb
*1
Liquid
^IF.M
Film
Liquid
i
>
Bio
7
Film
/
Sulk
Liquid
6=6
AV,
View Y-V
6=0
FIGURE III-6. SCHEMATIC OF DISC FOR
STEADY STATE MODEL
118
-------
that position.
The model will be developed by making mass balances on
1. Substrate in the liquid film
2. Substrate in the organism film beneath the liquid
film
3. Substrate in the organism film submerged in the
bulk liquid
4. Substrate in the complete mixing reactor
Several more assumptions are necessary before making the
mass balances.
Assumptions
1. There is no change in substrate concentration with
position on the radius either within the liquid film,
within the biological film, or within the bulk liquid#
2. The organism film is assumed to be completely mixed in
the direction perpendicular to the surface it presents for
substrate transfer i.e. the z-direction0
3. There is no significant substrate diffusion within the
biological film either in the 0- or radial directions.
4. Substrate concentration inside the biological film when
it is submerged in the bulk liquid does not change with
position in the 0- or radial directions.
5» The mass of liquid film adhering to the disc which is
moved per unit time by the dibcr Ff# is independent of
both 0- and radial position.
The model can now be derived by making the mass balances.
119
-------
lo Mass Balance on Substrate in an Elemental Volume
ih the Liquid Film at Position Ms
LF,M
Accumulation = (111-25)
at
Input
(111-26)
Output = (pf>CLp,M+AM(0+AG't> (111-27)
Utilization » (K^) (AA) ["c^-.ptm( 0»t) — (111—28)
Where C „(G«t) indicates that the concentration in the
LiF i M
liquid film is dependent upon position and time. M is
the concentration of substrate within the completely mixed
biological film in the air at position M in the O
directionD
Further relationships are
* (R. ) ( QA/2)
(111-29)
»V,M " '»>
(111-30)
where R^ is the disc radius0
By substituting into the mass balance
Accumulation =» Input - Output - Utilization
G't)
9t
(Rl)2(<5£/2)
CLF#M^®'t^ " CLF,M+ fj( Q+AS/t)
A0
-5
6,
(111-31)
120
-------
But, by definition
a_lLF.Ml{,) = lim
30
CLFW0+*9) " CLF,M(^
AG
0-+-O
(111-32)
Therefore*
3t
(R1)2(5L/2)J 30
— (^LF,^ "" (111—33)
2. Mass Balance on Substrate in an Elemental Volume AV^ M
in the Biological Film at Position M: '
Assume homogeneity in the z-direction and no significant
diffusion in the 0- or radial directions inside the bio-
logical film.
Accumulation = ^ 9C^M(0»t)
3t
Input
Output
(Kl)(aA) ^CLp^M(©#t) - C^^M(0,t)J
Utilization = (jj) (X) (AV3)Cc1>M(e,t)]]
(y) ^
-------
Accumulation °» Input - Output - Utilization
and simplifying by cancellation
3t Az
- ty) Mte.tQ (111-35)
(YjplKcXn) +^2^(0,0]]
3. Mass Balance on Substrate Inside the Biological Film
Submerged at Any Point in the Bulk Liquid:
Assuming that substrate concentration inside the biological
film does not change with position and making a mass balance
similar to that made for equation (111-35), an ordinary
differential equation results:
£Cg = Kl(Cjj - c£] - (u)(X) (C8) (111-36)
dt Az (Y)[jKc)(n) + Cj
where C is the substrate concentration inside the biological
film submerged in the bulk liquid.
4. Mass Balance on Substrate in the Complete Mixing Reactorx
Accumulation = Input - Output - Utilization
Vb ££b = r£o - cb] - Ffjcb - ClFiEJ - (KL)(AB)[cb - CSJ
dt (111-37)
where Clp#e is the substrate concentration in the liquid
film as it re-enters the bulk liquid and Afl is the area of
disk submerged in the bulk liquido
122
-------
Equations (111-33, 111-35, 111-36, and 111-37) could
represent a pseudo-homogeneous model of the system. At
steady state these equations become
££lF,M = (Kl) (Rj)2 [clp^ _ C1#mJ (111-38)
d0 2Ff
K [c C ""] a (ClM)
^LlfLF,M " 1#mJ a 1,fa (111-39)
Az (Y)[jKc)(n) + C1#^j
KLfeb " c2 a (yi) (X) (cs) (111-40)
AZ (Y)Q(Kc)(n) + c£j
P |c Q - CjQ «=¦ Ff |cb - + (KL) (As)[cb - cJJ (111-41)
Equations (111-38, 111-39, 111-40, and 111-41) represent a
steady state model for the rotating disc system, and are
easily solved by computer techniques. It would be desirable
however, to be able to solve these equations with only the aid
of a slide rule or desk calculatoro In order to do this,
the equations can be simplified by assuming that for re-
latively low reactor substrate concentrations (less than
50 mg/1, for example)e
(Kc)(n) > **i,M an^ cs
This assumption is justifiable because both and Cg
represent effective substrate concentrations within the
microbial film, which are less than the concentrations
in the reactor bulk liquid„ Moreover, in many cases the
reactor bulk liquid substrate concentration is itself
expected to be low (<50 mg/1) when compared to the influent
substrate concentratione
123
-------
Equation (111-39) then becomes
^fcuF.H *" Cl,*3 " (u)(X) C1>M (111-42)
tU
Az (Y)(K )(n)
or
CLF,M ** C1,M - (y> (X) (Az) C1(M (111-43)
(Y)(Kc)(n)(KL)
r , v ('0 (Az)
1 13 (111-44)
(Y)(Kc)(n)(KL) 1111 ^
then C1#M « Clp.m (111-45)
1 + K.
Substitution of (111-45) into (111-38) and rearranging
yields
C ®
?— UP #e r~ 2
\ . . (Pi>(Ri> de (m-46)
% CLF,M 2Ff
Where Px = (j^H^) (111-47
1 + Kx
Under the assumption that does not depend upon Q, then
in _ (P1)(R1)2(0) (111-48)
cb 2^
124
-------
-ripi) «a }/Pf~!
or £lp,E « e L (111-49)
Cb
where Aa is the area of the disc in the air0
Equation (111-40) can be arranged similarly to (111-39) to
give
cb
Cs ° (111-50)
1 + Kx
Substitution of ^111-50) into (111-41) and rearranging gives
P CQ o p + Ff - (Ff) + (AgMPjL) (111-51)
Cb cb '
Substitute (111-49) for C^g/Cj, in (111-51)
-[(PlXV/F^-l
£-
F CQ = P + Ff (1 - e
Cb
Re-arrangement of (111-52) yields
+ (AB)(PX) (111-52)
c r I
1 +" LPl) (As) + Ff " ® JJ
(111-53)
Ff is the quantity of liquid film attached to the biological
film which enters the reactor per unit time
125
-------
Ff = (K2)(ir) (RPM) £Rl)2 - (R2)^j(4L) (111-54)
where K2 3 1 if there is no dripping
R2 ™ length of the radius not submerged
a thickness of the liquid film if the
oisc were submerged up to its mid-
diameter (R2-0)
or Ff = (P2)(RPM) (111-55)
For N discs equation (111-53) becomes
£b
C„ r f -pPj,)(Aa)/P2)(RPMT]>ri
1 + N jjlPjLHAg) + (P2)(RPM)^1 - e J J
(111-56)
Equation (111-56) is a steady state equation expressing
reactor substrate concentration as a function of influent
substrate concentration, flow rate, number of discs* disc
rotational velocity, area of disc in the atmosphere and area
of disc submerged in the reactor bulk liquid. Such an
equation would be useful for a manufacturer who would most
likely fix the ratio of the submerged disc area to total
disc area as well as rotational velocity. Consequently, an
equation which could be used by a consultant or design en-
gineer would be even simpler than (111-56):
Cb = I (111-57)
C
o 1 +
r t -
-------
P2 a (P2)(RPM)
(111-59)
P
-------
Let K"= (p)(TF)n"1(X)(Az)
1 (Y)(Kc)(n)(KL)
(111-61)
where n is the stage number. can be redifined
(for reactors in series) as P1# where
" (KL)(K,-)
P. oo .. - ¦¦ ' t" (111—62)
1 + Kx
The Steady State Model
The steady state model (equation 111-56), as developed in
Chapter III, was used to simulate the data from a field
sized reactor. Torpey et al. (124) described results
of experimental work on a 10 stage rotating disc pilot
plant with New York City domestic sewage as the process
influentc Tables V-9 and V-10 present details of the
system used by Torpey and values of the parameters used
in the simulation of the steady states The values used
for the parameters in this model are in accordance with
those discussed earlier in Chapter III. The value for
x] was found by trial and error.
Pigure V-23 shows the simulation of the reactor of Torpey
et al. (124), using the steady state model,, This figure
compares the effect of assuming no change in growth rate
with stage number (TF=1) with the effect of including
growth rate changes i.e., including the effect of decreasing
treatability with increasing stage number, as discussed in
Chapter III0 For the simulation of this effect TF was
chosen to be 0.9. It can be seen that there is no ap-
preciable difference between the two curves up to and
including stage 5„ Beyond this stage the values of the
data points are probably in doubt — the accuracy of the
BOD test at these apparent low BOD values is open to
questiono Although the simulation is apparently improved
by inclusion of TF, it is doubtful whether this would be
practicalo Inclusion of TF would entail calculating, or
measuring, Pj_ for each stage, and so complicate the use of
the modelo
129
-------
Table V-9. Dimensions of the Rotating Disc System Described
by Torpey et al. (124)
Dimension Value Units
Disc Diameter
0.915
(3)
m
(ft)
Number of Discs
48
Available Surface
Area
56.1
(600)
2
m
(ft2)
% Area Submerged
4405
%
Number of Stages
10
Disc Rotational
Velocity
10.0
rpm
Time Spent in Air
By Disc per Rev.
0.055
min
Time Spent in Liquid
By Disc per Rev.
0.045
min
Nominal Tank Volume
0.194
(6.85)
ra3
(ft3)
Estimated Actual Tank
Volume
0.116
(4.09)
m3
(ft3)
Flow Rate
0.0282
(0.996)
m3/min
(ft3/min)
Influent Substrate
Concentration
124.00
mg/1 BOD
5
Nominal Detention
Time
6.9
min
Estimated Actual
Detention Time
4.1
min
Temperature Range
16.6-25.
6
°C
129
-------
Table V-10. Values of Parameters Used in the Steady State
Model to Simulate the System of Torpey et aln
(124)
Parameter
Value
Units
Area Factor*
RPM
co
P
X
Y
A
V
*0
n
Az
6l
Kt
Disc Width
Including
Organisms
TF
P,
1.0
10.0
124.0
0o0282
32,100
0.5
3o33xl0"3 (0o21) 1/rain (lAr)
40.0
5o0
rpm
mg/1 BODg
m 3/min
mg/1
mg/1 BODg
2.0xl0"4
l.OxlO"4
6.0xl0"3
0.458
0.015
0o005
0.9
2.2xl0~4
5o88xl0"5
m
m
m/min
m
m
m
m/min
m-
130
-------
160
Data Points
TFb=0#9
TFB 1*0
~ 100
40
Bio- Disc Stago Number
FIGURE V-23. SIMULATION OF THE SYSTEM
OF TORPEY ct r4. (124} BY THE STEADY
STATE MODEL
131
-------
swqnary
This chapter has presented examples of the dynamic data which
were collected from the two laboratory reactors. Steady
state data obtained by Torpey et al. (124) is also presented»
Simulation of the laboratory reactors has revealed that the
dynamic heterogeneous model could itself be represented by a
dynamic pseudo-homogeneous model0 These dynamic models,
because of inherent deficiencies in the organism growth
portion of the models, fit short term data better than long
term data* A sensitivity analysis has shown that the dynamic
models sore most sensitive to the value used to represent the
interfacial area for mass transfer between the liquid and
biological phaseso
The steady state model, utilizing first order substrate
removal Kinetics, was shown to adequately fit the data
from Torpey et al. (124)0 However, the fit was improved
by decreasing the organism growth rate by 10% below the
value used to simulate the previous stage.
132
-------
SECTION XII
DESIGN CONSIDERATIONS
Number of Stages
The removal of carbonaceous matter, measured in terms of
BoO.D.^, was shown to be concentration dependent, at least
between the limits of concentration encountered in this
investigationo By treating the pre-settled wastewater
sequentially through stages of partially submerged rotating
disk assemblies, the effective concentration of B.0.D.5,
which supplies the driving force across the slime-wastewater
interface, can be increased over that in a single stage to
achieve equivalent effluent quality» For that reason, the
number of stages used in an installation bears an inverse
relationship with the area of disk surface required. This
relationship, applies only to domestic wastewater, and must
be distinguished from treating high Btrength industrial
wastewaters where the process is not so rate-limited until
the higher concentration of organics is reduced towards
the range of that found in domestic wastewaters.
However, other design considerations compel a limitation on
the number of stages that might be used advantageously. It
became apparent during this investigation that, when treating
a constant flow of primary tank effluent at 7.5 gpm, five
stages of treatment, all exposed to nornal atmospheres, was
sufficient for the oxidation of about 90% of the Bo0oD„5.
The effluents from the upper two of these five stages of
treatment did not contain dissolved oxygen0 Although odors
were not detected in the enclosed structure where the work
was performed, examination of the slimes in those upper two
stages revealed that anaerobes were active„ which was
manifested by a black discoloration in the solids in the
layers of the slime beyond about 1/2 mm from the surface0
That hydrogen sulphide was being generated by this anaerobic
activity was attested to by the fact that Beggiatoa, which
utilize that compound as an energy source, were found to have
colonized areas of the disks, especially during the warmer
weathero Popel (1) found, when treating a somewhat stronger
wastewater, that offensive odors were being generated in the
upstream stages, which condition was correlated to excessively
high loading rates on the lsto stage of treatment, Accordingly
133
-------
he recommended that, the rate of B000Do5 loading of the first
stage not exceed about 1 lb/100 sq.fto/day (50 grams/M2/day)„
This loading rate limit was coincidentally, about the same
as that on the third stage of treatment in the pilot plant
where about 105 mg/1 of dissolved oxygen was present in the
effluent, under the above described conditions of operation®
Accordingly, in order to prevent the possibility of generating
offensive odors, especially during the warmer weather, it is
recommended that the load on the first stage of treatment be
limited to 1 lbo B.OoD.5/100 sq0ft. disk surface/day0 In
connection with the overloading of the upstream stages it was
observed especially during the warmer months that sphaerotilua
natans had developed on Stages 1 and 2. These filaments
exerted the adverse effect of increasing the torque required
for rotation by reason of their extensive surface0 This vast
surface was not found effective in improving treatment ef-
ficiency over zoogleal surfaces,, Consideration might be
given to constructing the first stage somewhat larger than
succeeding stages, or simply limiting the number of stages
used in order to insure the avoidance of odor production and
to suppress spaerotilus growtho
An increase in the number of stages does lessen the disk
surface requirement for the removal of B#0.D<,5, especially
when increasing from 1 to 2 stages<> However, a progres-
sively slower decrease in surface area requirements can be
realized with increases in the number of stages from 2 to 3
and 3 to 40 Attention is directed to the fact that, as the
number of stages are so increased the savings in area are
offset by having to increase the number of shafts, bearings
and drive equipment,, It would appear therefore that at the
cencentrations found in normal domestic wastewater, the
optimal number would lie between 2 and 4 stages as determined
by meeting the criterion of avoiding overloading of the first
stage with carbonaceous mattero
Although the biochemical reactions involved in the oxidation
of ammonia are consecutive, first to nitrite, then to nitrate,
these reactions do proceed simultaneously within the same
slimeo They cannot take place however until the filtrate
carbonaceous B.00D.5 has been reduced below about 15 mg/1.
The rate of oxidation of ammonia-N by the slimes is not
governed by the concentration but by the metabolic rate of
the active mass of nitrifying culture which rate follows the
134
-------
law of Arrhenius as to temperature. The oxidation of
ammonia-N is a function only of the metabolic rate of the
active mass as the biochemical reactions are relatively
slow and not limited, at normal rotational velocities, by
the rate of diffusion of oxygen from the atmosphere in the
slimes nor by the rate of diffusion of ammonia into the
slime. As such, the rate is dependent not upon reactor
detention time, but upon real time. One stage, of nitrifica-
tion would therefore be indicated to satisfy process con-
siderations when oxidizing the ammonia-N in the wastewater
subsequent to the removal of carbonaceous matter.
DEPTH OF IMMERSION
This pilot plant equipment was designed and operated at a
constant submergence of 45% of the disk diameter. By
submerging the disks to just below the shafts, a maximum
water volume was achieved without introducing the problem
of leakage through the shaft seals. Increasing the sub-
mergence would increase the liquid detention time in each
stage at the expense of reducing the length of the arc of
exposure of the slimes to the overlying atmosphere. Although
the depth of immersion was not varied, it would appear that
it might be varied in accord with the stage of treatment
under consideration. That is to say, less immersion in the
upstream stages of treatment for the removal of carbonaceous
matter might be considered as a means to overcome oxygen
limitations. Actually however it was found in this work
that reactor time exerts a greater influence than surface
during that phase of treatment when the B.O.D.,. is being
reduced to about 50 mg/1, which would contra-indicate such
reduction in immersion to solve oxygen deficiency problems.
As to the effect of immersion on oxidation of ammonia-N,
the only consideration would be to maximize area, without
interfering with atmospheric contact.
ROTATIONAL VELOCITY
The pilot plant was operated with the disk assemblies rotating
between 6 and 10 R.P.M. This rotation produced a corresponding
range in peripheral velocity from 1 to 1.5 ft/sec. Popel (1)
135
-------
has established that the oxygenating capacity of the disks
increased quite markedly when the peripheral velocity was
increased from .5 to lo0 ft/sec. and thereafter the oxygena-
tion increased quite slowly. Tests conducted during this
investigation, to relate dissolved oxygen to rotational
velocity, supported his findingso
From a process viewpoint some advantage in power requirement
could be gained by reducing the velocity of rotation
progressively while proceeding downstream through those
stages serving to remove carbonaceous mattero This reduc-
tion in rotational velocity would be based on the fact that,
while passing the wastewater successively through the treat-
ment stages, the requirements for oxygen decrease, which for
a particular stage is in proportion to the concentration of
BoO.D.e removed by the stage.
5
Because the unit area requirement for oxygen by the nitrifiers
is relatively email, a substantial decrease in rotational
velocity becomes possible. Peripheral velocities of .5
ft/sec* is normally adequate for this purpose.
POWER REQUIREMENTS
The torque required to rotate the disk assemblies depends on
three basic factors (1) overcoming bearing friction (2)
overcoming the hydraulic drag forces on the immersed disk
surfaces at low velocities and (3) the energy expended by
the pumping action of the disks at higher velocities of
rotatione The power requirement to force alternate contact
between the slimes and the wastewater and between the slimes
and the atmosphere is considerably less than that required
by other forms of biological treatment.. This saving in power
costs arises from the fact that the process requires only that
the 10' to 12' diamo disks be rotated at relatively slow
speed, say 1 to 2 R.P.M. When peripheral velocity of the
disks is increased beyond, say 1 ft/sec0, the power require-
ments do increase rapidly, varying directly as the third to
fourth power of the velocity, depending on disk confirmation.
An increase in peripheral velocity beyond the l'/sec level
adversely affects the economics of the process. Under normal
operating conditions in full scale plants employing 10 ft.
diameter disks the power consumption approximates 150 K.WoH./M.C
136
-------
treated to remove 90% of the B.O.D.g.
DIRECTION OF ROTATION
During the initial phase of the investigation, the disk as-
semblies were rotated both in the same and opposing
direction to the flow of wastewater through the tank. It
was observed that when operating with the disks opposing
the flow of wastewater through the stage about 1 quart of
sludge, formed at the base of each stage, was removed daily
through a valved drain. The sludge accumulation about
doubled when the disk assemblies were rotated in the op-
posite direction. In any event drains should be provided
for the removal of any accumulation that might occur., The
quantity of fluid held in each stage was slightly greater
when operating in a manner to oppose the flow of wastewater
through the stage because of the pumping action of the disks.
Popel (1) found that, when operating their particular equip-
ment, less sludge accumulated at the base of the tank in
the various stages when operating with the disks moving in
the same direction as the flow of wastewater through the
tank. In any case, the effect of the direction of rotation
does not influence the performance significantly.
Under some circumstances it could be desired to remove some
slime from the surfaces, especially in an upstream stage
involved with the removal of carbonaceous matter. In that
connection abrupt changes in direction and speed was found
quite effective in causing the separation of much of the
slimes and, as such, could be used to control slime thickness.
Rapid regrowth in the upstream stages restores substantially
full performance in less than 24 hours and, during the
interim, the subsequent stages maintain treatment deficiency.
SPACING
The clear spacing between the disk surfaces was varied only
between 1/4 and 3/8 inch, which the reactor volumes were
essentially unchanged. It was originally intended to vary
the spacing from 1/4 inch up to 1 inch, but sufficient labor
was not available to perform the necessary tasks of dis-
sembling and reassembling the disk units.
The removal of carbonaceous matter accomplished by a stage
of treatment is basically a function of disk area and
detention time. When the disk spacing approaches zero,
time exerts an infinite effect and surface no effect. When
1 "5 1
-------
the disk surfaces are spread beyond a certain limit,
further increase in spacing does not influence performanceo
The joint influence of both of these parameters gains signifi-
cance when the spacing is reduced to a region of interest,
which is below 1 incho The range of spacing between 1/4
inch to 1 inch is of particular interest,, That an optimal
relationship might exist in that range, between the disk
area and the disk spacing, was indicated by studies described
heretofore wherein the influent flow to the pilot was shut
off and trapped flow was treated with the disks turning for
1, 2, 2o5, and 5 additional periods, each equal to the
displacement time through one stage* These data showed that
only one, or possiialy less, additional detention period
was effective in lowering the B000D<,5 concentration in the
fluid in each of the 5 stages involved in carbonaceous
removalo Thereafter no further lowering in the concentration
of B.O.Do5 took place for four additional detention periodsa
These findings are interpreted to indicate that for the amount
of disk surface employed under those operating conditions, the
detention time should have been about doubled to maximize the
removal of BoO.Doj. Since the disk spacing used was 3/8 inch,
the indication would be to double the fluid volume in the
reactors to maximize the removal of B.O0D.50 Accordingly,
the disk spacing should be doubled to about 3/4 inch, which
spacing would appear optimalo Any significant increase in
the spacing beyond 3/4 inch would serve little useful purposeo
Actually the spacing between surfaces used in present day
commercial practice is 3/4 inch when removing carbonaceous
matter from wastewatere
As has been stated the oxidation of ammonia-N is not governed
by contact time in the reactor0 The slow growing nitrifying
slimes, which are afforded a favorable environment to propa-
gate after the soluble B000D05 has been reduced below about
15 mg/1, usually stabilize at a thickness of about 1/2 mm«
The amount of ammonia-N oxidized per unit area of such slimes
is independent of the spacing between the disksG Accordingly,
the disk surface can be concentrated greatlyo However, when
considering a reasonable lower limit of spacing, the thickness
of the slimes must be evaluated0 Based on the observations
of operation of this pilot plant, if it were practical to
construct the disk surfaces as little as 1/8 inch apart,
that apparatus would serve adequately to oxidize ammonia
nitrogen at the highest rate of fluid volume now conceivable.
138
-------
AREA OF DISK SURFACE REQUIRED
The data obtained during the pilot operation, when the slimee
were being exposed to normal atmospheres, indicated that the
concentration of B.O.D.g leaving the 5th stage of treatment
had been reduced to about 15 mg/l» This would represent a
removal of about 90% of the carbonaceous matter based on the
strength of 160 mg/1 of B.O.D.^ in the raw wastewater. During
that operating period the flow treated, at constant input, was
10800 gallons per day to the 5 stage of treatment, which had
a total area of disk surface of 3100 sq. ft. These values
indicate that the average disk surface loading rate was
10800 cral/day = 3.5 gals/day/sq.ft. Since the flow rate was
3100 sq.ft.
not varied in accord with the normal diurnal pattern that
average surface loading rate could not be applied to a proto-
type operation. It is likely that to satisfy such diurnal
fluctuation in flow rate the surface loading rate vrould need
to be reduced to cope effectively with the high flow rate
period. On the other hand, since the spacing between the
disks during the pilot operation, when the subject data was
being obtained, was 3/8 inch, the reactor time would have
been doubled if the spacing between the disks were 3/4 inch
as used in commercial practice.
The removal of 9094 of the carbonaceous matter in wastewater
is being effected commercially (2) at a surface loading rate
of 1.5 to 3.0 gal/sq.ft./day. Two to four stages are being
used successfully and much experience is being gained removing
90% of the B.O.D.^ from domestic wastewater.
The surface area required for the oxidation of 1 lb. of
ammonia nitrogen per day was found to be about 3600 sq. ft.
during the summer months. During such warmer weather much
of the nitrifying slimes were found to have been devoured by
predator activity, rotifers in particular, with resultant
development of bare spots on the disk surfaces. Loss of
surface due to bare spots increases progressively from a few
percent in the first stage of nitrification to as much as 50%
after 5 stages. ¦ During colder months sfuch loss of nitrifying
surface was not experienced. While the rate of nitrification
undoubtedly slows down, during the decrease in temperature,
in accord with the normal influence of temperature on
biochemical reaction rates, the nitrifying slimes were
not victimized by such predator activity, and moreover
additional culture was active due to deeper penetration
139
-------
of the oxygen into the slime0 The net influence was little
loss of nitrifying capacity of the surfaces as the temperature
of the wastewater decreased from 78° F0 to 58° F„
It should be pointed out, in connection with the oxidation
of ammonia-N, that an economic analysis should be made of
the increased surface requirements to cope with high flow
conditions vs. the use of a tank interposed between the
primary settling tank and the disk treatment to dampen the
variation in hydraulic flow rates„
When attached slimes are exposed to atmospheres enriched
with oxygen it will be found that a marked reduction in
surface requirements for the removal of B.OoD.g can be
realized* Such enrichment on the first and third stages
of a treatment system will increase the rate of removal
of carbonaceous matter to the extent of being able to re-
duce the surface required by one half, compared to that
required using normal atmospheres., The physical exclusion
of atmospheric oxygen has the effect of depressing the pH
about .3 to 64 of a unit value, mainly as a result of
accumulation of CO2 in the enclosed atmosphere resulting
from the respiration of the slimese This depression did not
produce noticeable effect on carbonaceous removal, A three
stage treatment system would be indicated to remove carbon-
aceous matter with the first stage exposed to an atmosphere
enriched with oxygen to the range of 50% to 75% of the total
gas present, the second stage exposed to normal atmosphere
and deriving dissolved oxygen from the first stage and the
third stage equipped and operated similar to the first stage..
Although the exposure of the slimes in the second stage to
normal atmosphere detracts from the overall efficiency of
the process with respect to low surface requirements, yet
this stage performs the function of decarbonation and eleva-
tion of pH„ The use of oxygen enriched atmospheres has
the liability of having to supply oxygen equivalent in weight
to 110% of the Bo0.D.^ removed. A comparison of the operating
cost of supplying oxygen vse the capital cost of doubling
the reactor value and surface area, would dictate the choice
of method*
While the organisms responsible for the removal of carbon-
aceous matter are tolerant to oxygen enriched atmospheres
at least up to 75% of the total gasses held in the enclosure.
140
-------
the nitrifiers are not. Acceleration of the nitrification
process involves special considerations. Firstly, the oxygen
should be fed to enrich the atmosphere at a rate so that the
oxygen content should not exceed about 55% by volume. Secondly,
the use of enriched atmosphere to accelerate the rate of
nitrification becomes progressively less effective proceeding
downstream from those stages involved in the removal of
carbonaceous mattero
141
-------
SECTION XIII
ACKNOWLEDGMENTS
Rutgers University and its Department of Environmental
sciences, wishes to express appreciation to Martin Lang,
Commissioner at the Department of Water Resources, City
of No Y., for his cooperation in providing necessary
facilities and personnel who contributed importantly to
the operation of the pilot plant at the Jamaica Pollution
Control Plant in New York City.
The Department of Environmental Sciences is grateful to
Dr, John Andrews and to Dr» Colin Grieves of Clemson
University for their counsel and derivation of a mathe-
matical modelo Their valuable aid has advanced the
understanding of the complexities of the fixed film
reactor with specific reference to partially submerged
rotating diskso
The conceptual design, installation and operation of the
pilot unit and report preparation was performed by Wilbur
N. Torpey, Project Research director. Dr. H. Heukelekian,
consultant and former chairman of the Department of
Environmental Sciences contributed during the planning,
execution, the study and reporting phases0 Analytical and
operational services were provided by Mr« R„ Epstein,
chemist and G. Dozsa, technician*
The support of the project by the Office of Research and
Development, Environmental Protection Agency and the help
provided by Drc David Stephen, Dr. Fred Bacher and Dr*
Hend Gorchev, the Grant Project Officer, is acknowledged
with sincere thanks.
143
-------
SECTION XIV
REFERENCES
Popel, P. "Leistung, Berechnung und Gestaltung von
Tauchtropfkorperanlangen (Estimating, Construction
and Output of Immersion Drip Filter Plants)0" Band
11 der Stuttgarter Berichte zur Siedlungswasser-
wirtschaft Kommissionsverlag. Munich:R. Oldenbourg
1964.
Hartmann, H. "Untersuchung uber die Biologische
Reinigung von Abwasser mit Hilfe von
Tauchtropfkorperanlangen (Investigation of the Bio-
logical Clarification of Wastewater Using Immersion
Drip Filters)o" Band 9 der Stuttgarter Berichte zur
Siedlungswasserwirtschaft Kommissionsverlag<> Munich
R. 01denbourgo 1960„
Grieves# C„ H. "Dynamic and Steady State Models for
the Rotating Disk Reactor", Aug0 1972 (see appendix
for complete literature listing).
145
-------
SECTION XV
PUBLICATIONS
Torpey, Wilbur N,, H. Heukelekian, A. Joel Kaplovsky, and
R. Epstein. "Rotating Disks With Biological Growths
prepare Wastewater for Disposal or Reuse." Jour. Water
Poll. Control Fed., Vol. £3, 11,2181-2188 (November 1971).
Torpey, W. and H. Heukelekian. "Preparation of Municipal
Wastewater by Attached Biological Growths on Rotating
Discs for Disposal or Reuse." Presented at the 5th Middle
Atlantis Regional Meeting of American Chemical Society,
University of Delaware, April 1-3, 1970. (Proceedings
Unpubli shed).
Torpey# W,, H. Heukelekian, A. J. Kaplovsky and R. Epstein.
"EffectB of Exposing Slimes on Rotating Disks to Atmospheres
Enriched With Oxyqen." Presented at the 6th International
Conference on Water Pollution Research, Jerusalem, Israel,
June 18-24, 1972.
Pretorius, w. A. Formal Discussion of paper, "Effects of
Exposing Slimes on Rotating Disks to Atmospheres Enriched
with Oxygen" by W. Torpey, H. Heukelekian, A. J. Kaplovsky
and R. Epstein.
Torpey, W., H. Heukelekian, A. J. Kaplovsky and R. Epstein.
Rebuttal to Formal Discussion by W. Pretorius of paper,
"Effects of Exposing Slimes on Rotating Disks to Atmospheres
Enriched with Oxygen."
147
-------
SECTION XVI
APPENDICES
PaS£jH£Lo
Experimental Data Detail - Operating
results Biological Section and Special
StudlCS 00000 00000000» 00»»0 1S1
Table 1: pH Values c. .000000.000 151
Table 2: Daily Profiles of T.O<,C, and
DoT.OoCo Carbon Adsorption at 765 gpm 154
Table 3» Daily Profiles of Suspended Solids
Mg/1 *• at 7„5 gpin ooooooooo 160
Table 4: Daily Profiles of B.00D„5 at 7.5 gpm 162
Table 5: Daily Profiles of C0OoD0 at 7.5 gpm 168
Table 6: Phosphates oo.ooooooooe 172
Table 7: Daily Profile-Albuminoid and
Ammonia N/Nitrate Nooooo..o 173
Table 8: Daily Profiles of Ammonia o » o o . 175
Table 9: Carbon Dioxide Alkalinity o 0 o o . 179
Table 10: Bicarbonate Alkalinity o • o <. « 181
Table Hi Daily Profiles of N02/to03-N
at 7« 5 gpm a o .ooa..o«oa 103
Table 12t Daily Profiles of T.00Co and
D.To0.Co at 705 gpm oooooooo 189
Table 13s Profiles of Orthophosphates o o o . 192
Table 14: Profiles of Orthophosphates
High Plow - Subsequent to F0S0T0 o 194
Table 15j Profiles of To0oC. & DoT„0oCo
High Flow o.ooooooooo « 19 6
Table 16: Profiles of To0„Co & DoT.0oCo
High Flow subsequent to F,S0T0 „ 0 200
Table 17: Profiles of Albuminoid & Ammonia N
High Flow oooo oooooooo 204
Table 18: Profiles of Albuminoid and Ammonia
N High Flow,, ooooooooooo 206
Table 19: Profiles of B„0.De5 - High Flow o 207
Table 20: Profiles of pll at High Flow o o o 208
Table 21: Profiles of pH High Flow
subsequent to F0S0T«, « «, o . o « o 210
149
-------
APPENDICES
Page No.
Table 22t Profiles of Co0oDo High Plow e » o » 212
Table 23: Profiles of C0.2 Acidity at
High Flow oe.oooo»ooooo 214
Table 24i Profiles of C02 Acidity
Subsequent to FoS^T® o o o o o • o o 216
Table 25: Profiles of Bicarbonate Alkalinity
High Plow o o . . o . • o o « o o o 218
Table 26i Profiles of Bicarbonate Alkalinity
Subsequent P 0S0T0 o o • oooooo 220
Table 27: Profiles of Nitrates-High Plow o « 0 222
Table 28: Profiles of Nitrates-HF
Subsequent F.S.T0 ooo.o.oo. 224
Be Algal Aspects of Disk Process ooe»o»*o» 227
C. Machine Drawings o.oooo.oooo.oo 231
D« Additional References Re: Dr0 Ce Grieves 0 o » 239
150
-------
pH values
1969
DATE
INFL
1
2
3
4
7/23
7.0
7.1
7.2
7.4
7.4
7/28
6.8
6.8
6.9
7.0
7.3
7/30
7.5
7.5
7.4
7.5
7.5
8/6
7.1
7.2
7.3
7.4
7.3
8/8
7.2
7.4
7.6
7.7
7.7
8/11
7.1
7.2
7.3
7.4
7.5
8/13
7.2
7.3
7.4
7.4
7.5
8/18
6.9
7.1
7.2
7.2
7.2
8/20
7.2.
7.3
7.3
7.4
7.5
8/25
7.0
7.1
7.1
7. 2
7.2
8/27
7.1
7.1
7.1
7.1
7.2
9/2
6.8
7.1
7.2
7.3
7.3
9/8
7.0
6.8
-
6.8
7.2
9/10
6.9
6.9
6.9
7.0
7.2
9/15
7.2
7.4
7.5
7.3
7.4
9/17
7.0
7.0
7.1
7.3
7.3
9/22
6.9
7.0
7.1
7.2
7.4
9/24
7.3
7.2
7.0
7.1
7.3
10/1
7.4
7.5
7.6
7.5
7.6
10/2
7.3
7.4
7.4
7.4
7.4
10/6
7.3
7.3
7.5
7.5
7.6
10/8
7.0
7.2
7.2
7.4
7.4
10/16
7.3
7.6
7.5
7.6
7.7
10/20
7.0
7.1
7.1
7.1
7.2
10/22
7.3
7.2
7.1
7.2
7.2
10/27
7.2
7.1
7.3
7.1
7.3
10/29
7.2
7.4
7.4
7.4
7.4
1
STAGE NO.
5 6
7.4. 7.3
7.3 7.2
7.4 7.2
7.4 7.5
7.7 7.4
7.6 7.6
7.5 7.6
7.3 7.3
7.5 7.5
7.3 7.3
7.2 7.1
7.4 7.4
7.5 7.4
7.2 7.3
7.5 7.4
7.2 7.1
7.1 7.5
7.4 7.4
7.8 7.7
7.3 7.4
7.7 7.7
7.7 7.5
7.7 7.6
7.3 7.2
7.0 7.1
7.5 7.8
7.4 7.5
7 8
7.3 7.1
7.2 7.4
7.1 7.1
7.6 7.5
7.6 7.5
7.5 7.3
7.4 7.4
7.2 7.2
7.3 7.2
7.2 7.2
7.1 7.0
7.4 7.4
7.4 7.4
7.2 7.2
7.4 7.3
7.1 7.1
7.5 7.5
7.0 7.0
7.8 7.7
7.3 7.2
7.6 7.5
7.5 7.5
7.5 7.5
7.2 7.2
7.1 7.1
7.7 7.8
7.5 7.4
9 10
7.1 7.2
7.3 7.4
7.2 7.3
7.4 7.3
7 i 4 7.4
7.3 7.2
7.3 7.2
7.0 7.0
7.1 7.0
7.2 7.2
6.8 6.9
7.3 7.3
7.4
7.2 7.1
7.3 7.4
7.2 7.3
7.3 7.5
7.1 7.3
7.5 7.5
7.4
7.7 7.6
7.3 7.1
7.6 7.6
7.2 7.3
7.1
7.6 7.6
7.4 7.5
-------
DATE
I NFL
1
2
11/3/69
7.1
7.3
7.2
11/12
6.9
7.0
7.1
11/19
7.1
7.2
7.4
11/24
7.2
7.3
7.4
12/5/69
7.3
7.3
7.4
12/12
7.3
7.1
7.2
12/18
7.2
7.2
7.2
12/24
7.3
7.4
7.5
12/26
7.2
7.3
7.4
12/29
7.1
7.3
7.3
12/30
7.3
7.3
7.4
1/1/70
7.2
7.3
7.2
1/5
7.2
7.4
7.4
1/6
7.1
7.1
7.2
1/8
7.2
7.3
7 . 2
1/13
7.1
7.2
7.2
1/14
7.2
7.3
7.4
5/6/70
7.3
7.3
7.3
5/12
7.3
7.4
7.4
5/18
7.4
7.6
7.6
5/22
7.4
7.4
7.4
5/27
7.2
7.2
7.3
6/2/70
7.4
7.4
7.5
6/5
7.4
7.4
7.4
6/8
7.3
7.4
7.4
6/11
7.2
7.4
7.4
6/14
7.3
7.4
7 . 4
Appendix Table
pH Values
1969 - 1970
3 4
7.3 7.3
7.2 7.4
7.5 7.4
7.4 7.4
7.4 7.3
7.2 7.3
7.2 7.3
7.6 7.5
7.5 7.4
7.3 7.4
7.3 7.4
7.3 7.4
7.5 7.4
7.4 7.3
7.2 7.4
7.3 7 3
7.4 7.6
7.4 7.4
7.6 7.6
7.7 7.7
7.5 7.6
7.5 7.4
7.6 7.7
7.5
7.5 7.6
7.5 7.5
7.4 7.6
1
STAGE NO.
5 6
7.4 7.5
7.5 7.5
7.3 7.5
7.6 7.5
7.5 7.5
7.4 7.5
7.5 7.5
7.4 7.5
7.3 7.4
7.4 7.3
7.5 7.5
7.5 7.4
7.4 7.4
7.3 7.3
7.4 7.3
7.4 7.4
7.6 7.5
7.5 7.6
7.6 7.6
7.7 7.7
7.6 7.6
7.5 7.6
7.7 7.7
7.5 7.5
7.7 7.7
7.6 7.5
7.6 7.6
7 8
7.4 7.4
7.4 7.4
7.5 7.4
7.5 7.5
7.4 7.4
7.4 7.3
7.5 7.4
7.6 7.5
7.5 7.6
7.2 7.0
7.4 7.4
7.5 7.3
7.3 7.2
7.3 7.4
7.3 7.4
7.4 7.3
7.4 7.4
7.5 7.4
7.6 7.5
7.6
7.8 7.6
7.6 7.4
7.5 7.5
7.4 7.4
7.6 7.6
7.4 7.4
7.6 7.5
9 10
7.3 7.3
7.2 7.1
7.3 7.4
7.6 7.6
7.3 7.3
7.4 7.5
7.4 7.4
7.5 7.6
7.4 7.5
7.0 7.1
7.5 7.5
7.4 7.5
7.3
7.4
7.4 7.3
7.4 7.4
7.4 7.4
7.3 7.3
7.5 7.5
7.6 7.6
7.5 7.6
7.4 7.5
7.5 7.5
7.4 7.3
7.6 7.6
7.5 7.5
7.6 7.6
Page 2 of 3
-------
DATE
8/4
8/6
8/12
8/17
8/20
8/24
8/26
8/31
9/9
9/14
9/16
10/5
10/8
10/13
10/16
10/19
10/22
10/26
10/29
11/2
11/5
11/9
11/12
11/16
Appendix Table
pH Values
1970
3 4
INFL
7.4
7.3
7.2
7.1
7.3
7.2
7.1
7.4
7.4
7.4
7.4
7.5
7.4
7.5
7.2
7.4
7.2
7.1
7.1
7.0
7.1
7.2
7.3
7.2
1
7.0
7.2
7.1
7.0
7.0
7.1
7.1
7.2
7.0
7.1
7.0
7.3
7.1
7.1
6.9
7.1
7.0
6.9
7.0
6.9
7.0
7.0
7.0
6.9
2
7.3
7.4
7.3
7.4
7.4
7.3
7.6
7.6
7.4
7.4
7.4
7.5
7.3
7.5
7.1
7.3
7.1
7.1
7.1
7.0
7.1
7.1
7.2
7.2
7.5
7.6
7.5
7.5
7.6
7.4
7.7
7.7
6.9
7.0
6.9
7.5
7.6
7.6
7.4
7.5
7.3
7.2
7.1
7.0
7.2
7.2
7.4
7.4
7.6
7.6
7.6
7.6
7.4
7.2
7.5
7.6
7.7
7.6
7.7
7.5
7 . S
7.3
7.3
7.2
7.1
7.2
7.4
7.5
7.4
1
STAGE NO.
5 6 7
7.5 7.4 7.3
7.5 7.4 7.4
7.4 7.4 7.2
7.4 7.3 7.2
7.3 7.2 7.1
7.0 7.0 6.9
7.5 7.4 7.4
7.5 7.3 6.9
8 9 10
7 . 6
7.6
7.6
7.4
7.4
7.2
7.2
7.2
7.1
7.2
7.3
7.4
7.3
7.6
7.6
7.6
7.4
7.4
7.2
7.2
7.2
7.1
7.2
7.3
7.4
7.2
7 .1
7 . 2
7.4
7.1
7.2
7.1
7.0
7.0
7.1
7.1
7.1
6.9
-------
TABLE 2 FLOW 7.5 gpm
Daily Profiles of TOC and DTOC Mg/1
DATE
EFFL .
EFFL.
CARBON
COLUMN NO.
ALGAL
MIXED
1
2
3
4
5
6
UNIT
MEDIA
FILTER
2/3/70
TOC
DTOC
8.5
—
3
1
1
1
1
1
2/12/7 0
TOC
—
DTOC
8.5
—
3
1
1
1
1
1
2/20/70
TOC
14.0
—
4
2
1.5
1
1.5
1.5
DTOC
11.0
—
2.5
—
1
1
1
1
2/28/70
TOC
8.0
—
8
5
5
2.5
3
4
DTOC
7.0
—
3
.5
.5
.5
.5
Feb. Av.
TOC
8.8
6.0
3.5
3.3
1.8
2.3
2.8
DTOC
11 .0
2.9
.8
.9
.9
.9
1.0
3/2/70
TOC
12
7
4.5
3
3
2
2.5
DTOC
11
5
5
3
2
2
1
3/5/7 0
TOC
7
4
2
1.5
1.5
1.5
1
DTOC
9
5
1.5
1
1
1
1
3/H/7 0
TOC
8
8
5.5
3.5
2
2
1.5
1.5
DTOC
10
6.5
4
3.5
2
2
1.5
1
3/18/70
TOC
11
7.5
4.5
2
1.5
1
1.5
DTOC
8
5
2.5
1.5
1
1
1
3/23/70
TOC
11
8.5
5
5
2
1.5
1
1
DTOC
11
6.5
3.5
2.5
2.5
1
1
1
3/29/70
TOC
6.5
6.5
7.5
2.5
2
1.5
1.5
1
DTOC
6.5
6
6
3.5
1.5
1.5
1
1.5
Mar. Av.
TOC
9
8
6
4
2
2
1
1
DTOC
9
6
5
3
2
1
1
1
Page 1 of 6
-------
FLOW 7.5 gpm
Daily Profiles of TOC and DTOC Mg/1
1970
EFFL.
EFFL.
CARBON
COLUMN NO.
ATE
ALGAL
MIXED
1
2
3
4
5
6
UNIT
MEDIA
FILTER
4/2/70
TOC
7.5
5
4
4
2
1.5
1
1
4/8
DTOC
6
5
4
4
1.5
1.5
1
1.5
TOC
7
10
5.5
8.5
3
2
1.5
1
4/14
DTOC
10
7
7
5.5
4
2
1.5
1.5
TOC
6
5.5
4.5
4
4.5
2
1.5
1
DTOC
6
6.5
5.5
4
3.5
2
1
1
4/20
TOC
5.5
5
4
3.5
3.5
1.5
1.5
1.5
DTOC
5
5
4
4
3
1.5
1.5
A/21
TOC
11
6
6
5
2
2
1.5
1.5
DTOC
10
9.5
6
4.5
4
3
1.5
1.5
4/30
TOC
4.5
4.5
4.5
3
2.5
1.5
1.5
1
DTOC
6.5
5.5
4.5
3.5
3
1.5
1
1
Apr. Av
TOC
•
7
6
5
4
3
2
1
1
DTOC
7
6
5
4
3
2
1
1
5/6/70
TOC
8.5
6
5
2.5
2
1.5
1
1
DTOC
9
4.5
4
2
1.5
1
1
1
5/12
TOC
7
5.5
4
3
3
3
1.5
1
DTOC
6.5
5.5
4.5
3.5
3
1.5
1
1
5/18
TOC
7
8
4.5
3.5
2
3
1
1.5
DTOC
8.5
8.5
6
4.5
2
3.5
2
3
5/22
TOC
6.5
7
7
2.5
2.5
1.5
1.5
1.5
DTOC
9
7
7
2.5
1.5
2.5
1.5
1
5/27
TOC
7
6
6
2.5
1.5
2.5
1.5
1.5
DTOC
6
6
5
4
3.5
2.5
2.5
1.5
May Av.
TOC
7
6
5
3
2
2
1.5
1.3
DTOC
7
6
5
3
2
2
1.6
1.5
Page 2 of 6
-------
FLOW 7.5 gpm
Daily Profiles of TOC and
1970
EFFL.
EFFL.
DATE
ALGAL
MIXED
1
UNIT
MEDIA
FILTER
6/2/70
TOC
13
4
4
DTOC
5.5
5.5
4
6/5/7 0
TOC
6
6
7
DTOC
7
4.5
6.5
6/8/7 0
TOC
10
6
5.5
DTOC
7
6
6
6/11/70
TOC
4
4
3
DTOC
10
8
7
6/14/70
TOC
8
5.5
5.5
DTOC
6
4.5
5
June Av.
TOC
8
5
5
DTOC
7
6
6
7/14/70
TOC
8
7
4.5
DTOC
4
4
4
7/22/7 0
TOC
8
8
4.5
DTOC
6.5
5.5
5
7/29/70
TOC
6
5
3.5
DTOC
6
5.5
3
7/31/70
TOC
7
6.5
4.5
DTOC
6.5
5
4
July Av.
TOC
6
5
4
DTOC
6
5
4
8/4/70
TOC
8
6.5
3.5
DTOC
8
6
3.5
8/6/70
TOC
8
DTOC
7
DTOC Mg/1
CARBON COLUMN NO.
2 3 4
2
4
3.5
7
3
2.5
2.5
4
4.5
4.5
3
4
3
2
3
4.5
2.5
3
2
4.5
2.5
4.5
3
4
1
2
1.5
3.5
2
2
2
2
1
2
2
3
1.5
1
1.5
3.5
1.5
1.5
1.5
2
1.5
2
1.5
2
1
1
1
1.5
2
2
1
1
1
1
1.2
1.3
3.5
4
4
3
4
2.5
4
3
4
3
5.5
3
2.5
3
2
2
3
2.5
3
3
2
3
2
2.5
2
2
2.5
2
2
2
2
2.5
1
1.5
1.5
2
2
2
1.6
2
1.5
1.5
1
1
3
2
1.5
1
1.4
1.4
2.5
2.5
2.5
2
2
1.5
1.5 1
1 1.5
-------
FLOW 7.5 gpm
Daily Profiles of TOC and DTOC Mg/1
EFFL.
EFFL.
CARBON
COLUMN NO.
DATE
ALGAL
MIXED
1
2
3
4
5
6
UNIT
MEDIA
FILTER
8/12/7 0
TOC
8
6
6.5
3
2
2
1
1
DTOC
5
5.5
3.5
5
3
2
2.5
1
8/20/70
TOC
8
5
4
3
2.5
1.5
1
1
8/24/70
DTOC
9.5
4.5
3.5
3
3
1.5
1
1
TOC
7
5
5
2.5
2.5
2.5
2.5
2
DTOC
5.5
5
5
2.5
1.5
1.5
2
1
8/2 6/70
TOC
6
6
6
3
1.5
2
1,5
1.5
DTOC
6
4
3.5
3
1.5
1.5
1
1
8/31/7 0
TOC
11
10
8
7
5.5
4
2
2
DTOC
10
10
7
7
5.5
4
2
2
Aug. Av.
TOC
8
6
6
4
3
2
1.6
1.3
DTOC
7
6
4
4
3
2
1.6
1.4
9/3/70
TOC
8
6
4.5
4.5
5
2.5
1.5
1.5
DTOC
7.5
7.5
5.5
4
4
2
1
1
9/8/70
TOC
8.5
6.5
3.5
3.5
3
2.5
2.5
3
DTOC
9
6.5
4.5
3.5
3.5
3
1.5
2.5
9/9/70
TOC
8
5.5
5
3.5
2
2
1.5
1
9/14/7 0
DTOC
7.5
6.5
4
3.5
2
2
1.5
1
TOC
11
7.5
4.5
4
4
1.5
1
1
DTOC
7.5
6.5
3.5
3
3
2.5
2
2.5
9/16/70
TOC
9
4
4.5
4
1.5
1.5
1
1
DTOC
7
4.5
4.5
3.5
2
2
1
1
9/22/70
TOC
7
6
5.5
4
5.5
1.5
1
1
DTOC
5.5
6
6
6
2.5
1.5
1.5
1
9/2 8/70
TOC
7
6
4.5
4
3
2
1
1
DTOC
7
5.5
3.5
2
1.5
2
1
1
Sept. Av.
TOC
8
6
5
4
3
2
1.3
1.4
DTOC
7
6
5
4
3
2
1.4.
1.4
Pace 4 of 6
-------
FLOW 7 . 5 gprti
Daily
Profiles
Of TOC
and DTOC Mg/1
EFFL.
EFFL.
CARBON COLUMN NO.
DATE
ALGAL
MIXED
1
2
3
4
5
6
UNIT
MEDIA
FILTER-
10/1/70
TOC
11
10
5
4
3.5
3
3
2
DTOC
10
10
4.5
4
3
2.5
2
2
10/5/7 0
TOC
6
5.5
5
3
2.5
2
2
1.5
DTOC
5
7
4
3.5
3
3
2
1
10/8/70
TOC
10
6
4.5
4.5
3.5
3
4
2
DTOC
9
6
4.5
4
2.5
2.5
2.5
1.5
10/13/70
TOC
6
6
4.5
3.5
5
3
2
2
DTOC
7
7
5
4.5
2.5
2.5
2
3
10/16/70
TOC
9
8
5
4.5
3
1.5
2.5
1.5
DTOC
8
7
5.5
4.5
4
1.5
3.5
1.5
10/19/70
TOC
7
7
7
4
3.5
2.5
2.5
2
DTOC
7
7
5
5
4
3.5
2.5
2
10/22/70
TOC
9
9
4
3
3
3
2.5
2
DTOC
9
6
3.5
3
2.5
2.5
1
1
10/26/70
TOC
9
7
4
3.5
2
2
1.5
1.5
DTOC
7
4
4.5
3.5
3.5
2
1.5
1.5
10/29/70
TOC
8 .
9
5
3.5
2.5
2.5
2.5
1.5
DTOC
Oct.. Av.
TOC
8
8
5
4
3
3
3
1.8
DTOC
8
7
5
4
3
3
2
1.8
11/2/70
TOC
7
3
3
2.5
2
1.5
1.5
11/5/70
DTOC
7
4.5
2.5
2
2
2
1
TOC
10
4.5
5
4
4
2
2.5
1
DTOC
7
5
4.5
3.5
3
2
2
1
-------
FLOW 7.5 gpm
Daily
Profiles
of TOC
and DTOC Mg/1
EFFL.
EFFL.
CARBON
COLUMN
NO.
DATE
ALGAL
MIXED
1
2
3
4
5
6
UNIT
MEDIA
FILTER
11/9/70
TOC
9
5
5.5
4.5
3
2.5
2.5
1.5
DTOC
6
8
5
5
2.5
Cf
2.5
1.5
11/12/70
TOC
8.5
6
3.5
4
3.5
3
2
1
DTOC
6
4.5
3.5
2
2
1
1
1
11/16/70
TOC
5.5
5.5
3.5
4.5
2
2
1.5
1
DTOC
6.5
5
3.5
4.5
3
2
1.5
1
Nov. Aver
. TOC
8
5
4
4
3
2
2
1.1
DTOC
7
5
4
3
3
2
1.6
1.1
cn
vo
-------
fASLi 3 P\Ow
Daily Profiles of
DATE
INFL
1
2
3
7/15/69
116
57
43
52
7/23/69
80
42
27
25
7/28/69
74
40
27
21
7/30/69
69
19
23
18
July Av.
85
39
30
29
8/6/69
101
67
59
41
8/8/69
110
84
49
44
'6/11/69
119
56
46
40
3/13/69
87
72
58
39
3/18/69
102
46
44
26
3/20/69
106
49
43
24
3/21/69
101
8/25/69
87
48
41
29
8/27/69
108
65
57
38
Aug. Av.
102
61
50
35
9/2/69
124
70
82
39
9/8/69
99
78
—
68
9/10/69
90
54
50
32
9/15/69
121
86
80
46
9/17/69
101
72
54
35
9/22/69
115
80
72
56
9/24/69
88
68
54
40
Sept. Av.
105
73
65
45
10/1/69
102
Step Fet-di
•ig
¦¦ V 2/6 9
1 20
Strac-s 1 i.
2
. ^2
l'/S/t9
? 4
S*-_-les
ken
- 2
I >/ 5/ b9
76
n Frror
60
. r j prr
Suspended So".ids Mg/I
STAGE
NO.
4
5
6
7
8
9
10
44
29
12
14
9
10
11
12
5
8
7
5
5
3
9
10
10
4
3
10
5
10
13
7
6
8
3
2
19
14
9
8
6
7
5
19
22
13
15
13
14
8
21
17
18
17
21
13
il
18
21
11
14
14
; 1
'•
24
23
23
13
9
*
25
19
13
/
6
x 3
0
18
8
6
8
6
5
"
11
8
12
2
7
19
7
6
5
1G
4
24
16
12
13
13
10
9
21
16
12
12
10
10
9
40
29
31
11
20
20
11
54
26
18
14
17
14
16
30
17
12
13
6
9
6
40
21
26
22
21
20
14
40
32
24
17
14
20
14
35
25
21
15
13
12
6
22
9
5
13
10
7
7
37
23
20
15
14
15
11
50
o
24
28
22
11
17
8C
24
22
28
22
13
¦ - <-
£
19
; t
13
28
14
i 2
"4
3
• r-
_ V_;
10
-------
FLOW 7.5 9pm
Daily Profiles of Suspended Solids Mg/1
STAGE
NO.
DATE
INFL
1
2
3
4
5
6
7
8
9
10
10/13/69
130
Step Feedi
ng
48
36
26
18
21
10
17
16
10/16/69
108
Stages 1 &
2 Sam-
58
50
19
22
20
23
14
16
10/20/69
125
pies taken
in error72
52
35
22
22
14
18
16
10/22/69
76
64
68
48
46
22
22
16
12
14
— —
10/27/69
129
98
32
48
28
21
14
21
16
11
11
10/29/69
125
112
98
76
48
23
24
19
11
9
8
Oct. Av.
109
63
46
25
21
20
16
15
13
11/3/69
165
106
76
68
18
19
18
13
18
15
10
11/12/69
116
72
60
36
24
22
13
12
13
12
14
11/19/69
116
90
38
34
26
7
8
11
7
6
7
13Z24/69
132
89
58
46
23
16
13
12
13
11
10
I'-ov. Av.
114
72
52
48
24
35
16
9
13
6
14
12/5/69
160
90
70
36
34
20
14
12
11
7
7
12/12/69
162
112
88
80
29
33
30
22
22
29
17
12/16/69
108
60
42
14
15
14
16
3
12
10
2
Dec. Av.
136
84
63
45
25
25
19
12
14
13
10
Page 2 of 2
-------
TABLE. < FLOW 7.5 gpm
Daily Profiles of B0D5 Mg/1
STAGE NO.
DATE
INFL
1
2
3
4
5
6
7
8
9
10
7/15/69
94
53
38
29
12
8
4
6
5
5
6
7/23/69
85
59
38
32
21
13
8
4
6
6
6
7/28/69
56
28
20
13
2
3
3
4
5
4
4
7/30/69
101
55
38
26
19
14
10
11
15
8
10
July Av.
84
48
34
25
14
10
6
6
8
6
6
8/5/6 9
100
58
50
39
28
21
19
18
12
21
8
8/6/69
124
93
60
48
29
18
15
9
5
7
6
8/8/6 9
120
81
59
41
27
20
19
16
18
17
12
8/11/6 3
152
96
33
24
19
15
19
13
14
10
8
8/13/6 9
91
50
53
38
24
16
8
9
7
6
5
8/15/6 9
34
69
43
41
29
20
15
8
7
5
5
8/18/69
111
72
48
37
23
10
8
9
5
4
5
8/20/69
124
66
43
32
15
8
9
7
7
6
4
8/21/6 9
105
—
—
—
14
14
11
10
9
7
8/25/69
140
62
62
45
22
17
15
10
10
1
4
8/27/69
79
44
31
27
15
14
13
8
8
1
Aug. Av.
112
69
48
37
23
16
15
11
9
9
7
9/2/69
128
76
41
31
22
21
21
12
8
7
7
9/8/69
112
85
—
64
40
31
36
17
10
9
7
9/10/69
128
87
64
50
36
25
15
13
10
11
9
9/15/69
109
74
53
37
26
24
19
17
13
10
8
9/17/69
121
87
57
44
23
19
19
15
14
11
11
9/22/69
150
113
80
58
28
19
21
19
18
16
15
9/24/69
125
87
66
48
32
20
23
17
16
14
14
9/30/69
140
121
78
62
41
30
32
14
15
12
12
Sept. Av
127
91
63
49
31
23
23
16
13
11
10
Page 1
of
6
-------
Daily
Pro
files o
1969
DATE
INFL
1
2
3
4
10/2
123
47
38
10/6
140
Step Feed-
56
46
10/8
102
ing
Stages
46
24
10/13
140-
1 &
2 Taken
47
38
10/16
136
In :
Error
50
37
10/20
160
68
43
10/22
108
93
91
63
48
10/27
156
115
88
63
35
10/29
188
124
102
74
48
Oct. Av.
, 139
—
57
40
11/3
210
139
97
71
51
11/19
136
84
66
30
25
11/24
120
82
63
47
18
Nov. Av.
173
112
82
51
38
12/5
140
96
71
48
42
12/12
104
94
56
38
21
12/16
132
77
51
36
27
Dec. Av,
Prim.
124
87
60
42
27
Eff.
STARTED
TO TREAT MODIFIED AERATION
12/18
63
37
34
33
27
12/24
52
26
25
21
19
12/26
36
27
25
20
12
12/29
51
34
28
24
18
12/30
43
32
21
23
25
Dec. Av.
Mod. Aer49
31
27
24
2C
Eff.
plil
f BODS Kg/1
STAGE NO.
5 6
27
16
20
20
14
14
17
13
19
11
34
14
30
34
26
24
20
19
23
18
39
29
22
12
22
17
31
21
21
17
15
21
16
20
16
EFFLUENT
16
16
15
14
14
8
15
10
14
10
7
8
9
10
17
15
15
13
22
20
20
19
—
16
15
15
12
11
12
15
9
11
11
9
19
19
16
17
22
22
14
19
17
12
14
19
17
14
13
17
16
14
14
26
19
0
10
11
13
Q
8
14
10
10
10
19
16
9
9
15
17
10
9
13
12
11
13
13
10
6
7
14
12
9
10
12
9
9
7
13
10
10
12
9
9
10
9
11
10
11
11
11
8
7
12
-
c
5
- n
-------
Daily P it o r I
DATE
I NFL
1
2
3
1/1/70
46
28
23
18
1/5/70
94
41
33
24
1/6/70
85
54
41
31
1/8/70
80
53
30
24
1/13/70
38
26
26
21
1/14/70
44
31
25
20
1/15/70
47/24
38/10
29/15
17/a
1/16/70
41/25
-/20
33/18
26/11
1/17/70
90/37
35/20
37/16
23/12
1/18/70
41/28
32/16
30/14
20/18
1/19/70
63/31
50/22
43/14
31/14
1/20/10
58/22
45/16
35/13
21/8
1/21/70
60/24
43/15
37/9
18/7
1/2 2/7 0
5 9/18
34/14
30/15
13/13
1/23/70
104/47
42/22
28/14
15/10
1/24/70
41/36
2 5/13
20/12
11/7
1/26/70
38/21
23/11
16/9
14/5
1/27/70
41/16
30/12
24/7
20/5
1/28/70
52/28
31/13
28/9
16/8
1/29/70
58/17
37/9
13/9
11/5
1/30/70
49/17
34/13
29/10
16/11
1/31/70
45/21
37/12
26/9
17/7
Jan. Av.
58/26*
37/15*
29/12*
19/9
2/2/70
76/25
41/10
28/14
21/12
2/4/70
59/19
48/17
43/17
26/17
2/6/70
76/42
51/20
33/15
18/10
2/7/70
47/23
35/16
24/10
15/8
2/9/70
54/27
31/18
32/10
24/14
2/11/70
50/31
32/10
18/10
* 2 ' 11
Feb. Avc
6 0/28
40/19
30/15
19/14
Mod.
r. ^ff.
\~Q+_£ ; *
The-e f
= -1 i c- n s
r ^~ --
--'jt:
Stopple
Treat;r
'.g .".od-;?i
i.ff !.-€
s of
BODS 'g/ 1
STAGE NO.
4
5 6
17
6 8
17
19 8
15
22 9
15
9 7
14
10 11
12
9 7
11
12
11
15
10
9
11
10
22
29
13
10
14
13
11
14
7
6
8
8
9
10
9
9
9
5
6
4
8
12
9
11
12
11 8
15
13
32
15
20
16
12
—
15
10
6
13
17
: 3
6
9
7
8
11
6
8
7
7
6
8
5
7
4
8
7
10
6
7
7
8
8
6
8 7 7 7
-------
I NFL
108
80
93
98
255
115
205
180
95
82
143
153
99
114
142
90
95
130
105
125
143
80
108
88
101
79
103
75
95
85
96
FLOW 7.5 gpm
Daily Profiles of BOD5 Mg/1
1970 STAGE NO,
4 5 6 7 8 9 10
13 9 6
30
19
17
21 23
23
13
38
23
36
19
43
18
12
105
54
36
57
32
18
64
33
28
23 22
20
17
65
34
22
20
40
26
19
12
35
17
15
14
35
22
15
19 15
22
19
53
32
20
16
48
12
5
8 15
12
15
39
24
18
15
48
28
15
13
34
18
14
9 9
7
7
30
22
12
18 14
15
13
38
21
18
20 21
14
13
36
20
17
16
46
25
18
16 17
16
14
42
19
OUT
OF SERVICE
14
24
12
8
28
15
n
n o
9
22
13-
7
31
13
n
n a
11
30
12
7
29
13
ti
» n
12
17
15
10
27
17
n
ii h
10
22
15
1C
27
14
10
4 of 6
-------
FLOW 7.5 gpm
Daily Profiles of BODS Mg/1
STAGE NO.
DATE
I NFL
1
2
3
4
5
6
Sept,22/70
100
29
16
18
14
14
13
" 29/70
73
30
14
10
9
8
10
" 30/70
95
38
19
15
11
10
14
Oct. 1/70
108
41
23
14
11
9
10
2/70
94
36
27
20
17
18
19
4/70
—
—
—
—
—
—
—
5/70
73
28
18
19
16
14
14
6/70
95
29
22
17
18
12
12
7/70
117
45
22
18
15
10
10
8/70
105
38
24
15
13
11
8
9/70
85
37
23
17
13
10
9
" 10/70
73
30
21
15
13
11
10
" 12/70
—
—
—
—
—
—
—
" 13/70
81
45
32
30
18
22
20
" 14/70
118
39
28
19
15
13
13
" 15/70
95
36
23
13
15
11
12
" 17/70
60
20
11
7
7
6
5
" 18/70
75
32
23
16
13
11
10
" 19/70
63
31
26
13
15
15
14
" 20/70
83
33
21
14
12
13
11
" 21/70
110
41
31
15
14
16
14
" 22/70
58
23
15
11
10
9
10
" 23/70
78
24
13
15
10
11
9
" 24/70
62
23
12
10
9
8
7
" 25/70
69
27
15
15
16
12
10
" 26/70
84
32
26
15
16
14
9
" 27/70
—
—
—
—
—
—
—
" 28/70
83
40
30
24
16
14
10
" 29/70
94
36
24
16
17
15
13
" 30/70
—
—
—
—
—
—
—
" 31/70
81
23
22
13
11
9
7
Oct. Aver.
84
32
22
16
14
12
11
-------
Daily Profiles of 30D5 Mg/1
DATE
INFL
1
Nov. 2/7 0
109
30
4/70
95
26
5/70
83
29
6/70
97
28
7/70
128
37
8/70
84
32
9/70
135
35
" 10/70
103
21
" 11/70
73
22
" 12/70
75
25
" 13/70
85
23
" 14/70
61
20
Mov. Aver.
94
27
STAGE
NO.
3
4
5
6
14
15
12
11
15
10
11
10
19
20
15
14
16
11
10
11
18
15
12
10
19
13
12
10
19
12
15
10
15
11
10
7
15
12
9
8
12
12
10
8
10
10
—
9
12
10
8
6
15
13
11
10
2
21
29
28
23
34
28
29
18
17
19
20
18
23
-------
TABLE 5 FLOW 7.5
Daily Profiles
1969
DATE
INFL
1
2
3
4
V15
245
162
158
121
100
7/23
414
178
118
126
74
7/29
207
143
82
86
69
7/30
138
56
39
26
9
July
Av.251
135
99
90
63
8/6
315
264
199
165
143
8/8
324
265
194
164
130
8/11
3 28
186
156
138
121
8/13
250
156
138
130
108
8/15
210
186
179
158
133
8/18
254
187
199
170
146
8/20
333
229
146
121
10 4
8/21
282
-
-
—
—
8/25
304
167
125
108
79
8/27
282
170
160
145
132
Aug„
Av„288
201
166
144
122
9/2
432
312
256
252
256
9/8
326
246
42
167
113
9/10
270
196
179
104
87
9/15
306
255
216
203
173
9/17
267
232
177
164
112
9/22
368
286
214
200
184
9/24
242
216
168
103
95
Sept.
Av316
249
179
170
146
10/1
326
Step
Fe«=>d-
210
163
10/2
241
ino
Stages
167
136
10/6
292
1 I
2 taken
144
96
10/8
211
T n
J. A i
Error
103
73
C.O.D. Mg/1
STAGE
NO.
5
6
7
8
9
10
96
71
63
58
71
88
57
65
52
57
78
52
30
39
30
26
26
13
17
26
39
9
22
13
50
50
46
38
49
42
130
78
91
121
86
103
112
104
99
116
79
43
125 '
104
73
99
91
69
78
95
78
52
56
47
120
124
99
79
62
54
116
108
112
104
100
100
87
79
66
62
58
58
104
121
96
58
67
67
50
46
29
33
25
17
158
166
158
153
132
124
108
103
90
88
76
68
260
260
248
236
224
200
96
83
71
54
58
50
79
67
75
83
-
-
151
138
134
121
121
112
95
95
86
73
65
52
128
115
90
81
81
72
65
73
48
48
48
125
126
111
99
100
89
133
116
103
107
103
99
114
114
105
IIS
110
92
7
56
4 c
39
4 S
52
6 5
6C
5 6
5 6
52
47
-------
FLOh7 7 . 5 gpm
Daily Profiles of C.O.D. Mg/1
1969
- 1970
STAGE
NO.
DATE
INFL
1
2
3
4
5
6
7
8
9
10
10/14/69 26 0
Step Feeding
162
128
128
118
118
103
93
69
10/16
288
Stages 1
& 2
191
147
127
122
108
93
73
54
10/20
359
taken in
error
177
168
130
115
100
88
68
64
10/22
277
200
172
148
120
96
81
72
67
62
~
10/27
376
342
272
232
158
99
64
69
69
50
45
10/29
322
253
99
100
99
89
84
79
79
69
7.4
Oct. Av.
295
—
-
163
129
105
91
86
82
73
66
11/3
406
318
300
260
172
142
123
108
108
103
93
11/12
338
214
157
124
91
86
76
67
76
57
52
11/19
368
216
172
-
106
-
-
59
-
-
49
11/24
296
252
185
170
136
117
97
68
73
68
63
Nov. Av.
371
249
210
192
126
114
100
76
92
8C
65
12/5
327
235
214
207
125
110
91
67
53
62
43
12/12
195
185
138
115
101
111
120
82
87
72
55
12/16
360
208
149
109
100
80
95
89
80
80
85
Dec, Av .
295
220
172
150
116
105
101
77
73
71
62
Prim.EffSTARTED TO TREAT MODIFIED
AERATION
EFFL.
ON 12/18/69
at 7.5
9pm
12/18
147
131
107
87
73
83
83
68
58
54
58
12/24
121
77
97
82
68
73
68
68
63
68
63
12/26
140
126
121
116
97
92
77
77
77
77
72
12/29
120
91
91
82
72
67
58
53
43
34
34
12/30
149
106
101
86
91
86
86
62
53
29
38
Mod. Aer
•
Dec. Av.
135
106
103
91
eo
80
74
66
59
52
53
1/1/70
144
130
116
86
86
91
91
72
67
62
62
1/5/70
187
139
91
101
77
72
82
72
58
82
1/6
139
120
115
77
67
6 7
52
5£
58
38
1/3
143
139
158
120
11C
81
7 6
c ^
r.io:
86
Pice 2 of 4
-------
FLOW 7.5 gpm
Daily Profiles of C.0.2. ."g/1
ST.1.
.31 NO
•
DATE
INFL
1
2
3
4
5
6
7
Jan.
13/70
147
103
97
88
88
84
84
78
n
14/70
114
89
85
76
51
57
41
47
n
15/70
126
96
84
74
65
56
i)
16/70
118
93
76
62
53
n
18/70
177
133
115
90
71
62
ii
19/70
17 7
130
115
93
65
78
ti
20/70
178
135
126
89
80
70
»
21/70
148
121
121
95
71
69
ii
22/70
176
156
109
106
82
74
n
23/70
154
125
109
107
102
£1
ti
26/70
158
112
89
86
86
76
ii
27/70
157
113
89
87
87
76
VI
28/70
139
120
110
87
63
58
n
29/70
157
123
103
90
79
70
Jan.
Aver.
153
121
105
92
78
69
72
67
Feb.
2/70
179
118
99
83
73
61
n
4/70
178
127
110
91
80
69
n
9/70
179
129
96
96
88
80
ft
11/70
115
83
57
52
47
47
Feb.
Aver.
163
114
90
80
72
64
STOPPED TREATING MODIFIED AERATION EFFLUENT
STARTED TREATING PRIMARY TANK EFFLUENT
Aug .
4/70
256
98
92
98
tl
6/70
224
133
101
62
TI
12/70
269
155
107
77
ti
17/70
253
184
94
94
ti
20/70
224
96
76
68
n
24/70
215
119
68
57
n
26/70
223
181
49
41
n
31/70
97
83
85
Anrr
Avor
1 ^
84
73
-------
FLOW 7.5 gpm
Daily Profiles of C.C.2. Mg/1
q r~. - ^7
DATE
INFL
1
2
3
4
Sept
. 8/70
277
128
86
Out
of Service
II
9/70
213
94
60
It
«i n
11
14/70
255
89
77
n
« n
fl
16/70
292
116
84
R
n «
n
22/70
228
80
104
ti
n n
Sept
. Aver.
253
101
82
Sept
.28/70
286
144
114
88
55
Oct.
1/70
240
120
104
76
11
ir
5/70
192
104
72
20
10
8/70
235
119
61
31
8
n
13/70
252
177
123
110
95
ti
16/70
170
103
83
87
87
it
19/70
267
151
136
91
74
ii
22/70
214
102
78
58
49
ii
26/70
222
128
115
86
132
n
29/70
250
170
125
103
112
Oct.
Aver.
233
132
101
75
63
Nov.
2/70
278
189
99
88
99
n
5/70
236
111
102
78
67
ti
9/70
222
106
102
106
74
n
12/70
327
102
84
56
48
n
16/70
266
135
91
61
—
Nov.
Aver.
266
129
96
78
72
NO.
6 7
64
38
38
72
40
50
-------
DATE
Aug. 4/70
6/70
" 12/70
" 17/70
" 20/70
" 24/70
" 26/70
" 31/70
Average
Sept, 8/70
9/70
" 14/70
" 16/70
Average
Oct. 1/70
5/7 0
8/70
" 13/70
" 16/70
" 19/70
" 26/70
" 29/70
Average
Nov. 2/70
5/70
9/70
" 12/70
" 16/70
Average
TABLE
INFL
1
12.3
11.7
11.8
10.7
20.0
19.0
13.4
12.8
17.5
13.0
24 .0
21.5
21.0
17.5
14.4
13 .8
16.8
15.0
21.0
17.4
17.5
12.8
23.0
19.1
22.6
21.0
21.0
17.6
23.2
19.8
21.6
17 .4
24.0
21.0
25.6
22.4
15.0
13.6
26.8
20.8
21.6
18.2
22.8
23.0
22.6
19.5
19 .0
15.6
20.0
15.0
27.2
21.8
20.3
17 .8
17.4
16.0
20 .8
17.2
Phosphates - Mg/1
2
3
4
5
6
7
11.7
11.3
10.0
9.4
—
7.5
7.5
10 .6
11.3
10 .7
—
10.4
18.3
17.0
—
—
15.8
15.5
12.8
12.8
—
—
12.8
12.8
13.6
13.0
12.5
—
12.0
—
19.1
19.1
—
18.7
—
18.4
16. 4
—
—
—
—
15.3
13.0
12.5
—
11.7
10.1
14.1
13 .8
11.3
12.1
13 .5
12.9
17.1
16.5
12.0
11.4
18.4
17.7
17.6
17.0
16.3
15.7
20.8
_ —
18.3
18.3
10.9
16 .8
16 .7
—
16 .7
16.4
20.8
18.7
18.3
—
17.7
17.7
22.4
21.4
—
20 .6
20.3
20.0
13.6
—
12.9
—
12.8
12.7
21.9
17.7
—
17.8
17.7
16.4
18.2
13.9
13.8
—
13.8
13.5
22.8
—
18.7
—
18.4
—
20.9
17.9
16.5
—
17 .0
15.4
17.4
—
15.9
15 .6
15.6
15.4
—
13.2
—
12 .8
—
21.8
—
14.9
—
14.9
—
16.8
—
13 .2
—
13 .4
13.7
14 .6
—
13.7
—
13 .7
13.2
17 .2
—
14.2
—
14.1
14.2
-------
TABLE 7 FLOW 7.5 gpm
Daily Profiles of Sum of Albuminoid and Ammonia N/Nitrate N Mg/l
EFFLUENT FROM
CARBON COLUMN
NO.
DATE
ALGAL
MIXED
1
2
3
4
5
6
UNIT
MEDIA
FILTER
5/6
3.4/27.6
2.6/24.6
2.6/16.2
2.6/20.4
2.3/15.6
2.1/18.8
2.1/18.2
2.1/11.4
5/12
6.2/11.9
5.5/13.5
5.5/12.5
5.5/12.7
4.7/12o0
5.5/12.8
4.7/13.1
4.4/12.2
5/18
8.8/13.1
9.1/12.6
7.8/15.7
8.1/16.5
7.0/15.0
6.2/13.2
5.5/13.7
4.9/14.8
5/22
1.3/13.4
1.3/12.6
.8/17.8
.8/12.4
.5/13.4
.5/11.8
.5/12.6
.5/12.8
5/27
2.8/15.4
1.3/15.6
1.3/12.5
1.3/14.8
,8/10.9
.5/13.2
.8/10.3
.5/12.1
5/70
Av.
4.5/16.3
4.0/15.8
3.6/15.0
3.7/15.4
3.1/13.4
3.1/14.0
2.7/13.9
2.5/12.8
6/2
1.6/15.5
1.8/17.4
1.6/15.9
1.0/15.9
.5/16.1
.5/13.6
.3/11.1
.3/12.4
6/5
.7/11.3
.3/13.0
.3/12.3
.3/9.3
.3/10.5
.3/11.3
.3/11.3
.3/12.0
6/8
.5/14.2
.3/17.3
0.16.3
0/16.4
0/16.4
0/16.9
0/16.8
0/17.1
6/11
3.9/16.1
2.7/17.2
2.6/16.2
2.5/15.8
2.2/15.4
1.7/15.0
1.3/14.6
1.0/16.4
6/14
2.7/18.9
2.2/21.8
2.3/21.2
1.8/18.9
1.4/17.8
1.2/17.8
.8/12.7
.8/19.5
6/70
Av.
1.9/15.2
1.5/17.3
1.4/16.4
1.1/15.5
.9/15.2
.8/14.9
.5/13.3
.5/15.5
7/14
3.1/16.5
1.3/17.4
1.1/17.9
.8/17.4
.5/15.8
.5/17.4
.3/15.8
.3/14.0
7/22
—/—
1.4/15.0
.7/10.0
.5/12.8
.3/11.5
.3/12.1
0.12.1
0/9.3
7/29
.4/17.0
.3/16.2
.1/17.2
.1/14.4
0/13.4
0/12.4
0/13.4
0/9.2
7/31
.3/11.1
.3/16.8
.3/16.2
.3/15.6
.3/12.6
0/14.7
7/70
Av.
1.3/14.9
.8/16.3
~6/15.3
.4/15.0
.3/13.6
.3/14.0
.2/13.5
.1/11.8
8/4
.8/16.0
0/16.4
0/12.4
0/12.6
0/11.8
0/12.2
0/12.6
0/12.0
8/6
.3/—
0/—
0/—
0/—
0/—
0/—
0/—
0/—
8/12
6.1/10.1
7.1/9.0
6.1/9.1
4.9/10.5
3.6/10.8
2.6/10.0
.2/5.7
* 2/4.8
8/20
.9/17.4
.8/18.4
.7/13.6
.7/—
.5/19.6
.5/--
.4/--
.3/18.4
8/24
2.3/15.0
.5/18.5
.5/16.4
o/—
0.15.0
o/~
0/—
0/13.6
8/26
.3/17.5
.3/18.5
0/18.8
0/—
0/—
o/—
0/—
0/16.8
8/31
0/13.4
0/14.0
0/13.0
0/—
0/13.5
0/—
0/—
0/13.4
ft /70
Av.
1.5/14.9
1o 2/15.8
1.0/13.9
.8/11.5
.6/14.1
.4/11.1
.1/9.2
.1/13.2
-------
Daily Profiles
EFFLUENT FROM
DATE ALGAL MIXED
UNIT MEDIA
FILTER
Sept
. 8/70
10.1/12.0
7.8/13.4
n
9/70
4.2/9.9
3.1/9.3
it
14/70
7.8/6.5
7.8/7.3
u
16/70
7.4/4.8
7.3/9.0
Sept
. Aver.
7.3/8.3
6.5/9.8
Oc t.
1/70
2.0/17.7
1.6/15.8
II
5/70
5.2/8.2
3.4/9.5
II
8/70
6.2/8.4
tr
13/70
7.5/6.1
ii
16/70
5.7/5.7
5.5/5.5
it
19/70
4.3/13.6
--/15.8
it
22/70
0.6/9.6
- -/ 8 .9
n
26/70
3.5/12.1
--/ll.1
ii
29/70
4.2/16.0
2.9/13.2
Oct.
Aver.
4.4/10.8
3.3/11.4
Nov.
2/70
.8/12.5
0/15.8
n
5/70
.8/11.2
--/10.6
r?
9/70
1.0/15.0
--/16.8
ti
12/70
.7/6.8
—/10.3
tT
16/70
0/15.0
0/14.3
Nov.
Aver.
.7/12.1
0/13.6
tLOiv 7 . 5 5pm
of Sum of Albuminoid and Ammonia K/Nitrate N Mg/1
CARBON COLUMN NO.
17.6/12.8
3.6/9.6
7.4/6.8
7.3/7.8
6.5/9.3
--/l6 .4
3.6/9.5
4.4/10.8
6.8/6.4
5.7/5.7
3.5/12.8
.1/11.2
3.5/11.4
3.6/17.1
3.9/11.3
0/11.0
.3/10.2
.3/16.2
.5/10.9
0/16.0
.2/12.9
8.6/10.6
3.1/9.6
6.8/6/8
6.2/9.0
7.8/5.0
3.9/5.0
6.0/4.5
7.8/6.4
6.4/5.2
0.8/13.4
2.0/9.2
2.6/10.5
6.8/5.2
3.9/3.9
2.9/12.0
0/8.8
3.1/13.4
4.2/11.2
2.9/9.7
.3/10.2
0/12.6
.5/5.2
0/14.4
.2/10.6
Page
2 of 2
-------
TABLE 8 FLOW 7.5 gpm
Daily Profiles of Ajrunonia - N
1969 STAGE
DATE
INFL
1
2
3
4
5
8/8/69
13.1
13 .3
12.3
10.9
11.5
13 .2
8/12
13.9
12.5
14.0
13.6
17.0
15.1
S/13
14.3
12.7
10.1
10.7
10.7
12.7
8/18
13.2
12.6
12.5
11.2
9.8
9.1
8/20
11.3
13 .0
14.4
14.8
11.3
11.1
8/21
17.1
15.8
8/25
15.2
13.8
13.7
12.3
12.0
11.7
8/27
1502
15.4
15.6
12.8
13 .6
12.8
8/59 Avl4.2
13.3
13.2
12.3
12.3
12.7
9/2
15.4
12.9
11.3
10 .1
10 .1
8.1
9/8
15.3
10.0
11. 5
10.2
9.8
9/10
14.3
13.6
13 .6
13.9
13.5
8.4
9/15
16.4
15.6
14.7
14.8
13.9
13. 3
9/17
12.1
12.9
13.2
12.7
13.0
13.3
9/22
8.7
16.8
14.7
17.8
17 .3
16 .8
9/24
llo 7
14.6
14 .8
14.1
14.3
13.8
9/69 Av
.13.4
13.8
13.7
13.5
13.2
11.9
10/1/69
17.9
17 .6
17.5
16.7
16.4
15.7
10/2
17.2
17.6
19.5
19.5
17.6
19.2
10/6
17.2
18.9
17.2
17.9
16.7
18.3
10/8
llo6
14.6
14.7
14. 4
14.6
14.8
10/14
20.3
22.5
22.5
22.1
21.7
21.4
10/16
16.8
21.0
20.0
19.9
17.1
18.9
10/20
15.4
19.2
18.9
18.9
19.2
16.8
10/22
13.0
17 .0
16 .8
17.1
17.1
17.1
10/27
15.0
15.9
15 .6
15.5
15.5
15.2
10/29
10.4
15.5
15.0
15.0
13.6
13.5
Oct.Av
15.5
18.0
17.8
17 . 8
17 .0
1~ . 1
Mg/1
NO.
6
7
8
9
10
14 .0
11.2
8.4
6.0
4.2
13 .4
10 .6
7.1
3.9
2.7
9.9
8.0
5.9
4.1
3.4
11.1
8.7
5.2
2.8
1.3
10 .4
6.9
4.6
2.4
0.8
14 .9
9.5
8.3
6.8
5.1
13.4
10 .6
8.6
5.6
4.4
13 .7
11.1
7 .9
4.9
3.2
12.6
9.6
7.0
4 . 6
3.2
9.7
6.7
5 .1
•J r
2.5
9.7
6.7
2.8
1.4
1.1
12.9
9.3
6.7
5.1
4.5
12.0
12.0
11.5
S .5
8.9
11.3
8.9
7.3
4.8
3.6
15.0
14.6
12.9
10. 2
9.4
12.2
10.6
8.1
5.5
5.3
11.8
9.8
7.8
5.7
5.1
16.1
15.4
14.5
13.3
11.5
19.5
17.8
16.2
15.1
13.0
16 .0
13.7
11.7
7.7
8.3
13.7
11.5
8.8
7.3
4.8
17.4
15.0
14.4
13.2
14.0
17.9
16.2
13.7
11.8
8.8
15.5
13 .4
12.7
11.6
10.8
16.0
14 .3
13 . 2
11.9
—
14 .5
13 .7
12.9
9.4
8.9
13 .7
13 . 5
11.9
10.6
10 .4
16 .0
14.5
13.0
11.2
10.1
-------
FLOW 7.5 gpm
Daily Profiles of Ammonia - N Mg/1
STAGE NO.
On
DATE
I NFL
1
2
3
4
5
6
7
8
9
10
11/3/69 9.8
15.4
14.9
14 .9
12.7
14.4
12.3
12. 2
10.6
9.0
7.1
11/12
10.8
16 .0
14 .6
14 .3
11.3
12.6
10.3
10.0
8.4
6.7
4.9
11/19
14.4
17 .0
16.8
16.8
15.3
15.0
15.5
14.5
12.8
10.5
9.4
11/24
14.7
15.8
16.0
15.8
16.2
18.0
14.7
14.4
12.0
10.8
11.3
11/69
» _ _
12.4
16 .1
15.6
15.6
13.9
15.0
13.2
12.3
11.C
9.3
8.2
Av »
12/18
1109
14 .0
17.9
15.4
16.3
16.8
12.7
12.8
11.7
10. 8
12/24
9.5
12 .2
11.1
9.8
11.5
13.2
10 .5
8.7
7.0
4.2
12/26
14.0
14.6
14 .7
15.3
13 .9
14.3
10 . 8
9 . 5
8.7
6.3
15.7
14 .6
14 .6
14 .4
14.7
15.1
11.5
9.3
5.6
3.9
12/30
11.2
15 .8
15.1
14 .6
12.9
11.9
11.5
10 .1
8.1
7 . 1
12/69
ft..
12.5
14.2
14.7
13.9
13 .9
14 .3
11.4
10 .1
8 . 2
6 . 5
AV,
1/1/70
9.9
10.9
11.6
12.0
11.1
9.5
7.0
5.7
4.6
3 .1
1/5
15„8
18.2
14.4
15.5
14.7
13.7
10 .8
8.8
6.4
1/6
11.3
16 .8
16.1
16.5
15.7
14.7
14.1
10 .6
9.7
1/8
10o8
18.2
18.6
17.2
16.2
15.0
10.5
10.8
10.2
1/13
10.2
16 .5
16.7
16.2
15.5
15.0
13.0
11.5
8.1
6.6
4.9
1/14
11.2
16.7
16.0
16.0
14.4
13.8
11.3
10.6
7.7
5.5
1/15
15.4
19.2
20.3
20.9
19.7
17.8
1/28
11.5
7.7
8.8
6.1
5.0
2.8
1/70 Ave.
16.6
16.2
16.3
15.3
13.9
10.5
9.5
7.5
4.9
4.4
Daily
Profiles
of Sum
of Albuminoid and
Ammonia
- N Mg/1
5/6
22
21
21
21
21
22
21
18
14
11
9
5/12
21
20
20
21
21
21
22
19
15
13
11
5/18
22
22
23
23
23
22
—
21
18
16
5/22
27
27
27
28
29
26
26
22
21
19
* .
5/27
21
22
23
24
23
20
20
16
15
14
May Aver.
22
22
23
23
r
£
22
21
IS
16
14
r ~ ~e
of 4
-------
Daily Profiles of Sum
DATE
INFL
1
2
3
June
2/70
24
23
24
24
n
5/7 0
25
24
24
—
n
8/70
24
23
24
24
n
11/70
21
21
21
22
n
14/70
22
24
24
23
June
Aver.
23
23
23
23
July
14/70
21
21
II
22/70
22
22
23
24
tl
29/70
21
20
21
22
11
31/70
21
20
21
21
July
Aver .
21
21
22
22
Aug.
4/70
20
2G
22
21
11
6/70
20
22
23
24
If
12/7 0
15
23
24
25
r»
17/70
18
15
16
17
H
20/70
21
20
21
21
tt
24/70
28
18
23
22
n
26/70
20
20
21
20
n
31/70
20
23
21
19
Aug .
Aver .
22
20
21
21
Sept.
8/70
25
25
25
tt
9/70
20
18
19
tt
14/70
25
25
25
n
16/70
26
25
25
Sept.
Aver.
24
23
24
FLOU" / . 5 5pm
of Aiburr-.inoid and Arx~onia - N Mg/1
STAGE
NO.
4
5
6
7
8
9
25
25
23
18
16
14
27
25
22
19
19
16
25
25
23
19
16
15
23
25
22
19
16
15
25
26
23
20
17
19
25
25
23
19
16
15
21
22
20
16
13
10
22
24
21
18
15
13
22
22
17
11
8
5
21
21
16
11
8
22
22
IS
14
11
S
19
16
13
8
18
21
16
11
23
21
18
14
15
12
9
4
18
14
10
7
16
14
11
7
16
14
11
7
15
12
8
3
18
16
12
8
Staaes
3 to 6
out
20
of
Service
11
«9
f»
20
m
n
21
18
10
14
12
14
15
15
14
8
10
3
3
6
3 of
-------
Daily Profiles of Sum
DATE
INFL
1
2
3
Oct.
1/70
24
23
24
23
IT
5/70
24
24
25
25
n
8/70
25
25
25
25
«
13/70
27
27
27
28
n
16/70
27
28
26
26
n
19/70
24
25
26
30
IT
22/70
22
21
23
22
II
26/70
27
27
28
28
n
29/70
24
23
25
26
Oct.
Aver.
25
25
26
27
Nov.
2/70
21
19
22
19
n
5/70
25
25
23
24
n
9/70
25
24
25
25
n
12/70
23
23
24
23
n
16/70
27
24
24
22
Nov.
Aver.
24
23
24
23
FLOW 7.5 com
of Albuminoid and Ammonia - N Mg/1
STAGE NO.
4 5 6 7 8
22
—
18
9
24
22
21
15
25
24
23
20
28
—
28
26
23
23
21
20
25
23
22
21
18
16
15
12
27
26
22
22
26
25
23
24
23
21
18
19
19
16
17
22
24
22
21
25
24
21
20
23
20
19
17
20
17
13
11
22
21
18
17
Page 4 of 4
-------
TABLE 9
Carbon Dioxide Acidity CC2~-^g/l
19 70
DATE
I NFL
1
2
3
4
5
6
7
8
9
10
5/6
28
24
22
22
20
20
20
18
20
22
16
5/12
42
32
24
22
18
18
16
20
16
16
14
5/18
40
32
32
22
22
20
20
—
26
26
20
5/22
22
18
16
20
22
20
20
16
20
24
24
5/27
28
26
22
18
22
12
14
14
14
14
14
5/70
Aver.
26
23
21
21
18
18
17
19
20
18
6/2
24
19
16
12
— —
12
12
— —
_ —
12
6/5
26
16
18
—
—
8
16
—
14
6/8
29
26
24
24
18
16
14
—
12
6/11
26
26
—
22
16
— —
4
14
22
14
6/14
38
30
24
—
—
22
—
24
18
—
14
6/70
Aver.29
23
21
19
17
17
10
17
—
13
8/4
16
20
12
10
8
8
1Q
8
_ _
—
8/6
28
34
26
19
18
24
—
17
—
—
—
8/12
30
46
14
12
—
14
12
10
—
—
—
8/17
16
30
14
10
14
10
10
—
—
—
—
8/20
40
54
20
20
18
24
18
22
—
—
—
8/24
16
40
22
26
20
—
26
18
—
--
—
8/26
40
52
14
10
12
12
—
10
—
—
--
8/31
20
36
14
11
13
12
13
—
—
—
—
8/70
Aver.
39
17
15
15
15
15
14
—
—
—
9/8
20
38
20
41
9/9
20
60
20
48
9/14
24
46
22
44
9/16
26
52
26
50
9/70
Aver.
49
22
46
Page 1 of 2
-------
DATE
INFL
1
2
3
Oct.
5/70
24
34
26
24
fl
8/70
26
51
35
25
a
13/70
26
42
26
24
n
16/70
29
47
29
25
n
19/7 0
34
50
40
30
n
22/70
28
54
48
—
n
26/70
49
64
42
38
n
29/70
44
48
38
26
Oct.
Aver.
32
45
36
27
Nov.
2/70
44
58
40
32
n
5/70
40
42
32
26
ft
9/70
44
62
36
28
ti
12/7 0
36
52
36
- —
11
16/70
34
59
44
Nov.
Aver.
40
55
38
29
£ Acidity CCj-Mg/l
4
5
6
7
22
—
20
38
23
22
27
32
18
18
20
24
18
19
14
25
26
—
18
32
32
—
28
40
32
24
28
36
26
—
24
—
25
21
22
32
30
22
24
24
24
28
28
—
28
—
36
--
31
40
22
34
30
34
28
—
27
32
Page 2 of 2
-------
TABLE 10 1970
Bicarbonate Alkalinity HCO3 in Mg/1
STAGE NO.
DATE
INFL 1
2
3
4
5
6
7
8
9
10
5/6
220
188
192
192
—
200
196
140
122
108
100
5/12
218
220
208
226
218
216
212
200
158
148
144
5/18
208
204
206
212
212
206
206
—
176
158
158
5/22
230
228
228
224
226
225
230
204
182
168
162
5/27
208
200
200
212
204
196
178
168
168
130
116
May Aver,
208
207
213
215
209
204
178
161
142
136
6/2
208
210
222
212
222
206
_
122
6/5
214
206
208
-
-
—
192
162
—
-
119
6/8
214
218
216
216
228
—
212
174
-
-
130
6/11
210
218
-
214
220
—
200
172
-
146
137
6/14
212
212
218
-
-
220
—
182
158
-
150
June
Aver.
213
216
214
224
221
203
173
158
146
132
8/4
196
187
190
192
180
157
135
106
8/6
198
206
210
205
192
169
118
8/12
198
198
200
196
—
176
159
121
8/17
144
146
162
156
140
120
100
—
8/20
190
182
178
178
161
128
101
76
8/24
280
260
250
240
200
—
140
90
8/26
206
212
212
200
166
150
—
104
8/31
190
210
198
182
152
130
100
66
Aug.
Aver.
200
200
194
170
147
127
97
9/8
226
186
226
186
9/9
176
174
146
118
9/14
226
232
212
194
9/18
240
228
240
192
Sept.
Aver.
205
206
170
10/5
234
224
234
232
236
200
150
.10/8
220
228
230
218
222
214
208
172
10/13
236
226
236
232
220
2 20
213
195
1 Of 2
-------
Bicarbonate
DATE
INFL
1
2
3
Oct.
16/70
228
222
224
214
ft
19/70
272
266
272
270
n
22/70
190
182
174
-
r
26/70
222
224
224
222
ri
29/70
220
208
218
220
Oct.
Aver.
228
223
228
229
Nov.
2/70
190
186
194
186
fl
5/70
216
216
214
218
11
9/70
232
226
222
220
If
12/70
204
216
214
-
II
16/70
220
202
202
-
Nov.
Aver.
213
209
210
208
a 1 i r. i ty
HC03 in
Mg/1
STAGE
NO.
4
5
6
7
212
200
182
172
264
240
230
228
156
-
128
114
218
202
186
184
228
-
186
-
219
215
192
173
182
174
160
212
-
186
190
190
-
154
130
210
-
188
170
178
-
122
106
194
-
165
151
-------
CO
DATE INFL
12 3 4
8/6
8/8
8/12
8/13
8/18
8/20 1.3/.3
8/21
8/25
8/27 .5/-
8 Aver.
9/2
co 9/8
9/10
9/15
V17 .6/. 3
9/22
9/24
9 Aver.
10/1
10/2
10/6
10/8
10/13 «5/. 4
10/16
10/20
10/22
10/27
10/29
10 Aver
- -'sily
Is s
5
6
-/19
.8/. 8
.3/-
2.5/.7
.3/-
.5/. 4
.2/-
.8/.2
1.0/.3
1.8/,8
.5/. 2
1.3/2.0
.5/.2
2.4/.2
.8/. 1
1.8/.5
~ 4/. 2
1.5/.7
1.0/.4
1.3/1.2
.3/-
1.3/1.4
.5/.4
.8/2.4
.5/.8
1.5/1.2
.8/.3
• 3/o 7
1.3/.8
1.8/.8
.8/-
.8/1.2
.8/. 4
1.2/1.3
.5/. 3
1.5/.9
• 1/.2
.8/. 4
.2/. 3
.7/.7
.5/. 2
1.5/1.6
.6/14
2.0/.8
.8/. 4
1.0/2.9
.5/-
.6/. 8
.6/. 5
1.3/.4
1.0/.3
1.5/.5
.4/. 4
1.2/.4
.6/.3
1.3/,5
. ~ V" "V /<. -
* - ~ 2" 3
-N rr-.c/l
STAGE IvO
7
8
1.6/2.0
2.0/4.5
2.8/3.0
2.8/4.9
.6/2.2
2.3/3.8
1.4/1.1
1.3/2.2
1.7/4.6
1.4/7.0+
1.4/4.6
1.3/5.0
1.0/3.1
1.3/6.3
1.8/2.4
1.3/4.0
1.6/2.9
1. "/-'. . 7 -
1.8/2.8
1.9/5.6
1.8/3.6
1.0/8.0
.8/4.4
1.0/6*4
2.0/1.2
2.3/1.3
1.0/3.0
.8/7.2
2.5/2.0
2.5/4.4
1.0/6.4
1.0/8.4
1.6/3.0
1.5/5.6
2.0/1.3
2.0/4.7
1.0/1.0
1.0/4.4
1.0/1.6
1.0/4.0
1.5/4.0
1.5/6.4
2.3/1.7
3.0/3.3
1.0/6.8
.9/8.8
.8/2.4
1.0/3.2
2.0/1.0
2.0/2.8
- / >
3£CS 1 Of
4
9
10
2.0/5.5
2.0/7
2.8/7.0+
3.0/7
2.0/5.7
2.4/7
1.3/4.3
1.4/7
1.0/7.0+
.8/7
1. 0/9 . 0
.9/1
1.0/9.1
.8/1
1.3/7.2
1. 3 /'?
I.7/c.8+
1 . 6/8
1.0/9.2
— *
.5/12.4
1, 3/1
1.0/8,0
1.3/8
1.5/2.3
1. / 5
.8/10.4
. a/io
2.0/6.0
2.0/7
1.0/8.4
1.0/8
1.1/8.1
1.3/10
2.1/5.2
2.3/S
.9/5.6
1.0/5
1.4/5.6
1.7/7
1.8/7.2
1.9/1
3.0/5.1
3.3/5
1.1/11.2
1.0/1
1.1/3.2
1.0/9
2.3/3. 6
-/-
L. 0-'6.8
1 .c-/s
-------
i: ;.U W
Daily Profiles
DATE 12 3 4
11/3/69
U/12
11/19
11/24
11 Aver.
12/18
12/24 . 1/ . 3
12/26
12/29
12/30
12 Av?r.
1/1/70
1/5
1/6
1/3
1/13
1/14
Jan. Aver.
.4/-
.2/.3 .3/;3
. 2/.1 .2/.1
-2/-
1.2/-
• 6/. 1
.6/1,4
.3/.4
.2/-
7/-
r.5 gprn
of N02/N0
Mg/'l
5
6
7
8
9
10
. 3/. 5
.5/. 7
.6/3.1
.6/4.8
.6/6.8
.6/8.0
1. 5/ . 5
2.3/1.2
1.4/3.4
1.3/6.0
1.1/9.6
1.3/11.2
1.3/.5
1.0/1.5
1.5/4.1
.8/6.8
1.0/9.2
1.0/11.2
.6/. 2
1. 0/ . 7
1.0/2.3
1.0/3.7
1.1/6.8
1.0/8.4
1.0/.5
1.2/1.0
1.1/3.2
.9/5.6
1.0/8.2
1.0/9.7
. 6/. 1
. 7/. 1
.5/3.0
.5/3.0
.4/8.4
.4/13.:
1.7/2.4
1.2/6.0
1.0/9.4
1.5/.4
1.2/2.2
1.2/5 .0
1.2/7.0
2.0/ 10 . C
1.8/11.
.7/. 6
1.3/3.4
1.4/7.2
. 4/n. 2
2.0/;: f-
i. 8 / .
.5/. 5
.6/2.2
1.4/1.0
1.3/5.2
1.5/1' . r
-¦ . 5/ 1 L ,
1.0/ .8
1.0/2 . 8
1.1/5.1
1.1/6.6
1.5/1° .8
1 . 3/ L .? .
.5/. 4
. B/2 . 2
1.0/5.6
1.5/7.2
.1.4/: 2.0
1.5/-
.9/4.8
1.2/6 . 8
1.1/9.2
-
1.5/11.
1.3/2.7
1.5/4.8
1.6/7.0+
-
2.0/14.
1.3/-
1.8/2.0
1.5/6.6
1.8/-
2.5/5.0
2.6/9.C
~/l • 3
-/3 .0
-/ 4.0
-/3 . 2
-/2.C
-8/-
.8/1.0
1.3/2.5
1.4/3.3
2.0/3.4
2.6/2.1
1.1/2.3
1.3/4.9
1.5/5.1
2.0/5.9
2.1/7.1
Fage
2 of 4
-------
Daily Profiles of NO^-N Mg/1
STAGE NO o
DATE INFL
1
2
3
4
5
6
7
8
9
10
5/6/70
.4
.9
3.1
4.4
6.2
8.9
5/12
0
.6
2.8
5.4
8.2
11.9
5/18
.2
1.3
Out Serv
. 5.2
7.4
8.8
5/22
.4
2.2
2.0
4.1
6.8
9.8
5/27
2.0
3.6
4.1
7.6
10.3
12.2
May Aver.
.6
1.7
3.0
5.3
7.8
10.3
6/2
1.0
3.0
7.4
11.0
14.0
14.0
6/5
2.4
6.5
7.9
11.0
12,0
6/8
1.3
4.1
6.2
10.0
11.0
6/11
1.2
6.2
10.0
11.0
12.0
6/14
1.0
1.8
:.o
5.0
7.3
June Aver.
1.8
5.2
6.6
10.2
11 o 3
7/14/70
1
7
11
13
18
7/22
1
3
3
3
3
7/29
1
2
9
15
15
17
7/31
1
3
10
13
14
15
July Aver.
00
•
7.2
10.5
11.2
13.2
8/4/70
1.0
1.2
2.8
9.2
13.0
Stages 8
,9, and 10
8/6
.2
.8
4.5
10.8
15.0
bypassed
- 3.
59pm of
8/12
.5
.9
1.9
2.5
9.6
stage 7
eff.
pumped
8/17
.2
1.4
3.0
7.0
14.5
to
FST
8/20
1.8
1.2
6.6
11.3
15.6
U
8/24
.1
2.5
5.5
7.0
15.2
u
8/26
.1
2.8
4.4
6.4
10.8
u
8/31
.1
5.8
9.8
14.0
17.6
II
Augc Aver.
.5
2.1
4.8
8.5
14.3
-------
Daily Profiles of NO-^-N Mg/1
1970
STAGE
NO.
DATE INFL 1
2
3 4
5
6
7
9/8/70
0
Stages 3 to 6 out
of Service
9.5
9/9
* 7
¦ It
n
a
7.7
9/14
.6
11 •
•«
N
6.9
9/16
.2
¦ m
it
a
6.4
Sept. Aver.
.4
7.6
10/1
.8
-
5.2
12.6
10/5
1.1
2.8
3.6
8.1
10/8
1.0
2.2
3.2
5.3
10/13
.1
.4
.5
4.1
10/16
. 2
1.8
3.6
6.4
10/19
0
.2
1.0
4.8
10/22
1.1
3.6
5.6
8.8
10/26
.9
3.2
7.0
7.3
10/29
.3
2.9
7.2
-
Oct. Aver.
.5
1.9
4.1
7.2
11/2
.8
1.8
5.0
7.2
11/5
.4
.4
1.6
2.4
11/9
.3
1.6
5.0
7.2
11/12
.4
2.5
4.0
5.4
11/16
5.7
8.3
12.7
12.9
Nov. Aver.
1.5
2.9
5.7
7.0
8
10
Stages 8, 9, and 10
bypassed - 3.59pm of
stage 7 effluent
pumped to FST
-------
FST
8
11
B
7
18
12
9
6
15
11
10
7
9
12
11
9
6
5
13
11
9
7
14
9
TABLE 12
FLOW 7
. 5 gpm
Daily
Profiles of
TOC and
DTOC :
ig/1
STAGE
NO.
INFL
1
2
3
4
5
6
7
8
9
TO C
91
64
40
34
25
24
32
32
Out Ser-
16
DTOC
60
34
29
26
24
19
16
14
vice
14
TOO
99
84
48
52
51
15
14
19
17
17
DTOC
32
23
23
26
22
—
—
16
14
13
TOC
95
87
65
47
33
27
22
11
19
10
DTOC
43
43
36
27
23
13
19
12
15
13
TOC
88
62
43
24
17
11
15
8
11
9
DTOC
40
35
30
24
18
16
12
12
11
9
TOC
96
71
56
39
37
21
21
18
18
18
DTOC
42
35
29
22
22
21
16
20
17
13
TOC
89
75
58
40
25
22
21
19
17
15
DTOC
42
21
18
18
15
15
15
14
13
13
TOC
86
70
58
41
31
27
21
18
17
16
DTOC
39
34
26
20
20
19
15
14
16
15
TOC
56
40
25
18
10
15
8
12
7
12
DTOC
20
20
20
14
10
8
10
10
10
10
TOC
85
67
51
35
26
21
18
14
15
13
DTOC
38
31
27
21
18
15
14
14
14
12
TOC
78
50
40
29
21
14
11
11
13
11
DTOC
25
21
19
13
11
11
13
9
8
8
TOC
84
75
52
46
32
14
23
11
19
15
DTOC
28
23
18
22
19
18
16
15
15
15
TOC
98
65
45
33
30
18
13
11
10
13
DTOC
47
28
22
19
18
12
16
14
11
10
TOC
83
48
37
33
30
16
19
12
16
14
DTOC
16
24
11
16
12
16
10
13
8
9
-e 1 of 5
-------
FLOW 7
Daily Profiles of
1970
DATE
INFL
1
2
3
4/^7/70
TOC
110
70
59
42
DTOC
33
32
22
24
4/30/70
TOC
94
54
44
39
DTOC
61
31
18
13
4 Aver.
TOC
91
60
46
37
DTOC
35
27
18
18
5/6/70
TOC
98
72
44
30
DTOC
36
20
21
17
5/12/70
TOC
93
59
51
43
DTOC
35
23
20
18
5/18/7 0
TOC
113
88
70
47
DTOC
50
45
32
25
5/22/70
TOC
88
47
39
19
DTOC
40
26
19
15
5/27/70
TOC
81
59
44
33
DTOC
25
26
25
18
¦ Aver.
TOC
95
65
50
34
DTOC
39
28
23
19
6/2/70
TOC
91
56
38
30
DTOC
23
24
16
13
6/5/70
TOC
90
40
40
32
DTOC
36
19
22
17
6/8/7 0
TOC
82
43
43
35
DTOC
26
22
17
18
6/11/70
TOC
107
63
49
51
DTOC
39
26
19
25
5 gpm
TOC and DTOC Mg/1
STAGE NO.
4
5
6
7
8
9
10
PST
40
32
20
18
17
12
15
11
24
22
17
15
14
10
12
10
12
15
10
16
8
12
6
6
11
10
12
16
15
14
11
6
33
18
3.9
13
14
13
12
10
19
15
17
14
12
11
11
£
26
20
20
16
13
13
9
12
18
15
14
8
12
9
10
10
32
20
20
15
15
13
12
9
17
17
15
14
13
9
10
10
45
25
23
8
16
16
13
20
17
12
14
12
10
9
17
14
9
14
13
11
9
9
15
9
12
9
11
10
11
9
22
20
18
19
15
12
11
10
18
15
14
14
12
11
11
8
28
20
18
16
13
13
11
11
18
15
13
11
12
10
10
9
30
10
18
15
9
11
11
7
13
10
13
13
10
13
10
10
29
10
16
17
12
12
7
7
17
8
12
12
11
11
11
11
26
17
16
13
12
12
11
10
17
14
13
12
11
10
10
6
31
10
16
15
10
11
8
8
17
15
9
15
7
11
7
11
Page 2 of
5
-------
FLOW 7.5 gpm
Daily
Profiles of
TOC and
DTOC
Mg/1
1970
STAGE
NO.
DATE
INFL
1
2 3
4
5
6
7
8
9
10
FS-]
6/L4/7 0
TOC
101
48
48 40
30
25
20
18
18
15
15
7
DTOC
25
25
12 13
13
—
15
14
14
9
12
6
6 Aver.
TOC
94*
50*
44* 38
29
14
17
16
12
12
10
8
DTOC
30*
23*
17* 17
15
12
12
13
11
11
10
9
Note:
*Flcw
split between Stages
1 and 2
7/8/70
TOC
80
Out Ser-
- 45 29
27
22
19
20
15
21
15
15
DTOC
24
vice
24 16
18
16
14
14
12
12
12
11
7/14/7 0
TOC
59
n
Out Ser-40
25
17
15
13
8
8
8
10
DTOC
29
ft
vice 17
15
14
13
9
9
8
8
5
Stage
s 1 and
2 being
modified.
Hood placed over stage enclosing
atmospher
e
7/2 2/7 0
earic
hed wit
h oxvgen
7/18/70
TOC
72
" 37
20 20
22
15
14
13
12
13
10
8
DTOC
27
16
13 11
13
11
10
9
8
8
8
6
7/29/70
TOC
68
34
23 20
21
13
12
12
11
10
8
7
DTOC
35
18
15 13
12
11
10
9
8
8
8
6
7/31/7 0
TOC
71
41
17 14
—
—
12
11
10
9
8
7
DTOC
41
16
13 11
11
9
9
9
7
7
7
7
7 Aver.
TOC
70
37
20 18
22
14
13
13
11
11
9
7
DTOC
34
17
14 12
12
10
10
9
8
8
8
6
8/4/7 0
TOC
70
29
20 16
14
12
11
11
12
9
8
9
DTOC
28
17
13 12
12
12
10
9
8
8
9
9
8/6/7 0
TOC
60
25
14 16
11
11
10
8
8
8
7
8
DTOC
23
14
13 11
11
8
10
9
8
7
8
8
8/12/70
TOC
62
38
23 23
17
17
11
13
10
DTOC
19
10
12 10
12
11
8
10
9
8/17/70
TOC
68
36
21 22
18
17
16
13
8/2 0/70
DTOC
28
20
17 15
13
11
10
13
TOC
56
23
23 20
20
13
13
15
8
DTOC
20
14
1? 11
1 j
11
10
9
10
Pace 3 of 5
-------
FLOW 7
Daily Profiles of
1970
INFL
1
2
3
8/24/7 0
TOC
63
24
19
16
DTOC
27
13
10
10
8/26/70
TOC
63
35
18
12
DTOC
28
17
14
11
8/31/70
TOC
69
37
21
18
DTOC
19
19
16
14
8 Aver.
TOC
64
31
20
18
DTOC
24
16
13
12
9/8/70
TOC
71
34
13
Out
DTOC
37
20
13
9/9/7 0
TOC
52
31
16
n
DTOC
34
13
11
9/14/70
TOC
81
31
20
r»
DTOC
48
20
14
9/16/70
TOC
75
24
17
ii
DTOC
41
21
11
9 Aver.
TOC
70
30
17
«
DTOC
40
19
12
9/22/7 0
TOC
64
14
16
16
DTOC
30
12
15
16
9/2 8/70
TOC
89
57
36
24
DTOC
47
25
22
19
10/1/7 0
TOC
68
36
25
17
DTOC
36
21
17
14
10/5/7 0
TOC
77
43
36
21
DTOC
44
25
20
16
10/8/70
TOC
70
38
28
22
DTOC
37
21
18
14
5 gpm
TOO and DTOC Mg/1
STAGE NO.
4
5
6
7
8
9
10
FST
14
10
9
11
10
12
9
9
9
7
12
12
12
15
6
12
11
11
11
6
15
15
15
14
14
15
11
11
10
10
15
13
12
11
9
12
11
10
11
8
of
Service
16
10
12
8
n
n
11
9
10
10
n
0
16
10
13
9
n
n
10
10
11
10
VI
it
13
10
11
9
16
13
16
13
11
13
7
7
13
11
13
10
10
8
6
6
23
20
19
13
13
11
10
10
16
13
13
13
10
10
7
7
17
16
14
10
8
8
8
10
14
13
12
9
9
7
9
10
18
--
17
15
10
10
6
6
14
16
14
13
12
9
8
7
17
15
15
15
11
10
10
10
13
12
12
11
12
8
8
8
Page 4 of 5
-------
FLOW 7 . 5 g-pm
Daily Profiles of TOC and DTOC Mg/1
1970
STAGE NO.
DATE
INFL
1
2
3
4
5
6
7
8
9
10
FST
10/13/70
TOC
73
53
33
17
11
20
11
16
9
11
6
8
DTOC
37
29
17
17
15
17
15
15
9
12
9
7
10/16
TOC
54
23
23
13
15
14
14
12
13
9
6
9
DTOC
28
13
13
12
10
9
9
9
9
8
7
7
10/19
TOC
75
42
34
24
23
20
18
15
14
13
9
8
DTOC
43
25
21
15
15
14
14
12
10
11
8
9
10/22
TOC
66
24
20
14
12
12
12
12
11
10
10
9
DTOC
23
15
13
11
10
9
9
8
8
9
8
7
10/26
TOC
79
44
36
29
21
23
16
16
9
9
9
9
DTOC
33
18
18
17
16
14
15
11
10
8
9
9
10/29
TOC
85
48
34
30
20
20
24
—
—
18
16
8
DTOC
45
24
20
18
18
18
20
—
—
15
14
8
Oct. Aver.TOC
78
38
29
21
18
17
16
14 *
11
11
9
9
DTOC
37
21
18
15
14
13
13
11*
10
10
8
8
Note:
*A 3.5
gpm portion of
the
effl.
from :
stage 7
transferred
by pump to
FST
11/2
TOC
85
45
34
27
26
20
19
17
18
15
15
7
DTOC
41
24
17
20
19
18
12
14
11.
12
12
7
11/5
TOC
82
50
39
35
26
18
17
15
26
12
11
8
DTOC
43
20
18
12
17
11
15
11
20
11
10
7
11/9
TOC
76
44
27
21
19
16
15
14
13
12
13
9
DTOC
39
19
17
15
14
14
14
14
12
10
11
10
11/12
TOC
88
40
27
31
18
17
15
11
12
10
11
9
DTOC
43
15
18
13
13
14
10
11
12
11
11
10
11/16
TOC
78
26
16
18
13
14
10
12
9
9
9
9
DTOC
41
13
15
13
11
14
10
9
9
7
8
7
Nov. Av.TOC
82
41
29
26
20
17
15
14
14
12
13
9
DTOC
41
18
17
15
15
14
12
12
13
11
11
8
Paoe S of 5
-------
TABLE j.3
DATE FLOW
GPM
11/23/70
17.7
11/25
17.7
11/20
12.0
12/3
11.0
12/8
11.0
12/14
13.0
12/17
12.0
12/21
13.0
12/22
12.0
12/28
14.0
12/29
i * n
— T. «
1/4/71
14. G
1/7
14.0
1/11
14.0
1/14
14.0
1/18
14.0
1/21
14.0
1/25
14.0
1/28
14.0
2/3
14.0
2/4
14.0
2/11
14.0
PROFILES CF OFTHO ?KOSFHATES Hg/1
High Flow Periods 11/23/70 tc 3/25/71
STAGE NO.
INFL 123456789 10 FST
19.0
17.8
17.4
-
13.3
-
12.6
—
12.6
-
11.5
11.4
20.O
14.6
16.0
-
12.3
-
11.8
—
11.9
-
12.0
12.4
32.2
25.0
-
-
-
—
21.8
—
-
-
21.4
20.1
33.2
-
28.0
-
-
-
25.4
-
—
-
25.2
22.2
<1.6
-
33.6
33o2
-
29.5
—
26.7
—
26.2
26.2
19.8
14.5
-
-
12.2
-
-
-
-
» ¦
15.5
16.7
15.9
16.7
-
16.8
-
17.0
—
17.4
17.4
22«e
22.2
16.7
18.1
17.3
-
17.5
-
17.8
-
17.8
18.7
i a
18.6
15.7
15.3
15.5
-
15.3
-
15.3
-
15.3
15.7
17.0
32.2
26.0
30.0
28.0
-
27.2
-
—
23.0
•
23.0
20.2
23.8
18.6
19.2
18.4
-
19.2
-
-
19.6
•
19.8
19.0
29.4
—
-
21.7
-
-
—
21.5
—
•
21.5
20.5
23o8
-
-
17.8
17.6
-
17.6
-
17.3
-
17 o0
17.6
22.4
16.2
16 o 5
15.8
-
-
—
-
—
15.8
15.8
16.4
15.4
10.9
-
11.5
-
-
11.5
-
-
11.7
11.7
14.4
17.5
15.5
16.6
15.4
15.2
15.7
—
—
—
16 o4
16.4
16.7
21.8
18.0
-
17.5
17.0
—
-
—
_
—
16.8
17.5
17.0
19.2
-
19.2
17.8
-
-
-
—
-
19.2
18.0
Page 1 of 2
-------
PROFIL
es cr
CRTHOP
HOSPHAT
ES
Mg/1
High Flc
v Per
iods 11/23/70
to
3/25/71
DATE
FLOW
INFL
1
2
3
4
5
6
7
8
9
10
FST
G.P.M.
2/16/71
14 o 0
24.8
20.3
—
20.5
19.7
—
_
19.0
18.4
2/19
14.0
27.8
24.3
—
24.7
22.7
-
-
-
—
—
20.4
19.0
2/22
14.0
21o2
-
-
19.9
18.9
-
-
-
—
—
18.9
19.2
2/25
14.0
250 2
—
—
18.5
18 „ 5
—
-
18.7
-
-
19.8
17.0
3/1
14.0
23.8
-
21.8
21.8
21.8
_
20.4
19.8
18.9
3/3
14.0
27 .S
21.5
-
21ol
-
-
17 „ 3
—
19.2
17.0
3/8
14 o 0
26. 6
13.7
-
1809
18.3
-
-
18.7
—
—
18.7
18.0
3/11
14 o 0
1906
13.7
-
1307
14.0
-
-
130 7
—
—
13.5
13.0
3/15
14,0
2S.0
-
-
160 4
15 o 9
-
-
15.3
-
—
15.3
14.6
3/18
T A
— Taw
25 .6
14.7
-
15 o 3
17.7
—
17.6
—
17.6
—
17.6
17.7
3/22
14.0
36,0
15.3
-
14.4
14.4
—
14.7
—
14.4
—
14.4
14. C
3/25
14.0
25.6
16.0
—
160 0
1507
-
-
15.5
-
-
15,0
14.5
Page 2 of 2
-------
DATE P.S.T.
11/23/70
11/25
11.4
11/30
12.4
12/3
20 o 1
12/8
22.2
12/14
19. S
12/17
* "! Q
J- « «•
12/21
27.2
12/22
20.4
12/28
19.7
12/29
22.8
1/4/71
19.3
1/7
17.0
1/11
20.2
1/14
19.0
1/18
20.5
1/21
17.6
1/25
16.4
1/28
14.4
TABLE 14
PROFILES OF ORTHOPHOSPHATES Mg/1
High Flew Periods 11/23/70 to 3/25/71
Through Treatment Subsequent to F.S.T.
ALGAL
16th
STAGE
MIXED CARSON COL. NO.
MEDIA 12 3 4
FILTER
11.8 11.7 11.5
12.0 12.4 12.4
21.4 - 21.4
25.4 - 24.8
23.3 - 23.8
15.5
26.5 Out Of
26.1
21.8
25.7
24.3
21.2 21.1 21.2
21.8
19.0 19.2
20.5 20.5
18.0 17.0
15.8 15.6
15.4 15.2
- 12.6
- 13.2
- 22.6
- 25.2
- 24.2
- 18.6
Service
M
It
M
tt
- 20.4
19.2
19.8
21.8
17.6
16.8
13.0
Page 1 of 2
-------
DATE
F.S.T,
PROFILES OF CRTHCPHOSPHATES >'g/l
High Flov; Periods 11/23/70 to 3/25/71
Through Treatment Subsequent to F.S.T,
ALGAL
16 th
STAGE
MIXED
MEDIA
FILTER
CARBON COL. NO,
3 4
vO
cn
2/3/71
16.7
21.5
21.8
24.4
2/4
17.5
23.0
22.7
23.4
2/11
18.0
17.5
18.0
17.5
2/16
IS. 4
20.5
19.7
21.2
2/19
19.0
17.8
17.6
19.0
2/22
19.2
21.2
20.8
21.8
2/25
17.0
20.8
19.3
20.5
3/1
1 p o
19.5
19. 2
19.5
3/3
17.0
21.5
20.1
18.0
3/8
18.0
17 o 2
17.2
18.0
3/11
12.0
13.8
13.8
13. 5
3/15
14,6
14.6
14.8
1408
3/18
17.7
18.4
18.4
18.4
3/22
14.0
13.7
13.7
13.7
3/25
14.5
14.5
14.5
15.7
Page 2 of 2
-------
DATE FLOW
GFM
11/23/70 17.7
11/25 17.7
11/30 12.0
12/3 11
12/8 11
12/14 13
12/17 12
12/21 13
TABLE 15
PROFILES 0? TOC ar.3 DTOC :*g/l
High Flow Periods 11/23/70 to 3/25/71
STAGE NO.
INFL 123456729 10 FST
TOC 58 38 35 25 25 21 20 21 19 18 16 11
DTOC 35 20 19 19 19 19 18 17 17 12 12 11
TOC 75 40 39 32 35 32 29 24 23 22 21 14
DTOC 31 19 19 12 19 12 17 9 16 11 14 13
TOC 66 26 35 24 19 21 21 16 16 13 12 11
DTOC 33 16 18 16 16 10 15 9 13 11 12 10
TOC 89 35 40 37 22 20 18 16 15 19 12 10
DTOC 45 18 19 12 16 14 13 13 12 12 11 9
TOC 86 29 29 35 25 25 16 16 15 14 9 10
DTOC 51 11 17 14 16 13 9 10 9 9 8 8
TOC 153 61 62 60 49 45 29 33 22 22 20
DTOC 68 39 22 28 19 20 15 19 19 19 18
TOC 61 37 37 33 33 28 21 20 19 17 9 13
DTOC 11 10 10 8 10 8 8 6 7 8 6 6
TOC 94 67 42 44 48 39 32 28 24 21 18 12
DTOC 36 26 20 23 22 21 18 15 15 16 10 12
Page 1 of 4
-------
CONTINUED
PROFILES OF TOC and DTOC
DATE
1970
12/22/
12/28
12/29
1/4/71
1/7
1/11
1/14
1/18.
1/21
FLOW
GPM
12
14
14
14
14
14
14
14
14
TOC
DTOC
TOC
DTOC
TOC
DTOC
TOC
DTOC
TOC
DTOC
TOC
DTOC
TOC
DTOC
TOC
DTOC
INFL
76
30
60
22
61
19
73
35
63
27
TOC 108
DTOC 48
78
27
87
44
71
32
48
20
37
15
31
17
38
16
28
14
68
18
43
19
48
21
34
18
43
13
34
15
25
19
33
12
39
12
79
32
50
21
47
23
44
20
36
18
37
15
24
15
29
16
28
16
57
21
42
20
46
23
33
22
30
13
28
15
25
14
30
11
28
11
52
26
38
19
36
17
31
i o
Ug/1
STAGE NO.
5 6 7
26
12
25
15
21
15
24
15
19
14
46
25
35
19
41
22
34
17
20
15
20
15
18
15
21
13
17
13
40
23
32
19
32
18
27
17
20
14
19
12
19
15
20
14
16
12
28
18
24
17
27
18
22
:e
8
19
n
17
10
17
13
12
14
12
31
19
24
15
13
13
25
16
9
20
13
16
14
10
11
13
10
24
17
22
15
19
15
24
15
10
15
10
16
10
10
19
12
14
10
25
17
23
14
14
18
22
FST
16
12
19
11
16
13
29
10
14
8
24
15
23
16
19
11
27
14
Page 2 of 4
-------
CONTINUED
PROFILES OF TOC and
DATE
1/25
1/28
2/3
2/4
2/11
2/16
2/19
2/22
FLOW
GPM
14 TOC
DTOC
14 TOC
DTOC
14 TOC
DTOC
14 TOC
DTOC
14 TOC
DTOC
14 TOC
DTOC
14 TOC
DTOC
14 TOC
DTOC
INFL
68
32
73
31
71
31
66
22
56
33
117
23
87
35
85
27
45
21
34
12
40
23
31
13
32
27
69
23
55
23
63
26
43
21
38
17
41
20
28
14
51
22
67
17
61
28
52
18
41
20
36
22
33
20
22
15
29
23
49
22
49
23
48
21
34
17
36
19
22
15
26
20
43
21
51
23
34
18
TOC Mg/1
STAGE NO.
5 6 7
31
24
27
20
31
19
24
13
26
16
41
21
28
22
29
20
30
19
30
15
23
17
16
14
23
19
40
19
29
19
28
16
24
16
27
16
23
16
16
13
20
18
28
19
27
16
28
15
S
23
17
18
14
24
16
17
15
18
13
30
18
27
15
18
14
23
20
21
15.
24
15
18
18
15
28
17
22
17
10
19
13
19
10
20
19
14
11
20
15
18
13
18
14
FST
22
16
21
8
18
15
11
8
9
11
12
11
15
11
16
8
Page 3 of 4
-------
FS
10
6
15
9
6
9
16
11
16
11
11
10
12
12
13
11
10
9
CONTINUED
PROFILES OF TCC and DTCC Mg/i
STAGE NO.
FLOW INFL 123456789 10
GFM
14 TOC 86 102 88 40 25 25 17 18 14 16 10
DTCC 43 28 41 22 14 11 12 11 10 10 8
14 TOC 79 54 43 49 35 30 21 21 17 15 14
DTOC 39 32 23 24 24 20 18 15 12 12 10
14 TCC 112 89 83 72 39 31 17 17 17 17 18
DTOC 39 14 12 13 10 14 13 14 12 12 12
14 TOC 76 51 54 45 33 23 22 23 13 16 14
DTOC 37 23 24 24 23 18 17 15 17 15 12
14 TCC 61 47 48 45 33 22 20 22 24 17 15
DTOC 27 20 19 17 17 17 15 15 17 17 11
14 TOC 66 44 32 43 29 27 20 19 16 13 14
DTOC 28 20 20 25 14 19 13 16 9 9 12
14 TOC 82 35 61 48 41 36 24 22 21 20 18
DTOC 33 18 23 21 - 19 16 16 14 13 12
14 TOC 79 44 41 34 34 33 20 19 18 16 16
DTOC 29 23 21 22 18 18 14 14 14 13 11
14 TOC 82 51 60 49 24 24 21 22 21 16 16
DTCC 37 20 20 20 18 18 15 14 15 13 10
-------
PROFILES 0? TCC and DTOC Mg/l
Through. Treatr.ant Subsequent to FST
HIGH FLOW PERIODS
11/23/70 to 3/25/71
DATE
F.S.T.
ALGAL
16th
STAGE
MIXED
MEDIA
FILTER
CARBON COL. NO.
2 3 4
11/23 TOC 10.5
DTOC 11.0
10.5
8.0
10.0
7.0
5.5
7.0
3.5
5.5
3.5
3,0
2.5
3.0
2.5
1.5
1.5
1.0
11/25 TCC 14.0
DTOC 13.0
9.0
8.5
8.5
8.0
4.5
6.5
4.5
3.0
3.0
3.0
2,0
2.0
1.5
1.5
1.5
1.5
NJ
O
o
11/30
12/3
TOC 11.0
10,0
TCC 10,0
DTOC 9,0
10.0
7.5
8.0
8.0
11.0
8.5
8.0
8„0
5.5
4 o 0
7.0
6.0
4.5
4.0
5.0
5.5
3.5
3.5
4.0
4.0
3.0
2.0
3.5
3.5
2.5
2.0
1.5
2.5
1.5
1.0
1.5
1.5
12/8 TOC 10.0
DTOC 8.0
11.0
7.0
8.0
7.0
7.0
5.0
4,0
4.5
4.5
4,5
3.5
4.0
1.5
4.0
2.0
1,5
12/14 TOC 7.0
DTOC 8.0
7o0
6,0
6.0
8.0
5.0
5,0
5.0
3.0
4.0
3.5
3.0
4.0
3,0
2.5
2.0
3.5
12/17 TCC 13,0
DTOC 6.0
6,0
6.0
10.0
4.0
4,0
3.0
6.0
4.0
4.0
3.5
3.5
3.5
3.0
3.5
3.5
3.0
12/21 TCC 12.0
DTOL 12.0
12.0
9.0
Out
Of
Service
Page 1 of 4
-------
PROFILES OF TOG and D'ruu -g/j.
Through Treatment Subsequent to FST
HIGH FLO*,; PERIODS
11/23/70 to 3/25/71
DATE
P.S.T.
ALGAL
16 th
STAGE
MIXED
MEDIA
FILTER
CARBON COL. NO.
2 3
12/22 TOC 16,0
DTOC 12.0
12.0
9.0
Out
«t
Of
Service
12/28 TOC 19.0
DTOC 11.0
13.0
9.0
to
o
12/29 TOC 16.0
DTOC 13.0
12.0
13.0
1/4 TOC 29.0
DTOC 10.0
17.0
5.0
n
u
1/7 TOC 14.0
DTOC 8.0
11.0
8.0
10.0
8.0
9.0
7.5
5.5
6.5
6.5
4,»0
4.5
4.5
4.0
3.5
4.
3.
1/11 TOC 24.0
DTOC 15.0
14.0
13.0
13.0
12.0
12.0
11.0
11.0
12.0
10.0
8.5
6.5
6.0
6.5
6.0
4.
4.
1/14 TOC 23.0
DTOC 16.0
16.0
15.0
15.0
15.0
13.0
10.0
10.0
8.0
5.5
6.0
6.0
6.0
5.5
7.0
8,
1/18 TOC 19.0
DTOC 11.0
9.0
16o0
8.0
9.0
10.0
10.0
6.0
6.5
7.0
7.0
4.0
4.5
6.0
C
3
Page 2 of 4
-------
PROFILES OF TOC and DTOC Mg/1
date
F.S.T.
Through Treatment Subsequent to FST
HIGH FLOW PERIODS
11/23/70 to 3/25/71
ALGAL
16 th
STAGE
MIXED
MEDIA
FILTER
CARBON COL
2 3
NO.
to
O
w
1/21
1/25
1/28
2/3
2/4
2/11
2/16
2/19
TOC
DTOC
TOC
DTOC
TOC
DTOC
TOC
DTOC
TOC
DTOC
TOC
DTOC
TOC
DTOC
TOC
DTOC
27.0
14.0
22.0
16.0
21.0
8.0
18.0
15 o0
11.0
8„0
9.0
lloO
12.0
11.0
15.0
11.0
14.0
13.0
14.0
11.0
11.0
10.0
23.0
15.0
6o0
6.0
8.0
5.0
10.0
12.0
10.0
10.0
14.0
11.0
13.0
12.0
10.0
9.0
13.0
9.0
7.0
7 o0
6.0
6.0
11.0
8.0
7.5
5.0
11.0
10.0
10.0
10.0
10.0
6.0
8.0
9.0
4.0
4.0
5.0
4.5
10.0
7.0
12.0
5.0
10.0
8.0
9.0
3.0
8 0 0
6.0
10cC
10.0
6.0
6o0
4.5
4.5
7.0
6.0
5 „5
5.0
7.5
8,0
5.5
5.0
6.0
3.5
6.0
4.0
5.0
2.0
4.5
4.0
7.0
6.0
4.5
4.0
7.0
5.5
6o0
6.0
€.0
2 o Q
5.0
5.0
3.0
3.0
4.0
3.0
5.0
6.0
5.0
5.0
5.0
7.5
5.0
5.0
8.0
3.0
8.0
8.0
3.5
2.0
3.0
3.5
5.5
6.0
4.5
4.0
6.<
3.!
5.
4.
4.
2.
2.
•3
2,
1,
3.
2
5
4
4
3
Pc.=?e 3 of 4
-------
PROFILES 0? TOC and DTOC g/1
Through Treatment Subsequent to FST
HIGH FLOW PERIODS
11/23/70 to 3/25/71
DATE
P.S.T.
ALGAL
16 th
STAGE
MIXED
MEDIA
FILTER
CARBON COL. NO.
2/22
2/25
TOC
DTOC
TOC
DTOC
NJ
o
3/1/71 TOC
DTOC
3/3
3/8
3/11
3/15
3/18
3/25
TOC
DTOC
TOC
DTOC
TOC
DTOC
TOC
DTOC
TOC
DTOC
TOC
DTOC
16.0
8.0
10.0
6.0
15.0
9.0
6.0
9.0
16.0
11.0
16.0
11.0
11.0
10.0
12.0
11.0
10.0
9.0
9.0
10.0
6.0
5.5
8.0
9.0
6.0
7.0
10.0
8.5
12.0
9.5
7.0
7.0
9.5
9.0
8.0
10.0
6.0
4.5
6.0
6.0
8.0
8.0
6.0
5o5
9.0
7.0
10.0
10.0
6.0
8.0
8.5
6.5
8.?
6.5
6.0
5.0
6.0
6.0
7.0
8.0
5.5
5.5
7.0
6.5
8.5
6.0
5.0
3.0
s.o
7.5
6.5
<= n
4.0
3.5
6.0
6.5
5.0
4.5
4.5
3.5
5.0
6.0
7.0
7.5
2.5
3.0
7.5
5.0
£ . 5
6.0
5.0
3.5
4.0
4.0
4.5
4.0
4.0
3.0
5.0
4.5
5.0
4.0
2.5
3.0
7.5
5.0
4.0
3.0
4.5
4.0
=; n
• -*r
4.0
3.0
3.5
4.0
4.0
5.0
5.0
2.0
3.0
4.0
3.5
4.0
4.5
3.5
3.0
4.0
^ n
. * «¦
4.0
2.0
2.0
3.0
4.0
4.5
4.0
2.0
2.5
4.0
4.0
3.5
2.5
3.0
4.5
1 c
—' • —'
3.C
2.C
1.5
2.7;
3.-"
4.
3.
2.
3.
4.
3.
4
2,
-------
TABLE 17
PROFILES OF ALEUMINOID and A NITROGEN Mg/
High
Flow
Periods
11/23/70 to
3/25/71
DATE
FLOW
I NFL
STAGE
NO.
GPM
1
2
3
4
5
6
7
1970
11/23
17.7
28
27
27
-
-
27
27
27
11/25
17.7
29
28
-
27
—
27
27
27
12/3
11.0
30
29
30
30
_
31
31
12/8
11.0
28
28
28
27
—
27
—
28
12/14
13.0
25
23
25
24
-
24
24
—
12/17
12,0
13
12
11
11
11
—
10
—
12/21
13.0
26
-
-
26
—
—
27
—
12/22
12.0
27
-
-
22
-
25
-
-
12/28
14.0
23
-
-
23
-
22
—
22
12/29
14.0
21
20
20
20
-
21
-
21
1971
1/4
14.0
27
26
27
27
26
—
27
—
1/7
14.0
30
26
27
27
-
27
—
26
1/11
14.0
30
-
-
29
-
—
—
—
1/14
14.0
29
29
28
30
-
—
30
—
1/18
14.0
31
-
¦-
29
- ¦
-
-
30
1/21
14.0
29
28
28
28
-
—
-
—
1/25
14.0
24
25
25
24
-
-
—
25
1/28
14.0
29
29
-
28
—
29
-
28
2/3
14.0
27
28
27
27
27
_
27
2/4
14.0
25
-
-
27
27
-
—
—
2/11
14.0
20
-
-
20
21
-
—
23
Page 1 of
-------
PRC?
ILES OF
A L SUM I In
¦OJD
end kMUONIA NI
. X - VU- Vj
H 3/1
High ?
low Peri
.ods
11/23/7 0 to 3/25/71
DATE
FLOW
I NFL
STAGE
NO.
GPM
1
2
3
4 5
6
7
8
9
10
FS1
1971
2/16
14.0
27
—
—
27
27
—
—
—
29
28
26
2/19
14.0
26
-
-
27
28
—
—
25
-
23
25
2/22
14.0
21
-
-
22
24
—
-
-
-
25
23
2/25
14.0
25
—
-
24
28
-
28
-
28
26
25
3/1
14.0
26
25
27
28
26
25
3/3
14.0
37
-
-
29
30
28
—
—
_
zc
18
3/8
14.0
24
-
-
—
25
27
—
-
2 5
23
24
3/11
14.0
24
-
—
—
27
—
—
—
25
24
22
3/15
14.0
26
-
-
26
27
27
27
25
25
26
3/18
14.0
28
-
-
29
29
31
—
30
28
29
27
3/22
14.0
28
-
—
28
28
—
29
28
26
25
24
3/25
14.0
27
-
28
29
30
30
24
28
24
27
21
Page 2 of 2
-------
TABLE 18
PROFILES OF ALBUMINOID and AMMGNI?. NITROGEN Mc/l
Through Treatment Subsequent to F.S.T.
High Flow Periods 11/23/70 to 3/25/71
DATE
FST
ALGAL
MIXED
CARBON
COL.
NO.
16th
MEDIA
1
2
3
4
5
6
STAGE
FILTER
11/23/70
16
7.7
O
•
00
8.0
_
_
6.5
11/25
16
7.5
-
8.6
-
-
—
—
8.6
2/3
27
18
16
-
—
-
-
—
16
2/4
25
16
17
-
-
-
—
-
14
2/11
25
10
10
-
-
-
-
-
9
2/16
26
21
21
—
-
-
-
-
18
2/19
25
18
18
-
-
-
-
-
12
2/22
23
15
16
-
-
-
-
-
14
2/25
25
11
11
-
-
-
¦-
-
9
3/1
25
14
14
-
-
-
-
-
12
3/3
18
5
4
-
-
-
-
—
2
3/8
24
13
12
-
-
-
-
—
8
3/11
22
9
10
-
-
. -
-
-
9
3/15
26
13
13
-
-
-
-
-
10
3/18
27
13
12
-
-
-
-
-
10
3/22
24
9
10
—
-
-
-
-
8
3/25
21
6
8
-
-
-
-
-
6
-------
TABLE 19
PROFILES OF BOD5 Mg/1
High Flow Periods 11/23/70 to 3/25/71
DATE
FLOW
INFL
STAGE
NO.
GPM
1
2
3
4
5
6
7
8
9
10
FST
11/23/70
17.7
90
46
45
41
48
26
33
24
15
10
13
14
11/25
17.7
105
45
52
37
38
26
28
26
24
31
27
14
to
o
12/23
14.0
74
27
26
21
20
16
13
13
10
10
7
14
-J
12/26
14.0
81
32
35
31
27
18
16
14
10
11
9
15
12/31
14.0
90
29
35
36
31
27
20
15
12
11
10
17
-------
TABLE 20
PROFILIS OF pH VALVES
High Flow Periods 11/23/70 tc 3/2 5/71
STAGE NO.
DATE
IMFL
T_
2
3
4
5
6
7
3
o
10
FST
1970
11/23
7.2
7.1
7.2
7.2
7.4
7.4
7.4
7.6
7.6
7.6
7.6
7.5
11/25
-
—
-
—
—
—
—
—
—
—
—
_
11/30
7.5
6.8
6.9
7.1
7.3
7.4
7.5
7.7
7.6
7.6
7.3
7.2
12/3
7.3
6.9
7.0
7.1
7.3
7.4
7.6
7.6
7.6
7.7
7.5
7.3
12/8
7.5
7.0
7.4
7 o 3
7.4
7.5
7.7
7.7
7.7
7.7
7.5
7.5
12/14
7.4
6.9
7.1
7.1
7.2
7.3
7.5
7.5
7.5
7.2
7.2
7.0
12/17
7.2
6.8
7.0
7.2
7.2
7.3
7.3
7.3
-7 -J
' •
7.0
7.0
7. C
12/21
7.7
7.2
7.3
7.5
7.5
7.6
7.8
7 . S
7.8
7.9
7.6
7.5
12/22
7 o 7
7.2
7.3
7.4
7.5
7.6
7.7
7.7
7.7
7.4
7.4
' • ^
12/23
7.7
7.2
7.2
7.3
7.5
7.5
7.6
7.7
7.7
7.5
7.5
7.3
12/29
7 o 5
7.1
7.1
7.2
7.4
7.6
7.7
7.7
7.3
7.6
7.6
7.3
1/4/71
7.6
7.1
7.2
7.2
7.4
7.5
7.5
7.5
7.6
7.6
7.6
7.4
1/7
7.5 .
7.3
7.4
7.4
7.5
7.6
7.6
7.6
7.6
7.5
7.6
7.4
1/11
7.5
7.2
7.3
7.4
7.4
7.4
7.5
7.5
7.5
7.4
7.4
7.4
1/14
7.3
7.1
7.2
7.3
7.3
7.4
7.4
7.4
7.4
7.3
7.3
7.3
1/18
7.4
7.2
7.1
7.4
7.4
7.4
7.5
7.5
7.5
7.5
7.5
7.3
1/21
7.6
7.2
7.2
7.4
7.4
7.4
7.5
7.5
7.6
7.6
7.6
7.4
1/25
7.6
7.2
7.2
7.4
-
7.5
7.6
7.6
7.7
7.7
7.4
7.2
1/28
7.6
7.4
7.3
7.5
7.5
7.5
7.6
7.5
7.6
7.6
7.6
7.4
2/3
7.9
7.2
7.3
7.4
7.3
7.5
7.5
7.6
7.6
7.7
7.7
7.5
2/4
7.4
7.0
7.0
7.3
7.2
7.2
7.3
7.3
7.3
7.4
7.4
7.2
2/11
7.8
7.2
7.0
7.3
7.2
7.4
7.5
7.6
7.5
7.6
7.5
7.4
2/16
7.2
7.0
6.9
7.2
7.2
6.9
7.0
7 . C
7.1
7.1
7.2
7.1
Pags 1 of 2
-------
PROFILZ!S OF pH VALUES
High Flow Periods ii/23/70 tc 2/25/71
STAGE NO.
DATE
INFL
1
2
3
4
5
6
7
8
9
10
FST
2/19
7.1
6.9
6
8
7.0
6.9
6.9
7.3
7.3
7.4
7.4
7.4
7.2
2/22
7.7
7.0
7
0
7.1
7.1
7.1
7.2
7.2
7.2
—
7.2
7.1
2/25
7.4
7.1
7
1
7.3
7.2
7.3
7.5
7.7
7.7
7.7
7.6
7.5
3/1
8.0
7.1
7
1
7.3
7.1
7.3
7.5
7.6
7.7
7.7
7.7
7.4
3/3
7.3
7.2
7
1
7.2
7.1
7.3
7.5
7.4
7.5
7.6
7.5
7.4
3/8
7.6
7.0
7
1
7.3
7.2
7.3
7.5
7.6
7.6
7.7
7.4
7.5
3/11
7.6
7.2
7
1
7.3
7.2
7.4
7.6
7.7
7.7
7.8
7.6
7.5
3/15
7.6
7.2
7
4
7.3
7.2
7.4
7.6
7.7
7.7
7.7
7.5
7.5
3/18
7.5
7.2
7
2
7.4
7.3
7.4
7.6
7.5
7C 6
7.6
7.5
7.5
3/22
7.5
7 o 0
7
1
7.4
7.3
7.4
7.6
7.6
7.6
7 c 6
7.5
7.5
3/25
7.3
7.0
7
2
7.2
7.2
7.3
7.5
7.6
7.6
7.4
7.5
7.3
o
vO
Page 2 of 2
-------
TABLE 21
DATE F.S.T.
1970
11/23
7.5
11/25
-
11/30
7.2
12/3
7.3
12/8
7.5
12/14
7.0
12/17
7.0
12/21
7.5
12/22
7.2
12/28
7.3
12/29
7.3
1971
1/4
7.4
1/7
7.4
1/11
7.4
1/14
7.3
1/18
7 o 3
1/21
7.4
1/25
7.2
1/28
7.4
2/3
7.5
2/4
7.2
2/11
7.4
op*
-U2S
High Flcv:
Periods
11/23/70
to 3/25/7
1
Through T
reatrrient
Subseqve
nt to F.S.
T.
ALGAL
.MIXED
C.-_R30N
COL.
NO.
16 th
MEDIA
1
2
3
4
5
6
STAGE
FILTER
7.5
7.5
7.4
7.4
7.3
7.3
7.3
7.3
7.4
7.4
7.4
7.4
7.4
7.4
7.4.
7.4
7.4
7.4
7.4
7.4
7.4
7.4
7.4
7.4
7.5
7.4
7.5
7.4
7.5
7.5
7.5
7.5
7.3
7.1
7.1
7.1
7.1
7.1
7.1
7.0
7.3
7.1
7.1
7.1
1 T
' •
7.1
7.1
7.1
7.4
OUT
OF
SERVICE
7.5
II
II
It
7.6
•f
t«
It
7.6
(1
n
II
7.5
«
ts
It
7 06
7.5
7.6
7.6
7.6
7.6
7.6
7.6
7.5
7.6
7.4
7.4
7.3
7.3
7.3
7.3
7.5
7.6
7.6
7.5
7.4
7.4
7.4
7 04
7.7
7.8
7.5
7.5
7.5
7 c 5
7.6
7.6
7.7
7.7
7.6
7.6
7.6
7.6
7.6
7.7
7.6
7.7
7.6
7 „7
7.6
7.7
7.5
7.6
7.5
7.5
7.6
7.5
7.6
7.4
7.5
7.5
7.6
7.6
7 „ 6
7.5
7.6
7.6
7.6
7.6
7.2
7.2
7.1
7.1
7.1
7.2
7.2
7.3
7.5
7.5
7.5
".4
-04
7.4
7 c4
P=ge 1 of 2
-------
PROFILES <
CF pH V.-.L
-JES
High Flo
>v Periods
11/23/70
to 3/25/71
Through
Treatment
Subsequent to F.S.T.
DATE
F.S.T.
ALGAL
MIXED
CARBON C
:ol.
NO.
16th
MEDIA
1
2
3
4
5
6
STAGE
FILTER
1971
2/16
7.1
7.1
7.3
7.1
7.0
6.9
6.9
7.1
7.1
2/19
7.2
7.5
7.5
7.4
7.4
7.4
7.4
7.4
7.4
2/22
7.1
7.4
7.5
7.5
7.5
7.5
7c 5
7.4
7.4
2/25
7.5
7.6
7.6
7.5
7.5
7.5
7.5
7.5
7.5
3/1
7.4
7.6
7.6
7.4
7e5
7.3
7.3
7.3
7.4
3/3
7.4
7.2
7.3
7.2
7.0
7.1
~ • -»¦
7.2
7.3
3/8
7.5
7.5
7.4
7.3
7.2
7.3
7 "3
' • o*
7.3
7.3
3/11
7„ 5
7.4
7.5
7.5
7.5
7.5
7.5
7.5
7.4
3/15
7.5
7.6
7.5
7.4
7.4
7.4
7.4
7.4
7.4
3/18
7.5
7.7
7.6
7.4
7.4
7.4
7.4
7.4
7.4
3/22
7.5
7.5
7.5
7.3
7.3
7.4
7.3
7.3
7*3
3/25
7.3
7.0
7.4
7.1
7.1
7 o 1
7.2
7.1
7.1
Page 2 of 2
-------
TABLE 22
PROFILES OF C.O.D. Mg/1
DATE FLCVr INFL
G.P.M.
1970
11/23
17.7
232
11/25
17.7
193
12/3
11.0
362
12/8
11.0
276
12/14
13.0
444
12/17
12.0
197
12/21
13.0
327
12/22
' "> . c>
2S0
12/28
14.0
227
12/29
14.0
211
1/4/71
14.0
233
1/7
14.0
237
1/11
140 0
420
1/14
14.0
292
1/18
14 o 0
300
1/21
14.0
260
1/25
14.0
280
1/28
14. 0
248
2/3
14.0
237
2/4
14.0
233
2/11
14.0
120
to 3/25/71
STAC-E NO.
2 3 4
132 92 72
84 112 40
130 104 72
136 112 68
164 192 164
106 98 95
157 161 150
124 144 136
119 119 88
92 96 84
99 88 77
130 101 93
265 222 140
190 140 140
184 160 160
138 118 94
160 150 152
148 136 116
127 138 Hi
115 103 87
91 122 82
Page 1 of 2
/23/70
1
110
72
100
96
192
169
213
124
131
108
111
107
197
232
160
126
160
144
142
103
91
-------
PROFILES O?
C.C.D. >'g/l
High. Flow Periods
11/23/70 to 3/25/71
DATE
PLOW
INFL
STAGE NO.
G.P.M.
1 2
3
4
1971
2/16
14 o0
348
186 187
168
137
2/19
14 o0
312
152 152
100
67
2/22
14.0
252
193 184
156
97
2/25
14.0
382
286 315
111
63
3/1
14.0
292
172 161
175
140
3/3
14.0
583
272 256
272
217
3/8
14.0
375
163 144
153
101
3/11
14.0
223
140 184
157
88
3/15
14.0
211
169 196
203
150
3/18
14.0
285
124 170
158
106
3/22
14.0
27 3
167 144
106
117
3/25
14.0
220
128 120
150
116
Page 2 of 2
-------
TABLE 23
PROFILES CF C02 ACIDITY Kg/1
High Flow
Period
11/23/70 to
3/25/71
DATE
FLOW
INFL
1
2
3
4
5
6
7
8
9
10
FST
GPM
1970
11/23
170 7
44
70
48
48
50
-
50
-
48
38
28
26
11/25
17.7
46
58
48
40
38
-
40
—
30
30
32
28
11/30
12.0
42
78
72
48
38
-
34
-
24
28
36
26
12/3
11.0
36
74
70
58
44
36
_
26
_
38
22
30
12/8
11.0
38
86
58
61
- .
52
- ¦
34
-
34
38
26
12/14
12. C
40
78
70
46
—
40
34
-
34
38
32
28
12/17
12.0
22
48
30
22
22
—
20
—
20
20
20
14
12/21
13.0
33
58
51
44
35
36
38
34
16
36
52
45
12/22
12.0
37
53
43
46
44
36
34
43
33
45
42
37
12/28
14.C
30
72
46
44
28
32
32
34
34
34
40
32
12/29
14.0
40
44
60
44
40
34
32
34
30
24
32
20
1/4
14o0
34
48
44
38
34
36
_
36
_
26
34
36
1/7
14.0
32
48
42
42
—
32
-
24
—
34
34
26
1/11
14.0
28
48
48
34
-
—
34
-
30
26
28
22
1/14
14o0
28
36
38
40
—
30
-
26
-
38
22
34
1/18
14.0
26
56
58
38
-
48
-
44
-
-
28
44
1/21
14.0
40
50
56
34
—
44
-
32
—
30
32
26
1/25
14.0
27
36
38
36
38
—
26
—
40
40
20
1/28
14.0
22
44
44
34
-
28
-
32
-
36
30
34
2/3
14.0
24
34
44
32
40
32
_
34
30
30
30
2/4
14.0
34
44
-
38
38
34
-
—
40
—
42
42
2/11
14.0
26
34
-
34
42
40
-
—
34
—
36
38
Page 1 of 2
-------
PROFILE OF C02 ACIDITY Mg/1
High
Flow
Period
11/23/7
0 to
3/25/71
DATE
FLOW
INFL
1
2
3
4
5
6
7
8
9
10
FST
GPM
1971
2/16
14.0
30
—
56
38
34
-
—
32
-
40
38
28
2/19
14.0
20
62
—
62
58
52
60
-
-
54
50
52
2/22
14.0
20
48
—
42
34
34
-
34
-
-
40
38
2/25
14.0
40
50
—
36
46
20
-
36
—
-
32
26
3/1
14.0
26
56
—
42
52
46
-
28
—
-
28
30
3/3
14.0
24
36
-
34
-
24
-
14
-
-
14
12
3/8
14.0
36
44
—
32
34
-
36
-
-
38
42
20
3/11
14.0
24
46
-
38
38
—
36
-
—
32
32
28
3/15
14.0
30
34
—
56
58
40
28
30
38
3 5
40
30
3/18
14.0
32
36
—
30
38
34
24
30
34
32
28
30
3/22
14.0
24
38
42
32
42
28
34
30
28
24
24
24
3/25
14.0
29
44
38
44
30
30
42
36
32
22
26
24
Page 2 of 2
-------
TABLE 24
PROFILES OF C02 ACIDITY Mg/1
Through Treatment. Subsequent, to FST
High Flow Periods 11/23/70 to 3/25/71
DATE
F.S.T.
ALGAL
MIXED
CARBON COL.
NO.
16 th
MEDIA
1
2 3
4
5
STAGE
FILTER
1970
11/23
26
20
-
16
-
-
-
11/25
28
20
¦ -
18
-
-
-
11/30
26
14
20
18
-
-
-
12/3
30
18
-
18
- -
-
—
12/8
26
16
-
16
-
—
—
12/14
28
14
-
13
- -
-
—
12/17
14
10
-
14
- -
—
—
12/21
45
25
Out
Of
Service
12/22
37
20
u
II
ii
12/28
32
24
tf
n
u
12/29
20
24
u
u
a
1971
-1/4
ye
22
D
a
a
1/7
26
14
16
16
-
-
—
1/11
22
18
16
18
— —
-
_
1/14
34
22
30
26
- ¦ -
—
—
1/18
44
36
18
20
— -
—
—
1/21
26
20
-
14
— —
—
_
1/25
20
46
24
38
- -
—
—
1/28
34
26
-
26
- -
—
_
6
18
12
14
16
13
13
18
16
18
28
24
16
23
18
Page 1 of 2
-------
PROFILES OF CO2 ACIDITY g/1
Through
Treatment
Subsequent
to FST
High Flov Periods
11/23/70 to
3/25/71
DATE
F.S.T.
ALGAL
MIXED
CARSON COL
16 th
MEDIA
1
2 3
STAGE
FILTER
2/3
30
24
30
2/4
42
30
26
—
— —
2/11
38
24
24
—
_ -
2/16
28
26
26
24
_ -
2/19
52
48
76
70
— —
2/22
38
22
—
22
— —
2/25
26
16
24
-
- -
3/L
30
18
16
18
_
3/3
12
12
10
10
— -
3/8
20
16
16
—
— —
3/11
28
20
16
—
— —
3/15
30
20
16
—
_ —
3/18
30
18
10
12
— —
3/22
24
12
14
12
— —
3/25
24
18
16
14
— —
Page 2 of 2
-------
TABLE 25
PROFILES OF BICARBONATE ALKALINITY mg/1
High Flow Periods 11/23/70 to 3/25/71
Flow
DATE
GPM
Infl.
1
2
3
4
5
6
7
8
9
10
F.S.T.
1970
11/23
17 .7
23 .4
23.4
23 .4
23.6
23.6
-
22.6
-
218
206
202
172
11/25
17.7
214
230
248
242
254
-
222
-
238
222
224
184
11/30
12.0
250
226
230
220
220
—
220
—
204
202
184
164
12/3
11.0
242
234
234
238
238
234
—.
232
_
218
192
174
12/S
11.0
242
232
232
226
-
232
-
228
-
204
184
152
12/14
13 .0
236
232
226
228
-
230
232
-
228
184
170
158
12/17
12.0
106
100
104
106
98
-
98
-
86
72
76
76
12/21
13.0
223
223
213
215
222
233
216
224
218
210
202
194
12/22
12 .0
192
208
200
212
208
212
211
210
210
192
171
178
12/28
14.0
206
184
188
194
190
170
196
194
188
176
176
178
12/29
*9 71
14.0
184
180
188
182
184
180
182
178
174
162
170
172
1/4
14.0
232
212
212
222
226
222
-
218
208
202
194
1/7
14 .0
236
218
224
232
-
222
-
248
-
204
208
188
1/11
14.0
248
234
232
244
-
-
244
-
236
232
238
220
1/14
14 .0
222
224
222
230
-
230
-
224
-
232
224
232
1/18
14 .0
236
240
238
244
-
238
-
242
-
-
230
234
1/21
14.0
228
220
226
222
-
216
-
224
-
220
218
224
1/25
14 .0
202
194
19P
156
-
198
-
19 6
-
204
186
188
1/28
14.0
226
222
220
214
—
236
—
212
—
220
206
196
2/3
14.0
234
208
222
218
210
218
—
216
—
218
220
208
2/4
14 .0
252
242
-
246
254
258
-
-
236
-
224
230
2/11
14.0
232
208
-
206
208
208
-
-
212
-
200
210
2/16
14 .0
260
-
250
244
242
-
-
248
-
246
236
222
2/19
14 .0
260
210
-
218
218
210
230
-
-
232
214
202
2/22
14 .0
250
222
-
218
228
218
-
216
-
-
206
228
2/25
14.0
218
232
—
232
232
238
—
232
—
-
230
210
Page 1 of 2
-------
PROFILES OF BICARBONATE ALKALINITY (Continued)
DATE
Flow
GPM
3/1/7114.0
3/3
3/8
3/11
m
3/22
3/25
14.0
14.0
14 .0
14.0
14.0
14.0
14 .0
Infl.
10
F.S.
274
256
- 262
256
258
-
248
—
-
236
230
-
242
- 222
-
220
-
210
-
-
202
184
240
226
- 230
230
-
216
-
-
234
206
144
208
197
- 206
210
-
220
-
-
202
200
184
232
228
- 234
232
240
232
234
240
220
218
220
244
232
- 250
234
240
232
244
240
228
236
219
240
241
- 226
238
240
232
226
228
216
204
205
248
247
- 248
256
258
262
252
252
224
222
221
Page 2 of 2
-------
TABLE
26.
PROFILES OF BICARBONATE ALKALINITY mg/1
Through Treatment Subsequent to F.S.T.
High Flow Period 11/23/70 to 3/25/71
o
DATE
1970
11/23
11/25
11/30
12/3
12/8
tsj 12/14
m 12/17
12/21
12/22
12/28
12/29
1/4
1/7
1/11
1/14
1/18
1/21
1/25
1/28
2/3
2/4
2/11
2/16
2/19
*> /"3">
F.S.T.
Algal
Mixed
16th
Media
Carbon
Col. No.
Stage
Filter
1
2
3
4
5
6
172
118
120
_
120
184
136
132
-
-
-
-
- ¦
134
164
114
116
118
-
-
-
122
174
100
—
106
_
_
104
152
104
-
98
-
-
-
—
94
158
92
-
68
-
-
-
-
72
76
52
-
66
-
-
—
-
86
194
128
—
—
—
_
—
_
178
125
-
—
—
—
—
—
178
140
-
—
-
-
-
-
—
172
150
-
-
-
-
-
-
-
194
146
188
152
140
140
-
—
-
—
1'38
220
200
204
200
-
—
—
—
160
232
218
236
220
-
-
-
-
200
234
210
218
208
-
-
-
-
202
224
194
-
194
-
—
-
—
188
188
170
174
200
-
-
-
—
152
196
174
—
178
—
-
-
•
146
208
168
—
178
172
230
176
163
—
-
-
-
-
182
210
142
120
—
-
-
-
-
146
222
212
192
200
-
-
-
-
192
202
146
164
170
—
—
-
—
142
228
166
178
—
-
-
-
-
170
144
-------
PROFILES OF BICAR30NATE ALKALINITY (Continued)
DATE
F.S.T.
Algal
16th
Mixed
Media
1971
Stage
Filter
1
2
3
4
5
6
3/1
230
176
170
174
—
—
—
170
3/3
184
106
106
106
-
-
-
—
104
3/8
144
134
128
-
-
-
-
-
126
3/11
184
116
120
-
-
-
-
—
132
3/15
220
142
146
-
-
-
-
-
142
3/18
219
152
146
148
-
-
-
-
150
3/22
205
128
132
132
-
-
-
-
126
3/25
221
134
128
124
-
-
-
-
124
Page 2 of 2
-------
TABLE PROFILES OF NITRATES mg/1
27
Through treatment subsequent to F.S.T.
High Flow Periods 11/23/70 to 3/25/71
DATE
F.S.T.
Algal
Mixed
16th
Media
Carbon Col. No.
1970
Stage
Filter
1
2 3 4
5
6
11/23
1.0
6.2
7.4
8.0
7.0
11/25
0.8
6.4
7.2
7.0
4.2
11/30
0.8
8.4
8.3
7.0
5.4
12/3
3.0
11.6
13 .5
11.8
11.7
12/8
2.9
11.2
12 .2
14.7
14.4
12/14
4.8
9.0
9.0
11.4
13.7
12/17
2.1
6.8
11.1
9.1
5.8
12/21
0.0
6.4
12/22
-
4.7
12/28
2.7
4.9
12/29
2.2
5.4
1/4
1.0
4.3
1/7
0.4
4.8
3.7
3.7
3.7
-
3.3
1/11
0.0
.6
0
0
0
1/14
0.0
.4
.6
0
0
1/18
. 2
* 8
.8
0
1/21
.2
1.5
2.0
0.5
0.2
1/25
.2
2.6
3.6
2.2
0.0
1/28
.5
4.0
3.8
3.0
0.7
2/3
7.8
6.8
7.2
7.7
4.9
2/4
5.0
4.3
5.1
3.5
1.0
2/11
-
14.0
14 .7
14 .6
12.1
2/16
5.8
10 .3
11.6
9.1
- - -
—
6.4
2/19
2.6
6.4
6.9
6.3
- - -
-
5.3
7/22
2.9
8.8
8.2
7 .0
•— — —
-
6.7
rt
-------
PROFILES OF NITRATES (Continued)
DATE
F.S.T.
Algal
Mixed
16th
Media
Carbon Col. No.
Stage
Filter
1
2
3 4
5
6
3/1
6.4
8.4
10.4
10.6
—
- —
-
8.4
3/3
6.1
16.1
17 .0
17.4
-
- -
—
8.4
3/8
4.2
13.2
13.2
12.6
-
-
-
14.1
3/11
6.4
13.8
13.6
13.4
-
-
-
9.3
3/15
2.3
7.0
8.8
8.8
-
- -
-
6.5
3/18
1.0
3.6
8.8
7.2
-
-
-
8.2
3/22
8.0
13.8
12.9
12.0
-
-
-"
11.8
3/25
9.4
13.4
12 .0
15.2
-
- -
-
11.2
Page 2 of 2
-------
TABLE 28 PROFILES OF NITRATES rng/1
High Flow Periods 11/23/70 to 3/25/71
Date
Flow
Staae
No.
GPM
Infl.
1
2
3
4
5
6
7
8
9
10
F.S.T
1971
11/23
17.7
-
-
-
.1
.1
.1
.2
1.0
1.9
1.9
2.0
1.0
11/25
17.7
-
-
-
-
0
.1
.5
.5
1.0
1.4
1.5
0.8
11/30
12.0
-
—
-
-
0
.2
.2
.5
1.4
1.4
3.2
0.8
12/3
11.0
-
-
—
—
0
0
0
.1
1.2
1.8
7.1
3.0
12/8
11.0
-
-
-
-
0
0
.2
.8
.8
1.8
5.0
2.8
12/14
13.0
-
-
-
0
0
-2
.2
.5
1.6
4.8
4.2
4.8
12/17
12 .0
-
-
-
-
-
-
1.5
2.1
3.0
3.1
3.9
2.1
12/21
13.0
-
-
-
-
0
0
0
0
.5
.5
2.6
0
12/22
12.0
-
-
-
-
-
0
0
0
.8
3.6
4.2
—
12/28
14.0
-
-
-
0
0
.6
.4
.4
1.0
2.6
2.6
2.7
12/29
14.0
-
-
-
0
0
.2
.5
.6
1.1
2.2
2.3
2.2
1971
1/4
14.0
-
-
-
-
0
0
0
0
.5
1.2
1.0
1.0
1/7
14 .0
-
-
-
-
-
-
0
0
0
.8
.6
.4
1/11
14.0
-
-
-
-
—
—
0
0
0
.8
.6
0
1/X4
14.0
-
-
-
-
-
-
-
0
0
0
0
0
1/18
14 .0
-
-
-
-
-
-
-
0
0
0
.3
.2
1/21
14.0
-
-
-
-
-
-
-
0
0
0
.5
.2
1/25
14 .0
-
-
-
-
-
-
-
0
0
.1
1.6
.2
1/28
14 .0
—
—
—
—
—
—
—
0
.2
.2
1.3
.5
2/3
14 .0
6.4
18.9
4.3
12.0
12 .2
10.4
—
—
—
9.0
11.0
7.8
2/4
14 .0
2.1
8.2
2.4
5.8
4.4
4.0
-
4.1
-
4.3
5.7
5.0
2/11
14 .0
13.2
20.8
11.2
15.6
17 .1
16.7
-
14.1
-
14 .6
14.7
-
2/16
14 .0
-
5.8
-
5.3
4.9
-
-
-
-
5.2
7.8
5.8
2/19
14.0
-
-
-
-
2.0
-
-
-
-
2.6
3.7
2.6
2/22
14.0
-
-
2.4
2.7
-
-
2 . 8
2.0
-
3.1
2.9
2/25
14 .0
-
1.4
-
0.4
0.5
-
-
-
.5
-
2 .0
2.4
Paga 1 of 2
-------
PROFILES OF NITRATES (Continued)
Flow
Stage No
•
DATE
GPM
Infl. 1
2
3
4
5
6
7
8
9
10
F.S.T.
3/1
14.0
9.0 7.0
4.9
4.9
5.1
_
4.9
7.1
6.4
3/3
14.0
-
-
-
2.8
-
-
-
6.8
-
7.6
6.1
3/8
14.0
.3 .3
.2
. 2
.4
-
-
-
-
1.6
3.0
4.2
3/11
14 .0
.1 3.2
-
2.6
1.7
-
-
-
-
3.1
3.2
6.4
3/15
14.0
-
-
-
2.2
1.0
1.0
1.7
2.1
4.0
2.3
3/18
14.0
4.0
.2
1.9
2.4
.6
1.0
.5
.6
1.4
1.4
1.0
3/22
14 .0
- -
6.6
2.6
2.3
2.2
2.0
2.2
2.8
5.2
6.6
8.0
3/25
14 .0
—
11.6
4.4
8.0
6.8
5.9
5.0
8.0
6.4
8.0
9.4
Ni tra tes
were added to infl. during Feb
i. and
March
'71- .
The
time
elapsed
between
sampling
and analysis was
sufficiently
high
to have
effe cted
a reduction i
n most
of the values in the upper stages of treatment.
Page 2 of 2
-------
APPENDIX B
Consultant Report on Algal Aspects of Process
December 1969
This constitutes a brief summation, for record purposes* of
the observations and findings made as a result of a site
visit December 11-12, 1969. These findings, together with
suggestions for certain modifications which would improve
the algal growth section of the experimental pilot plant,
have already been presented orally to Mr« Torpey and Dr.
Heukelekian. This presentation was made as a part of the
conference which immediately followed ray examination of
the research unit near the Kennedy Airport. At that time
a brief official report was also made (over the telephone)
to Dr. Joel Kaplovsky, chairman. Department of Environmental
Sciences, Rutgers University.
Further, this report will concern itself with the results of
the microscopic examination of a series of samples collected
from representative points along the line of flow of this
experimental waste treatment plant. Por the purpose of
establishing a permanent record of the findings, 72 photo-
micrographs have been prepared showing the important
organisms and the characteristic microscopic appearance of
the slimes or other growths which typified each section of
the treatment unit. These results have not been reported
previously since it was necessary to carry the samples back
to Minneapolis for the detailed microscopic study and for
photomicrographic work. The fully labeled photomicrographs
which accompany this report are in themselves an official
record and constitute a visual means for the characteriza-
tion of the microscopic details of the biological ecosystem
which has been developed in the rotating disc waste-treatment
procedure.
At the time of the site visit, December 12, each stage of the
experimental, rotating disc waste-treatment plant was examined
carefully together with all chemical and physical data which
were available at that time. Illuminated as well aB non-
illuminated unit stages were observed and light readings
were taken to determine the quality as well as intensity of
the incident light being applied to the algal
227
-------
section,,* The incoming untreated waste and the effluents
from various units were examined to note improvements in
the clarity of the treated waste as it progressed through
the experimental plante
The first ten units have been set aside to deal with that
phase of the treatment which is carried out by organisms
other than algae. The subsequent units, intended to
carry treatment further by promoting an algal growth which
can remove nitrogen and phosphorus, are illuminated. All
were examined on a comparative basis to see if changes
could be made to encourage greater algal growth in the
illuminated section,,
The overall impression, as one views the Rutgers rotating
disc experimental waste-treatment unit is that the biological
life which has developed closely parallels that seen in a
small heavily polluted creek or brook when the organic wastes
added have a point source, and there is only one sewer outlet0
By microscopic examination one can follow the improvement of
the water step by step as sucessive groups of organisms
"work over" the material. I believe that the process has
great potential, in terms of nitrogen and phosphorus removal
as well as in the reduction of carbonaceous matter. This
should readily be apparent if the algal growth can be stepped
up in the illuminated section.
Appreciable growths of filamentous green algae and diatoms
were already apparent in sections which were illuminated
and they were especially extensive where extra spot lights
had been installed to increase illumination,. If these areas
of intensive growth could become general throughout the
illuminated units and if the surface areas within these units
were increased to an equivalence with that of the carbonaceous
treatment section one could expect a very effective and
satisfactory reduction of nitrogen and phosphorus in the final
effluent. At the present time one of the difficulties is
that the illuminated units are not receiving enough light.
Also it might be advisable to change the quality of the light
* Quality was measured with a Harrison color temperature
meter which provides a color-temperature reading in
degrees Kelvin.
228
-------
by trying other types of illumination,, In nature and in
my own laboratory experiments, periphyton has made good
growth at light levels of approximately 1000 foot candles
and at a color temperature of approximately 3400 degrees
Kelvino In the laboratory this has been on the basis of
constant illumination at a fixed distance from the growth
surfacee
In the Rutgers Experimental Unit, modified discs rotate
slowly under an overhead canopy of light and the intensity
of illumination at any given time will depend on the sector
of rotation which has been reached by that part of the
surface<> Since microseconds of light exposure will suffice
for photosynthetic purposes such rotation is effective
because all portions will eventually be exposed but the
maximum effectiveness is not achieved because rotation is
too slow. On the basis of the study made it seems advisable
to increase the incident illumination to 1000 or 2000 foot
candles and to place the fluorescent tubes between the discs
(just above the axle) where better efficiency can be achieved.
To achieve this# the modified tapered discs now employed
should be replaced by straight sides discs like those in the
1st ten units. These discs should be spaced just far enough
apart to clear the light tubes when the latter are moved
down from the canopy where they now are installed. The
material used for the discs in the algal unit could also be
improved. This point was discussed in detail with Mr. Torpey
and Dr. Heukelekian on December 12th and several alternative
materials were agreed upon as likely media for effective
surface growths of algae.
If the treatment method is to be employed in a practical way
the discs of each drum must be "harvested" at certain inter-
vals to keep the biological ecosystem functioning at its
maximum efficiency. If this is not done the buildup of
organisms will produce thick films which cannot be penetrated
effectively by oxygen or which cannot give off gases which
need to be voided. A simple design for a knife-type scraper
which could be employed to strip the growth off each disc
while it continues to rotate was proposed to the investigators
so that the results from this experimental plant might be
more comparable to an eventual full scale installation with
a mechanized film removal device.
229
-------
The laboratory work associated with this consultation report
included a detailed microscopic examination of samples
collected at selected points along the rotating disc unito
The selection was based on a preliminary microscopic examina-
tion made at the plant and the data presented by Mr. Torpey
and his associates0 Samples were examined within 16 hours
of collection, while still fresh. When the typical biological
forms had been identified, a series of photomicrographs were
taken in color to record the findings.
In keeping with the original agreement these photomicrographs
are included with this report so that they may be used for
reference and for ultimate presentation of a report.
-------
APPENDIX C
MACHINE DRAWINGS
231
-------
18.0
ini'. irr »•,/.
»N (Ti'l
. OlA. 4-MffvR*.
g MC« OF IT".* 3, v.
**» ^
LfL .1
' -»K .1 f— e.5 (rrs)
Lj. y-?rO-
*1 r.
«,h
{ry<0 I
A. .
J .7
S O 'cot. owr
• —•'•TsTrj.rMi
40
4.0
|» 4 lit **0,
#*!.«. , »» *4
10 S Ni.r<«o
232
-------
<11 »?*. ' ty.c tc,_§i;£rT
ill ca. l.UM » «,OA.T_< icf
y I'Aii.'i
-------
-------
3) »«*•*<
t
V"~v
—o
VT,:.a ,,,<
,i3_?0O 1'
235
-------
236
-------
237
-------
APPENDIX D
Literature Cited
1* Frankland, E. First Report# British Rivers Pollution
Commission 1868, Cited by Waring (20)e
2. Allen, K0 "The Biologic Wheel." Sewage Disposal
Bulletin. Citv of New York. 14c 1929.
3. Hutchinson, G„ D. and R. Baumann. "Variation of Sewage
Flow in a College Town." Sew. Ind. Wastes 301 157.
1958.
4* Duttweiler, D. W0 and L. T. Purcell. "Character and
Quantity of Wastewater from Small Populations." Journ.
Wat. Pollut. Contr. Fed. 3jl»63. 1962.
5« Hubbel, J« W. "Commercial and Institutional Wastewater
Loading0" Journ. Wat. Pollut. Contr. Fed. Us 962. 1962.
6. Ferguson, K. G. "Variations in Municipal Sewage Flow and
Water Consumption in Washington State Cities." Journ.
San. Enana. Div„. Proc. Am. Soc. Civn Enars- 88»SA5.
19. 1962.
7, Knowles, Gc "Mathematical Models as an Aid in the
Solution of Water Pollution Control Problems®" Chem.
& Ind. Nfi„ 22*697 1970.
8* Blackwell, L. G. "A Theoretical and Experimental
Evaluation of the Activated Sludge Process." Ph.Do
Thesis. Clemson Univ. 1971.
9. Grady, C. P. L. "A Theoretical Study of Activated
Sludge Transient Response." Presented at the 26th.
Purdue Ind. Waste Conf. 1971.
10. Storer, F. and A. F. Gaudy, Jr. "Computational Analysi®
of Transient Response to Quantitative Shock Loadings of
Heterogeneous Populations in Continuous Culture."
Envir. Technol. 1:143. 1969,
239
-------
11* Smith, R. and R. G. Eilers. "Simulation of the Time-
Dependent Performance of the Activated Sludge Process
Using the Digital Computer," U0S„D.I. F0W.Q.A.
Advanced Waste Treatment Branch# Division of Research*
Cincinnati# Ohio» 1970.
12* Andrews# J«F. and S.P. Graef. "Dynamic Modeling and
Simulation of the Anaerobic Digestion Process." Am.
Chem. Soc. Adv. in Chema Ser. 105:126. 19710
13. Thomann, R. V. "Variability of Waste Treatment Plant
Performance." Journ. S*n. Enang. Div.. Proc. Am. Soc.
Civ. Enqrs. 2£iSA3. 819 1970.
14. Bungay# H. R. Ill and J. F0 Andrews. "Dynamics of
Microbial ProcessesWat« Sew* Wks. 117:77» 1970.
15. Graef# S. P. "Dynamics and Control Strategies for the
Anaerobic Digester." Ph.D. Thesis. Clemson Univ.
1972.
16. __________ Deuteronomy 23# xi-xiv.
17. Burr, W. H. Ancient and Modern Engineering and the
Isthmanian Cnnal. 1st Edn. New YorktJohn Wiley and
Sons. 29« 1902.
18. ___________ "Purification of Water and Sewage."
Special Report of the Massachusetts State Board of
Health. 1880o
19. Chase# S. E„ "Trickling Filters — Past Present and
Future." Sew. Wks. Journ0 17:929. 19450
20. Waring# G. E. Modern Methods of Sewage Disposal.
New York:D. Van Nostrand Co. 1896„
21. Schaetzle# T. C. "Operation of Trickling Filters."
geV« Wfr8« JPUEfl* 17:602o 1945.
22. Sewage Treatment Plant Design. A.S.C.E.
Manual of Engineering Practice. No. 36. New Yorki
American Society of Civil Engineers. 155. 1959.
240
-------
23. Jenks, H. N. "Experimental Study of Biofiltration"
Sew. Wks. Jourrin 8:888. 1936«
24. Venable, W. M. Methods and Devices for Bacterial
Treatment of Sewage. New York:John Wiley and Sons.
1908.
25. Isaac, P.C0G. Public Health Engineering,, London:E.
and F. N0 Spon Ltd. 144. 1953.
26. Levine, M., Luebbers, R., Galligan, W. E. and R. Vaughn.
"Observations on Ceramic Filter Media and High Rates
of Filtration." Sew. Wks. Journ. 8:701 1936
27. Bryan, S. H. "Molded Polystyrene Media for Trickling
FilterSo" Proc. 10th Purdue Ind. Waste Conf. 164.
1955c
28. Egan, J. T. and M0 Sandlin. "The Evaluation of Plastic
Trickling Filter Media." Proc« 15th Purdue Ind. Waste
Conf. 107. 1960.
29. Porter, J. A. and P. H« Dutch. "Phenol-Cyanide Removal
in Plastic-Packed Trickling Filter." Journ. Wat. Pollute
Contr. Fed. 12:622. 1960.
30. Dunbar, W. Pa Guidlines to the Question of Wastewater
Clarification. Munich:R. Oldenbourg0 1954. Cited
by Hartmann (31).
31* Hartmann, H. "Untersuchung uber die Biologische
Reinigung von Abwasser mit Hilfe von Tauchtropfkorperan-
lagen (Investigation of the Biological Clarification of
Wastewater Using Immersion Drip Filters)." Band 9 der
Stuttgarter Berichte zur Siedlungswasserwirtschaft
Kommissionsverlag. Munich:R0 Oldenbourg. I960.
32. Inihoff, F. "Bio-Immersion Filters." Technical Com-
munity Papers. 22sNo* *3* 1926. Cited by Hartmann
(31).
33* Buswell, M0 and E. L. Pearson0 "The Nidus Rack. A
Modern Development of the Travis Colloider." Sew..
Ijfcfi.. jZfliiia. 1:187. 1929.
241
-------
34* Clarkt H. W. "Past and Present Developments in Sewage
Disposal and Purification." Sew. Wks. Journ. 2:5610
1930.
35« Steel, F. W. "Bio-Flocculation and Contact Aeration.
A Report of Experimental Development at Two Texas Plantso
Water Works and Sewerage 85,:158. 1938.
36. Stroganow, and Basjakina. "Clarification Experiments
with Air Filters." Moscow Community Economy. Section
I* Part 4, 1923. Cited by Hartmann (31).
37. Bach, H. "Das Emscherfilter, eine neue Form des
Biologischen K&rpers fur die Abwasserreinigung (The
Emscher Filter, a Form of Filter for the Clarification
of Wastewater)." Wasser und Gas. 16:373. 1926.
38. Weigand, Ph. "Verfahren zur Biologischen Reinigung
von Abwassern (A Process for the Bio-Clarification of
Wastewater)." German Patent No. 135755» 1900.
39. Bach, Ho Die Abwasserreinigung (Wastewater Clarification)
Munich:R0 Oldenbourg. 1470 1934.
40. Bach, h. Grm^iagep wfl vgrffrhren fley nemseiUiichen
Abwasserreinigung (Basic Rules and Procedures of Modern
Wastewater Treatment). Leipzig:Academic Publishers.
288. 1936. Cited by Hartmann (31).
41* Sierp, "Die Biologische und Chemische Abwasserreinigung
mit Hilfe von Luft (Biological and Chemical Wastewater
Clarification with the Aid of Air)." Prussian Dept. of
Water. Soil, and Air Hvgene. 1927• Cited by Hartmann
(31) o
42. Schmitt, "Die Ausbildung der Frischwasserrinne und der
Einbau von Tauchkorpern in mechanische Kl&ranlagen
(The Development of Fresh Water by Means of and the
Installation of Immersion Filters in Mechanical Clari-
fication Plants)." Gesundheits j.ngenieur. 40o 1930.
Cited by Hartmann (31).
43. Bevan, J. G« "Sewage Treatment." United States Patent
No. 2559704. 1951.
242
-------
44. Doman, J. "Results of Operation o£ Experimental
Contact Filter with Partially Submerged Rotating
Plates,," Sew. Wks. Journ. Jj555o 1929.
45. Hartmann, H. "Improvements in or Relating to Sewage
Plant." British Patent No. 935162„ 1963.
46. Hartmann, H. "Der Tauchtropfkorper (The Dipping
Contact Filter)." Oesterreichische Wasserwirtschaft
11/12*264. 1965.
47. Popel, F. "Leistung, Berechnung und Gestaltung von
Tauchtropfkorperanlagen (Estimating# Construction and
Output of Immersion Drip Filter Plants)." Band 11
der Stuttgarter Berichte zur Siedlungwasserwirtschaft
Kommissionsverlag. Munich:R. Oldenbourg. 1964.
48. Stengelin, J. C. "Sewage Clarifying Plant", British
Patent 940861. 1963.
49. Gulevich, G0 "The Role of Diffusion in Biological
Waste Treatment." Ph.D. Thesis. Johns Hopkins UnivG
1967.
50• Bringmann, G. and R. Kuhn. "Biologischer Abbau von
Mineralolprodukten im Scheibentauchkorper-Verfahren
(Decomposition of Mineral Oil Products with Rotating
Disc Filters)•" Gesundheitsinginieur. 78:179. 1968.
51. Hemens, J. "Biological Systems for the Removal of
Nitrogen and Phosphorous from Sewage Effluents.*
Water Research 2;99. 1968.
52* Welch, F. M. "Preliminary Results of a New Approach
in the Aerobic Biological Treatment of Highly Concen-
trated Wastes." Proc. 23rd Purdue Ind. Waste Conf„
428. 1968.
53. Welch, F. M. "New Approach to Aerobic Treatment of
Wastes." Water and Wastes Engng. 6«No 7. D 12. 1969.
243
-------
54. Welch, F. M. "Potential Use of the BIO-DISC Process
in Treating Waste Water from the Canning Industry."
Presented at the Conf. on Treatment and Disposal of
Wastes from Vegetable Processing. 1970.
55• Antonie, Rc Lc and F. M. Welch. "Preliminary Results
of a Novel Biological Process for Treating Dairy
Wastes." Proc. 24th Purdue Ind. Wa3te Conf- 115. 1969.
56. Antonie, R. L. "Response of the BIO-DISC Process to
Fluctuating Wastewater Flows." Proc. 25th Purdue Ind„
Waste Conf. 427. 1970.
57. Antonie, R„ L. "Application of the BIO-DISC Process
to Treatment of Domestic Wastewater." Presented at
the 43rd An. Conf. Wat. Pollut. Contr. Fed. 1970.
58• Antonie# R„ L, and K. Van AAcken. "Rotating Discs
Fulfill Dual Wastewater Role." Water and Wastes Enana.
8:NOo 1. 37. 1971.
59. Birk, C. W. and R„ J0 Hynek. "Treatment of Cheese
Processing Wastes by the BIO-DISC Process." Proc.
Purdue In£. Wafiifi. Conf. 1971.
60« ___________ "Municipal Sewage Treatment with a Rotating
Biological Contactor." Allis-Chalmers Report to the
Federal Water Pollution Control Administration Department
of the Interiore Contract No. 14-12-24 Modification
No. 2. May 1969.
61® Joostp R. Ho "Systemation in Using the Rotating Bio-
logical Surface Waste Treatment Process." Proc. 24th
Purdue Ind. Waste Conf. 365* 1969.
62. Reinish, P. "Der Tauchtropfkorper (The Dipping Contract
Filter)." Ost. Rdsch. 15:10. 1969.
63* Aluko, T. M. "The Use of the Disk Filter for the Aerobic
and Anaerobic Treatment of Milk WastesM.Sc. Thesis*
Univ. Newcastle Upon Tyne, U.K. 1970o
244
-------
64* Burnt, R. J., and Cochrane, M. W. and K. A. Dostal.
"Cannery Waste Treatment with the R.B.C. and Extended
Aeration Pilot Plants*." Presented at the 2nd National
Food Wastes Symposium. Denver, Colo0 March 197lc
65. Chittenden, J, A. and W„ J. Wells* "Rotating Biological
Contactors Following Anaerobic Lagoons." Journ. Wat.
Pollut. Contfc Fed. 43:746. 1971.
66. Stealy, R. F. "Miniature Sewer Plant Operates in Tucker
Co." Parkersburg Sentinel. Parkersburg WQ Va. 1971.
67. Ziemba, J. V. "Reduces BOD 99% ... At Low Cost." Food
Engncr. 43: No. 6 66. 1971e
68. _________ "Unique Sewer System to Open." The Reporter
Dispatch. White Plains. Mon. June 14, 1971.
69. Pretorius, W. A. "Some Operating Characteristics of a
Bacterial Disc Unit." Water Research 5;1141. 1971.
70. Stengelin, J. C. "Immersion Trickling Filter for Bio-
logical Sewage Purification." German Patent 1,815,001
(June 25, 1970); Chem. Abs. 73:48388. 1970.
71« Welch, F. Me "Rotating Biological Contactor in Sewer."
U.S. Patent 3,484,836, (Dec0 16, 1969); Chem. Abs.
7^:58877
72. Torpey, W« N„ "Biological Treatment of Wastewater®"
German Patent 1,961,201 (June 18, 1970); Chem. Abs.
21:91062o 1970.
73. Pescod, M. B. Photograph. AsjLap jlnpt. Technol.
Newsletter. £s5. 1970. and Personal Communication,
June 1971.
74. Pescod, M. B. and J. V» Nair. "Biological Disc
Filtration for Tropical Waste Treatment: Experimental
Studiese" In Press. To be Published in Water Research-
1972.
75. Nair, J« V. "Biological Disc Filters for Tropical Waste
Treatmento" M.S. Thesis. Asian Inst. Technol. Bangkok*
1971,
245
-------
76. Monod, J. "La Techniques de Culture Continue* Theorie
et Applications," Annals Inst. Pasteur 79:390, 1950.
77. Monod* J. "The Growth of Bacterial Cultures." Ann.
Rev. Microbiol. 3:371. 1949.
78. Herbert, D. R., Elsworth, Re and R. C0 Telling. "The
Continuous Cultivation of Bacteria, a Theoretical and
Experimental Study." Journ. Gen. Microbiol. 14:601.
1956.
79. Herbert, 0. fi. Recent Progress in Microbiology.
Stockholmi Alonquist and WiksellSo Tunevall, G.
(Editor). 381. 1959.
80o Powell, E. 0. "The Growth Rate of Microorganisms as
a Function of Substrate Concentration" in Microbiology
and Continuous Culture. London:H.M.S.O. 34. 1967.
81. Humphrey, H. E. and S„ Koga. "Study of the Dynamic
Behavior of the Chemostat System." Biotechnol. and
Bioengng. 9:375. 1967c
82. Fuld, G. J., Mateles, R« 1. and Bo W0 Kusmierek. "A
Method for the Study of the Dynamics of Continuous
Fermentation." S.C.I. Monograph No. 12. New Yorki
The Macmillan Coc 1961„
83« Gilley, J0 W. and H0 R» Bungay III. "Oscillatory Growth
Rate Responses of S. cervisiae in Continuous Culture./'
PA9teghngJ-» and Bioengng. 9:617. 1967.
84. Mateles, R. I., Ryu, D, Y. and T. Yasuda. "Measurement
of Unsteady State Growth Rates of Microorganisms."
Nature 208;263. 1965.
85a Aiba, S.# Nagai, S., Endo, I. and Ye Nishizawa. "A
Dynamic Analysis of Microbial Growth." Am. Inst. Chenu
Eng. Journe AS.:624. 1969.
860 Young, T# B. "A Dynamic Analysis of Microbial Growth
in a Chemostat Continuous Culture." E>h.D. Thesis..
Clemson Univ. 1971.
246
-------
87. Blackwell, L. G. and H. R. Bungay IIIo "Dynamics
of Biosorption and Substrate Utilization in the
Activated Sludge Contact Stabilization Process.M
Presented at the 69th Nate Meet. Am. Insto Cherru
Engrs. 1971.
880 Tomlinson, T. G. and D.H.M. Snaddon0 "Biological
Oxidation of Sewage by Films of Microorganisms."
Int. Journ. Air and Wat. Pollut. ifi.5865<> 1966.
89. Kornegay, B. He "The Characteristics and Kinetics of
Fixed-Film Biological Reactors." Ph.D. Thesis.
Clemson Univ. 1969e
90o Hoehn, R„ C. "The Effects of Thickness on the Structure
and Metabolism of Bacterial Films,," PhnD« Thesis.
Univ. Missouri (Columbia)* 19700
91. Atkinson, B., Swilley, E0 L., Busch, A. W0 and De A„
Williams* "Kinetics, Mass Transfer, and Organism
Growth in a Biological Film Reactor." Trams. Instn.
Cftepu Enarsn 45;T257n 1967.
92e Atkinson, B., Busch, A. W. and G. S. Dawkins.
"Recirculation, Reaction Kinetics, and Effluent Quality
in a Trickling Filter Flow Model." Journ. Wat. Pollut.
Contr. Fed. 1307. 1963*
93. Behn, V. C. and P0 Monadjemio "Developments in Bio-
logical Filtration." in Gloyna and Eckenfelder (94).
204. 1968.
94. Gloyna, Ee F. and W. W. Eckenfelder0 (editors).
Advances in Water Quality Improvement. 1. AustintUniv.
Texas Press. 1968.
95. _____National Research Council Subcommittee
Report, "Sewage Treatment at Military Installations."
Sew. Wks. Journ. 18.:969. 19460
96. Galler, W. So and H. B. Gotaas. "Analysis of Biological
Filter Variables." Journ. San. Engnq. Div.. &fl. Soci.
Civ. Engrs» 20.* 59. SA6. 1964.
247
-------
97. Lamb, R. and S. G. H. 0weno "A Suggested Formula for
the Process of Biological Filtration." Wat. Pollut. Contr.
£2.: 209. 1970.
98» Swilley, E. L. and B. Atkinson6 "A Mathematical Model
for the Trickling Filter." Proc. 18th Purdue Ind. Waste
Conf. 706. 1963o
99. Swilley, E. L., Atkinson, B. and A. W. Busch. "Trans-
port Phenomena and Rate Control in Trickling Filter
Flow Models." Progress Report on NSF Research Grant
GP-998. Lab. of Environmental Science and Engineering#
Vftne M. Rice Univ., Houston, Texas0 1965.
100. Atkinson, B. and I. S„ Daoud. "The Analogy Between
Microbiological "Reactions" and Heterogeneous Catalysis."
Trans. Instn. Chem. Engrs. 4£:T19. 1968.
101. Atkinson, B., Daoud, I0 S. and D. A. Williams. "A
Theory for the Biological Film Reactor." Trans. Instn.
Chem. Engrs. 46:T245. 1968.
102. Atkinson, B. and I, S. Daoud. "Diffusion Effects Within
Microbial Films." Trans. Instn. Chem. Engrs. 48:T245«
103* Atkinson, B. and D. A. Williams. "The Performance
Characteristics of a Trickling Filter with Hold-Up of
Microbial Mass Controlled by Periodic Washing." Trans.
Instn. Chem. Engrs. 42.:215. 1971.
104* Ames, W. F., Behn, V„ C. and W. Z. Collings. "Transient
Operation of the Trickling Filter." Journ. San. Engng.
Div., Am. Soc. Civ„ Engrs0 88:21. SA3® 1962.
105. Popel, F. "Construction, Degradation Capacity and
Dimensioning of Rotating Biological Filters." Eidg.
Technische Hochschule ZurichiFortbildungskurs der
EWAG. 1964. Cited by Antonie (56).
106. Hawkes. H. A. The Ecology of Waste Treatment. Oxford!
Pergamon Press. 154. 1963.
107. ___________ Royal Commision on Sewage Disposal, 5th
Report. Appendix 1. Minutes of Evidence. 22350-51.
Also Interim. Report Vol. 1. Minutes 7021-3, 7453-4.
1908. Cited by Hawkes (106).
248
-------
108. Stanbridge, H. H. "The Development of Biological
Filtration." Wat. Sanit. Engr. 4:297. 1956. Cited
by Hav&es (106).
109« Byrom, Dc "A Short Exercise on the Periodicity of
Dosing of Laboratory Percolating Bedse" Journ. Insta
Sew. Purif. 2:155. 1957.
110. Marki, E. "Results of Experiments by EWAG with the
Rotating Biological Filter." Eidg. Technische
Hochschule. Zurich: Fortbildungskurs der EWAG.
1964. Cited by Antonie (56)„
111. Perry, J. H. Chemical Engineers' Handbook. New York:
New York: Mcgraw-Hill. 14-25. 1969.
112. Danckwerts, P. V. Gas-Ljguid Reactions., New York:
McGraw-Hill. 214, 1970o
1130 Satterfield, C. N. Mass Transfer in Heterogeneous
Catalysis. Cambridge, Mass.:MIT Press. 1970,
114. Levenspiel, 0. Chemical Reaction Engineering* New
YorksJohn Wiley and Sons, Inc. 19620
115. Haug, R, T. and P. L. McCarty. "Nitrification with
the Submerged Filter." Report to the Water Quality
Office, Environmental Protection Agency, Research
Grant No. 17010EPM. Technical Report No. 149.
Stanford. 23» 1971.
116. IBM Application Program H 20-0367-2, "System/
360 Continuous System Modeling Program. (360A-CX-16X)
User's Manualo" White Plains, New YorkiIBM Corp. 1968.
117. Gomori, G. "Tables for Buffer Solutions." Methods in
Enzvmologv i.. New York:Academic Press, Inc. 138, 1955.
US* Standard Methods for the Examination of
Water and Wastewater» 12th Edn. New York:American
Public Health Association Inc. 1965.
119• Hoffman, W. S. "A Rapid Photoelectric Method for the
Determination of Glucose in Blood Urine." Journ.
Biologic. Qvejn. 120x51. 1937.
249
-------
120. Nemerow, N. L. Liquid Waste of Industry. Theory.
Practices and Treatment <> Re ading, Mass. * Add i son-
Wesley Publishing Co* 341. 1971.
121* Heukelekian, Hc and M, C. Rand* "Biochemical Oxygen
Demand of Pure Organic Compoundso" Sew. Ind. Wastes
27:1040c 1955.
122* Porges, N., Jasewicz, L„ and S. R0 Hoover0 "Principles
of Biological Oxidation,," in Treatment. Cited by
Young (86)e
124, Torpey, We Ne, Heukelekian, H*, Kaplovsky, A. J. and
R. Epsteino "Rotating Discs with Biological Growths
Prepare Wastewater for Disposal or Reuae." Journ»
Wat. Pollut. Contr. Fed. 42:2l8lo 1971.
125. Bryant, J. O. Jr„, Wilcox# L0 C. and Jo F. Andrews0
"Continuous Time Simulation of Wastewater Treatment
Plants." Paper Presented at A*I.Ch*Ee Meeting*
Cincinnati, Ohio* 1971*
1260 Danckwerts, P0 V. "Continuous Flow Systems — Distribute
of Residence Times." Chem* Eng. Sci* 2.:lc 1953.
250
-------
,f -'L'.JI'I 1. ~ •J~- 0..' i'lvji-a.-¦ J. a'/
GROWTHS CM ROTATING DISCS FOR DISPOSAL OR IISUSE
PART I. INITIAL INVESTIGATIONS "
sy VT. Torpey1, I-I. Heukelefcian2, A.J. KaplovsXy3 and R. Epstein4
The purpose of. this paper is to report on the development
of a system of treatment o£ waste water designed to produce
different quality effluents suitable for disposal into re-
ceiving bodies of water or for reuse. The system has three
component parts which can be used either separately or sequentially.
The waste water is- treated first on a series of rotating discs
with attached biological growths. Depending upon the number of
sequential units used it is possible to produce an effluent with
successively greater degrees of removal of carbonaceous organic
natter which may or may not be followed by the oxidation of ammonia
to nitrates. The effluent from this component of the system is
then treated on a series of rotating illuminated discs on which
is generated attached algae for the purpose of the removal of
nutrients. Finally, if so desired, the waste water having been
~e prepared can be treated by activated carbon for the removal of
residual biodegradable and non-biodegradable organic materials.
'.Paper of the Journal Series, New Jersey Agricultural Experiment
Station, Rutgers, the State University of New Jersey, Department
of Environmental Sciences, New 3ru.nsv.-ic]':, New Jersey.
-'-v. / ptc'isc - Di-Tocto-f
"eukelokian, Research Consultant
-''A. J. KaplovsTcy, Grant Director
Epstein, Senior Chemist
-------
The effluent from this treatment can tnen be ieut;eu
purposes or made potable through dcmineralization and disinfection.
The system of treatment can accordingly be tailored to a wide spectrum
of needs demanded by local situations.
The above conceptual system has been developed on the basis
of pilot plant work located at the Jamaica Water Pollution Control
Plant in New York City.
I• The System for the Removal of Carbonaceous Hatter and the
Oxidation of Ammonia.
The first component is comprised of ten sequential stages.
(Slides 1 &. 2) . Each stage consists of a horizontal shaft on
¦which are mounted 48 three-foot diameter aluminum discs,
1/16 inch thick and spaced on 1/2 inch centers. Each shaft is
driven separately by a hydraulic motor. The rotation alternately
submerges the attached biological growths and exposes them to air,.
The flow has been 7.5 to 9 gpm of primary effluent which results
in a theoretical detention time of 5 to 6 minutes in each stage.
The shafts are rotated at an average speed of 10 rpm and are
generally operated in a direction opposing the flow of waste
water.
Samples of influent to the biological unit and effluents
from each stage were taken from 3:00 to 6:00 P.M. during the
higher load conditions. Initially, the samples were settled
-------
and the supernatant was composited for analysis. Subsequently,
;he samples were filtered through a small 35 micron microstrainer.
The following determinations were made regularly: BOD, COD,
suspended solids, NH^-N, N09-N, and NO -I*. Additional tests were
mace for special purposes. Allylthiourea was used to suppress
nitrification in the BOD tests in stages manifesting nitrification.
The paper presents only the results of the initial period of
operation from July to November 1969. The temperature of the sewage
during this period ranged between 62 and 73°F.
The average results of 33 samples of the operation of the
biological units are presented in Table 1. The average BOD of
the influent (the effluent of the primary tanks from the Jamaica
Plant) was 124 mg/1 which was lowered by the first stage to 82 itu^l,
thus effecting a reduction of 34% in approximately 5 to 6 minutes
contact time. In the second stage it was further lowered to 59 m£/l
for an additional 28% reduction. An effluent with 19 mg/1 of BOD
was obtained at the end of the fifth stage for an overall reduction
of 35% in 25 minutes of contact time. The effluent from the ninth
and tenth stages had a BOD of only 9 mg/1 for an overall reduction
exclusive of primary treatment of 93%.
The COD was lowered from 303 mg/1 to 220 mg/1 in the first
stage for a 27% reduction. At the fifth stage it decreased to
103 mg/1 for a 66% removal, while the overall removal after
-------
ig tenth stage was 78%. The reason for the lower rates of
CCD reduction in comparison with the EOD must be ascribed
to the presence of non-biodegrada?ole materials. The EOD and
COD concentrations in the effluents from each -unit is presented
in Fig. 1.
The average suspended solids in the influent to stage 1
was 107 mg/1 which was reduced to 69 mg/1 in the effluent from
that stage for a 37% reduction (Table 1). After stage 5 the
suspended solids were reduced to 20 mg/1 for a reduction of 87%.
The effluent from the 10th stage had 9 mg/1 suspended solids,
giving an overall reduction of 91% exclusive of primary treatment.
The suspended solids settled readily and filtered through the micro -
strainer with increasing rapidity after each successive stage.
The NE3-N at the first stage increased slightly over the
influent due to the hydrolysis of organic nitrogen in the
biological growths. At the fourth and.fifth stages a slight
decrease was obtained. Thereafter the decrease was more rapid
down to 5.7 mg/1 at the tenth stage, .nitrification started at
the fifth stage and increased thereafter by about 2 mg/1 at each
stage for a total of 10.4 mg/1 of combined oxidized nitrogen within
a total of half hour of contact time. Higher concentrations were
obtained during the warmer months.
-------
It is apparent from these results that rapid nitrification
-akes place with specialized and established flora under optimum
sludge
environmental conditions in contrast with activated/process which
requires long periods of aeration and high mixed liquor solids con-
centration .
Microscopic examinations of the biological growths revealed
a succession o£ different types of microorganisms starting with
a predominance of zoogleal bacteria and Sohaerotilus in the first
three stages, followed by an abundant and diversified fauna con-
sisting of free-swimming and stalked protozoa, rotifers, and nematodes
in the subsequent stages. The activities of the abundant and diver sifiec
microfauna played a major role in the high degree of clarificationjof
—.vaste^vatcr and the destruction of substantial amounts of organic
matter. (Slides 3-7) The extent of the effects of animal predation
became evident in the last four stages which, at times, resulted iri
bare spots on. the disc surfaces, the magnitude of which depended oh
the relative rates of growth of predators versus bacterial slimes.
It was apparent that, in contrast with the activated sludge process
a succession of morphologically and biochemically specialized micro-
organisms developed in the various stages in step with the changes in
the substrate composition which resulted in a high efficiency of
treatment.
-------
As would be expected, the accumulation of biological growth
in the first three stages was more rapid than on each of the
succeeding stages. It was hence necessary to remove the growths
to prevent bridging and anaerobic conditions in the attached part
of the growth. The growths from the first and second states were
removed once in four or five days with decreasing frequency there-
after down to the sixth stage. The succeeding stages were cleaned
only once in several months. The cleaning in the pilot plant was
accomplished by using water jet. Thus, none of the biological growths
were allowed to reach a thickness greater than 1.5 mm.
After cleaning, a biological growth was restored on the disc
surfaces of the first stage after about eighteen hours with the re-
establishment of normal efficiency of treatment. The time required'
for the establishment of growths increased only slightly down to
stage three. Beyond this stage increasing time was required for
the establishment of growth.
dissolved oxygen was absent or was present in less than 1 mg/1
concentration in the first and second stages. Thereafter it increased
progressively to a range of about 4 to 0 mg/1 in the tenth stage.
The pH- values increased slightly :o a range of 7.3 to 7.6
up to stage six and then decreased to a rar.gg of 7.1 to 7.5 at
stage ten. At the same time the bicarbonate alkalinity decreased
due to the production of nitric acid.
-------
It is significant to note that the chlorine demand decreased
progressively from an initial value of 17 mg/1 down to 3 mg/1 at
the sixth stage and down to 1 ng/1 at the tenth stage.
Surfactants were not attacked by. the growths in stages one
ana two but thereafter they decreased from an initial value of
about 3 n\g/l to 1 mg/1 at stage eight with no further decrease
thereafter.
II- The System for the Removal of Nutrients.
(Slides 8 & 9) The algal unit consisted of six stages of
partially submerged rotating discs with triangular cross section.
'The number of discs oh the shafts decreased from twelve on the first
stage to two on the sixth stage. The discs were constructed of 1/15
inch thic?< aluminum, 3-feet in diameter and were hollow. The discs
were exposed alternately to overhead light source of grow lux
fluorescent lights enclosed in a hood and immersed in the flow.
Filamentous algae grew only along the outer rims of the discs,
since only in that area was the light intensity adequate. Exposure
of an outer disc to 1000 fc of illumination from cool white fluorescent
tubes produced a luxurient growth of filamentous algae (Slides 10-13).
On the basis of a number of observations with varying light intensities
it is planned to replace the triangular discs with flat discs parallel
to each other, with sufficient space in between for the insertion of
light source of proper intensity and quality.
-------
III. Adsorption on Activated Carbon¦
Carbon adsorption treatment of the affluent from the algal
unit was practiced during the last- two months. About 27 pounds
of virgin granular carbon (12 x 40 mesh) was placed in six
packed bod columns 5 feet, 10 inches long and 3 inches in
diameter, each providing for a bed expansion of about 5C%
during th.e back washing operation. The hydraulic loading
rate was maintained at about 5 gpm per square foot and the
six columns operated in series.
'Preliminary analytical results indicated that the dissolved
total organic carbon (TOC) in the effluent from the algal unit
varici from 3 to 12 mg/1, while the effluent from first carbon
column varied from 3 to 5 mg/1. (Table 2) The effluent from
carbon column 3, 4, 5, and 6, varied from 1 to 2 mg/1. Since,
to date, the results did not indicate a significant'rise in the
TOC leaving carbon column #1, although some 15,000 gallons had
p.?.cscc" through 5 pounds of carbon in that column, it was not
possible to determine the exhaustion rate.
The pressure across carbon column #1 increased at a rate
cf about 4 pounds in 24 hours. A daily backwash schedule was
practiced to keep the pressure at lov; levels. In order to further
reduce the increase in pressure a mixed media filter was installed.
As a result the increase of pressure was reduced to 1 pound in 24 hou
-------
Based on these preliminary findings, it appears that the
biological treatment/ as practiced, was capable of preparing
the waste water for carbon adsorption to such a degree as to
make it possible to remove the organics in the effluent completely.
suyjyj~
-------
The cooperation and assistance given by Commissioner
Felclman and Assistant Commissioner M- Lang of the Environmental
Protection Administration of New York City, is gratefully acknowledge
-------
forof cho Bj.olo';icr.l UnJ.
BOD (itig/1)
CCD (mg/1)
Susp, Sol ids
(-g/1)
MM 3 - N
(nvj/1)
N02 HO3 - H
f /
(-j/1)
N
(2)
Inv].,
.St?-r-:C_i70._
4" 5"
33
33
3.1
27
124
303
107
82 59 44 23 19 17 14 12
220 174 152 121 10 3 94 85 81 7 3
;9 47
A A
31
20 16 14 13 12
_10
9
64
9
13 14,2 14.0 14.4 13,6 13.2 12,8 11.0 S,9 6.9 5.7
1.0 2.2 4.3 6.7 3.6 10,4
(1) Avs.rs.ga results for period from July to November.
(2) LIuiobcj." of gam^ 1-
-------
Tabic 2
Performance of Carbon Columns
colv.nn 1
colum 2
CcO.uiTu-; 3
r.o.l'irr.rv 4
Co^u:mn a
Co.VJim 6
rn^r*
(1)
r;;c?/l
10.0
5.7
/
J • Sr
2.6
2.0
1.9
2.1
(2)
9.6
4.0
2.6
1.4
1.2
1.0
0.9
Color
(3)
p-jrrs „
17,5
2.5
Turbidity
0'TU
(3)
2.0
no /I
0.1
0.9
.04
(1) Total organic C average of 5 sarnies
Dissolved organic C average of 5 samples
{Z) Average of 2 samples
-------
Eioiogicai rotating discs
tr u ii
Zocglea ramigera Unit 1
Sphaerotilus Unit 3
Zooglea, carchesiun & Sphae'rotilus Unit 3
Vorticella & difflugea Unit 7
Rotifers, aiffiugea, amoeba & ciliate Unit
Algal unit
11 H
II II
Filamentous algae - Kormidium Algal unit
Nematode egg, Nitschia & Hormidium " "
Oscillatoria & Arcella
-------
14 O
120
100
GO
G
o
o
CD
GO
AO
1
r\
\
\
\
\
G
\.
20 .
\
\
s,
BIO DISC.
SETl
o
>r~
n
mr;FormmcE per
STAGE
V3
LED BOD GiCOD in
-------
PREPARATION OF MUNICIPAL WASTEWATER BY ATTACHED BIOLOGICAL
GROWTHS ON ROTATING DISCS FOR DISPOSAL OR REUSE
W. Torpey and H. Heukelekian*
The purpose of this paper is to report on the development
o£ a system of treatment of waste water designed to produce
different quality effluents suitable for disposal into re-
ceiving bodies of water or for reuse. The system has three
component parts which can be used either separately or
sequentially. The waste water is treated first on a series
of rotating discs with attached biological growths. Depend-
ing upon the number of sequential units used it is possible
to produce an effluent with successively greater degrees
of removal of carbonaceous organic matter which may or may
not be followed by the oxidation of ammonia to nitrates.
The effluent from this component of the system is then treated
on a series of rotating illuminated discs on which is generated
attached algae for the purpose of the removal of nutrients.
Finally, if so desired, the waste water paving been so prepared
can be treated by activated carbon for the removal of residual
*w. Torpey - Project Director, Rutgers University
H* Heukelekian - Research Consultant
-------
-2-
biodegradable and non-biodegradable organic materials.
The effluent from this treatment can then be reused for
certain purposes or made potable through demineralization
and disinfection. The system of treatment can accordingly
be tailored to the particular needs of local situations.
The above conceptual system is being developed on the
basis of pilot plant work located at the Jamaica Water
Pollution Control Plant in New York City.
I. The system for the removal of carbonaceous matter and
the oxidation of ammonia.
The first component is comprised of ten sequential stages.
(Slides 1 and 2). Each stage consists of a horizontal shaft
on which are mounted 48 three-foot diameter aluminum discs,
1/16-inch thick and spaced on *s-inch centers. Each shaft is
driven separately by a hydraulic motor. The rotation alter-
nately submerges the attached biological growths and exposes
them to air. The flow has been 7.5 to 9 gpm of primary
effluent which results in a theoretical detention time of
5 to 6 minutes in each stage. The shafts are rotated at an
average speed of 10 rpm and generally operated in a direction
opposing the flow of waste water.
Samples of influent to the biological units and effluents
from each stage were taken from 3:00 to 6t00 P.M. during the
-------
-3-
higher load conditions. Initially, the samples were settled
and the supernatant was composited for analysis. Subsequently,
the samples were filtered through a small 35 micron micro
strainer.
The following determinations were made regularly: BOD,
COD, suspended solids, NH3-N, NO2-N, and NO3-N. Additional
test8 were made for special purposes. Allylthio urea was
used to suppress nitrification in the BOD tests in stages
manifesting nitrification.
The average results of the operation of the biological
units from July to November, 1969, are presented in Table 1«
(Slide 3). The average BOD of the influent to the first
stage (from plant primary effluent) was 124 mg/1 which was
lowered by the first stage to 82 mg/1, thus effecting a re-
duction of 34% in approximately 5 to 6 minutes contact time.
In the second stage it was further lowered to 59 mg/1 for an
additional 28% reduction. An effluent with 19 mg/1 of BOD
was obtained at the end of the fifth stage for an overall
reduction of 85% in 25 minutes of contact time. The
effluent from the ninth and tenth stages had a BOD of only
9 mg/1 for an overall reduction exclusive of primary treat-
ment of 93%*
-------
-4-
The COD was lowered from 303 mg/1 to 220 mg/1 in the
first stage for a 27% reduction. At the fifth stage it
decreased to 103 mg/1 for a 66% removal, while the overall
removal after tenth stage was 78%. The reason for the lower
rates of COD reduction in comparison with the BOD should be
ascribed to the presence of non-biodegradable materials.
The BOD and COD concentrations in the effluents from each
unit are presented in Fig. 1. (Slide 4)
The average suspended solids in the influent to stage 1
was 107 mg/1 which was reduced to 69 mg/1 in the effluent
from that stage for a 37% reduction. (Slide 3). After stage
5 the suspended solids were reduced to 20 mg/1 for a re-
duction of 87%. The effluent from the 10th stage had
9 mg/1 suspended solids, giving an overall reduction of 91%
exclusive of primary treatment. The suspended solids settled
readily and filtered through the micro strainer with increas-
ing rapidity after each successive stage.
The NH3-N at the first stage increased slightly over the
influent due to the hydrolysis of organic nitrogen in the
biological growths. At the fourth and fifth stages a slight
decrease was obtained. Thereafter the decrease was more
rapid down to 5.7 mg/1 at the tenth stage. Nitrification
-------
280 140
240 120
200 IOO
CT> 160 CP 80
E E
o o
O O
U CD
120 60
80 40
40 20
0
£
) \
BIO DISC. PERFORMANCE PER S"
VS
SETTLED BOD &COD in mg/l
rAGE
A \
\
\
\
\
a
\
\
\
$
LE
GEND
-
\
\
s.
\ «
\
\
»
1
A
«
COD
8 QC
-
'v,
N
N
4
—A
-
1
.
s- (
>
&
>
INF. I
4 5 6 7
]AGE NUMBER
8
10
-------
-5
started at the fifth stage and increased thereafter by about
2 mg/1 at each stage for a total of 10.4 mg of combined
oxidized nitrogen within a total of half hour of contact time.
Higher concentrations were obtained during the warmer months.
Microscopic examinations of the biological growths re-
vealed a succession of different types of microorganisms
starting with a predominance of zoogleal bacteria and
Sphaerotilug in the first three stages, followed by free-
swimming and stalked protozoa, rotifers, and nematodes in the
subsequent stages. (Slides 5, 6, 7, 8). 'The effects of
animal predation became evident in the last four stages
which, at times, resulted in bare spots on the disc surfaces,
the magnitude of which depended on the relative rates of
growth of predators versus bacterial slimes. It was apparent
that, in contrast with the activated sludge process a
succession of morphologically and biochemically specialized
microorganisms developed in the various stages in step with
the changes in the substrate composition which resulted in
a high efficiency of treatment.
As would be expected, the accumulation of biological
growth in the first three stages was more rapid than on
each of the succeeding stages. It was hence necessary to
-------
-6-
remove the growths to prevent bridging and anaerobic con-
ditions in the attached part of the growth. The growths
from the first and second stages were removed once in four
or five days and with decreasing frequency thereafter down to
the s ixth stage. The succeeding stages were cleaned only once
in several months. The cleaning in the pilot plant was
accomplished by using water jet and brush. Thus, none of
the biological growths were allowed to reach a thickness
greater than 1.5 nun.
After cleaning a perceptible amount of growth appeared
on the disc surfaces of the first stage after about eighteen
hours. The time required for the establishment of growths
increased only slightly down to stage three. Beyond this
stage increasing time was required for the establishment of
growth.
Dissolved oxygen was absent or was present in less than
1 mg/1 concentration in the first and second stages. There-
after it increased progressively to a range of about 4 to
6 mg/1 in the tenth stage.
The pH values increased slightly to a range of 7.3 to
7.6 up to stage six and then decreased to a range of 7.1 to
7.5 at stage ten. At the same time the C02 and bicarbonate
-------
-7-
ilkalinity decreased, contrary to expectations because of
the influence of nitrification.
It is significant to note that the chlorine demand de-
creased progressively from an initial value of 17 mg/1 down
to 3 mg/1 at the sixth stage and down to 1 mg/1 at the tenth
stage.
Surfactants were not attacked by the growths in stages
one and two but thereafter they decreased from an initial value
of about 9 mg/1 to 1 mg/1 at stage eight with no further
decrease thereafter.
II. The system for the removal of nutrients
(Slide). The algal unit consisted of six stages of rotat-
ing discs with triangular cross section. The number of discs
on the shafts decreased from twelve on the first stage to two
on the sixth stage. The discs were constructed of 1/16-inch
thick aluminum, 3-feet in diameter and were hollow. The
discs were exposed to overhead light source of grow lux
fluorescent lights enclosed in a hood.
Filamentous algae grew only along the outer rims of the
discs which was later found to be due to the low intensity of
light. Exposure of an outer disc to 1000 fc of illumination
from cool white fluorescent tubes produces a luxurient growth
-------
-8
of filamentous algae. On the basis of a number of obser-
vations with varying light intensities it is planned to
replace the triangular discs with flat discs parallel to
each other# with sufficient space in between for the in-
sertion of light source of proper intensity and quality.
III. Adsorption on activated carbon
Carbon adsorption treatment of the effluent from the
algal unit was practiced during the last two months. About
27 pounds of virgin granular carbon (12 x 40 mesh) was
placed in six packed bed columns 5 feet, 10 inches long
and 3 inches in diameter, each providing for a bed expansion
of about 50% during the back washing operation. The hydraulic
loading rate was maintained at about 5 gpm per square foot and
the six columns operated in series.
Preliminary analytical results indicated that the dis-
solved total organic carbon (TOC) in the effluent from the
algal unit varied from 8 to 12 mg/1, while the effluent from
carbon column varied from 3 to 5 mg/1. (Slide). The effluent
from carbon column 3# 4, 5, and 6, varied from 1 to 2 mg/1.
Since, to date, the results did not indipate a significant
rise in the TOC leaving carbon column #1, although some
15,000 gallons had passed through 5 pounds of carbon in
that column, it was not possible to determine the ertiaustion
-------
rate.
The pressure across carbon column #1 increased at a
rate of about 4 pounds in 24 hours. A daily backwash schedule
was practiced to keep the pressure at low levels. In order
to further reduce the increase in pressure a mixed media
filter was installed. As a result the increase of pressure
was reduced to 1 pound in 24 hours.
Based on these preliminary findings it appears that the
biological treatment, as practiced, was capable of pre-r
paring the waste water for carbon adsorption to such a
degree as to make it possible to remove the organics in
the effluent completely.
Summary
A method of treatment of primary effluent by a series
of rotating discs with attached growths has been developed
capable of producing removals of carbonaceous BOD up to
95% and the oxidation of ammonia to nitrates. The removal
of N and P from the effluent of these units is being
attempted by promoting the growth of attached filamentous
algae on illuminated rotating discs which are readily
harvestable in contrast with the removal of planktonic
algae grown in oxidation ponds. The effluent thus pre-
pared ia highly amenable to adsorption on activated carbon
-------
-10-
without the usually observed leakage of organic carbon.
Acknowledgements
This investigation is supported by a grant from FWPCS
(WP-01322) to the Department of Environmental Sciences of
Rutgers University.
The cooperation and assistance given by Commissioner
M. Feldman and Assistant Commissioner M. Lang of the
Environmental Protection Administration of New York City,
is gratefully acknowledged.
-------
EFFECTS OF EXPOSING SLIMES ON ROTATING DISKS
TO ATMOSPHERES ENRICHED WITH OXYGEN
W. Torpey} H.. Heukelekian2, A.J. Kaplovsky^ and R. Epstein4
lw. Torpey, Project Director
2*1. Heukelekian, Research Consultant
3A.J. Kaplovsky, Grant Director and Chairman# Department of
Environmental Sciences, Rutgers University# New Brunswick, N.J. 08?
4r. Epstein, Senior Chenu.6t
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A paper entitled# "Rotating Disks with Biological Growths
Prepare Wastewater for Disposal or Reuse/" was published in
November, 1971, issue of the Journal of WPCF by the above
authors. It presented results of the operation of a rather
sophisticated pilot plant utilizing rotating disks to treat
effluent from the primary tanks of the Jamaica Water Pollution
Control Plant in New York City, for the period July to
November, 1969. This pilot plant was operated with partially
submerged disks, alternately immersed in the wastewater and
exposed to normal atmosphere in all stages of treatment.
The purpose of this paper is to present the results of
subsequent pilot plant studies wherein one or more stages of
treatment were enclosed with a hood so that the Blimes were
exposed to atmospheres enriched with oxygen. Accordingly,
for comparison purposes, the results obtained during the base
period when all stages were operating under normal atmosphere
are included.
EQUIPMENT
The pilot plant comprised three main component partsj
(a) Ten stages of rotating disks for the removal of organics
and for oxidation of ammonia to nitrate, (b) six stages of
illuminated rotating disks for the removal of nitrogen and
phosphorous from the effluent of the preceding system by
synthesis into attached algal cells, and (c) six packed beds
of granular activated carbon columns for the adsorption of
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-2-
residual organica from the preceding algal system. Sedi-
mentation of 1.5 hours was interposed between the effluent
from the ten stage unit and the algal unit. A mixed media
filter preceded adsorption in carbon columns for removing
particulates, mainly irt the form of algal cells, which had
been generated on the illuminated disks.
The flow through the ten stages was 28.39 1/min i 10%r
whereas the algal unit rate was 11.3 5 1/min. Flow to the
pressure downflow carbon columns was at a surface loading of
203.6 1/min./M2.
Each of the ten stages consisted of a horizontal shaft
with 48, ,91M diameter, .16 cm thick aluminum disks which
were spaced on 1.27cm centers. Effective area was sacrificed
to the extent of 11% by the use of , 30M diameter spacers
between the disks. These aluminum spacers were used to
provide rigidity and proper alignment to the thin aluminum
disks. Each shaft was driven by a hydraulic motor at
rotational velocities of 6 to 10 R.P.M. The disk assembly
was placed in a half-formed cylindrical tank so that 45% of
the disks were submerged. Flow was perpendicular to the shaft.
There was no intermixing between stages. Disk rotation was
opposite to the direction of flow through the stages, The
theoretical detention time was six minutes in each stage,
measured when the disks were devoid of slime. The actual
time was somewhat less, depending on the degree of displacement
of fluid volume by the slimes. The primary tank feed
originated from a 600,000 population wastewater plant.
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-3-
Enrichment of the atmosphere over the specific stages was
iccomplished by enclosing the disk assembly above the water
surface with 1.27cm thick transparent plexiglass placed in
i box-like form to provide a sealed hood. Oxygen was fed at
.5 to 2-liters per mirtute and gas pressure was maintained
Detween 0 to 2.54cm of water. The hood was found to contain
small leaks which, in conjunction with a pressure of less
than .32 cm of water under the hood, were able to emit the
nitrogen evolved from the wastewater and the CO2 generated
by respiration.
The carbon adsorption system consisted of six packed
bed columns 1.78M long and 7.62cm in diameter. About 10.08 Kg
of virgin granular carbon (12 x 40 mesh) was used resulting
in a bed expansion of about 50% during the daily backwashing
operation. The pressure across the six columns, operated
in series, at first was found to increase at a rate of about
1.49 Kg in 24 hours until the mixed media filter was inter-
posed and the rate was lowered to less than 703.1 Kgs/M^ in
24 hours.
Samples of influent were taken during the afternoon
between 3 and 6 P.M. The samples were prepared for analysis
by microstraining through a 5.08cm diameter 35 micron "hand"
microstrainer.
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OPERATING RESULTS
A. Organic Removal in Terms of B.O.p.t;. From previous inves-
tigations (1) the effluents from stages .3 to 10 contained
from 2 to 5 mg/1 of dissolved oxygen, yet the effluents from
stages 1 and 2 were generally devoid of dissolved oxygen.
The oxygen demand of the slimes in the upper two stages were
not being satisfied. As a means of overcoming this limitation,
stage 1 was modified by increasing the number of disks from
48 to 60 and installing a hood for oxygen enrichment studies.
Oxygen gas, fed at 1.5 liters/min., increased the percentage
of oxygen under the hood of stage 1 from 50% to 70%. The
dissolved oxygen in the effluent from this stage varied between
8 and 14 mg/1, and provided oxygen for stage 2. Coincident
with the changes to stage 1 equipment, the disks in stage 2
were increased from 48 to 71.
Data obtained for the base period, July to November, 1969,
as to the B.0.D.5 in the effluents from the 10 stageB is
shown in Figure 1. The influent B.QtD.j of 124 mg/1 was
reduced progressively to 19 mg/1 at stage 5. Thereafter the
rate of removal decreased and, at stage 10 to 9 mg/1.
Also shown in Figure 1 is the profile of B.0.D.5 when
stage 1 was equpped with a hood. This data was obtained under
the same flow conditions as the base period. The B.O.D.5 of
101 mg/1 in the influent was reduced to 35 mg/1 by stage 1
alone and to 16 mg/1 after stage 3. During treatment through
stages 4 to 6, the rate of removal of B.O#D*5 decreased, and
remained at 12 ma/i after stage 6.
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Comparison of Profiles
of
BOD5 Remaining
Legend
% Jul. to Nov. 1969, no
atmosphere over all etc
O Aug. to Nov. 1970 (e
Sept.) with oxygen
enrichment over stage
Stage No.
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The stability of the process with respect to the B.O.D.5
remaining after the various stages is evident from the daily
maximum, minimum and average values for influent and the stage
effluents. In general the B.0.D.5 of the downstream stage
effluents varied from one half to twice the average.
B. Organic Removal in Terms of C.O.D. The C.O.D. data
obtained for the same periods and conditions described above
are shown in Figure 2. During the base period, 40% of the
initial C.O.D. concentration remained after stage 4 and 21%
after stage 10. With the oxygen enriched atmosphere over
stage 1, only 50% of the C.O.D. remained after stage 1, and
2 8% was left after stage 4.
C. Organic Removal in Terms of Total Organic Carbon (T.O.C.)
The data pertaining to Total Organic Carbon. (T.O.C.) and
the Suspended Organic Carbon (S.O.C.) which is the difference
between the T.O.C. and the Dissolved Total Organic Carbon
(D.T.O.C.), has been plotted in Figure 3 for two periods when
T.O.C. data was available. The flow rates were1 the same and
the operation in the same temperature range (62^ to 7 8°F.).
Profile 1 shows a straight line decrease from 87 mg/1 to a
value of 17 mg/1 at stage 6. Thereafter the slope decreased
and 12 mg/1 remained at stage 10. Operating with an enriched
atmosphere over stage 1, profile 2, shows that a value of
75 mg/1 for the influent had been reduced to 37 mg/1 by stage 1
alone. A break in slope occurred between stages 1 and 5.
After stage 5, the T.O.C. had been lowered to 15 mg/1.
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Comparison of Profiles
of
C.O, D. Remaining
Le g e n d
•Vjul. to Nov. 1969,
normal atmosphere ov
all stages.
©Aug. to Nov. 1970
enrichment over
stage
Stage No.
3 4 5 6 7 8 S
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-6-
The S.O.C. data is shown as profiles 3 and 4. An S.O.C.
value of 10 mg/1 was reached after 4 stages during the first
period/ whereas 2 stages were required to attain the same
value during the latter period. During both periods the
S.O.C. removal proceeded without resistance, at least to the
extent extent of removing 95% to a level of 2 mg/1.
NITRIFICATION
The effect on nitrification of enriching the atmosphere
with oxygen over stage 1 is evident in Table 1. Nitrification
was observed to begin at stage 5, in the first period, while
nitrification moved upstream to stage 3, when operating with
enrichment of the atmosphere over stage 1. In the first period,
it required 9 stages to cope with the oxidation of organics
and produce 9 mg/1 of NO3-N (NO2-N not determined). Coinci-
dentally, the alkalinity was reduced by 76 mg/1. In the
latter period, the same work was accomplished by 7 stages.
OPERATING RESULTS - USING THREE STAGES ONLY
Since enrichment of the atmosphere with oxygen over stage 1
had accelerated the removal of organics, enrichment of an
additional stage was tested to observe possible further
acceleration. Accordingly, an additional hood was placed
over stage 7, and equipped with 71 disks. The flow of waste-
water was bypassed from the effluent of stage 2 to the influent
of stage 7. Thus, stage 7 became stage 3 during the month of
September, 1970. Using these three stages, oxygen was fed
at ,8 to 1.2 liter per minute, the oxygen rose under the hood
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TABLE
1. EFFECT ON NITRATE PRODUCTION OF ENRICHING
THE ATMOSPHERE OVER STAGE 1 WITH OXYGEN
Stage 3(3)
4
5
6
7
8
9
10
No Enrichment (1)
N03~N mg/l
0
0.3
1.8
4.1
6.5
9.0
10.8
With Enrichment (2)
NO3-N mg/1
___
1.7
3.5
6.0
9.0
(1) May and June, 1970? (2) Aug., Oct.,Nov. 1970? (3) Inf. 0., NO3-1
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of 6tage 3 to 35% to 40%, whereas under stage 1 hood the
range remained 50% to 70%. The results are compared in Table
2 with the former operation of three stages using a hood over
stage 1 alone. The B.0.D.5 s^age 3, with oxygen enrich-
ment on the first stage alone was 16 mg/1, as compared with
10 mg/l, when using an oxygen enrichment over the first and
third stages. The S.O.C. was markedly reduced to 1 mg/1 in
the latter. No nitrification was evident in the effluent
from stage 3 when the oxygen enrichment was confined to
stage 1. When the third stage was enriched with oxygen,
7.6 mg/1 of nitrates were produced. Thus, about 18 minutes
of contact with the slimes was required to carry the oxidation
process through the carbonaceous zone into the nitrogenous
zone.
OPERATING PROCEDURES AND GENERAL OBSERVATIONS
The accumulation of biological growths, without oxygen
enrichment, was rather rapid in the first three stages. By
controlling the thickness of the slimes bridging was prevented
across the disks and anaerobic conditions in the lower layers
of the slimes. Thickness was controlled by removal of the
growths from the first/ second and third stages every three
to five days. The fourth stage was harvested on a weekly
basis, the fifth stage after 10 days and the sixth stage every
two weeks. The downstream nitrification stages did not require
thickness control. The slime thickness was maintained at
less than 1.5 mm and to operate with a relatively high surface
concentration without bridging. Cleaning was accomplished
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TABLE 2. THREE STAGE TREATMENT RESULTS
Aug.,Oct. ,Nov. ,1970 C>2 Sept.,1970 O2 Enrich
Enrichment Stage 1 ment Stages 1 and 2
Pilot Inf-. Stage 3 Eff. Pilot Inf. Stage 3 Eff.
b.o.d.sj mg/1
101
16
96
10
T.O.C. "
74
21
70
13
S.O.C.
40
7
30
1
NOo-N "
0
0
0
7
Note: Stages 3 to 6 bypassed so that Stage 7, equipped with 71
disks and a hood enriched with oxygen, served as Stage 3.
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¦~u-
either by a water jet or reversing the direction of rotation
of the disk assembly for a few minutes.
After the disks were cleaned by water, the biological
growths recovered in the first stage after about 18 hours and
the very thin slimes, so formed, were capable of restoring the
efficiency thereafter. The time required for the growths to
recover remained substantially the same downstream to Stage 3.
Beyond this stage, increased time was required as the organic
concentration was being reduced and slower-growing biological
forms colonized those stages.
When using the hood over stage 1, the frequenoy of
removing the excess slimes was reduced markedly. For stage
1 and 2, reversing the direction of rotation weekly prevented
bridging even though the spacing between disks was about ,64cm.
Most of the organias were removed by stages 1 and 2. Reversing
direction of rotation of Stages 3 to 6 no more often than
every 3 to 4 weeks controlled slime thickness effectively.
In the base period, sphaerotilus and zooglea constituted
the predominant biological species in the slimes on stages
1-3. When these growths sloughed off, they had a rope-like
form, probably due to rotation, and settled rapidly at 4.57 M/hr.
Upon microstaining the successive effluents from stage 1
through 10 showed a progressive increase in filterability
proceeding downstream. Coincident with that particular stage
which effected about 90% removal of B.0.D,5, a sharp increase
in the rate of filtration was found.
The performance of the algal units will not be reported
herein aa it 1b outside the scope of this paper.
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ADSORPTION OF ACTIVATED CARBON
Treatment of the effluent from the algal unit to remove
residual organics was started in March, 1970/ and continued
through November, 1970. All the data secured during the three
periods of operation is presented in Table 3 and compares the
quality of the product water with respect to T.O.C. and
D.T.O.C. The effluent from the algal unit was quite constant
at 8 mg/1 notwithstanding the widely different operating
procedures for the three periods. The particulate load,
as represented by the difference between the T.O.C. and
D.T.O.C. or the S.O.C., varied from 0 to 1 mg/1. After
passing through the mixed media filter, which, removed about
25% of the load imposed on the carbon columns, the concentration
of T.O.C. and D.T.O.C. that leaked through carbon column 6
was quite constant, for all three periods, at 1.4 mg/1.
Because the carbon adsorption system was called upon to
remove only about 4.5 mg/1 of organic carbon and, probably
because the particulate and colloidal loads were low (S.O.C.
of 0 to 1 mg/1), the practical exhaustion rate of the carbon
was in the range of 15 to 20 mg/1.
DISCUSSION
The results presented have demonstrated that direct
exposure of slimes enriched with oxygen accelerated the rate
of removal of carbonaceous matter from wastewater measured
either in terms of B.0.D.5, C.O.D. or T.0,C.
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TABLE 3» PERFORMANCE OF ACTIVATED CARBON ADSORPTION COLUMNS
No Enrichment(1) ^2 Enrichment(2) ^2 Enrichment(3)
TOC
DTOC
TOC
DTOC
TOC
DTOC
mA
psA
P»9A
ra?A
ssr/1
2SrA
Algal Unit Eff.
7.9
7.8
8.1
7.2
8.4
7.3
Mixed Media Eff.
6.3
6.1
6.2
6.0
5.9
6.1
Eff* from Col. 1
5.3
5.2
4.5
4.3
4.6
4.5
Col. 2
3.6
3.7
3.7
3.7
3.9
3.6
Col. .3
2.5
2.7
2.8
2.7
3.4
2.6
Col. 4
1.9
2.0
2.3
2.2
1.9
2.1
Col. 5
1.5
1.5
2.0
1.8
1.3
1.4
Col. 6
1.3
1.3
1.4
1.4
1.4
1.4
(l)Mar. to June,1970; (2) Aug. to Nov.,1970 Enrichment over
Stage 1» (3)Sept.,1970 Enrichment over Stage 1 and 3.
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-aU-
The reactions are concentration dependent (Fig. 1) within
the ranges encountered and follow first order kinetics. For
this reason the organic concentrations can be converted to
percentage removals in order to facilitate qualifying the
relative rates of removal with and without oxygen enrichment
of the atmospheres.
Specifically, the measured B.O.D.5 reduction across
stage 1 was found to be 34% during the base period, whereas
when operating with an oxygen enrichment over stage 1, the
comparable value was 65%. Since the number of disks on stage
1t in the first period, was 48 and in the second period 60,
appropriate allowance for such increased surface should first
be made. On the basis that the removal of oifganics is
essentially proportional to the surface area for the same
contact period, the corrected value for the second period
would be 52%. The rate of B.0.D.5 removal# attributable to
oxygen enrichment# was therefore increased from 34% to 52%.
The ratio of the rates waB therefore 1.53.
The C.O.D, reduction rates across stage 1, based on the
data presented in Figure 2, were 27% during the base period
and 50% during the latter period when stage 1 was enriched
with oxygen. Making allowance for increased surface# the
latter rate was 40% and the ratio of ratep was 1.48.
Similar calculations relative to the rates of removal
of T.O.C. (see Figure 3) indicate that during the first period
the measured removal was 33% whereas in the latter period the
actual rate of reduction was 51%. Making allowance for the
rate for the latter period was
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41%. The relative rate of the latter period with respect to
that of the first period would have thus been 1.24.
The relative rates of S.O.C. reduction, after making
appropriate allowance for increased surface was 1.1. There-
fore the S.O.C. rate did not increase as rapidly as did the
T.O.C. rate, which indicated that the acceleration must have
been due mainly to the increased rate of removal of dissolved
organic matter (D.T.O.C.). Calculations involving the actual
dissolved organic removal rates indicate a ratio of rates
for the latter period with respect to the first period of
1.68. Operating with oxygen enrichments in the range of 50%
to 70%, the oxygen conceivably diffused deeper into the slime
thus increasing the active biological mass by a calculated
68%.
Microscopic examination of the slimes that developed on
the disks of stage 1 with oxygen enrichment revealed that in
addition to zoogleal masses, the animal population, which
formerly did not appear until stage 4, had moved upstream.
Sphaerotilus, which was present in the first period, was found
to have completely disappeared.
For the purpose of comparing the above described
performances with conventional processes, as to time of
contact, refer to Figure 1. Based on the raw wastewater
strength of 160 mg/1, 90% of that B.0.D.5 was removed by 6
stages (36 minutes) of treatment during the base period
{constant flow) and 3 stages (constant flow) were able to
accomplish the same rate of removal in 18 minutes when stage 1
was operated with oxygen.
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-12-
When three stage operation was practiced, stages 1 and 3
were enriched with oxygen. Stage 2 received dissolved oxygen
from upstream and Berved to restore the pH of the influent
to stage 1 by raising the pH from 7.0 to 7.3. The decrease
in pH was the result of containing the CO2 from the respiration
of the slimes in stage 1. The data obtained during this
three stage operation has been compared in Table 2 with the
first three stages of operation when stage 1, alone, was
equipped with a hood. In the first period the B.O.D.5 of
the influent was reduced by 86% while in the latter period a
B.O.D.5 reduction Of 90% was effected by three stages of
treatment. Improved results were also noted with respect
to the parameters of T.O.C. and S.O.C. In conjunction with
the latter operation it was found that a substantial amount
of nitrification, that is 7.6 mg/1 of nitrates, were produced
in stage 3. Under these specific operating conditions not
only had nitrification been brought upstream but the rate was
increased substantially.
During the 2 year period of operation there were no
biological upsets which would deteriorate the quality of the
effluent. Considering the normal range of variation of the
influent the daily profiles through the treatment system show
that the maximum B.O.D.5 of the effluents exceeded the average
by not more than 10 mg/1.
Referring to Table 1, base period stages 6 to 10 produced
10.5 mg/1 of nitrates or 2.1 mg/1 per stage during 6 minutes
of contact. When operating with oxygen enrichment over
stage 1, stages 4 to 7 oxidized 8.7 mg/1 or 2.2 mg/1 per stage.
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The oxidation of ammonia by these fixed slimes followed zero
order kinetics. According to Jenkins (2) a survey of
activated sludge plants in England disclosed that a maximum
rate of 4.2 mg/1 of nitrogen was oxidized per hour of contact
With a mixed liquor solids concentration of 7000 mg/1.
Comparison of the operating results for summer and
winter months did not indicate any substantial difference
in the rate of nitrification, that is within the temperature
range of 62 to 78°F. Since these findings are in conflict
with the observations of various investigators regarding the
effect of temperature on nitrification, it is believed that
other factors such as the influence of predation exerted a
compensating effect. Predatory activity was suppressed during
the colder months leaving a greater coverage of the surfaces
by nitrifying slimes.
In the upstream stages of treatment which are concerned
with removal of carbonaceous matter the nitrifiers cannot
propagate as they are smothered and starved for oxygen by
heterotrophic organisms.
After the bulk of carbonaceous matter had been removed
down to a B.O.D.5 level of 15 mg/1, a highly specialized
nitrifying culture, brown in color, developed on the disk
surfaces and was able to utilize the ammonia in the stream
as its source of energy. The attached nitrifying culture was
selfregenerating and not wasted as in the case of using a
suspended culture to oxidize carbon and nitrogen. However,
the low growth rate of nitrifiers, in the presence of a predator
population results in the periodic development of bare spots
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-14-
SUMMARY
The results of operating a 41,635 liter per day staged
rotating disk pilot plant have been presented for three modes
of operation, namely, (1) the slimes in all stages exposed to
ambient atmospheres, (2) the slimes in stage 1 exposed to
oxygen enrichment, and (3) the slimes in stages 1 and 3 of a
3-stage operation exposed to oxygen enrichment. The first
mode of operation about 30 minutes of contact with the 9limes
was sufficient to remove 90% of the B.0.D.5 whereas the second
mode of operation 18 minutes accomplished the same rate of
removal of B.O.D.5. In the third mode not only was 90% of
the B.0.D.5 removed during 18 minutes of contact with the
slime but a substantial portion of the nitrogenous demand was
satisfied.
Nitrification normally proceeded at a rate of 2.2 mg/1
per Btage of 22 mg/1 per hour of contact with the slimes.
Under the specific operating condition prevalent in the third
mode described above, nitrification proceeded at a rate of
76 mg/1 per hour of contact.
A portion of the effluents from all the above modes was
subjeated to treatment using partially submerged, illuminated
disks for the purpose of extracting nutrients from the stream
by synthesis into attached algal cells. The effluents from
the algal unit was subjected to adsorption of residual organics
on packed beds of granular activated carbon. The total
leakage of organics through the system was 1.4 mg/1, all
soluble, for all three modeB of operation/ while the practical
was in the range of 15 to 20 mg/1.
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-- J. J • ¦
ACKNOWLE DGEMENTS
This investigation was supported by a grant from the
Environmental Protection Agency (WP-17010 EBM) to the Department
of Environmental Sciences of Rutgers University.
The cooperation and assistance given by Commissioner
M. Feldman and Assistant Commissioner M. Lang of the
Environmental Protection Administration of New York City, is
gratefully acknowledged.
REFERENCES
1) Torpey, W., H* Heukelekian, A.J. Kaplovsky, and R. Epstein.
"Rotating Disks with Biological Growths Prepare Wastewater
for Disposal or Reuse". Jour. Water Pollution Control
Federation, November 1971.
2) Jenkins, S.H., "Nitrification". Jour. Inst, of Water
Pollution Control, Vol. 68, Part 6, pp. 610-618, 1969.
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FORMAL DISCUSSION - PAPER 1. HALL 1D'. SESSION 1
EFFECTS OF EXPOSING SLIMES ON ROTATING DISCS TO
ATMOSPHERES ENRICHED WITH OXYGEN
W» Torpey, E. Heukelekian, A.3, Kaplovaky end R. Epstein
Discussion by
V.A. Pretoriue
The use of rotating biological discs (KBD) for the treatment of
industrial (Antonie and Welch 1969) and domestic ¦wastes has substantially
inoreaaed since Hartraann (19^5) published hie paper on this subject.
At present over 400 installations are in operation (Borchardt 1971).
Contrary to the conventional activated sludge systems which operate mninly
as "completely mixed" units, the generally employed RDB Systems are operated
as "plug flow" systems. Owing to this plug flow nature a natural
separation of the different biological processes responsible for wosie
treatment is obtained along the direction of flow. This separation of
biological activity is also a feature of the RDB system, making it ide.il
for use in the study and optimization of the requirements for each
partioular step in the process.
When sewage is treated in such a RBD system the oxidation of the
carbonaceous material first takes place and is then followed by the
oxidation of the nitrogenous compounds. The present authors used th??:
fact firstly to determine the oxidation rate of oarbon and secondly, Lc
do experiments where both the carbon and nitrogen oxidation stages were
enriohed with oxygen. The improvements made in the oxidation ratee
ware qui to conHidarable and were gonerully in agreement with similar rjrk
done (Albertaeon et al 1970) on the use of pure oxygen in the convention!
aotivated sludge prooeso.
It is not yet olear whether or not the use of oxygen enriched nir
for the RBD eyetema i'e economical, The authors mentioned that the rlis-
Av^irnn in thn first, two comportments was nil and that to 5»r:p""
-------
conventional activated sludge unifca i« of utmost importance for proper
biological aotivity, whereas thin Boeinn to be of leaser importanco to the
HDD system. Owing to the fact that practically all the active micro-
organisms in the RBB system are attached to the di,scs and that these
discs rotate, a thin layer of waste liquid plus micro-organisms is con-
tinuously exposed to the atmosphere, where saturation with oxygen is
reached almost immediately. Whether the bulk of the liquid itself is
aerobic or not is of leaser importance. However, if one would be
interested in maintaining a positive dissolved oxygen level in the bulk
of the liquid this could easily be attained by increasing the rotation
rate of the discs (Welch 1968). In this case the discs would function
as both a biological support as well as a mechanical aerator, indicating
the flexibility of the RBD system.
The authors' observation that, in the presence of oxygen, nitrifica-
tion occurred only when most of the soluble organic matter had been
oxidized, points to an important indication that high concentrations of
dissolved organic matter might be an inhibiting, faotor during nitrification.
This study has again shown the flexibility of the RBD system.
Owing to the separation of the process? into individual stngsn .it is pon-
eible to carefully follow the different reactions and therefore produrio
quite a range of effluents, each suitable for its own particular purpo::rj.
In this respect, ae the plant was operated on settled sewage, why oper^.tr
it as an extended aeration unit to oxidise the sludge while it could bo
romoved immediately after carbon oxidation? Furthermore, as the mil.ho is
aimed at producing a high quality effluent by the inclusion of an
Btage, why should the nitrogen be oxidised all the way to nitrate wlion
Hemena and Stander (1968) have shown that perhaps better nitrogen removal
rates could be obtained if the nitrogen is present as ammonia during th«
algal Btage?
Although this study h«r? contributod to o\|r knowledge of tlifi RBD
system, unfortunately no data is given on the cost aspeot of this system
as oompared with other existing biological systems.
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H INFERENCES
ALBEHTSSON, J.G., McWHIRTER, J.R., ROBINSON, E.K. and VALDIECK, H.P. (197C).
Investigation of the use of high purity oxygen aeration in the
, conventional activated sludge process. Wat. Poll, Contr.
Res. Series ^ 17050DNW05/70# Federal Water Quality Administra-
tion, Washington B.C.
ANTONIE, R.L. and WELCH, F.M. (1969). Preliminary results of Novel
Biological Process for Treating Dairy Wastes. Proo. of the
£ (?¦ 1/L"' ' ' 24th Ind. Waste Conf., Part I. Purdue University.
BORCHARDT, J;A. (l97l). Biological Vaete Treatment Using Rotating Msca.
Biotechnol. & Bioeng. Symposium No. 2, 131 - 140. John Wiley
& Sons, Ino,
HARTMANN, H. (l965)« The Bio-Disc Filter. Oesterreich. Wasswirtsch.
11/12.
HEMENS, J, and STANDER, G.J. (i960). Nutrient Removal from Sewage
Effluents by Algal Activity. Advances ill Water Poll. Research.
. f, v '¦¦k H*1 '-'-'v Proceedings of tho 4th International Conf., Prague 1969*
Edited by S.H« Jenkins, Pergaraon Prose pp 701 - 715>
WELCH, F»M. (l968). Preliminary Results of a New Approach in the
Aerobic Biological Treatment of Highly Concentrated WasteR.
• ^1 '* ,1 Proceedings of the '23rd Ind. Waste Conf. Purdue University.
•'! Vol. a. PP 428 - 457.
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REBU'l IAjl, 1U
FORMAL DISCUSSION - PAPER 1, HALL 'B', SESSION 1
EFFECTS OF EXPOSING SLIMES ON ROTATING DISCS TO
ATMOSPHERES ENRICHED WITH OXYGEN
W. Torpey, H. Heukelekian, A.J. Kaplovsky and R. Epstein
In his discussion of the paper "Effects of Exposing Slimes
on Rotating Discs to Atmospheres Enriched with Oxygen",
Dr. W.A. Pretorius, perhaps inadvertently, made certain
assumptions about the authors work which were not entirely
correct resulting in a somewhat incomplete assessment.
Initially, this was an in-depth research effort to
develop new fundamental information to enhance removal of
pollutantB employing biological slimes on rotating discs.
The study was not intended to repeat or duplicate the state
of the art.
Secondly, so that the wrong impression does not remain
as portrayed by the discussant's comments, the following re-
emphasis appears warranted.
This is not an activated sludge process and, therefore,
we were;not concerned withj
(1) suspended cultures or recycling
(2) we were not using submerged bubbles for solution
of oxygen
(3) nor were we dealing with differences of dissolved
oxygen across a biological interface.
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As the title of our paper indicates we dealt with exposing
attached biological growth to atmospheres enriched with oxygen.
Our findings showed:
(1) that this enrichment affected a marked acceleration
in oxidation of both carbon and nitrogen as compared
with the acceleration formally achieved by exposing
to ambient air and reported previously by the author
(2) we have maximized reactor velocity by concentration
of self regenerated biological surface. The follow-
ing examples are pertinent for comparison:
sq. ft./cu.ft.
(a) activated sludge (by Schropher) e 4
(b) trickling filter t 13
(c) synthetic surfaces e 25
(d) the authors original ambient
air studies total surface = 100
volume of reactor
(e) with enriched atmosphere * 150
The authors were thoroughly familiar with the discussants
referenced literature, which was deemed irrelevant to our studies
except the basic experiments by Hartmann.
The discussant makes reference to increasing rotational
speea as a moans of increasing D.O. This approach would be
cont_ _ indicated in that the power requirements vary as the
cube of| the rotating velocity (in excess of 1 ft. per second
speed).
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The system was not operated as an extended aeration unit
as indicated by the discussant because the biological growths
were prevented from accumulating on the rotating discs in order
to negate anaerobic conditions. However, as the paper emphasized,
such conditions were not present and slime control was rarely
needed or practiced.
With regard to costs the authors re-emphasize the objective
of the study namely to develop fundamental process information
from which a consulting engineer could initiate the design and
reduction to practice. Understandably, the latter would entail
such inputs as cost of materials, labor, structural, electrical
and mechanical design all of which was beyond the scope of this
investigation. Certainly we were concerned with the economics
as to the capital and operating charges with regard to comparison
of rotating disc treatment with respect to other forms of
biological treatment in addition to economics of the use of
atmospheres enriched with oxygen. It was the considered opinion
of the authors that any costs should not be evaluated by University
research personnel but such evaluation should be delegated to thost
who specialize in such matters. Hopefully, someone interested in
the findings would undertake a complete cost analysis and thereby
a further contribution.
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