FIRST SEMI-ANNUAL
I JUNE THROUGH DECEMBER, 1968)
DATA REPORT
FOR
MEAD - FWPCA PROJECT
ON
ADVANCED BIOLOGICAL TREATMENT
JANUARY, 1969
MEAD
research
THE MEAD CORPORATION
CHILLICOTHE, OHIO
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ABSTRACT
The Report presents the data collected for the first six month period
of operation of the test facilities. The performance of the equipment
is discussed and recommendations made for the operation of the facilities
for the next six month period. The methods of sampling, testing and
analysis are presented.
Abstracted by:
¦tcSw'Ct.
D. W. McAnaney
January 30, 1969
This project has been author-
ized, supported and financed
in part, by the Department of
Interior, pursuant to the
Federal Water Pollution Control
Act.
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First Semi Annual Data Report
for
Mead-FWFCA Project on Advanced Biological Treatment
June through December, 1968
Project Director
V. A. Minch
Project Leader
K. C. Ayers
Design Engineer
D. W. McAnaney
Project Officer
R. H. Scott
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FIRST SEMI-ANNUAL DATA REPORT
MEAD-FWPCA PROJECT ON ADVANCED BIOLOGICAL TREATMENT
MEAD CENTRAL RESEARCH LABORATORIES-CHILLICOTHE,OH10
TABLE OF CONTENTS
Abstract Page
I. Introduction 1
II. Purpose of Report 1
III. Project Objectives 2
IV. Summary of Results and Conclusions 2
A. General 3
B. Pilot Feed Characteristics 3
C. Aerated Lagoon 4
D. Oxidation Ditch 5
E. Mead Trickling Filter 6
F. Trickling Filter 2 8
G. Cross Comparison 9
V. Recommendations on Equipment, Operation and Testing 10
A. General 10
B. Aerated Lagoon 11
C. Oxidation Ditch 11
D. Mead Trickling Filter 11
E. Trickling Filter 2 12
F. Combinations 12
VI. Acknowledgements 12
VII. Procedures 13
VIII. Discussion 18
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APPENDIX A -
TABLE A1
TABLE A2
TABLE A3
TABLE A4
FIGURE A1
FIGURE A2
FIGURE A3
APPENDIX B -
FIGURE B1
EXHIBIT B1
FIGURE B2
FIGURE B3
FIGURE B4
FIGURE B5
FIGURE B6
FIGURE B7
FIGURE B8
FIGURE B9
APPENDIX C -
FIGURE CI
FIGURE C2
FIGURE C3
FIGURE C4
APPENDIX D -
FIGURE D1
FIGURE D2
FIGURE D3
FIGURE D4
Test Results
Summary of Test Results on Aerated Lagoon
Summary of Test Results on Oxidation Ditch
Summary of Test Results on Mead Trickling Filter
Summary of Test Results on Trickling Filter 2
Summary of BOD Efficiency on Pilot Aerated Lagoon &
Oxidation Ditcn
Hydraulic Loading vs. Efficiency of Pilot Trickling Filters
Organic Loading vs. Efficiency of Pilot Trickling Filters
Pilot System
View of Pilot Treatment Plant
Description of Pilot Treatment System
Schematic Diagram of Pilot Treatment System
Alternate A - All Systems in Parallel
Alternate B - Filter Ahead of Lagoon
Alternate C - Filter Ahead of Oxidation Ditch
Alternate D - Oxidation Ditch Ahead of Filter
Alternate E - Oxidation Ditch Ahead of Lagoon
Alternate F - Filters in Series
Alternate G - Filter to Oxidation Ditch to Lagoon
Project Plans
Completed Project Plan for Pilot Lagoon and
Oxidation Ditch for First Six Months
Completed Project Plan for Pilot Trickling Filters
for First Six Months
Proposed Project Plan for Pilot Lagoon and Oxidation
Ditch for Second Six Months
Proposed Project Plan for Pilot Trickling Filters
for Second Six Months
Additional Data
Pilot Plant Feed and Aerated Lagoon Effluent
Pilot Plaint Feed and Oxidation Ditch Effluent
Pilot Plant Feed and Mead Trickling Filter Effluent
Pilot Plant Feed and Trickling Filter 2 Effluent
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APPENDIX E - List of Symbols
APPENDIX F - Daily Log Sheet Form
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The information presented herein covers the first portion of a
three phase project plan. This is a interim report consisting
of preliminary data derived from operating the several treatment
systems in parallel to determine single step treatment efficiencies.
Continuing experimentation will be directed toward confirming
present findings, operation at higher loading rates and examining
various series combinations of facilities to optimize sequences
providing highest treatment efficiencies* These present data and
findings may, or may not, form a basis for final project conclusions.
FWPCA Review Notice
This report has been reviewed in Federal Water
Pollution Control Administration and approved
for publication. Approval does not signify that
the contents necessarily reflect the views and
policies of the Federal Water Pollution Control
Administration.
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I. Introduction
The Mead Corporation was awarded research grant WPrd-55-01-67 by the
Federal Water Pollution Control Administration late in 1966. The
qrant project is entitled "Evaluation of the Role of High Rate
Trickling Filters and Aeration Devices Separately and in Combina-
tion for the Advanced Biological Treatment of Integrated Kraft
Pulp and Paper Mill Effluents." Following tentative budget review,
a pilot plant was engineered and constructed in Chillicothe, Ohio.
A picture of the system is attached as FIGURE 1 in APPENDIX B and
a complete description of the system with schematic diagrams of
the project alternates is contained in APPENDIX B.
The constructed system includes two high rate trickling filters
packed with PVC media, an oxidation ditch with brush aeration, an
earthern lagoon with mechanical surface aeration, and two mechanical
clarifiers. A special flow splitting box permits many possible
combinations of operation for study.
The project began June 10, 1968, and followed the project plan
shown in APPENDIX C. This first project plan was six month's
long and terminated on December 6, 1968.
II. Purpose of Report
It is the purpose of this report to discuss the operation and show
a summary of the data for this six-month period. No rigid mathe-
matical analysis has been attempted on this portion of data nor will
be attempted until more data have been collected in later project
plans.
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III. Project Objectives
A. The overall project objectives as stated in the revised appli-
cation are:
1. To determine effect of influent solids and organics on
biological treatment efficiencies.
2. To evaluate potential of plastic trickling filters as:
a. Main process for biological treatment
b. Roughing filters prior to conventional aerated lagoons
c. Roughing filters prior to and polishing filters after
oxidation ditch utilizing the brush-type aerator.
3. To evaluate role of secondary clarification and sludge return
in conjunction with biological methods described above.
4. To evaluate combinations of the methods of treatment dis-
cussed above in providing higher levels of organic and
solids removals than are conventionally obtained. BOD
removals up to 90 per cent should be possible.
B. The specific objectives for the first six months were fourfold:
1. Learn the overall operation of the multi unit pilot system.
2. Learn the function of each system.
3. Evaluate limited process changes with the systems in
parallel (Alternate A) only.
4. Cross compare operating efficiencies of the four systems.
IV. Summary of Results and Conclusions
Averages referred to in this section are averages over a test
period.
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A. General
Data for the pilot feed (PF), the aerated lagoon (AL), the oxi-
dation ditch (OD), the Mead trickling filter (MTF) and trickling
filter 2 (TF2) have been summarized as averages and ranges for
each test series and are contained in TABLBS Al, A2, A3, and
A4 and Figures Al, A2 and A3 in APPENDIX A.
Computer generated plots of the raw BOD5 data and weekly averages
for each system are contained in Figures Dl, D2, D3, and D4 in
APPENDIX D.
B. Pilot Feed Characteristics
1. The pilot feed consisted of all waste waters generated by
the Chillicothe Division of The Mead Corporation and
settled in their primary clarifier. Not included during the
first six months was the mill bleach plant effluent because
it bypassed the primary plant.
2. Over the first six months, the range of average characteris-
tics for the pilot plant influent were:
a. Temperature! 35 to 41° C
b. BOD5: 172 to 223 mg/1
c. Total Solids: 1047 to 1584 mg/1
Per cent Volatile: 34 to 44%
d. Suspended Solids: 202 to 493 mg/1
Per cent Volatile: 37 to 468
e. Settleable Solids: 0.2 to 6.3 ml/l/hr.
f. Apparent Color: 1216 to 2126
g. pH: 7.5 to 8.6
h. Conductivity: 1015 to 1795 uMhos/cm @ 25° C
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3. This pilot feed was supplied continuously to the pilot
plant except for maintenance downtime which totaled less
than 10 per cent of the time during the first 6 months.
Aerated Lagoon (See Table Al, Figure Al and Figure Dl)
1. The pilot aerated lagoon was essentially free of mechani-
cal difficulties during the first 6 months and all tests
were completed as planned.
2. Concerning dissolved oxygen in the aerated lagoon, the
range of averages for the first six months was 2.6 to 5.3
mg/1 throughout the lagoon which indicates that dissolved
oxygen was not limiting to the biological process.
3. The average temperature of the aerated lagoon contents
o
ranged from 16 to 29 C. which indicates that temperature
is a variable to be considered in data interpretation.
4. Average BODg reduction across the aerated lagoon ranged from
39 to 68 per cent for the test conditions during the first
6 months.
5. The maximum removal of 68 per cent occurred during test AL-i
at 3 days detention time and 1335 lbs./day of BOD5 per acre.
6. Lagoon effluent suspended, total and settleable solids con-
centrations exceeded influent concentrations in all cases.
The range of averages is shown below:
Influent
Effluent
a.
Total Solids (mg/1)
1047 to
1450
1086
to 1604
Per cent Volatile
34 to
41%
30
to 41%
b.
Suspended Solids (mg/1)
202 to
463
288
to 707
Per cent Volatile
40 to
44%
48
to 55%
c.
Settleable Solids (ml/1)
0.4 to
3.9
6
to 49
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7. For aerated lagoon tests, the pounds of BOD^ removed per
pound of ammonia nitrogen used ranged from 11.5 to 16.8.
8. The pilot aerated lagoon facility contains sufficient
flexibility to accomplish the desired test work in the
foreseeable future.
Oxidation Ditch (See Table A2, Figure Al and Figure D2)
1. The pilot oxidation ditch system was plagued with mechanical
problems primarily in the brush aerator itself. Three tests
were successfully completed in the 53 per cent of the time
it was functioning. The brush aerator manufacturer did
provide redesigned parts and it would appear that the
original problems have been solved.
2. Concerning dissolved oxygen in the oxidation ditch, the
range of averages for the completed tests during the first
six months was 1.8 to 6.0 mg/1 throughout the basin which
indicates that dissolved oxygen was not limiting to the
biological process.
3. The average temperature of the oxidation ditch contents
ranged from 23 to 31° C which indicates that temperature
is a variable to be considered in data interpretation.
4. Average B0D5 reduction when the oxidation ditch was run
without clarification and with sludge return ranged from
55 to 71 per cent.
5. The maximum removal under these conditions occurred during
test OD-1 at a detention time of 3 days and an organic
loading rate of 1100 pounds of BOD^ per acre per day.
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6. With clarification and with sludge return the oxidation
ditch after clarification reduced BODs an average of
79 to 88 per cent.
7. The maximum removal of 88 per cent under these conditions
occurred during test QD-EQ3 at one day detention time, an
organic loading rate of 3425 pounds of BOD^ per acre per
day and clarification with 100 per cent sludge return.
8. Oxidation ditch effluent suspended, total and settleable
solids concentrations exceeded influent concentrations
in all cases. The range of averages is shown below:
Effluent
Without With
Sludge Sludge
Influent Return Return
a. Total Solids (mg/1) 1047 to 1528 1074 to 1436 2057-2620
Per cent Volatile 34 to 41* 32 to 39% 37-40%
b. Suspended Solids (mg/1) 202 to 458 371 to 489 1234-1645
Per cent Volatile 41 to 44% 51 to 53% 36-49%
c. Settleable Solids (ml/1) 0.6 to 3.9 3 to 16 59-157
9. The BOD^ removed per pound of ammonia nitrogen used range from
14.3 to 20.7.
10. The pilot oxidation ditch facility contains sufficient flex-
ibility to accomplish the desired test work in the foresee-
able future.
E. Mead Trickling Filter (See Table A3, Figure A2, Figure A3 and
Figure D3)
1. The pilot Mead trickling filter was essentially free of
mechanical difficulties through the first five of a
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planned seven sets of test series. Recycle pump problems
and media handling limitations caused a revision in the
project plan before the final tno tests could be completed.
All tests were completed on schedule.
Concerning dissolved oxygen within the mixing ring under
the filter, the range of averages for the first six
months was 0.2 to 1.7 mg/1. Occasionally, no dissolved
oxygen was present, which would have been limiting to
that biological process occurring within the inner ring.
Both slime growth and activated floe growth are promoted
in the Mead Trickling filter. The observed dissolved
oxygen limitation would only affect the activated sludge
portion of the process.
The average temperature within the system ranged from
o
20 to 34 C which indicates that temperature is a
variable to be considered in data interpretation.
Average BOD^ reduction across the Mead trickling filter
ranged from 33 to 70 per cent for the test conditions
during the first six months.
The maximum removal of 70 per cent occurred during test
MTF-1 at 24 foot heighth, 4000 gallons per day per square
foot hydraulic loading, one to one recycle ratio and
organic loading of 125 pounds per day per 1000 cubic feet.
Suspended, total and settleable solids concentrations were
less than the influent in all tests because samples were
taken after clarification. The settled sludge was recycled
to the top of the filter.
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7. From 14.0 to 39.6 pounds of B0D5 were removed per pound
of ammonia nitrogen used.
8. The Mead trickling filter facility must be slightly modi-
fied if media is to be removed for desired test *ork
beyond the next six months project plan.
Trickling Filter 2 (See Table A4t Figure A2, Figure A3 and
Figure 04)
1. The pilot trickling filter 2 was essentially free of
mechanical difficulties throughout the first six months.
All tests were completed as scheduled.
2. Concerning temperature, the range of averages was 23
to 34° C which indicates that temperature is a variable
to be considered in data interpretation.
3. Average BODs reduction across trickling filter 2 without
clarification ranged from 17 to 56 per cent during the
first six months. Clarification raised the efficiency
to a range of 38 to 81 per cent.
4. The maximum removal of 56 per cent occurred during test
TF2-1 at 24 foot height, 4000 gallons per day per square
foot hydraulic loading, one to one recycle ratio and
organic loading of 125 pounds per day per 1000 cubic feet.
5. Suspended, total and settleable solids concentrations were
less than the influent in all tests mhere samples were
analyzed after settling. Unsettled trickling filter
effluent was the recycle back to the top of the filter.
6. From 10.9 to 65.0 pounds of BOD^ were removed per pound
of ammonia nitrogen used.
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7. The trickling filter 2 facility must be modified the same
as the Mead trickling filter facility discussed above.
G. Cross Comparison
The following general observations can be made on the data from
the first six months of operation:
1. At comparable loading rates for comparable biological
treatment during the same time span (i.e., the same waste
water), the pilot aerated lagoon removed 68 per cent of
the BODg at three days detention while the pilot oxidation
ditch removed a nearly identical 71 per cent. Likewise
at two days detention, the aerated lagoon removed 52 per
cent while the oxidation ditch removed 55 per cent. These
differences may be related to temperature but have not
beei proven to be significant. FIGURE Al compares all
aerated lagoon and oxidation ditch BOD5 test efficiencies.
2. At 4,000 gallons per day per square foot loading rate and
one to one recycle rate both the Mead trickling filter
and the conventional high rate filter achieved 62 to 70
per cent BOD^ reductions. The major difference in the
two operations is that settled sludge is recycled in the
Mead filter vriiile it must be wasted and disposed of from
the conventional filter. FIGURES A2 and A3 compare all
trickling filter BODg test efficiencies.
3. The oxidation ditch running as an extended aeration plant
achieved the highest B0D5 reductions of any system during
the first six months ranging from 79 to 88 per cent removal.
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4. All systems were capable of efficiencies above 60 per cent
BOD^ removal and there was no indication that absolute
limits in treatment efficiencies were reached in any of
the systems.
V. Recommendations on Equipment. Operation and Testing
A. General
It is recommended that:
1. More BOD5 data be gathered under each test condition by
adding a minimum of one week to each test condition for
the oxidation ditch, Mead trickling filter and trickling
filter 2.
2. BCD data for each system be evaluated for the determina-
tion of time required to reach test equilibrium.
3. Continuous plots of solids, and temperature data be
started and maintained on each system with respect to
influent and effluent as has been done for BOD,, data in
FIGURES Dl, D2, D3, and D4.
4. Detailed mathematical analysis of data with respect to
controlling variables be postponed at least until the
third test series has been completed and more complete
data are available.
5. Long term BOD's and oxygen uptake rates be included as
special tests during the next project plan.
6. Nutrient addition rates be adjusted downward as possible
to give credit to existing nutrient concentration in
untreated wastewater.
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Aerated Lagoon
It is recommended that:
1. Less mixing energy be added to the aerated lagoon during
the next test series. Excess energy raises the dissolved
oxygen content higher than necessary and drops the pounds
of BOD^ removed per horsepower hour. It also can suspend
solids and drive them over the weir.
2. BOD's on settled effluent samples be added to the routine
tests.
3. Additional data be obtained at detention times from 2 to
5 days through changing seasons for correlation with
corresponding temperature changes.
Oxidation Ditch
It is recommended that:
1. Future test series be directed toward more of an evalua-
tion of the extended aeration process with respect to
temperature, depth, and detention time with occasional
repeats of previous test conditions.
2. Total and volatile suspended solids determinations on
grab samples of return activated sludge be added to the
routine analysis so as to be able to compute sludge
volume index.
Mead Trickling Filter
It is recommended that:
1. Future test series be directed toward more of an evalua-
tion of hydraulic loadings above 4000 gallons per day per
square foot and recycle ratios of less than two to one with
respect to temperature and depth.
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2. Total and volatile suspended solids determinations on grab
sanples of recycle sludge be added to the routine analysis
so as to be able to compute sludge volume index.
3. The clarifier under the Mead trickling filter be desludged
whenever the recycle sludge settleable solids exceed 500 ml/
1/hr.
4. The trickling filter frame be modified to permit easier
removal of the trickling filter media for possible tests
in the third project plan.
E. Trickling Filter 2
It is recommended that:
1. Future test series be directed similarly to the future
test series for the Mead trickling filter.
2. The trickling filter frame be modified to permit easier
removal of the trickling filter media.
F. Combinations
It is recommended that:
1. Series combinations of the trickling filters be studied
for improved overall BOO^ removals during the second six
months.
2. Series combinations of the oxidation ditch ditch and aerated
lagoon be studied for improved overall BOD5 removals during
the second six months.
Acknowledgement s
The authors wish to acknowledge the preplanning and data compiling
efforts of Jack Robbins, the technical talents of Bob Smith, Dave
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Robinson and Viola Loel and, certainly, the technical advice and
moral support of Ralph Scott prior to and during the first test
series of this joint project.
VII. Procedures
A. Sampling
Samples of main feed, pilot feed and effluent from each system
were obtained using twelve minute interval timers and Little
Giant submersible pumps. Ihe sampling period was sixteen
hours per day (4 P.M. - 8 A.M.). Samples were collected four
days per week.
B. Flow Measurement
Flows into each system were measured by V-notch weirs at the
flow-splitting box each week day morning. Flows into the
lagoon and oxidation ditch were double checked using a five
gallon bucket and stopwatch. Effluent rate from the ditch
was checked also with bucket and stopwatch method.
C. Power Consumption
Power readings on the brush aerator and surface aerator were
obtained on three phase watt meters connected to the respective
units. Monthly readings on all pumps, lights and other uses
were taken by the Chillicothe Area electrical department to
determine kilowatt hours used per month for the project.
D. Nutrient Addition
Nutrients were added to the main feed at a dosage of 100-5-1
(BOD-N-P). Nitrogen was obtained from aqua ammonia 26° Be,
and was added direct from the drum. Phosphorus was obtained
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from 75% phosphoric acid (H3FD4) which was diluted 1 to 8
with water in order to obtain a pumping rate comparable to
the ammonia (approximately 30 ml/min.). Pumping was done
with a dual plexiglass head pump by Precision Chemical Pump
Corporation. Rates were checked daily to insure proper
addition.
E. Temperature and Dissolved Oxygen
Dissolved oxygen was measured by the polarographic method
using a Y. S. I. model 51 oxygen meter by Yellow Springs
Instrument Company. Ihis meter was calibrated in saturated
air at the sample temperature. Occasionally a Winkler test
was also run for comparison.
Temperatures were taken with the thermistor on the Y. S. I.
meter.
F. Conductivity
A Beckman RB-3 battery powered conductivity meter with dip
cell was utilized for conductivity readings. This meter
has manual temperature compensation. It was calibrated with
0.01 normal KCL at a given temperature.
G. pH
A Beckman Zeromatic pH meter was used for pH testing. The
meter was buffered daily.
H. Color
This test was performed on a Bausch and Lamb Spectronic 20
using one inch tubes, 400 millimicron wavelength, and platinum
cobalt standard. Apparent color was run on the sample as
received. True eolor was obtained by centrifuging the sample,
- 14 -
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and reading the supernatant solution. Unless noted, all
color values on the summary sheets are apparent color.
Settleable Solids
This test was done as described in the 12th edition of
Standard Methods for the Examination of Water. Sewage
and Industrial Wastes. 1965. pages 425, 426.
Total and Volatile Suspended Solids
These tests were performed as described on pages 424, 425 of
Standard Methods except for the use of glass fiber filter
paper instead of the asbestos mat. Sample volume was 50 ml,
rather than 100 ml. A Mettler One Pan Automatic balance
weighing to 4 places was used.
Total and Volatile Total Solids
Page 423 of Standard Methods gives the procedure used for
testing of total solids. The Mettler balance was used for
weighing.
BOD
5
Five day biochemical oxygen demand tests were performed
essentially as stated in Standard Methods, pages 415 -
421. Three hundred (300) ml bottles were used for the
tests. A 20° C water bath was substituted for the refrigerator-
incubator on August 1, 1968. An average of 43 IDO values of
dilution water showed 7.7 mg/1. After 5 days incubation, the
dilution water showed an average dissolved oxygen of 7.3 mg/1
resulting in 0.4 mg/1 depletion due to seed.
The seed used was Paint Creek water above the mill clarifier out-
fall. Amounts used ranged from 2.5 to 5.0% to keep the desired
depletion to 0.2 - 0.6 mg/1.
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A standard glucose-glutamic acid solution (BOD 221 - 10) was
checked frequently, resulting in an average value of 229 mg/1.
The initial dissolved oxygen in the sample and the dissolved
oxygen in the seeded dilution water after five days incuba-
tion were used as the initial dissolved oxygen in calculating
B0Ds results.
M. Total Nitrogen
The procedure for this test is the total Kjeldahl method as
described in Standard Methods, pages 402 - 404. The only
deviation from the standard test was in using a new indi-
cator specially made for ammonia. This is a commercial
product called N-point available from Matheson-Coleman-Bell.
N. Ammonia Nitrogen
The distillation method for ammonia nitrogen was used. This
method is found in Standard Methods, pages 391 - 392. Boric
Acid was used as the receiver in the total and ammonia nitrogen
testing.
O. Nitrate Nitrogen
This determination was made by the polarographic method using
the Sargent Manual Polarograph, Model III, and is essentially
the test as shown in Standard Methods, pages 398 - 400. All
samples submitted to chemical testing for nitrogen were pre-
served with 0.8 ml sulfuric acid per liter of sample.
P. Total Phosphate
Sample was wet ashed before starting test. The phosphate test
is derived from Standard Methods, pages 234 - 236. It has been
modified from Boltz by substituting sodium molybdate and
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hydrazine sulfate for ammonium molybdate and stannous chloride
respectively. A blue color is formed which is read on the DK-2
Beckman Spectrophotometer at 830 millimicrons. All soluble
nutrient tests were centrifuged for thirty minutes at 85 G's.
Tests were performed on the supernatant liquid.
Q. Velocities and Sludge Depth
Flow direction and velocity were obtained in the oxidation
ditch and lagoon using the Marine Advisors Q-9 current meter.
Sludge depths in the ditch and lagoon were obtained using a
photo electric cell fabricated by Mead Research Instrument
Department.
R. Data Analysis
All daily solids (total and suspended) and BODg computations
were submitted to the computer group for calculation and
tabulation on the digital computer. The raw data was submitted
approximately every three weeks which resulted in a short time
lag in obtaining final results; however, this presented no
problem in coordinating the data.
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Discussion
The facilities for the effluent treatment project consists of
four basic treatment devices with the flexibility to run these
devices in parallel or in nearly any set of combinations. There
is an aerated lagoon, an oxidation ditch and two trickling
filters. One of the trickling filters (MTF) is combined with
a mixing chamber and settling tank underneath. The second
trickling filter (TF2) can be combined with a clarifier (CL2)
or run without clarification. The clarifier may also serve
with the oxidation ditch.
The key to flexible operation is the flow splitting box located
atop the trickling filter tower. The flow splitting box is made
up of four chambers, each of which proportions a flow into two
parts and one chamber which controls the influent flow. The first
two chambers are fed by the influent, the third by TF2 effluent
and the fourth by MTF underflow. Outlets from the splitting box
go to every point where wastes are applied.
This first six-month period consisted of parallel operation of
the basic treatment devices under lower hydraulic and organic
loadings. The following test series will include higher loadings,
combinations of devices and repeats of some test runs under
different ambient temperature conditions.
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APPENDIX A
Test Results
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SUMMARY OF B0D5 EFFICIENCY - FIRST 6 MONTHS
PILOT AERATED LAGOON a OXIDATION DITCH
MEAD FWPCA PROJECT
100
90 -
<
>
o
2E
UJ
oc
tO
a
o
CO
o
oc
Ui
Q.
80
70
60
50
40
30 -
? 23° C
#31#C
6 29#C 1
31°C
29°C
6 22CC
9l6°C
20
10
CODE
Aerated Lagoon
© No Recycle
Oxidation Ditch
• No Recycle
® Sludge Return
2 3 4 5
DETENTION TIME IN DAYS
FIGURE A1
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SUMMARY OF B0D5 EFFICIENCY-FIRST 6 MONTHS
PILOT TRICKLING FILTERS
MEAD - FWPCA PROJECT
HYDRAULIC LOADING vs. EFFICIENCY
100
90
80
70
60
| No Recycle
Recycle s 11
Recycle s 2 1 |
1 i
1 1
-
O 0
Oft
•
•
G
•
O
i
t
o o
-
•
-
-
l i
CODE
G Mead Trickling Filter
• Clarified Trickling Filter 2
>
50
40
30
20
10
2000 4000 0 2000 4000 6000 8000 0 2000 4000
HYDRAULIC LOADING IN GALLONS PER DAY PER SQUARE FOOT
FIGURE A2
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SUMMARY OF BOD5 EFFICIENCY-FIRST 6 MONTHS
PILOT TRICKLING FILTERS
MEAD-FWPCA PROJECT
ORGANIC LOADING vs EFFICIENCY
100
90
80
70
§
1 60
UJ
q:
»
o
2 50
UJ
g 40
UJ
Q.
30
30
10
| No Recycle
Recycle = 1:1
Recycle - 2 -1 |
i i
1
-
G °
G»
•
•
0
•
0
• •
® 0
-
•
-
CODE
0 Mead Trickling Filter
• Clarified Trickling Fitter 2
0 100 200 0 100 200 0 100 200
ORGANIC LOADING IN POUNDS PER DAY BOD5 PER 1000 CUBIC FEET
FIGURE A3
-------
APPENDIX B
Pilot System
-------
-------
APPENDIX B
EXHIBIT B1 DESCRIPTION OF PILOT SYSTEM
Figure B1 is an overall view of the pilot treatment system. A
description of this system follows.
A. Pilot Aerated Lagoon
1. Description
Square earthen basin with rounded corners and sloping
sides lined with PVC and crossed laterally with a steel
truss bridge for walkway and surface aerator support.
2. Size
Volume at 8-foot depth is 250,000 gallons.
3. Special Equipment
3 hp turbine aerator by Mixing Equipment Company.
4. Flexibility
a. Lagoon depth (and surface area and volume) can be
varied from 2 feet minimum to 8 feet maximum by
means of adjustable overflow dam.
b. Lagoon detention time can be varied from 1.5 days
to 5 days by means of flow splitting arrangement
provided.
c. Aerator power consumption can be varied by adjust-
ment of submergence at the aerator shaft and/or
main support and change of impeller. Actual power
consumption will be monitored by 3-phase wattmeter
on loan from Mead Research.
d. Bottom sludge can be monitored frcro the bridge by
means of special equipment on loan from Mead Research.
e. Lagoon velocities can be monitored from the bridge
by means of special equipment on loan from Mead
Research.
f. Lagoon can be run in series behind any one of the
other unit treatment processes in this pilot plant.
g. The lagoon, as constructed, is a complete system
in itself and does not depend upon any other unit
for its independent operation except for the flow
splitting box and main feed pumps.
-------
B. Pilot Oxidation Ditch
1. Description
Rectangular reinforced concrete basin with vertical sides
and rounded ends of steel plate. Massive concrete pillars
support brush-type aerator. Center column supports flow
baffles, mid feather, and steel walkway. Space limitations
required major porticn of construction above ground.
2. Size
11 foot height for 10 foot maximum liquid depth; constant
surface area of 3005 square feet. Volume at 10 foot depth
is 225,000 gallons.
3. Special Equipment
7 hp massive rotor aerator by Beloit Passavant.
4. Flexibility
a. Ditch depth (and volume) can be varied from 4 feet
minimum to 10 feet maximum by means of unique flexible
joint embedded in ditch bottom.
b. Ditch retention time can be varied from less than 1 day
to 5 days by means of flow splitting arrangement provided.
c. Ditch can be completely emptied by gravity due to con-
struction above ground.
d. Ditch contents cam be overflowed at any depth at or
below desired surface depth by means of unique float
and valve device mounted on flexible joint embedded
in ditch bottom.
e. Ditch contents can be overflowed in channel either
ahead of or behind brush aerator (at any depth as
just discussed).
f. Ditch feed can be added into the channel either ahead
of or behind brush aerator.
g. Basin velocities can be monitored in the channel ahead
of, behind, and opposite the aerator with special equip-
ment on loan from Mead Research by use of the special
walkway provided. The vertical sides permit well defined
velocity patterns not possible in less expensive con-
struction.
h. Basin sludge can be monitored at representative points
from this walkway by means of special equipment on loan
from Mead Research.
-------
i. Aerator power consumption can be varied by adjust-
ment of submergence with level float and/or by
removing six-inch increments of brush width. Actual
paver consumption will be monitored by 3-phase
wattmeter on loan from Mead Research.
j. Oxidation ditch can be run in series ahead of or
behind trickling filters and ahead of aerated lagoon.
k. Oxidation ditch can be run as conventional activated
sludge with measured sludge return from the REX
secondary clarifier.
1. The oxidation ditch, as constructed, is a complete
system in itself and does not depend upon amy other
unit for its independent operation except for the flow
sp?v.itting box and main feed pumps.
C. Trickling Filters
1. Description
Two columns of high rate media in three 8-foot removable
sections supported on 4-story steel beam structure. This
structure also supports access stairs and walkways, media
storage space on each level, and unique flow splitting
boxes and piping for other systems.
2. size
Each trickling filter media column has 16 square feet
of surface area and is 24 feet high.
3. Special Equipment
Koroseal Vinyl Rack media by B. F. Goodrich.
4. Flexibility
a. Each column can be run as separate trickling
filter independent of remaining column.
b. Columns can be run in parallel.
c. Columns can be run in series.
d. Columns can be packed from two feet to 24 feet
in depth in two-foot increments.
e. Sludge from one trickling filter and filtrate from
other can be recycled to respective trickling filters
by means of unique flow splitting box provided.
Recycle rates up to 2:1 are possible.
-------
f. Hydraulic loadings in excess of 8000 gallons per
day per square foot are possible.
g. Monitoring at any level in media column without
affecting operation is possible due to unique
exposed construction and removable panels.
h. Storage space for removed media is provided on
each level of steel structure.
i. The trickling filters can be run in series or
parallel ahead of either the oxidation ditch
or the aerated lagoon.
j. Trickling filter 2 can be run ahead of REX
secondary clarifier.
k. The two trickling filters, as constructed, are
each complete systems and do not depend upon any
other unit for independent operation except for
the flow splitting box and main feed pumps.
D. Clarifiers
1. Description
One rim flow with sludge arm and one center feed with
cone bottom and center mixing, both of steel plate
construction.
2. Size
Rim flow unit is 12 feet in diameter by 12 feet high
for a total volume of 9300 gallons and a detention
greater than one hour for high design flows. Cone
bottom unit is 15 feet in diameter by 11.5 feet deep
for a total volume of 10,000 gallons, of which 2850
gallons is in mixing zone and 7150 gallons is in
clarifier zone for greater than one hour detention at
high design flows.
3. Special Equipment
Rim Flow, Tow Bro Clarifier Mechanism for 12-foot unit
by REX Chain Belt.
4. Flexibility
a. Cone bottom unit must be used with Trickling Filter
Number 1.
b. REX unit can be used with either Trickling Filter
Number 2 or Oxidation Ditch.
-------
c. sludge withdrawal rate can be varied as required by means
of unique pumping and piping system. Sludge can be
wasted or put back in respective systems.
d. Both clarifiers can be completely emptied by pumps
provided.
E. Pumps and Piping
1. Description and Flexibility
Two main feed pipes and six small process pumps permit
the return of virtually any treated or untreated waste
water to amy pilot treatment system. Sixteen independent
and dependent flow systems have been provided.
2. Special Equipment
Pumps by Goulds and Yeoman; piping of plastic, PVC, and
black iron; cast iron valves.
F. Electrical
1. Description and Flexibility
550 volt, 3-phase electricity was brought to the control
center at the pilot site. Separate breakers and switches
are provided for each of the two main feed pumps, each of
the six process pumps, the REX clarifier mechanism, the
Mixco aerator, and the Beloit brush. A transformer steps
the voltage down to 110-220 volts for pilot area lighting,
control center lighting and receptacles, said sampling
station receptacles at each pilot unit.
-------
SCHEMATIC DIAGRAM OF PILOT TREATMENT PLANT
The Mead Corporation - Chillicothe, Ohio
Clarified Mill Effluent
MEAD - FWPCA PROJECT
"*0"
Bleach Plant Effluent
I I
Excess To Overflow "TJiLr*" Excess To
Overflow
OXIDATION
DITCH
CLARIFIER
TRICKLING
FILTERS
-*X~
I
Excess
Sludge
CLARIFIER
Discharge
-------
SCHEMATIC DIAGRAM OF PILOT TREATMENT PLANT
The Mead Corporation - Chill i cot he» Ohio
Clarified Mill Effluent
Bleach Plant Effluent
Excess To Overflow -<-| |f| [-> Excess To
Overflow
MEAD - FWPCA PROJECT
ALTERNATE A
All Systems In Parallel
Ll I LL
RETURN TO ANY SYSTEM
TRICKLING
FILTERS
Excess
Sludge
CLARIFIER
Discharge
-------
SCHEMATIC DIAGRAM OF PILOT TREATMENT PLANT
The Mead Corporation - Chillicothe, Ohio
Clarified Mill Effluent
H-
OQ
c
l-i
fD
W
MEAD-FWPCA PROJECT
ALTERNATE B
Filter Ahead Of Lagoon
Recycle
\
-J
L
J
.
NO.
1
1
u
Excess
Sludge
Discharge
-------
SCHEMATIC DIAGRAM OF PILOT TREATMENT PLANT
The Mead Corporation - Chill i cot he, Ohio
Clarified Mill Effluent
MEAD - FWPCA PROJECT
ALTERNATE C
Filter Ahead Of Oxidation Ditch
Discharge
-------
SCHEMATIC DIAGRAM OF PILOT TREATMENT PLANT
The Mead Corporation - C hi 11 i cot he, Ohio
Clarified Mill Effluent
MEAD - FWPCA PROJECT
ALTERNATE D
Oxidation Ditch Ahead Of Filter
Excess
Sludge
Discharge
-------
SCHEMATIC DIAGRAM OF PILOT TREATMENT PLANT
The Mead Corporation - Chill i cot he 9 Ohio
*r
Clarified Mill Effluent
Bleach Plant Effluent
Excess To Overflow
|*| | |->- Excess To
*—¦1^ Overflow
MEAD - FWPCA PROJECT
ALTERNATE E
Oxidation Ditch Ahead Of Lagoon
Excess
Sludge
Discharge
-------
SCHEMATIC DIAGRAM OF PILOT TREATMENT PLANT
The Mead Corporation - Chilli cot he 9 Ohio
Clarified Mill Effluent
Bleach Plant Effluent
Ijii
rS
Excess To Overflow -*-| 11| Excess To
Overflow
UL
RETURN TO ANY SYSTEM
MEAD - FWPCA PROJECT
ALTERNATE F
Filters In Series
Recycle
TRICKLING
FILTERS
NO.
2
Recycle
r
NO.
1
OXIDATION
DITCH
CLARIFIER
-<
-
-------
SCHEMATIC DIAGRAM OF PILOT TREATMENT PLANT
The Mead Corporation - Chillicothe9 Ohio
Clarified Mill Effluent
Bleach Plant Effluent
MEAD - FWPCA PROJECT
ALTERNATE G
Filter To Oxidation Ditch To Lagoon
Excess To Overflow |fj I*" Excess To
Overflow
I I If
n. I I I
Excess
Sludge
Discharge
-------
APPENDIX C
Project Plans
-------
No. 1
First 6 Months
COMPLETED PROJECT PLAN FOR PILOT LAGOON AND OXIDATION DITCH
MEAD-FWPCA PROJECT
Actual
Beginning
Weeks Hydraulic Rate
Detention
BOD Loadina
Rate
Sludge
Return
Clarification
Alternate
Test
Date
Required Depth Gallons
Davs qpm
Acres
ppd/Ac
ppd/lOOOcf
qpm
Provided
Oxidation Ditch
A
Equilibrium - 1
OD-1
6-17-68
7- 8-68
3 6.75
3
152,000
3 35.2
O.07
1,100
3.8
0
None
A
Equil. - 2
OD-2
Contingency
7-29-68
8-19-68
3 7.0
3
8
157,500
2 54.6
O.07
1,725
5.8
0
None
A
Equil. - 3
OD - 3
10-28-68
11-25-68
4 7.0
2
157,500
1 109.4
0.07
3,425
11.4
60
Clarifier 2
TOTAL
3 Tests Completed
18 Operating
Weeks
Aerated Lagoon
A
Equilibrium - 1
AL-1
6-10-68
7- 8-68
4 6.75
3
175,000
3 40.6
O.07
1,335
4.0
O
None
A
Equil. - 2
AL-2
7-29-68
8-19-68
3 6.75
3
175,000
2 60.8
0.07
2,005
6.1
0
None
A
Equil. - 3
AL-3
9- 9-68
lO- 7-68
3 6.75
3
175,000
4 30.4
0.07
995
3.0
0
None
A
Equil. - 4
AL-4
10-21-68
11-11-68
3 6.75
4
175,000
3 40.6
0.07
1,335
4.0
0
None
TOTAL
4 Tests Completed
26 Operatinq
Weeks
Note: Nutrients were added into the feed of all systems at a 100s5:l BOD:N:P ratio from 6-10-68 through 12-6-68.
FIGURE C 1
-------
No. 1
First 6 Months
COMPLETED PROJECT PLAN FOR PILOT TRICKLING FILTERS
MEAD-FWPCA PROJECT
Actual
Hydraulic
Beginning
Weeks
Rate
Feed
Heighth
BOO Rate
Recvcle
Rate
Clarif ication
Alternate
Test
Date
Required
qpdpsf
qpm
Feet
ppd/1000cf
R/I Ratio
qpm
Provided
Mead Trickling Filter
A
Equilibrium
- 1
6-10-68
4
4000
22.2
24
125
1:1
22.2
Clarifier 1
MTF-1
7- 8-68
3
A
Equil.
- 2
7-29-68
1
6000
33.3
24
188
1:1
33.3
Clarifier 1
MTF-2
8- 5-68
2
A
Equil.
- 3
8-19-68
1
8000
44.4
24
250
1:1
44.4
Clarifier 1
MTF-3
8-26-68
2
A
Equil.
- 4
9- 9-68
1
2000
11.1
24
62
1:1
11.1
Clarifier 1
Contingency
9-16-68
1
MTF-4
9-23-68
2
A
Equil.
- 5
10- 7-68
1
4000
22.2
24
125
1:1
22.2
Clarifier 1
MTF-5
10-14-68
2
A
Equil.
- 6
10-28-68
1
2660
29.6
22
182
0
0
Clarifier 1
MTF-6
11- 4-68
2
A
Equil.
- 7
11-18-68
1
1330
14.8
22
91
0
0
Clarifier 1
MTF-7
11-25-68
2
TOTAL
7 Tests Completed
25 operatinq weeks
Tricking Filter 2
A
Equilibrium
- 1
6-10-68
4
4O00
22.2
24
125
1:1
22.2
Clarifier 2
TF2-1
7- 8-68
3
A
Equil.
- 2
7-29-68
1
2000
22.2
24
125
0
0
Clarifier 2
TF2-2
8- 5-68
2
A
Equil.
- 3
8-19-68
1
4000
44.4
24
250
0
0
Clarifier 2
TF2-3
8-26-68
2
A
Equil.
- 4
9- 9-68
1
4000
22.2
16
187
1:1
22.2
Imhoff Cone
Contingency
9-16-68
1
TF2-4
9-23-68
2
A
Equil.
- 5
10- 7-68
1
4000
14.8
16
125
2:1
29.6
Imhoff Cone
TF-2-S
10-14-68
2
A
Equil.
- 6
10-28-68
1
4000
14.8
24
84
2:1
29.6
Imhoff Cone
TF2-6
11- 4-68
2
A
Equil.
- 7
11-18-68
1
4000
22.2
24
125
1:1
22.2
Imhoff Cone
TF2-7
11-25-68
2
TOTAL
7 Tests Completed
25 operatinq weeks
Note: Nutrients
were
added
into the
feed of all systems at
a 100:5:1
B0D:N
:P ratio
from 6-10-68
through 12-6
-68.
FIGURE C 2
-------
No. 2
Second 6 Months
PROPOSED PROJECT PLAN FOR PILOT LAGOON AND OXIDATION DITCH
MEAD-FWPCA PROJECT
Tentative
Beginning
Weeks Hydraulic Rate
Detention
BOD Loading
Rate
Clarification
and
Alternate
Test
Date
Allowed Depth
Gallons
Davs aom
Acres
ppd/Ac
ppd/lOOOcf
Sludae Return
Comment s
Oxidation Ditch
A
Equilibrium - 4
OD-4
1- 6-69
2-10-69
5
4
4.0
90,000
1 62.5
0.07
1,960
11.4
Yes
A
Equil. - 5
OD-5
3-10-69
4- 7-69
4
4
4.0
90,000
2 31.2
0.07
960
3.3
Yes
E
Equil. - 6
OD-6
Contingency
5- 5-69
6- 2-69
4
4
1
5.6
126,000
1 87.5
0.07
1,880
11.4
Yes
PF is Feed.
TOTAL
3 Tests
26
Weeks
Aerated Lagoon
A
Equilibrium - 5
AL-5
1- 6-69
2-10-69
5
4
6.75
175,000
5 24.4
0.07
800
2.4
No
A
Equil. - 6
AL-6
3-10-69
3-17-69
1
3
6.75
175,000
4 30.4
0.07
995
3.0
No
A
Equil. - 7
AL-7
4- 7-69
4-14-69
1
3
6.75
175,000
3 40.6
0.07
1,335
4.0
No
E
Equil. - 8
AL-8
Contingency
5- 5-69
6- 2-69
4
4
1
8.0
250,000
2 87.0
?
6.1
No
OD is Feed.
TOTAL
4 Tests
26
Weeks
Note: Nutrients will be added to the main pilot feed in varying quantities as needed to maintain a total ratio
of 100-5-1 B0D:N:P. Past history of approximately 5 mg/1 N and 0.5 mg/1 P in wastewater leaves initial
net of 4 mg/1 N and 1.3 mg/1 P to be added.
FIGURE C 3
-------
No. 2
Second 6 Months
PROPOSED PROJECT PLAN FOR PILOT TRICKLING FILTERS
MEAD-FWPCA PROJECT
Alternate
Mead Trickling Filter
Test
A
Equilibrium ¦
MTF-8
A
Equil. -
9
MTF-9
A
Equil. -
10
MTF-10
F-l
Equi1.
- 11
MTF-11
A
Equil. -
12
MTF-12
F-2
Equil. -
13
MTF-13
Contingency
6 Tests
Tentative
Beginning
Date
1- 6-69
1-20-69
2-10-69
2-17-69
3-10-69
3-17-69
4- 7-69
4-14-69
5- 5-69
5-12-69
6- 2-69
6- 9-69
Weeks
Allowed
2
3
1
3
1
3
1
3
1
3
1
3
1
Hydraulic
Rate
qpdpsf
Feed Heighth BOD Rate
qpm Feet ppd/lOOOcf
Recycle Rate
R/I Ratio qpm Comment
6000
33.3
24
188
1:1
33.3
6000
44.4
24
188
0.5:1
22.2
40 OO
35.5
24
125
0.5:1
8.9
4000
22.2
24
125
1:1
22.2
PF
is Feed
6000
33.3
24
188
1:1
33.3
4000
22.2
24
?
1:1
22.2
TF
2 is Feed
TOTAL
26 Weeks
Trickling Filter 2
A
Equilibrium - 8
TF2-8
1- 6-69
1-20-69
2
3
6000
33.3
24
188
1:1
33.3
A
Equil. - 9
TF2-9
2-10-69
2-17-69
1
3
6000
44.4
24
188
0.5:1
22.2
A
Equil. - lO
TF2-10
3-10-69
3-17-69
1
3
4000
35.5
24
125
0.5:1
8.9
F-l
Equil. - 11
TF2-11
4- 7-69
4-14-69
1
3
4000
22.2
24
j
1:1
22.2
MTF is Feed
A
Equil. - 12
TF2-12
5- 5-69
5-12-69
1
3
6000
33.3
24
188
1:1
33.3
F-2
Equil. - 13
TF2-13
Contingency
6- 2-69
6- 9-69
1
3
1
4000
22.2
24
125
1:1
22.2
PF is Feed
TOTAL 6 Tests 26 Weeks
Note: Nutrients will be added to the main pilot feed in varying quantities as needed to maintain a total ratio
of 100-5-1 B0D:N:P. Past history of approximately 5 mg/1 N and 0.5 mg/1 P in wastewater leaves initial
net of 4 mg/1 N and 1.3 mg/1 P to be added.
FIGURE C 4
-------
APPENDIX D
Additional Data
-------
PAGE NOT
-«r
sk
AVAILABLE
DIGITALLY
-------
PAGE NOT
tc
k\
vx
vx-
AVAILABLE
DIGITALLY
-------
APPENDIX E
List of Symbols
-------
APPENDIX E
List of Symbols
Symbol
AL
bod5
°C
EQ
GPM
GPDPSF
MC
mg/1
ml/l/hr
Mhos/cm
MTF
OD
PF
PPD
PPD/1000 CF
Identif ication
Pilot aerated lagoon. Symbol was used primarily in desig-
nating test series; i.e., AL-1 meant test series one on the
pilot aerated lagoon.
Conventional 5-day biochemical oxygen demand.
Degrees Celcius (formally Centigrade)
Equilibrium period. Symbol was used primarily in designating
extent of test series set aside after changing operational
parameters in order to equilibrate the biological process to
the new conditions.
Gallons per minute flow rate.
Gallons per day per square foot of surface area.
Main clarifier effluent from the Chillicothe Division of The
Mead Corporation which served as influent to the pilot treat-
ment plant. MC is not to be confused with PF which was the
same wastewater after supplemental nutrients had been added.
Milligram per liter
Milliliters per liter in one hour
Conductivity units read as micro Mhos per Centimeter
Mead trickling filter or trickling filter one. Symbol was
used primarily in designating test series.
Pilot oxidation ditch. Symbol was used primarily in
designating test series.
Pilot feed or influent to pilot plant after supplemental
nutrients had been added.
Pounds per day
Pounds per day per 1000 cubic feet of volume
TF2
Trickling filter 2. Symbol was used primarily in designating
test series.
-------
APPENDIX F
Daily Log Sheet Form
-------
Date
FEED PUMP OPERATION
Clarified Feed Pump
Bleach Feed Pump
Daily Log of Operation
Mead-FWPCA Project
Page 1
Work by
Reading
Time
Hours of Operation
% Total
Time
Check if
Reset to 0
Actual
Possible
SYSTEM FLOW CONTROL
Clarifier Feed
Bleach Feed
Total
Weir
Ident.
Inches of
Overflow
Seconds
to 10 gal.
Actual
Flow-qpm
Desired
Adjust¦
Trickling Filter 1
Feed
Check Overflow
Recycle
Return to Clar. 1
Trickling Filter 2
Feed
Check Overflow
Recycle
Aerated Lagoon
Feed
Check Feed
Check Overflow
Leak
Oxidation Ditch
Feed
Check Feed
Check Recycle
Clarifier 2
Feed
Other (specify)
SAMPLE COLLECTION
Main Feed
Timer
Ident.
Hours of
Collection
Liters
Collected
Timer
Adjust
Imhoff Cone
Setup
System Effluents
Tricklinq Filter 1
Trickling Filter 2
Aerated Laqoon
Oxidation Ditch
Clarifier 2 i
CHEMICAL ADDITION
Aqua Ammonia
Phosphoric Acid
Defoamer (
Dilution
_:1
":l
":1
Flow-.-ml per minute
Actual
Desired
Adjust
Check if
New Batch & Time
ELECTRICAL CONTROL
Surface Aerator Loaded Kilowatts
No Load Kilowatts
Brush Aerator Loaded Kilowatts
No Load Kilowatts
HP Submergence
HP Depth
HP Submergence
HP Depth |
(OVER)
-------
Daily Log (Continued)
Mead-FWPCA Project
Page 2
Date
Weather
Work by
Air Temp
Sample Point
Time
Temp
°C
D.O.
mg/l.
Sett. Solids
ml/l/hr.
Conductivity
fiMhos/cm®25 C
Comments
TRICKLING FILTER 1
XXXXXX XXXXXX XXXXXX CXXXXXXXXXXXXX ocxxxxxxxxxxxxx xxxxxxxxxxxxxxxxxxxxx
Feed
Recycle
l2l
-LSI
Inner Ring
Overflow
TRICKLING FILTER 2
XXXXXXCXXXXXXXXXXXXOCXXXXXXXXXXXXxxxxxxxxxxxxxxxxxxxxx
Feed
Recycle (Overflow)
AERATED LAGOON
Feed
Point 1
Point 2
Point 3
Point 4
Point 5
Overflow
OXIDATION DITCH
Feed
Point 1
Point 2
Point 3
Point 4
Overflow
CLARIFIER 2
Feed
Overflow
Sludge
MILL CLARIFIER
Influent
Effluent
XXXXXX ocxxxx: KXXXXX ocxxxxxxxxxxxx xxxxxxxxxxxxxxxxxxxxx
xxxxxx xxxxxx: cxxxxxx xxxxxxxxxxxxxxxxxxxxx
XXXXXXKXXXXX)
XXXXXX (XXXXXXXXXXXXX
xxxxxx xxxxxx: :xxxxxx
cxxxxxxxxxxxxxxxxxxxxxxxxxxxxxxxxxxx
Sal
121
ocxxxxxxxxxxxx: cxxxxxxxxxxxxxx xxxxxxxxxxxxxxxxxxxxx
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