SECOND SEMI - ANNUAL
(JANUARY THROUGH JUNE, 1969)
DATA REPORT
FOR
MEAD - FWPCA PROJECT
ON
ADVANCED BIOLOGICAL TREATMENT
MEAD
research
THE MEAD CORPORATION
CHILLICOTHE, OHIO

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SECOND SEMI-ANNUAL DATA REPORT
The Evaluation of High Rate Trickling Filters
and Aeration Devices for the Treatment of
Integrated Kraft Paper Mill Effluents
FEDERAL WATER POLLUTION CONTROL ADMINISTRATION
DEPARTMENT OF THE INTERIOR
by
The Mead Corporation
Chillicothe, Ohio

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FWPCA REVIEW NOTICE
This report has been reviewed in the Federal Water Pollution Con-
trol 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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ABSTRACT
Treatment efficiencies of trickling filters and oxidation lagoons have
been analyzed under differing conditions of loading. These treatment
devices have been operated separately and together to determine which
arrangements provide the best advantage for treatment of wastes from
the Pulp and Paper industry. This data report summarizes the second
six month's data and shows relationships between efficiency of treat-
ment and loading. No firm conclusions from this interim data are pre-
sented in this report. A tentative plan for the third six month period
is presented.
Key Words: Efficiencies/Trickling Filters/ Oxidation Lagoon/ Pulp and
Paper Industry.
This project has been authorized, supported, and financed in part by
the Federal Water Pollution Control Administration, Department of in-
terior persuant to the Federal Water Pollution Control Act under Re-
search and Development Grant Number 12040 EMY.
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ii
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3
6
6
7
9
10
11
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16
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CONTENTS
Introduction
Conclusions
Summary of Results
A.	General
B.	Pilot Feed
C.	Aerated Lagoon
D.	Oxidation Ditch
E.	Trickling Filter 1
F.	Trickling Filter 2
G.	Combinations of Units
Acknowledgments

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SECTION 1
INTRODUCTION
The information presented herein covers the second portion of a
four-phase project plan. This is an interim report consisting
of preliminary data derived from operating the several treatment
systems in series and in parallel to determine potential treat-
ment efficiencies. Continuing experimentation will be directed
toward confirming present findings, examining various series com-
binations of facilities to optimize sequences providing highest
treatment efficiencies. These present data and findings may, or
may not, form a basis for final project conclusion.
This report supplements the first semi-annual data report pub-
lished in January, 1969. The studies performed were financed in
part by FWPCA Research and Demonstration Grant 12040 EMY (origi-
nally WPRD 55-01-67) entitled "Evaluation of the Role of High
Rate Trickling Filters and Aeration Devices Separately and in
Combination for the Advanced Biological Treatment of Integrated
Kraft Pulp and Paper Mill Effluents". The second period of study
began operation on February 3, 1969 and terminated June 27, 1969.
It is the purpose of this report to analyze the data from the
second period as well as from the first to determine relation-
ships between the variables and to present the plan to be fol-

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lowed during the third period of operation. The plan for the third
period should be made up of combinations of units, each of which
have shown potential as efficient treatment schemes.
The overall project objectives as stated in the revised application
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 treat-
ment discussed above in providing higher levels of
organic and solids removals than are conventionally
obtained. BOD removals up to 90% should be possible.
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SECTION 2
CONCLUSIONS
Figure A1 indicates that Aerated Lagoon treatment without clari-
fication can achieve BOD5 removals as high as 78 percent at five
days retention and that with clarification can achieve BQD5 re-
movals as high as 84 percent at four days retention.
Figure B1 indicates that the Oxidation Ditch can achieve BOD^
removals as high as 69 percent without clarification at three
days retention and as high as 85 percent with clarification and
sludge return at one day retention.
Figure CI shows that Trickling Filter 1 BOD5 removal efficiency
decreases with hydraulic loading and that the data (averages for
each test) can be contained within a linear envelope of height
27 percent.
Figure C7 shows that Trickling Filter 1 BQD5 removal efficiency
decreases with organic loading and that the data (averages for
each test) can be contained within a linear envelope of height
20 percent.
Figure D1 shows that Trickling Filter 2 BOD5 removal efficiency
(lab settled effluent samples) decreases with hydraulic loading
and that the data (averages for each test) can be contained
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within a linear envelope of height 29 percent.
Figure D7 shows that Trickling Filter 2 BOD5 removal efficiency
(lab settled effluent samples) decreases with organic loading and
that the data (averages for each test) can be contained within a
linear envelope of height 20 percent.
If the organic loading to Trickling Filter 2 is calculated in-
cluding the recycle organic loading and if removal efficiency is
calculated including recycle (that which leaves the filter against
that which enters the filter, recycle included), then a plot of
BOD5 removal data versus organic loading data can be contained in
a linear envelope of height 12 percent (see Figure D8). If the
centerline of this envelope is used as an equation describing the
data, it can be written as follows:
Percent Removal = 54.5 - .075X -6
where X is the organic loading in lbs/day/1000 cu. ft.
When the same TF2 BOD5 removal calculations as in the above are
plotted against hydraulic loading, the data can be contained in
an envelope of height 12 percent (see Figure D9).
From the above, it appears that trickling filter BOD5 removal
efficiency can best be predicted based on total organics into
and out of the filter, including recycle. The TF2 recycled organic
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loading was calculated using settled BOD5. The same approach could
not be taken with Trickling Filter 1 because no settled BOD5 data
was available for the recycle.
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SECTION 3
SUMMARY OF RESULTS
A. General
In this report, emphasis will be made on weekly averages of
data, since this interval lacks the scatter shown by daily
data yet is short enough to show variation with time.
B• Pilot Feed Characteristics
The pilot feed was clarified effluent from the Chillicothe
Division of The Mead Corporation. Sixty-five percent of the
total mill bleach plant effluent entered the clarifier from
December 26, 1968 to June 11, 1969. During the remaining
time, the pilot feed did not contain bleach plant wastes.
Over the second six months, the extreme values for the pilot
plant feed were:
Temperature
Daily Data
27°C. - 40°C
Weekly Averages
29°C. - 38°C.
BOD
5
94-454 mg/1
156-282 mg/1
Total Solids
1220-4370 mg/1
1410-2100 mg/1
Percent Volatile TS 17-48
Suspended Solids
40-1474
218-629
Percent Volatile SS 5-82
6

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Daily Data
Weekly Averages
Apparent Color
950-4100
1380-2360
pH
6.8-10.0
The pilot feed was supplied continuously except for 16% per-
cent of the time. Seven percent of this downtime occurred in
January when freezing conditions prevented normal operation.
The remainder is repair and maintenance downtime.
C. Aerated Lagoon (See Table Al, Figures A1 through A6)
The Aerated Lagoon aerator suffered a broken blade in January
because of ice, but experienced no other mechanical difficulties
during the second six month period.
Dissolved oxygen in the Aerated Lagoon varied from 0.5 mg/1 to
7.5 mg/1. If D.O. was limiting to the biological process, it
was not restrictive for any extended period of time. Only two
samples were less than 1.5 mg/1 D.O. BOD removal per unit of
electrical energy consumed does not seem to correlate well
with the dissolved oxygen concentration. The maximum value
observed occurred during Test 6 when 2.4 lbs. BOD were de-
stroyed per HP-Hr. based on net horsepower (no load horse-
power subtracted). Based on gross horsepower, the figure is
1.7 lbs. BOD/HP-Hr.
The temperature in the Lagoon varied between 12°C. and 29°C.
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through the six months period.
The weekly average of BOD5 reduction through the Lagoon varied
between 30 and 81 percent unsettled and between 70 and 87 per-
cent for the lab settled samples. (See Figure A4)
The maximum lagoon settled BOD5 removal occurred during Test 6
when the retention time was four days and the organic loading
1125 ppd/acre. (See Figure A4)
Lagoon suspended, total and settleable solids did not always
exceed influent concentrations as they did in the first six
months. This is probably due to the lesser submergence of
the aerator causing better solids retention in the basin. The
submergence during this six months period has been kept at a
minimum to try to get meaningful power consumption figures.
Lagoon BQD5 destruction in pounds per pound of ammonia nitrogen
used ranged from 29 during Test 7 to 133 during Test 5. Based
on the lab settled samples, these figures are 45 and 142#
bqd5/#nh3-n.
During the second six months period, the portion of Lagoon ef-
fluent BQD5 which could be removed by settling increased with
time. The suspended and settleable solids in the effluent
increased with time. This may be due to solids growth, to the
increase in temperature over the six months period, or both.
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D. Oxidation Ditch (OD)
The Oxidation Ditch brush aerator ran 84 percent of the time
during the second six months period. Regular chain replace-
ment was required to achieve this reliability. The chain drive
supplied on the pilot rotor is no longer used on Beloit Passavant
rotors, but has been superceded by belt drives.
Oxidation Ditch dissolved oxygen ranged between 0 and 5.0 mg/1
during the test period. The zero D.O. values occurred occa-
sionally at certain points in the ditch, but since complete
mixing always occurred, it is felt that D.O. was not limiting
to the process. The maximum value of BOD5 destroyed per unit
of energy occurred during Test 4 when 5.8 lbs. B0D5/HP-Hr. were
destroyed based on net horsepower (no load horsepower subtracted).
Based on gross horsepower, the figure is 2.7 lbs. B0D5/HP-Hr.
The temperature in the Ditch varied between 19°C. and 33°C.
through the six months period.
The weekly average of B0D5 reduction through the Oxidation Ditch
varied between 67 and 89 percent removal following clarification.
(See Figure B4)
The maximum Oxidation Ditch BQD5 removal occurred during Tests
5 and 6 when the retention time was two days and one day
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respectively. The highest average treatment efficiency was
achieved in Test 6 with a retention time of one day. (See
Figure B4)
The BOD5 removed in the Ditch per pound of ammonia nitrogen
used ranged from 16 to 60.
E. Trickling Filter 1 (TF1)
No mechanical difficulties were experienced with Trickling
Filter 1 during the second six months period.
Trickling Filter 1 dissolved oxygen concentration was typi-
cally half a mg/1 in the inner ring, never above 2 mg/1 and
on four occasions was zero, and probably limiting to the
biological processes.
Trickling Filter 1 effluent temperatures varied from 21°C. to
34°C. with a general warming trend through the period.
Weekly average B0D5 removal by Trickling Filter 1 ranged from
25 to 75 percent during the second six month period.
The maximum B0D5 removal by Trickling Filter 1 occurred during
Test 11 at 137 ppd/1000 cu. ft. organic loading (the lowest)
and 4000 gpd/sq. ft. hydraulic loading (1:1 recycle).
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Trickling Filter 1 suspended, total and settleable solids
concentrations were less than the influent in all tests
except TF1-10 when total and suspended solids were higher in
the influent. Test TF1-10 was interrupted by a shutdown
(main feed pump breakdown) and experienced low influent
solids.
From 23 to 130 pounds of BOD5 were removed by Trickling Filter 1
per pound of ammonia nitrogen used.
F. Trickling Filter 2 (TF2)
No mechanical difficulties were experienced with Trickling
Filter 2 during the second six months period.
Temperature of the effluent varied from 21°C. to 37°C. with a
general warming trend through the second six months period.
Dissolved oxygen in the effluent varied between 1.0 and 7.5
mg/1. The weekly average of D.O. concentration varied between
3,5 and 7.5 mg/1.
The weekly average of BOD5 reduction through Trickling Filter 2
varied between 14 and 47 percent removal for unsettled effluent
and between 25 and 57 percent for laboratory settled samples.
(See Figure D4) The maximum removal of 57 percent occurred
during Test TF2-8 when the organic loading was 284 ppd/1000
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cu. ft., and the hydraulic loading was 6000 gpd/sq. ft. (1:1
recycle).
Trickling Filter 2 suspended, total and settleable solids
concentrations in the effluent were greater than influent con-
centrations during Tests TF2-12 and TF2-13 except that total
solids were slightly reduced in Test TF2-12.
From 13 to 23 pounds of BOD5 were removed by Trickling Filter 2
per pound of ammonia nitrogen used, based on unsettled samples.
Based on the lab settled samples, the range is 24 to 45 pounds
of BOD5 per pound of ammonia nitrogen.
G- Combinations of Units
TF2 as a polishing filter for TF1 was Test TF2-11. This test
is a filter-clarifier-filter test. During this test, the ef-
fluent BOD concentration increased across the TF2 unit. This
increase may be scrubbing out of bio-solids which cannot be
supported by the low BOD5 effluent from the TF1 unit. Refer-
ence to the daily BOD data plotted on Figure D2 during May,
1969 shows the unclarified effluent (X plots) increasing with
time to a level near 140 rag/1 while the feed (0 plots) and
settled effluent (+ plots) remain near the 50 mg/1 level.
This performance seems to indicate that a sudden decrease in
organic loading is detrimental to overall performance, and
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that if the filters are to be tested as polishing units, they
will either need a long equilibrium period or will need to
have bio-solids removed by some other means.
TF2 as a roughing filter for TF1 was Test TF1-13. This test
is a filter-filter-clarifier test. During this test a 37 per-
cent reduction in BOD was realized across TF2 and a 60 percent
reduction across the combination of TF2 and TF1. The organic
loading to the TF1 unit was not decreased appreciably since
Test TF1-13 was accompanied by an increase in PF BOD5. It is
difficult to determine if the filter of the TF1 unit sloughed
solids as did TF2 during Test TF2-11 because of the clarifier
in the TF1 unit. The suspended solids in the recycle of TF1
did reach a high value of 27,000 mg/1 during the test.
Aerated Lagoon following the Oxidation Ditch and Clarifier 2
was Test AL-8. Although this test was run for five weeks,
the BOD5 of the effluent from the Aerated Lagoon was still
higher than the clarified effluent from the Oxidation Ditch.
The lab settled Aerated Lagoon effluent had a higher BOD than
the influent to the Lagoon. This indicates that after five
weeks time the mass transfer of soluble {or at least unset-
tleable) organic material was from the biomass to the liquid.
The last five data points of Figure A3 shows a decreasing
trend in both the settled and unsettled B0D5 samples. From
that figure, it might be assumed that for this test equilibrium
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is closer to ten weeks than to five.
Under activated sludge treatment conditions (clarification
with sludge recycle), the Oxidation Ditch can achieve treat-
ment efficiencies near 80 percent with one or two days re-
tention whereas the Aerated Lagoon required five days re-
tention with no settling or three or four days if settling is
provided. (See Figures A1 and Bl)
The most consistent effluent quality was observed in the lab
settled Aerated Lagoon samples (+ plots of Figure A2), but the
deified Oxidation Ditch effluent is nearly as good (X plots
of Figure B2).
BQD5 removal efficiency appears to be better at higher organic
loadings for Trickling Filter 1 than for Trickling Filter 2
(lab settled), but at lower organic loadings the efficiencies
are about the same (see Figures C7 and D7).
The recommended schedule for the third six months period is
included as Tables 3 and 4. The completed second six months
period schedule is included as Tables 1 and 2. The third six
months will include single unit runs on the Aerated Lagoon at
five days retention and on Trickling Filter 1 at a 5:1 recycle
rate. Series tests include the filters in series (TF1 first),
OD to Al, CO to TF2, TF1 to AL, TF2 to OD, and TF2 to TFl to
QD to AL.
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alternates (A through G) refer to Figures B3 through B9
the first semi-annual report.
IS

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SECTION 4
ACKNOWLEDGMENTS
The author wishes to acknowledge the organizational assistance of
J. E. Robbins; the technical talents of R. E. Smith, G. R. Laessle,
D. T. Robinson, W. E. Woodbridge, and Viola Loel; and the technical
advice of R. H. Scott.
16

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APPENDIX
17

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FIGURES
Aerated Lagoon (AL)
A1 Summary of BODg Efficiency First and Second Six Months -
Efficiency vs. Detention Time.
A2 BOD Data - Pilot Feed and Aerated Lagoon Effluent.
A3 BOD Data - Aerated Lagoon (Weekly Averages).
A4 BOD Removal - Aerated Lagoon (Weekly Average Efficiency).
A5 Suspended Solids Data - Pilot Feed and Aerated Lagoon
Effluent.
A6 Suspended Solids Data - Aerated Lagoon (Weekly Averages).
A7 Effluent Suspended Solids vs. Contents Dissolved Oxygen.
Oxidation Ditch (OD)
B1 Summary of BOD5 Efficiency First and Second Six Months -
Efficiency vs. Detention Time.
B2 BOD Data - Pilot Feed and Oxidation Ditch Effluent.
B3 BOD Data - Oxidation Ditch (Weekly Averages).
B4 BOD Removal - Oxidation Ditch (Weekly Average Efficiency)
B5 Suspended Solids Data - Pilot Feed and Oxidation Ditch
Effluent.
B6 Suspended Solids Data - Oxidation Ditch (Weekly Averages)
Trickling Filter 1 (1F1)
CI Summary of BODg Efficiency First and Second Six Months -
Efficiency vs. Hydraulic Loading.
C2 BOD Data - Pilot Feed and Trickling Filter 1 Effluent.
C3 BOD Data - Trickling Filter 1 (Weekly Averages).
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C4 BOD Removal - Trickling Filter 1 (Weekly Average Efficiency)
C5 Suspended Solids Data - Pilot Feed and Trickling Filter 1
Effluent.
C6 Suspended Solids Data - Trickling Filter 1 (Weekly Averages)
C7 BOD5 Removal Efficiency vs. Organic Loading - Trickling
Filter 1 (Weekly Averages).
Trickling Filter 2 (TF2)
D1 Summary of BOD5 Efficiency First and Second Six Months -
Efficiency vs. Hydraulic Loading.
D2 BOD Data - Pilot Feed and Trickling Filter 2 Effluent.
D3 BOD Data - Trickling Filter 2 (Weekly Averages).
D4 BOD Removal - Trickling Filter 2 (Weekly Average Efficiency)
D5 Suspended Solids Data - Pilot Feed and Trickling Filter 2
Effluent.
D6 Suspended Solids Data - Trickling Filter 2 (Weekly Averages)
D7 BOD5 Removal vs. Organic Loading - Clarified TF2 Effluent
(Weekly Averages).
D8 BOD5 Removal vs. Organic Loading - Clarified TF2 including
Recycle.
D9 BOD5 Removal vs. Hydraulic Loading - Clarified TF2 includ-
ing Recycle.
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TABLES
1	Summary of Test Results - Aerated Lagoon.
2	Summary of Test Results - Oxidation Ditch.
3	Summary of Test Results - Trickling Filter 1.
4	Summary of Test Results - Trickling Filter 2.
5	Completed Project Plan for Pilot Lagoon and Oxidation Ditch.
6	Completed Project Plan for Pilot Trickling Filters.
7	Proposed Project Plan for Pilot Lagoon and Oxidation Ditch.
8	Proposed Project Plan for Pilot Trickling Filters.
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AERATED LAGOON - FIRST AMD SECOND SIX MONTHS
BOD REMOVAL VERSUS RETENTION TIh£
FIGURE A1
100
80
60
M 40
20
clarified
X unclarified
0
*-
o
1
2	3
RETENTION TIME - DAYS

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J&.
~
FIGUBE A2
~	g2-
~
x
X
X	X

X):
xx
X X
XH I *
t , "X +
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+ *

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MAR
B3
BOD DATA
®	iff
PILDT PLANT FEED AND AERATED LAGDON EFFLUENT
~ - PILOT «-n-l I » - CLARIF- CD EFFL- X - /M_ EFF1_- * - LAB SETTLED
SB

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AERATED LABODN -
SIX MONTHS
BOD DATA
FIGURE A3
AL-5
AL-8
*	* ¦ ~ I	t	I	>	*	i	i	«	*
O
10
15
20

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BOD REMOVAL
AERATED LAGOON - SECOND SIX MONTHS
FIGURE AA
AL-5
AL-6
AL-7
AL-S
100
80
60
0 40
20
¦i	1	1-
O
LAB SETTLED
EFFLUENT
EFFLUENT
\
\
\ /
u
-m	«-
10
Tide - WEEKS
15
20

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—I
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APR	MAY	JUN JUL
GS	69	B3 69
SUSPENDED SOLIDS DATA - PILOT	PLANT	FEED AND AERATED LAGDDN EFFLUENT
a - PILOT PUW FEED	X - AERATED LjAGCCN EFFLUENT

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AERATED LAGOON - SECOND SIX MONTHS
EFFLUENT SU5FEMJED SOLIDS
FIGURE AG
800
600
400
200
H	1	1	1	1	•-
o
10
TlfcE - WEEKS
15
20

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AERATE13 LAGOON - SEDObtJ SIX MONTHS
EFFLUENT SUSPENDED .SPL.TDF? VERSUS CONTENTS D-O-
FIGURE A7
1000
800
600
400
2O0



X
X
X
X





* X
X
f






i-






	*
CONTENTS D-0- - MG/L

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OXIDATION DITCH - FIRST AMD SECOND SIX MONTHS
BOD REMOVAL VERSUS RETENTION TIME
FIGURE HI
100
80
60
40
20
® unclarified
X clarified with sludge return
2	3
RETENTION TIME - DAYS

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_J
\
13
i
300*
250
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150


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*x X x
x x
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MAR
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APR
ES
MAY
G3
JUN
ES
69
BOD DATA - PILOT PLANT FEED AND OXIDATION DITCH EFFLUENT
q - pQ mr Bt Mir n;m
¥ - n ASTTTITI rHTrUTTTM nTTn-l cm I rMT
AUG

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axiiJATxaN arroH - sejoc*cj sxx hcnrs
BOD DATA	FIGURE S3
TBC - 1EEKS

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BOD REMOVAL
OXIDATION DITCH
OD-4
OD-5
lOO
XV
80
- 1~
CLARIFIED EFFLUENT
-*	*
60
40
20
-i	»	i	i	i	i	i	>
10
TIME - WEEKS
SIX MONTHS
OD-6
FIGURE B4
i	i	i
15
i
20

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300 r*
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SUSPENDED SOLIDS DATA - PILOT PLANT FEED ANDOXIDATION DITCH EFFLUENT
~ - PILDT	X - CLARIFIED CKH3ATXCN DITCH EFFULENT

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(JXIOATION DITCH - SEJOOhMJ SIX MONTHS
CLARIFIED EFFUJENT SUSPENDED SOLIDS
FIGURE BB
800
600
400
200
O
i	i	i	>	
10
TIME - WEEKS
i	i	i
0
15
20

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jDH^CjlCLrjC-NG jp~j:jL,X££ii ~ - ~ f	J /W>
BOD REMOVAL VERSUS HYDRAULIC LOADING
FIGURE CL
100
80
60
LJ
40
J
§
S 20
M
K
o
2000
4000
HYDRAULIC LOADING - GPtVSF
6000
8000

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30Or


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i
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MAR
69
APR
63
MAY
63
JUN
69
JUL
63
BCD DATA - PILOT PLANT FEED AND MEAD TRICKLING FILTER EFFLUENT
O - PILOT *»¦»*• I ' X - l«CAO TRIOM-INB FILTER EFR I FNT ~ - TF3 EFFLLENT
AUG
69

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BOD DATA
TRICKC.ING FIL.TBR J. -
SIX MONTHS
FIGURE C3
TFl-8
TF1-9
300
TF1-10
TF1-11	TF1-12	TF1-13
20O
I nfluf.nt
A
V
100 . -
FFFLUENT
V
V'
o
i	i i	i «
4	 I	I	I	I	«
I	I
o
10
TIME - WEEKS
15
20

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TRICKLING FILMIER ± - SEXJLJUD SIX MONTHS
BOD REMOVAL	FIGURE CA
TFl-8	TF1-9	TF-10	TF1-11	TF1-12	TFX-13
TIME - WEEKS

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900
800
o o
nWuntf1 ¦
FIGUPE C5
\
U 700-
' BOO
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m 400.
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-X- X
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X X*
^
SUSPENDED SOLIDS DATA - PILOT FEED AND MEAD TRICKLING FILTER EFFLUENT
AUG
69
O - PILOT fUNT FEED
X - fc€>V3 1RICKL-INB FILTER EFFLUENT

-------
TRICKLING FILTER 1
EFFUUENT SUSPEMJED SOLIDS
- SEJJObO SIX MONTHS
FIGURE DB
TIME - WEEKS

-------
TRICKLING FIITBK l - F^TFSEjT AhtD SECOND SIX MONTHS
BOD REMOVAL VERSUS ORGANIC LOADING	FIGURE C7
ORGANIC LOADING - LBS/DAY/1000 OJFT

-------
-ZNG FILTER S - FIRST AND SECOND SIX MONTHS
BOD REMOVAL VERSUS HYDRAULIC LOADING
FIGURE 01
100
L)
H
I
0J
80
60
40
20
«> no recycle
J( recycle
O
2000	4000
HYDRAULIC LOADING - GPD/SF
6000
8000

-------
300
250
200
150
°	x
f)
ft#, ift..

x n
\
ID
i
x X
*o
X
O +
-B-	£&_
	 o
X X
X Op
x X
in
~
o
OQ loo
so

+
+
X*
* X
* . X *
X u I	
+0
X
+
+ +
JUN
63
JUL
63
•e	s	®
BDD OATA - PILOT PLANT FEED AND TRICKLING FILTER E EFFLUENT
D - FT TF3 IX - LN3-ARIFIED ~ - LAB SETTLED) - - MIF EFFLLENT
AUG
69

-------
TRICKLING m-TER S - SECOND SIX MONTHS
SOD DATA
FIGURE £33
TF2-8
TF2-9
TF2-10
TF2-11
TF2-12	TF2-13
300
200
¦x
INFLUENT	\
/
-J
EFFLUENT
/ \
LAB SETTLED
FFFLUENT *
\
N.
'/
!
i 'x
/
K
/ \
100 .
' Ik
/ x	.x
' / X
X* /
\ t<
O
O
10
TBC - KEEKS
15
20

-------
mzCKi-JAG fTZLTEJ* £? -	sac.x Mar>m-es
TF2-8
BOD REMOVAL
TF2-9
TF2-10
TF2-11
TF-»-I2
LAB SETTLED
EFFLUENT
FFF1I'FNT
lO
TIME - WEEKS
FIGURE OA
TF2-13
20

-------
900
800
_l
\
Q 700
I
boo
If!
~
H 500
_J
a
LD 4oo
~
UJ w
~ 300
Z
Ld
Q_ 200
01
ID
in ioo
~ ~
¦ w , ,, .
FIGURE D5
X*
Ox X

69*	69*	G9	KT	eif
SUSPENDED SDLIDS DATA - PILDT PLANT FEED AND TRICKLING FILTER E EFFLUENT
Q - PILOT HM i	X - 7F5 EFRJJENTT

-------
TRICKLING FILTER S -
EFFLUENT SUSPENDED SOLIDS - MG/L
SECOND SIX MahfTHS
FIGURE DB
TIME - WEEKS

-------
77ZIDKLING FILTER S - FIRST AND SECOTsCJ SIX MONTHS
BOD REMOVAL VERSUS ORGANIC LOADING
FIGURE 07
ORGANIC LOADING - LBS/DAY/1000 CUFT

-------
CLARIFIED 7FH INCLUDING RECYCLET
BDD REMOVAL VERSUS ORGANIC LOADING
FIGURE OB
~RGANIC LOADING - LBS/DAY/1000 QJFT

-------
CJUSFariEEJ TFS XHOLJJDING HEXrm FT
BCD REMOVAL VERSUS HYDRAULIC LOADING
FIGURE OS
2000
4000
HYDRAULIC LOADING - GFD/SF
6000
8000

-------
StHWAJRY OF TEST RESULTS
(Mead-FWFCA Project on Biological Effluent Treatment)
SYSTEM 1 A«»ted Laanon
Aerated Laooon
Aerated Lapoon
Aerated Laooon


TEST I Af.
-5


AL
-6

AL-7
At
-8


bATE 1 3-3-69
to
3-31-69
3-31-
-69
to
5-5-69
5-5-69
to 5-26-69
5-26-69
to 6-27-69

TP«1T CONDITIONS: 1




Feed Rate
GPM 1
24.4


30.
4
40.6
RO.O

Depth
FEET 1
6-75
6.75
6.75
7.75

Reevele Rate
GPM I
Nm»
None
None
Nmo

Hvdraulic Loadina
GPDPSF1
12

15
20
28

flraanic I^oadina PPD/IOOO efl 3.5 IMS md/arr^
4.0 (119S ppd/aere)
4.8 (1360 ppd/acre)
0.9 (300

Retention Tine
DAYS I
5

4
3
2

CIarifier-Surface Loadina GPtt'SF
None
None

None


HOURS 1
Mane
Nniu»
None
Nnrie


l»mi ci»rifi»d R«-
Mill
Claris ori Rff.
Mill



TOST RESULTS:
1 Avq.

Range
Avg


Range
Avg.

Range
Avg.
Range

Dissolved Oxvaen
Influent! 5-8

4.0-8.3
5.6


3.6-6.8
6.6

5.8-7.5
See CL2
-6 Eff.

(¦a/1)
Contents 6.4

4.4-7.0
4.1


0.5-6.9
1.7

O.5-3.2
6.B
5.2-7.5




4-R-R.7
4.5


1.0-6.8
2.1

0.7-3-O
7.0


Temperature
Influent! 32

27-35
32


28-34
33

28-35



<°C)
Contentsl










19


}3-22
24

20-26
24
20-29

BOD.
Inf luent| 240

127-454
313


156-340
194
163-256



fmo7l\


34-136
.62


£6—91
97

44-157
88-
31-138

Total Solids
Inf luentl 1998

1503-4370
1679

1284-2060
1503
1390-1721

«•«» -»

(mo/1)
Effluent! 1402

1283-1594
1SOQ

132Q-1 aai
1524
1246-1672
1349
1069-2247

Percent Volatile
Inf luentl 34

17-48
36


30-53
33

28-36



f*)


24-31
33


27-42
30

26-34
29
22-37

Susoended Solids
Inf luentl 511

166-996
417

214-1474
329
40-534



(ma/1)
Effluent! 208

142-396
371

46-734
530
242-700
329
46-1IOO

Percent Volatile
Inf luentl 37

5-SO
45


3L2-R2
4R

30-74




Effluentl 54

25-R1
57


13-07
50

41 -62
42
4-66

Settleable Solids
Inf luentl 7. a

0-36t0
O-O

0-2-2-5
O.R
Q-2-1-5



(ml/l/hr)
Contents!







Effluentl C1.4

o - i.a
9.9

2.0-26.0
3O.0
2.5-54.0
5.9
0.5-22.0

Apparent Color
Inf luentl 19O0

1300-2900
1545

950-2550
1680
llno_9ino



Effluent! 1065

Rnn-1500


6m-i9on
1440
700-2300
915
450-2150

PH
Inf luentl 7.9

7.1-Q.6
7.9

7.1-9.0
7-4
6-8-8-2






7-1-7-R
7.4

7-2.7.6
7.
5
7.4-7.6
7.9
7.4-8.6

Conductivitv
Inf luentl 2130

1200-6000
17 lO

1400-2000
1660
1500-1950



(uMhos/cm 0 25°C)
Effluent] 1705

1400-1900
173D

1500-1900
1720
1150-1950
1635
1250-1900

Ammonia Nitroaen
Added 17.1


7.8
lO.
1

1.8

(ma/1 (rt
Measured 1^*7


_ .. 4-5 .. . .
6.6
1.5

PhosDhate PhosDhorous Added 1 3.0
2.4
2.7
1.6

(raq/1 P)
Measured ll.2


2-3
2.4
2.3

Efficiencies: JCBOD^ Removed 1 7H(m'
54-R2(6R-R6)
6R(
R4l
51 —76/67—AO)
51
[79]
4-93(55-94)



Pounds BODe Removed 155158

¦531
661
49
77




Per Gross HP-HR
11.7(1.8)

1.7(2.1)
l.«
if 2.
4)


Per Net HP-HR
I2.4(2.6)

2.4(2.9)
2.2(3.4)
i

Per lb. Ammonia
N Used 1133fl42\

44 (55)
29 (45)







BOD- Clarified Effluent 141

28-78
35


15-55
41

17-78
35
16-67

(mp/1)















1 1



















TABLE 1
«moo 9ib ( ) Clarified Effluent

-------
SUMMARY Of TEST RESULTS
Mead-FWPCA Project on Biological Effluent Treatment)
SYSTEM
(WiHatimi Ditch
Clarifipr 2
Oxidation Ditch
Clarifier 2
OTridm
Hon Ditch
Clarifier 2
TEST
CT>-&
With OD-4

OD-5
With OD-5

OD-6
With 0D-6

3-3-69
to 3-31-69
3-3-69
to 3-31-69
4-21-69
to 5-19-69
4-21-
69 to 5-19-65
5-26-69
to 6-27-69
5-26-69
to 6-27-69
TEST CONDITIONS:






Feed Rate
GPM
62.5
62.5
31.2
31.2
81.0
81.0
Depth
FEET
4

4

5.2

ReeveXe Rate
GPM
60

40

40

Hvdraulic Loading
GPDPSF
30

15

39

Organic Loading PPD/IOOO cf
15.0 (2574 ppd/acrel

6.6 (1130 rod/acre)

11.9 (2646 ppd/acre)

Retention Tine
DAYS
1

2

1

Clarifier-Surface Loading GPE
PSFSee Clarifier 2
950
See Clarifier 2
494
See Clarifier 2
1230
_
HOURS

2.2

4.4

1.7
Svsten Feed Source


Mill Clarified Eff.
0D
Effluent


TEST RESULTS:
Avg.
Range
Avg.
Range
Avg.
Range
Avg.
Range
Avg.
Range
Avg.
Ranqe
Dissolved Oxvaen
Influent
5.8
4.0-8.3
See OD-4 Eff.
6.0
3.6-7.5
See CD-5 Eff.
4.6
0.7-6.5
See 0D
-6 Eff
(mg/l)
Contents
0.8
0 - 5.0

1.1
0-3.3

1,5
0.2-4.8

Effluent
n.o
0.3-4.8

1.2
0.6-3.3

1.4
0.4-4.5

Teroerature
Influent
32
271-35

32
28 - 35

37
34-39

<0c>
Contents






Effluent

10-24

23
19 - 27

30
27-33

BOD.
Inf luenl
240
137-454

209
156 - 340

1B9
94-264

fao/ll


, 66
29—Oft

38
21-69

29
11-63
Total Solids
Influent
1998
1503-4370

1620
1284-2060

1546
1222-1930

(¦a/1)
Effluent

1497
1259-1652

1269
1190-1406

1146
930-1451
Percent Volatile
Influent
34
17-48

35
28-53

36
31-40


Affluent

31
28-35

28
24-37

*7
19-34
SuSDended Solids
Influent
511
166.996

377
40-1474

397
86-732


Effluent
AA7

3«4
1M-6RO
5470
224-17476
197
HO-324
2551
878-9472
133
32-428
Peri-ont Volatile
Influent
37
5-50

. .46
. 22-82

43
19-83

(X)
Effluent
56
41-79
57
.. 42-78
43
26-75
57
3-100
48
41-54
51
28-68
Settleable Solids	
Influent
7-B
0-36.0

o.a
0.2-2.5


2.8
0.5-20.0

(¦1/1/hr) Contents







Effluent
*.6
0.1-33.(1
Q.5
0-1.5
350
3.5-975
0.5
0-3.5
241
31-845
1.8
0-15
ADoarent Color
Influent
19QO
1300-2900

1610
1100-2550

1720
1250-2200

Effluent
t-7 An
A5D-5200
1490
1000-2000
134SO
1200-4000
> 1090
800-1400
5500
1300-21000
650
300-1100
dH
Influent
7.9
¦7,1-0,*

7.7
7.1-9,0

7,9
6.9-10.0

Effluent
T •>
6-9-7-6
,7.3
6.9-7.6
7.4
7.2-8.1
7.5
7.3-7.6
7.7
7.3-8.1
7.7
7.4-8.1
ConH»*- ti oity
Influent
91*1


17*»
1600-1 950

1840
1200-5000


Effluent
1700
1300-1900
1630
1400-1R00
1735
1500-1950
1715
14QO-1925
1635
1250-1950
1615
1250-2000
Amnnia Nitrogen
Added

7-1

11.4

11.9




8.5

1.8
Phosphate PhosDhorous Added

3.0

3.3

3.8
(ma/1 PI Measured

1.4

2.0

1.6
Efficiencies: JCBODc
Removed

73
52-Rft

82
63-93

85
64-93
Pounds BDDr- Removed

131

65

156
Per Gross HP-HR

2.7

1.4

2.1
Per Net HP-HR

¦i-R

2.9

3.2
Per lb. Amiaonia N
Used

49

60

16







Sattlaahla SflliMc
SIllHn*

23
5-40

340
5-590

520
25-9RO
{¦1/LA tir.)













SntnwM Snlirie
Slariop

1227
332-4344

4984
11e-17619

5491
<>04-12ft36















Percent Volatile Susp-Sludi
ie
46
.. 37-77


44
21-79

47
42-53









¦94IM • 9i h Sludge Valine Index

19

-- - 	
68
—	

95
TABLE 2
—

-------
SUMMARY OF TEST RESULTS
, iTCau-rwrv-/i rjroject on Biological Effluent Treatment)
SYSTEM
Tricklina Filter I
Tricklinq Filter I
Trickling Filter I
Trickling Filter I
Trickling Filter I
Trickling Filter I


TEST
TFI-8
TFI-9
TFI-lO
TFI-11
TFT-12
TFT-13


DATE
2-17
-69 to 3-10-69
3-10-
69 to 4-7-69
4-21-
69 to 5-5-69
5-5-69 to 5-26-69
5-26-69 to 6-16-69
6-16-69 to 7-4-69

TEST CONDITIONS:







Feed Rate
GPM
33.3
44.4
29.6
22.2
33.3
22.2

Depth
FEET
24
24
24
24
24
24

Recycle Rate
GPM
3 1 1
22.2 0.5:1 1
14.8 0.5:1
22.2 1:1
33.3 1:1
22.2 1 • 1

Hydraulic Loading
GPDPSF
6000
6000
4000
4000
6000
4000

Organic Loadina PPDAOOO CF
284
284
207
137
175
94

Retention Tiae
DAYS







Clarifier-Surface Loadina GPE
*SF
588
784
522
392
588
392

-
HOURS
i.a
1.4	
2.1
2.7
1.8
2
.7

System Feed Source
mu.
Clarified Eff.
Mill
n an" fi od Rff _
Mill Clarified Eff.
Mill
Clarified Eff.

TF2 Effluent

TEST RESULTS:
Avq.
Range
Avq.
Range
Avg.
Range
Avg.
Range
Avg.
Range
Avg.
Range

Dissolved Oxvaen
Influent
6,4
2.0 - 9.0
5.9
4.0 - 8.3
5.3
3.6 - 6.2
6.6
5.8 - 7-5
3.2
0.7 - 6.5
See TF2 #13 EFF

(mo/U
Contents
0,7
0.2 - 1.7
0.3
O - 0.7
0.4
0.1 - 0.6
1.1
0.4 - 1.9
0.5
0.4 - 0.7
0.6
0.4 - 1.3









Teaoerature
Influent
31
28 - 35
32
27 - 34
32
29-34
33
28 - 35
36
34-38



(°C)
Contents
23
21 - 25
26
22-29
27
25 - 29
26
21 - 30
33
30-34
31
25-34

Effluent







BOD_
Influent
271
174-454
205
127 - 303
221
166 - 340
194
163 - 256
168
94 - 215

———



JZfi_
oa-am
006
	 ..47. =..134..
127
56 - 174
63

79
41 - 114
84
52 - 113

Total solids
Influent
1RR7
1503-2000
1828
1284-4370
1531
1427-1584
1503
1390-1721
1637
1342-2532


(aa/1)
Effluent
1651
1415-2301
1538
1271-1810
1542
1257-2097
1310
1130-1603
1383
1157-1585
1298
1005-1451

Percent Volatile
Influent
3S
24-45
34
17-48
38
30-41
33
28-36
3*
32-4*1
		


fS J

9JI
18-4n
Ml
25-35
33
21-50
9R
23-32
31
27-36
31
28-36

Susoended Solids
Tnfluml
462
166-996
542
214-1474
293
220-428
3*9
40-534
402
86-682



(aa/1)
Effluent
353
170-662
1*1
44-570
355
124-570
247
110-628
307
116-570
208
10-434

Percent Volatile
Influent
30
5-46
42 18-82
4ft
22-74
48
30-74
41
10-61



l%\

«
18-62
40
32-70
SO
34-70
46
32-67
50
33-69
44
18-85

Settleable Solids
Influent
5.7
0.1-35.0
4-4
O-36-O
0.8
Q.2-2.5
0.8
Q-2-1.5
2.0
O.5-8.O



f«l/l/hrl
Contents







Effluent
1.3
0-3.0
It®
Q.l-12.0
4.5
l.O-lO.O
1.7
0.1-5.5
2.3
0 - 11.0
0.7
0 - 3.5

ftnarent Color
Influent
3140
1500-4100
1715
950-2400
1645
1200-2550
1680
1100-2100
1640
1250-2000
_ _ _
_ _ _


1805
1330-3400
1580
1050-1900
1520
1000-2150
1140
900-1600
1450
900-2100
L440
800-2100

dH
Influent
7.6
7.1 - 8.7
7-0
7-1-0.6
7.0
7.2 - O-O
7-4
6-R—8.2
7.6
6.0-10.0
	
		 1

Effluent
7.4
6.0 - a.5
7-3
6-0-7-0
7-3
7-0 - 7-5
7.4
7-2-7-O
7.5
7.0-8.9
7.9
6.8-8.6

Conduc tivitv
Influent
17QO
14S0-2000
101 5
1200-2100
1715
1500-1000
1660
1500-1050
2200
1500-5000



fuMhOs/ca fi 25 CI
Effluent
1740
1400-2000
1710
1400-1000
1705
1400-1900
1750
1600-1950
1800
1600-2000
1600
1300-1850

Aaaonia Nitroaen
Added
6.3
7.4
8.5
lO-l
7.5
14.1

Ima/1

2-1
3-4
4-8
9.1
3.7
14.8

Phosnhate Phosnhorous Added
2.6
2.7
2.9
2.7
3.4
3.4


Measured
1-5
1-6
2-6
1.6
3.9
4.1

Efficiencies: *Bon-j
3B
13-62
49
14-70
43
29-66
68
44-78
53
37-72


Pounds BODj Removed
39
54
34
35
35


Per Gross HP-HR







Per Net HP-HR







Per lb. Ammonia
N Used
23
26
26
130
24
	









Settleable Solids
Roevele
375
110.77(1
40O
30-000
112
15-370
155
30-340
540
285-040
B50


(al/LA hr.)















Sasnended Solids
Recycle
W»6
B07-17510
14055
5756-18900
4835
630-18944
7956
2332-18902
15670 7534-19384
18071
13Q76.26702

(as/1) 	







Perc«t Volatile Susp.-Reeve]
f 37
27-48
47
38-51
51
43-78
46
41-50
42
37-40

37-43











Slndae Voluae Index
42
29
23

19

35
47


tWM - »l»

.
— •
	

-------
SUMMARY OF TEST RESULTS
(Mead-FWPCA Project on Biological Effluent Treatment)
SYSTEM
Trirklina Filter 2

inq Filter 2
Trickling Filter 2
Trickling Filter 2
Tricklino
F i 11 pr 2
Tricklino Filter 2

TEST
TF2-8

TF2-9
TF2-10
TF2-11

TF2
-12
TF2-13

DATE
2-17-69
3-10-69
3-10-69 to 4-7-69
4-21-69
to 5-5-69
5-5-69
to 5-26-69
5-26-69
to 6-16-69
6-16-69 to 7-4-69
TEST CONDITIONS:






Feed Rate
GPM
33.3
44.4
29.6
22-2

33.
3
22.2
Depth
FEET
24
24
24
24
24
24
Recycle Rate
GPM
33-3 1:1
22.2 0.5:1
14.8 0.5:1
22.2 1:1

33.
3 1:1
22.2 1:1
Hvdiaulic Loadinq
GPDPSF
6000
6000
4000
4000
6000
4000
Oraanic Load in a PPD/lnon CF
284
284
207
44
17S
149
Retention Tine
DAYS






Clarifier-Surface Loadinq GPE
>SF
None
None
None
None
None
None
-
HOURS
None
None
None
None
None
None

Mill Clarified Eff.
Mill
Clarified Eff.
Mill Clarified Eff.
TFI Effluent
Mill Clarified Eff.
Mill Clarified Eff
TEST RESULTS:
Avq.
Range
Avg.
Range
Avg .
Range
Avg.
Range
Avg.

Range
Avg.
Ranqe
Dissolved Oxvoen
Influent
6-4
2.0-9.0
5,9
4,0-83
5.3
3.6-6.2
See TFI
#11 Eff.
3.2

0.7-6.5
5.9
4.8-6.4
f ma/1)
Contents






Effluent
4.1
1.0-6.1
5.0
5.2-5.8
5.1
4.2-7.0
7.2
6.3-7.5
5.3

4.0-6.7
6.5
5.3-7.5
Temperature
Influenl
31
28-35
32
27-34
32
29-34
	 	
36

34-38
37
35-40
(°C)
Contents






Effluent
24

28
24-30
29
28-30
24
19-27
33

31-35
34
31-37
BOD.
Influent
273

205
1 27—303
221
166-340
___
	
16R

04-215
212
154-264
(nq/ll
Effluenl
onn
137-371
163
99-234
147
100-217
101
51-152
129

74-160
134
80-194
Total Solids
Influent
1897
1503-2900
1828
1284-4370
1531
1427-1584


1637

1342-2532
1491
1222-1930
(ma/1)
Effluent
1818
1514-2717
1628
1351-1857
1448
1240-1686
1326
1134-1562
1521

13 50-1660
1846
1225-5230
Percent Volatile
Influent
33
24-45
34
17-48
38
30-41


36

32-40
35
31-39
(*1

32
21-55
32
28-40
35
29—50
29
25-33


28-36
32
9-37
SusDended Solids
Influent
462
166-006
542
214-1474
293
220-428


402

86-682
381
244-732
(mg/1)
Effluent
46O
¦5R-QOO
424
178-684
246
82-468
285
112-422
432

300-640
393
120-778
Percent Volatile
Influent
30
5-46
42
18-82
48
22-74
	

41

19-61
46
22-83
/*!
Effluent
44
30-72
47
30-78
»
24-88
60
44-91
45

30-60
44
7-81
Settleable Solids
Influent
5.7
0.1-35.0
4.4
0-36.0
0.8
0.2-2.5
	 ___
.2.0

0.5-8.0
3.2
0.5-<>n r»
(ml/l/hr) Contents






Effluent
3.8
0 - 7.0
4.1
1.1-8-5
4.5
0 - 15.0
3.6
1.2 - 7.5
5.2

4.0-7.0
5.0
2.0-13.O
ADoarent Color
Influent
2140
1 500-4100
1715
050-2400
1645


— — _
1640

1250-2000
1800
1250-2200
Effluent
1QQO
1450-3700
160S
1100-2100
1420
900-2000
1100
800-1300
1440

850-2020
1690
900-2500
dH
Influent
7.6
7-1 - 8-7
7.9
7-1-0-6
7.0
7-2-9.0


7-6

6.9-10.0
7.9
6.7-8.8
Effluent
7-6
7.1 - 8.6
7.2
6.0-7.0
7-4
7-1-8-3
7.5
7-4—7.8
7-5


7.9
7.2-8.6
Condwc tivity
Influent
1790
1450-2000
iois
1200-2100
171 5
1500-1900


220O

1500-5000
1530
1200-1900
fuMhos/cm 0. 25 C)
Effluent
1675
1300-2000
1740
1400-1000
1740
1500-1900
1700
1500-1925
1750

1600-20SO
1620
1150-1900
Ammonia Nitroaen
Added
6.3
7.4
ft.5

7.5
17.6
(ma/1 N*
Measured
,2.7 		
4-1 	- - -
5.2
4.0
5.8
14.1
Phosohate Phosnhorous Added
2.6
2.7
2.9
1.6
3.4
5.1
f mo/1 P)
Measured
1.7
1.9
2.3
1.7
3.!
3.4
Efficiencies: &BODg Removed
27(411
15-52(8-711
21(40)
15-43(10-531
34(441
10-49(38-571


23(45) 7
-37 (29-67)
37(40)
10-6R)
Pounds BODrj Removed
29145)
23(44)
27(35)


15(301
21(23)
Per Gross HP-HR






Per Net HP-HR






Per lb. Ammonia
N Used
21(32J
13(24)
23(30)
18(291
23(451
23(25)







B0D5 Clarified Effluent
161
93-341
124
R9-1 57
123
87-192
44
30-64
93

52-131
127
qr>_lQ3
(ma/1)
























































TABLE 4
( ) Clarified Effluent


.

				 .
	

-------
Second 6 Months
COMPLETED PROJECT PLAN FOR PILOT LAGOON AND OXIDATION DITCH
MEAD-FWPCA PROJECT
Alternate
Oxidation Ditch
A
A
Test
Actual
Beginning
Date
TOTAL
Equilibrium - 4	2/3/69
OD - 4	3/3/69
Equilibrium - 5	3/31/69
Contingency	4/7/69
OD - 5	4/21/69
Equilibrium - 6	5/19/69
OD - 6	6/2/69
3 Tests Completed
Weeks
Required
4
4
1
2
4
2
4
Sludge
Hydraulic Rate Detention	BOD Loading Rate	Return
Depth Gallons Days GPM Acres PPD/Ac PPD/IOOO CF GPM
4.0
4.0
5.2
90,000
90,000
117,000
19 Operating Weeks
1	62.5
2	31.2
0.07
0.07
81.0 0.07
1,960
960
2,514
11.4
3.3
11.3
Yes
Yes
Yes
Comment s
PF is Feed
Aerated Lagoon
A
A
E
Equilibrium - 5
AL - 5
Equilibrium - 6
Contingency
AL - 6
AL - 7
Equilibrium - 8
AL - 8
2/3/69
3/3/69
3/31/69
4/7/69
4/21/69
5/5/69
5/26/69
6/2/69
4
4
1
2
2
3
1
4
6.75 175,000
6.75 175,000
6.75 175,000
7.75 230,000
5 24.4 0.07	800
2 30.4 0.07	995
3 40.6 0.07 1,335
2 80.0 O.095
2.4
3.0
4.0
No
No
No
No
OD is Feed
TOTAL
4 Tests Completed
19 Operating Weeks
NOTE: Nutrients were added into the feed of all systems at approximately 8.5 M3/L NH3 Nitrogen and 1.3 MG/L P.
TABLE 5

-------
Second 6 Months
COMPLETED PROJECT PLAN FOR PILOT TRICKLING FILTERS
MEAD-FWPCA PROJECT
Alternate
Trickling Filter 1
A
Test
Equilibrium - 8
TF1 - 8
Equilibrium - 9
TF1 - 9
Contingency
Actual
Beginning
Date
2/3/69
2/17/69
3/10/69
3/17/69*
4/7/69
Weeks
Required
2
3
1
3
2
Hydraulic
Rate
GPDPSF
6,000
6 ,000
Feed
GPM
33.3
44-4
Heighth
Feet
24
24
BOD Rate
PPD/IOOO CF
188
250
Recycle Rate
R/I Ratio GPM
1:1
0.5:1
33.3
22.2
Comment s
Main Pump Down
A
TF1 - 10
4/21/69
2
4,000
29.6
24
167
0.5:1
14.8


F-l
TF1 - 11
5/5/69
3
4,000
22.2
24
125
1:1
22.2
TF1
is Feed
A
TF1 - 12
5/26/69
3
6,000
33.3
24
188
1:1
33.3


F-2
TF1 - 13
6/16/69
3
4,000
22.2
24

1:1
22.2
TF2
is Feed
TOTAL
6 Tests Completed
16 Operating Weeks
Trickling Filter 2
A
A
F-l
A
F-2
Equilibrium - 8
TF2 - 8
Equilibrium - 9
TF2 - 9
Cont ingency
TF2 - lO
TF2 - 11
TF2 - 12
TF2 - 13
2/3/69
2/17/69
3/10/69
3/17/69
4/7/69
4/21/69
5/5/69
5/26/69
6/16/69
2
3
1
3
2
2
3
3
3
6,000
6,000
4,000
4,000
6,000
4 ,000
22.2
44.4
29.6
22.2
33.3
22.2
24
24
24
24
24
24
125
250
167
44
188
125
1:1
0.5:1
0.5:1
1:1
1:1
1:1
22.2
22 .2
14.8
22.2
33.3
22.2
Main Pump Down
TF1 is Feed
PF is Feed
TOTAL
6 Tests Completed
16 Operating Weeks
NOTE:	Nutrients were added into the feed of all systems at approximately 8.5 MG/L NH3 Nitrogen and 1.3 MG/L P.
TABLE 6

-------
Third 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
Days
GPM
Acres
PPD/AC
PPD/IOOO CF
Sludqe Return
Comments
Oxidation Ditch
B
Equi1.-7
CO -7
6/30/69
7/28/69
4
4
5.2
117,000
2
40.5
0.07
1257
5.6
Yes
PF is feed.
D-2
Equi1.-8
OD -8
8/25/69
9/8/69
2
4
8.57
193,000
2
66.7
0.07


Yes
PF is feed.
C-2
Bquil.-9
OD -9
10/6/69
10/20/69
2
4
8.57
193,000
2
66.7
0.07
¦?
j
Yes
TF2 is feed.
G
Equil-10
11/17/69
2
8.57
193,000
2
66.7
0.07
•>

Yes
MTF is feed.
TOTAL
4 Tests

26 Weeks








Aerated Laqoon
E
Equil. -9
AL -9
6/30/69
7/28/69
4
4
5.5
115,000
2
40.0
0.066
¦?
¦?
No
OD i s feed.
A
Equil-lO
AL -10
8/25/69
9/8/69
2
4
7.75
230,000
5
32.0
0.095
¦?
*?
No
PF is feed.
B-2
Equil-11
AL -11
10/6/69
10/20/69
2
4
7.2
193,000
2
66.7
0.080
¦>

No
MTF is feed.
G
Equi1-12
AL -12
11/17/69
12/1/69
2
4
7.2
193,000
2
66.7
0.080
j
?
No
CL2 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 BOD:N:P.
Past history of approximately 1 mg/1 ammonia nitrogen and 0-5 mg/1 P in wastewater leaves initial net of 8 mg/1 ammonia
nitrogen and 1.3 mg/1 P to be added.
TABLE 7

-------
Third 6 Months
PROPOSED PROJECT PLAN FOR PILOT TRICKLING FILTERS
MEAD - FWPCA PROJECT
Alternate
Test
Tentative
Beginning
Date
Weeks
Allowed
Hydraulic
Rate
GPD/SF
Feed
GPM
Heighth
Feet
Approximate
BOD Rate
PPD/IOOO CF
Recycle Rate
R/I Ratio GPM
Comment s
Trickling Filter 1
F-l
Equil.-14
TF1 -14
7/14/69
7/28/69
2
4
4000
22.2
24
125
1:1	22.2 PF is feed to sump
beneath filter.
Equil.-15
TF1 -15
8/25/69
9/8/69
2
4
8000
14.8
24
83
5:1	74.O Influent through
filter.
Bquil.-16
TF1 -16
Equil.-17
TF1 -17
10/6/69
10/20/69
11/17/69
12/1/69
2
4
2
4
600O
6000
66.7
24
188
66.7	24
0:1
0:1
TF1 modified to
eliminate sump
beneath.
XF1 modified.
TF2 is feed.
TOTAL
4 Tests
24 Weeks
Trickling Filter 2
F-l
Equil.-14
TF2 -14
7/14/69
7/28/69
2
4
4000
22.2
24
1:1	22.2 XFl is feed.
D-2
Equil.-15
TF2 -15
8/25/69
9/8/69
2
4
6000
66.7
24
0:1
O OD is feed.
C-2
Equil.-16
TF2 -16
10/6/69
10/20/69
2
4
6000
66.7	24
188
0:1
0 PF is feed.
Equil.-17
TF2 -17
11/17/69
12/1/69
2
4
6000
66.7	24
188
0:1
0 PF is feed.
TOTAL
4 Tests
24 Weeks
NOTE: Itatrients will be added to the main pilot feed in varying quantities as needed to maintain a total ratio of 100-5-1 BOD:N:P.
Past history of approximately 1 mg/1 ammonia nitrogen and 0.5 mg/1 P in wastewater leaves initial net of 8 mg/1 ammonia
nitrogen and 1.3 mg/1 P to be added.
TABLE 8

-------