-------
does not discharge the whey from cottage cheese manufacturing. Milk and cus-
tards (seasonally) are also produced there.
Pulp Mill Wastes
The industrial source was a sulfite process plant. The pulp mill wastes
contained a very high BOD, (70(30lrng/1). As evidenced by the low percent by
volumes used in the experiment the waste was very "strong." The large ADO
indicated easy utilization of the ambient BOD by the unacclimated biomass.
Poultry Waste--
Inexplicably, the poultry waste proved the most problematic of the ten
wastes. Despite the high BOD and its ostensibly noninhibitory nature, the
change in DO was positive (increase) upon application of a shock load, re-
flecting inhibition. The shock load experiments were run twice. Both series
of tests produced anomalous behavior. The initial results are given below.
They were essentially the reverse of what would be anticipated.
TABLE 11. POULTRY WASTE SHOCK LOADING-EXPERIMENT 1
shock
5
10
20
Avg.
ADO @ 4 min
0.88
0.84
0.69
ADO @ 12 min
1.20
1.10
0.91
Average
%. return
101
104
114
106
ADO @ 4 min
ADO @ 12 min
74
76
75
75
A second test was performed to verify these unexpected results. The
findings are reported in Tables 11 and.12. As originally anticipated, the
DO now decreased with the application of the shock and the magnitude of the
change increased with increasing shock strength. However, the "% return"
after removal of the shock was generally not very good and very erratic with
respect to both magnitude and sign. This could be attributed to a natural
grease in the waste but the cause was hard to establish in conjunction with
the other unexpected behavior. Table 12 lists the detailed results of the
second poultry waste analysis. "To 5%" means the change from baseline feed
to a 5% by volume poultry waste shock; "from 5%" means the return from the
5% shock load to the baseline feed.
Since the source of this waste was not local, it proved impossible to
follow up our investigation with questions of the poultry plant personnel and/
or additional samples for further analysis.
Textile Waste--
The textile waste came from a natural fibers plant. They employed no
carriers or chromium dyes. The results were straightforward and predictable
from the BOD concentration. The shock runs employing this waste exhibited
32
-------
SSliit?* reproducfbl'm"- T»e average percent return, 91%, was lltartit ex-
TABLE 12. POULTRY HASTE SHMK
to 5%
from 5%
to 5%
from 5%
to 20%
from 20%
to 50%
from 50%
to 50%
from 50%
| Average)
-0.05
-0.03
-0.07
-0.03
-0.12
0.02
-0.25
0.11
-0.13
0.20
-0.13
-0.02
-0.16
-0.12
-0.30
0.07
-0.57
0.36
0.30
0.40
15
75
-23
-63
-
75
50
38
44
(25)
40
(28)
44
(31)
43
(50)
42(33)
38
Tannery Waste--
This waste was the effluent from the manufacture of baseball covers.
The high BOD (1700 mg/1), and COD (4000 mg/1), were easily accounted for in
the resultant DO decrease. The result from the K.a study produced the more
linear response anticipated. The percent return, however, is not very high.
Again, this probably reflects the relatively high oil and grease content of
the waste (400 mg/1). The solids and chromium content had no distinguishable
effect on the response.
Meat Packing Waste--
This meat packing waste came from a plant which did not reclaim blood
and fats. The presence of the former in the waste could account for the re-
latively small decrease in DO level for large changes in loading. Although
the BODwasabout 900 mg/1 (cf the changes induced in the DO by a textile
waste with a BOD of 800 mg/1) there was inhibition possible from the high TDS
contribution of the blood. The presence of fats caused
return. These results were reproduced in the KLa runs.
Chemical Waste T1 nnn
This waste came from the manufacture of pesticides. The BOD value of
150 mg/1 was a result of analyses with acclimated seed. The COD is 2500 mg/1.
The increase in DO level upon introduction of the shock was anticipated. Im-
portantly, the system was not "knocked out" during the runs. The results
showed a steady increase with increasing percent shock load. These values
33
-------
were very reproducible also (Tables 7 and 8).
Electroplating Waste--
The electroplating facility used in this test discharged negligible
BOD in their raw waste. This is reflected in the sharp increase (cf response
to chemical waste) in DO upon shock loading. Since the system exhibited an
excellent percent return, <(9635)it is assumed that no permanent damage was in-
curred by the viable biotnass even with the relatively high total chromium
content.
ON-SITE INVESTIGATIONS
The BioMonitor was to be located at two joint wastewater treatment
plants. Specific criteria had to be met by those WWTPs selected. It was re-
quired that the plants selected:
treat sanitary (municipal) sewage and industrial wastes
employ biological treatment - preferably activated sludge
be in routine running form
experience possible upsets from a known industrial contribution
preferably have a flow < 10 MGD (so events could be sorted and
analyzed for research purposes)
preferably have an industrial contributor amenable to the posi-
tioning of a companion BioMonitor at their discharge point
have analytical and operational data available.
Site Set One
Description of Joint Municipal/Industrial Wastewater Treatment Plant 1 and
the BioMonitor Setup--
The BioMonitor system was set up at an activated sludge-type wastewater
treatment plant which is part of Metro Nashville's system. The daily flow is
3 MGD (capacity, 6 MGD). Figure 5 is a diagram of the wastewater treatment
facility. The BioMonitor, set up in a newly designed enlarged "monitor" sta-
tion (see Figure 6 ), was located on the "influent structure." (See Figure
6 ) for relative location). Figure 7 is a picture of the BioMonitor on lo-
cation. Flow time from its location to the aeration basin was approximately
3 hours.
At this point, the waste stream has been through preliminary screening
and the bar minutors (maximum solids size = 1"). Suspended solids still re-
mained a problem in that they tended to clog the pump tubing. The screening
device shown in Figure 8 eliminated this problem. The outside screen is
common aluminum house screening. The interior screen is a stainless steel
mesh with openings of 0.004". Since the waste flow was - 12 feet beneath the
influent structure the feed tubing was contained in a metal conduit and the
entire apparatus was weighted down because of the current and turbulence in
the flow. Required maintenance, i.e., a hosing down to remove "caked" solids
was required approximately once every 10 days to 2 weeks.
At this location, we were able to use air from the blowers used to
aerate the treatment tanks. (The biopopulation for the BioMonitor was taken
34
-------
KEY
Number
1
2
3
4
5
6 -
7
8
9
10
11
12
13
14
15
16
Component
Pump Station
BioMonitor (Influent Structure)
Grit Removal
Pre-Aeration
Primary Clarifier
Aeration Basin
Final ClaHfier
Chlorine Contact Chamber
Sludge Digester
Sludge Filtering Bldg.
Blower Bldg.
Contact Wing
Operations Control Bldg.
Administration Bldg.
Sludge Burial Site
Creek
Average Retention/Flow Time
15 min
45 min
1.8 hours
6.2 hours
1.8 hours
45 min
Figure 5. Diagram of wastewater treatment facility - site 1
35
-------
Door
Hinge
co
Door
Hinge
Pump
n
Bio-
Monitor
Chart
tecorder
-------
o
I
Figure?. BioMonitor on Location Site 1
-------
FEED TUBING
PROTECTIVE CONDUIT
TOP WOODEN SUPPORT
INTERNAL FINE SCREEN
EXTERNAL COARSE SCREENING
EXIT PORT FOR FEED TUBING
BOTTOM WOODEN SUPPORT
CONDUIT PLUG
Figures- Design of screening device.
38
-------
^ration basins.) The biopopulation increased in the Bio-
laHtinVJi tha* lev?] held in the treatment plant's basin. Due to
If Jo * ln/lo"» the Plant maintains a comparatively low biomass (900
i^ Ihl" t0 P^ev?nt.ash1ng during periods of low flow (which occur
d i Mrn In P ;i912^ 2umidnight - 8 am flow - 2 MGD; 8 am - 4 pm flow -
Anc^ ; J P^ " I2 rtlldni9!?t flow ' 3 MGD). In the BioMonitor, however, a
constant feed rate was applied. Secondly, it should be noted that the plant
runs at a high ambient DO in the aeration basins ( 7 mg/1 average) in order
to accommodate daily high BOD loadings discharged from a meat processing
plant. Average daily influent BOD is approximately 150 mg/1. Percent remov-
al is approximately 91%. Suspended solids (SS) average 150 mg/1. Percent
removal is approximately 90%.
Description of Industrial Plant Site 1 and BioMonitor Setup
The BioMonitor system was set up at a luncheon meat processing plant
which contributes to the joint municipal system under study. The waste is
composed of sanitary waste, floor washings (includes meats, fats, blood,
cleaning agents, disinfectants, etc.), process water and smoker ash slurry.
The industry pretreats the discharge only to the extent of skimming off fats,
settling, and screening. Weekday flow rates vary from less than 400 gpm to
above 800 gpm. Weekend flow rates often drop below 100 gpm. The average
total daily assessed flow is 0.4 MGD. This represents over 13% of the flow
to the wastewater treatment plant described above. It is the largest, single
contributor. The average BOD is approximately 450 mg/1. However, recent BOD
values have averaged approximately 325 mg/1. The screening device shown in
Figure 9 was employed here, also. The only difference was that it was smaller.
Due to the periods of low flow it was necessary to install a weir at the end
of the waste trough. The minimum sampling depth was 4 inches.
The feed to the BioMonitor was diluted 1:1 with tap water. This was ne-
cessary because we wished to maintain the same retention time in 'both Bio-
Monitor units and the BOD is too high in the industrial waste to permit a
100% flow at a feed rate of approximately 25 ml/min. Feed and water rates
variedfrom 10 to 14 ml/min each for a combined range of 24 to 28 ml/min. The
biomass used in the monitor system was taken from the wastewater treatment
plant described above. Air to this unit was delivered from a portable com-
pressor. Again, the DOwaskept at a high level in order to accommodate the
high shock loadings routinely experienced from this plant.
Operational Procedures and Data Collection--
The maintenance schedule at both locations included daily calibration of
the DO probe to maintain accuracy of the results. Solids were also taken and
subsequent necessary wasting performed to maintain desired levels at the
wastewater treatment plant. Backwashing of the feed tubing with bleach fol-
lowed by water was performed every week to keep the tubing clean and flow
rates constant Since oil and grease is a common constituent of the waste
from the meat processing plant, feed line coating was experienced. Therefore,
routine maintenance included backwashing the feed tubing system with isopropyl
alcohol and/or acetone followed by excess water. We have experienced no dif-
ficulties with the dilution water system. Appendix D contains the maintenance
procedures followed at the wastewater treatment plant and industrial sites.
Included also is the daily log maintenance sheet. This level of maintenance
39
-------
was higher for research purposes than that proposed during actual use.
The wastewater treatment plant intermittently discharges the supernatant
and filtrate from the anaerobic sludge digester and centrifugal filter direct-
ly into the water flow at the influent structure. This is an anaerobic, zero
DO, contribution. The discharge is manually controlled which enabled the
BioMonitor to be tested on intraplant discharges in the early stages of setup.
Figure 9 is a graph of DO versus time obtained by a 24-hour run on the
BioMonitor. Points 1 and 5 represent a decrease in the DO due to domestic
usage in the AM diurnal cycle. Points 2 and 3 correspond to the intraplant
discharges described in the last paragraph. The volume of anaerobic waste
discharged will vary. Point 4 represents a decrease in the DO due to the in-
flux of the meat processing industry's waste. Range 6 reflects the higher
DO normally found in the PM diurnal cycle due to lower usage and temperatures.
Points 2, 3, and 4 coordinate well with known (recorded) times of discharge.
The record of ambient DO is obtained at a rate of 7.5 inches of chart paper
per hour and must be manually reduced to the more usual display presented in
Figure 10 . Figures 10 and 11 are a set of early graphs of the DO levels at
the industrial site and wastewater treatment plant, respectively. These
graphs represent the same date and time period. The sharp decrease in DO
level experienced at the meat processing plant begins at approximately 6:00
a.m. It was first seen in the wastewater treatment plant BioMonitor at ap-
proximately 7:30 a.m. (beginning of DO sag). The steady increase in DO from
about 11:00 p.m. (inFigurell ) reflects p.m. diurnal cycle of low tempera-
tures and usage. The decrease at approximately 1:30 a.m. most likely corres-
ponds to the intraplant discharge of anaerobic filtrate/supernatant from the
digester. Figure fti'from the meat processing plant indicates some plant dis-
charge at approximately midnight with the DO leveling off until the large
6:00 a.m. shock. The second shift at the plant comes on duty at midnight.
The sanitation (or clean up) crew is on duty between 10:30 p.m. and 7:00 a.m.
Tables 13 and 14 give the operating parameters for the two companion
BioMonitors at the wastewater treatment plant and industrial site, respective-
ly. Effort was extended to run the systems as similarly as possible. Consid-
eration was also afforded to the WWTP's operating procedure. Whenever possi-
ble the operating parameters of the WWTP were employed in the operation of
the BioMonitor.
These operating parameters represent the culmination of efforts to es-
tablish the BioMonitor as a steady, routinely operating system. Following
this period of troubleshooting the system, a period of intensive data collec-
tion was provided at both sites. Appendix D contains the sampling routines
for both sites. Appendix E contains the complete set of results (graphically)
of this data collection period. Two periods of intensive data collection
were planned. These periods were each 5 days long and each day of the week
was included at least once. At these times, 24-hour surveillance was main-
tained at both sites. Composite (every 20 minutes for an hour) samples were
gathered manually. When the recorder indicated a change in DO level, grab
samples were taken. Samples were collected from the influents to the Bio-
Monitor at both the meat processing plant and at the wastewater treatment
40
-------
Q_
CL
9.0
8.0
7.0
ao
5.0
8 4.0
3.0
2.0
1,5 A.M. DIURNAL CYCLE
(DOMESTIC USAGE)
2,3 INTRA-PLANT DISCHARGE
4 INDUSTRIAL DISCHARGE
6 P.M. DIURNAL CYCLE
I2:40A.M. -* 7:40 A.M.
(§)
6 8 10 12 14 _ 16 18
TIME, HOURS (t*0 @v 10:40A.M.)
20 22
24
Figure 9 . Preliminary graph - BioMonitor response - joint
wastewater treatment plant - site 1.
-------
-p.
ro
O.
Q_
9.0
8.0
7.0
6.0
5.0
§ 4.0
3.0
2.0
1.0
"I2NOO
M2-MIDNITE
6AM
~1IAM
i I I i I
i i i i I I I I I
I i I I i i i
I
234 5 6 7 8 9 10 II 12 13 14 15 16 17 18 19 20 21 22 23 24 25
TIME, HOURS
Figure 10 . DO vs time (industrial site 1).
-------
9-12-76 to 9-13-76
~6AM
~IIAM
i t I i I t t i i I i i I l I i i i I i I I I I I
I 2 3 4 5 6 7 8 9 10 II 12 13 14 15 16 17 18 19 20 21 22 23 24 25
TIME. HOURS
Figure 11 . DO vs time (wastewater treatment plant - site 1).
-------
plant. Additional samples similarly composited over one hour were taken from
the final effluent of the wastewater treatment plant. Oxygen uptakes were
performed hourly on the biomass from one of the aeration basins at the waste-
water treatment plant. A recording pH meter continuously monitored the pH
of the influent to the system at the meat processing plant. The presence of
cleaning agents are known to cause wide fluctuations of pH in the waste.
Acidified and filtered TOC analyses were run on the composite and grab samples,
This study was performed to determine any correlations among variations in
loading in the specific plant's effluent quality and the response of the Bio-
Monitor.
TABLE 13. OPERATION PARAMETERS: WASTEWATER
TREATMENT PLANT SITE
Parameter Average Value
Solids, main reactor, MLSS, mg/1 1500
MLVSS*, mg/1 1300
Feed flow, ml/min 25
Return flow**, ml/min 65-70
Baseline DO, side car, ppm 4
Main reactor retention time, hrs 6,5
Side car, retention time, minutes 5.5
*MLVSS in the contact chamber avg approximately 80% of those in main reactor
**Return flow is defined as flow from the top exit port of the side car back
into the main reactor
TABLE 14. OPERATION PARAMETERS: INDUSTRIAL SITE
Parameter Value
Solids, main reactor, MLSS, mg/1 2000
MLVSS*, mg/1 1800
Feed flow, ml/min 13
Dilution flow, ml/min 13
Return flow**, ml/min 80
Baseline DO, side car, ppm 3
Main reactor retention time, hrs 6.5
Side car retention time, minutes 5
44
-------
*MLVSS in contact chamber avg approximately 80% of those in main reactor
**Return flow is defined as flow from the top exit port of the side car back
into the main reactor.
This data can be seen in Appendix E. Data from the meat processing industry
will help substantiate the preliminary data on lag times, degree of DO de-
cline and also indicate a possible source and extent of a high BOD loading.
The correlation of the change in influent TOC to change in DO was demonstra-
ted.
The DO and TOC values from the same sampling point are drawn on the
same graph so response and correlation can be visually assessed. The varia-
tions in the TOC graphs are exaggerated because they are plotted from hourly
composites. The DO graphs vary more smoothly since they reflect continuous
monitoring. Temperatures are listed periodically on the X-axis. This indi-
cates the direction of thermal influence on the observed trends in DO level.
The following conclusions were drawn from this data:
There is generally good correlation between TOC values and DO
at both the industrial and WWTP sites. The industrial response,
by the nature of the discharge, is the more dramatic.
Evaluation of WWTP influent/effluent TOC values indicate a
range of flow times ranging from 5 to 10 hours. This is in
agreement with plant design and known variations in flow. The
TOC values obtained in our study (plant influent and effluent)
are consistently higher than those reported by the metropolitan
government.
The average TOC required to change the DO level one (1) mg/1
at the industrial BioMonitor is 496 ± 33 mg/1. Evaluation of
this TOC requirement at the WWTP lead to the discovery of two
distinct influents. Specifically, there is one waste that has
a value of 70.2 ± 11% mg/1 TOC for a 1 mg/1 change in DO and a
second waste with a value of 175 ± 22% mg/1 TOC. The proba-
bility that these groups of values result from an actual dif-
ference in the influent is greater than 99.5%.
The sewer flow time from one BioMonitor to the second unit ran-
ged from 1.5 to 3 hours as measured by peaks in DO. This again
agrees well with the unreported Metro time of flow studies of
2 to 3 hours.
The early afternoon TOC peak at the industrial site appears to
be production intensive (i.e., which products are being pre-
pared). It routinely appears but has more variation in its
peak time than the midnight or 6 a.m. peaks. The decrease in
activity at the plant on Sunday is clearly seen. A somewhat
different profile can also be seen at the WWTP on weekends.
Site Set Two
Description of Joint Municipal/Industrial Wastewater Treatment Plant 2 and
BioMonitor Setup
45
-------
The second municipal site is also a Metro Nashville Wastewater Treat-
ment facility which employs activated sludge for biological treatment. It is
a new plant (operating for approximately 1 year at the time of this investiga-
tion) with a design hydraulic load of 25 MGD. Current flow is approximately
10-12 MGD. Figure 12 is a diagram of the facility. The BioMonitor station
was located on the channel after the grit removal structure (see location on
Figure 13 ). Figures 13 and 14 are pictures of the BioMonitor setup at this
site. Because of colder weather conditions a heat lamp was installed in the
monitor station to prevent system freezing. The main problem was freezing
of the effluent line after it left the protection of the station. It appear-
ed the influent raw waste was sufficiently warm to prevent influent line
freezing.
The influent solids level at this municipal site was higher than that
encountered at the first municipal site. The problem of feedline clogging
was continuously encountered with the screening system employed at site one.
Therefore, a different screening device was required. Figure 15 is a dia-
gram of the new device. Figure 16 gives an actual perspective of the screen-
ing device in use. All other aspects of the setup were identical to those
used at the first wastewater treatment plant.
The average operating parameters of this second WWTP are given in Table
15. Sludge from primary and secondary treatment is piped to the Metro Central
facilities where it is combined with Central's waste and incinerated.
Description of Industrial Site 2 and BioMonitor Setup--
The second industrial site was an industry which manufactured project-
iles for 106 millimeter shells. The wastewater included heavy metals, pro-
prietary cleaning and wetting agents (TOC source) and acids (e.g., chromic,
phosphoric). The wastewater analysis used for sewerage charges is given in
Table 16. Although the TOC concentration was significant, the.BOD averaged
less than 30 mg/1. Therefore, the plant's waste stream feed was diluted 1:1
with a milk solution before entering the BioMonitor. The milk created an
F/M of approximately 0.25. The screening device was similar to the one de-
scribed in Figure 8. Because of minimal solids problem and nonturbulent flow
in the waste trough, only one screen (the fine mesh one) was required.
The plant was run on two shifts and operated from approximately 6 a.m.
to 11 p.m. (when it is locked up), 5 days per week. The plant was closed
weekends. Other work is performed at this location but the resultant aqueous
waste streams are small and segregated. It was not anticipated that the
variations observed via BioMonitor readings would be identifiable at the WWTP.
It was possible, however, due to the toxic nature of various waste stream
constituents, that a singularly large spill, etc., could impact the WWTP ad-
versely. This did not occur during the monitoring period.
Operational Procedures and Data Collection--
The two companion BioMonitors were stabilized in their new locations.
When daily results indicated a properly functioning system another intensive
data collection period was begun. Operating parameters were similar to these
given in Tables 13 and 14,
46
-------
fiiiir NEUOVM.
Figure 12. Wastewater treatment facility - site 2.
-------
Figure 13. Photograph of BioMonitor at Wastewater
Treatment Plant - Site 2
-------
Figure 14.. Close-up of BioMonitor at Wastewater
Treatment Plant - Site 2
-------
fine screening
coarse screening
submersion
level
wastewater
flow
plywood
sides
Frame: 2" x 2" and 2" x 4" construction
Suspended by ropes into wastewater to level indicated
Intake tubing suspended between section defined by fine screening
Entire screen stabilized in wastewater flow by 15 Ib weight
attached to bottom
Figure T5. Modified screening device. .
50
-------
Figure 15. Photograph of Modified Screening Device
-------
TABLE 15- DESIGN AND OPERATING PARAMETERS -
WASTEWATER TREATMENT PLANT 2
Parameter
Flow, MGD
Influent suspended solids, mg/1
% Removal
Influent BOD, mg/1
% Removal
Design Value
25
300
97
350
97
Operating Value
7.8 - 9.5
88
91
102
95
TABLE 16. INDUSTRIAL SITE 2 -
WASTEWATER CHARACTERISTICS*
Constituent Concentration (mg/1)
BOD5 23
Suspended Solids 69
Grease 24
Chromium 0.03
Copper 0.03
Zinc 0.45
Iron 82.5
Nickel 40.0
*Source - Metropolitan Government analysis for municipal
sewer discharge.
52
-------
A 3-day around-the-clock test period was conducted. Maintenance and
sampling routines were identical to those described in Appendix D. Addition-
al samples were taken at the industrial site for metal analysis. As indicat-
ed previously, it was not anticipated that under "normal operating" conditions
this industrial waste source would identifiably impact the municipal site.
However, this afforded the opportunity to study a problem very different from
that created by the first industrial site. The heavy metal content of the
waste was analyzed in an effort to correlate variations in DO with variations
in the metal concentration. The metals investigated were iron, zinc, total
chromium and copper. Tests were run for nickel. Trace amounts, less than
0.01 mg/1 were detected. Similarly, tests for lead concentrations were less
than 0.1 mg/1. All metals analyzed were run on the acidified aqueous samples
using atomic absorption spectrophotometry with an acetylene/air flame.
Appendix F contains the graphical representation of the data amassed
over this 3-day period. Again, corresponding DO and TOC curves are drawn on
the same graph to facilitate the evaluation of correlation. The following
conclusions can be drawn from the review of this data:
The second WWTP was a larger treatment facility with more and
varied contributing industries. The overlaying of DO and TOC
curves show the BioMonitor picks up the overall trend in TOC
variation very well. Since the system did exhibit sufficient
sensitivity at site.l, it can be assumed that no significant
shock occurred at WWTP 2 during the surveillance period. The
larger the WWTP facility the more of an equalizing effect
experienced.
The heavy metals monitored exhibited similarly shaped curves,
with the possible exception of copper. Zinc was the highest
average concentration followed by iron. There was also a simi-
larity between the shape of the metals'curves and the corres-
ponding TOC curves.
The corresponding DO and TOC curves at the industrial site do
not present as dramatic a profile as obtained from site 1 tests.
The biomass in the BioMonitor could have been continuously in-
hibited by various small slugs of metals, acids, and propriet-
ary organics. Again, overall trends of TOC increase and DO de-
crease (and the reverse relationship) are exhibited.
Efforts to substantiate these assumptions were made. The BioMonitor
was shock loaded with a high concentration of chromic acid. The system re-
sponded immediately. The resultant curve was smooth and showed a continuous
increase in DO over an extended period.
53
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REFERENCES
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3. Jackson, S. and Brown, V.M., "Effects of Toxic Wastes on Treatment Pro-
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54
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13. Blok, J., "Respirometric Measurements on Activated Sludge," Water Res.,
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14. Blok, J., "Measurements of the Viable Biomass Concentration in Activated
Sludge by Respirometric Techniques," Water Res., Vol. 10, pp 919-925
(1976).
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Barnes & noble, Inc., New York (1970).
16. Coackley, P., and O'Neill, J., "Sludge Activity and Full-Scale Plant
Control," Water Poll. Control, 74, 404 (1975).
17. Weddle, C.L., and Jenkins, D., "The Viability and Activity of Activated
Sludge," Water Res., 5, 621 (1971).
18. Genetelli, E.J., "DNA and Nitrogen Relationships in Bulking Activated
Sludge," J. Water Poll. Cont. Fed., 39, R32-44 (1967).
19. Standard Methods for the Examination of Water and Wastewater, 13th Ed.,
Amer. Pub. Health Assn., Washington, D.C. (1971).
20. Arthur, R.M., and Hursta, W.N., "Short Term BOD Using the Automatic
Respirometer," Proc. of the 23rd Ind. Waste Conf., Purdue Univ., 242
(1968).
21. Mancy, K.H., Instrumental Analysis for Water Pollution Control. Ann
Arbor Science Pub. Inc., Ann Arbor, Michigan (1975).
22. Patterson, J.W.; Brezonik, P.L.; and Putnam, H.D., "Measurement and
Significance of Adenosine Triphosphate in Activated Sludge," Environ.
Sci. and Techno!.t 4, 569 (1970).
23. Brezonik, P.L., and Patterson, J.W., "Activated Sludge ATP: Effects of
Environmental Stress," Jour. San. Eng. Div., Proc. Amer. Soc. Civil
Engr., 97, SA6, 813 (1971).
24. Holm-Hansen, 0., and Paerl, H.W., "The Applicability of ATP Determina-
tion for Estimation of Microbial Biomass and Metabolic Activity," Proc.
IBP-UNESCO Symp. on Detritus and Its Role in Aquatic Ecosystems,
Pallanza, Italy (May 23-27, 1972).
25. Chiu, S.Y.; Kao, I.C.; Erickson, L.W.; and Fan, L.T., "ATP Pools in
Activated Sludge," J. Water Poll. Cont. Fed., 45, 1746-1758 (1973).
26. Upadhyaya, A.K., and Eckenfelder, W.W., Jr., "Biodegradable Fraction as
an Activity Parameter of Activated Sludge," Water Res., 9, 691 (1975).
27. Lenhard, G.; Nourse, L.D., and Schwartz, H.M, "The Measurement of Dehy-
drogenase Activity of Activated Sludges," Proc. 2nd Int'l Conf. Water
Poll. Res., Tokyo, Japan (1964).
55
-------
28. Bucksteeg, W., "Determination of Sludge Activity: A Possibility of
Controlling Activated Sludge Plants," Proc. 3rd Int'l Conf. Water Poll.
Res., Munich, Germany (1966).
29. Ford, D.L.; Yang, J.T.; and Eckenfelder, W.W., Jr., "Dehydrogenase En-
zyme as a Parameter of Activated Sludge Activities," Proc. of 21st Ind.
Waste Conf., Purdue Univ., 534 (1966).
30. Ryssov-Nielsen,H., "Measurement of the Inhibition of Respiration in Ac-
tivated Sludge by a Modified Determination of the TTC-Dehydrogenase
Activity," Water Res., Vol. 9, pp 1179-1185 (1975).
31. Klapwijk, A.; Drent, J.; and Sternvoorden, J.H.A.M., "A Modified Proce-
dure for the TTC-Dehydrogenase Test in Activated Sludge," Water Res.,
8, 121 (1974).
32. Jones, P.M., and Prasad, D., "The Use of Tetrazolium Salts as a Measure
of Sludge Activity," Journ. Water Poll. Control Fed., 41, R441 (1969).
33. Vaicum, L., and Eminovici, A., "The Effect of Trinitro-Phenol and y-
Hexachlorocyclohexane on the Biochemical Characteristics of Activated
Sludge," Water Res., 8, 1007 (1974).
34. Sulzer, F., and Westgarth, W., "Continuous DO Recording in Activated
Sludge," Water and Sew. Works, 109, 10, 376 (1962).
35. Albertson. O.E., and DiGregorio, D., "Biologically Mediated Inconsis-
tancies in Aeration Equipment Performance," Jour. Water Poll. Control
Fed., 47, 976 (1975).
36. Young, B.A., "Development and Evaluation of a Continuous Monitor for a
Biological Wastewater Treatment System," Master's Thesis, Vanderbilt
University, Nashville, Tennessee (1976).
37. Hartman, L., and Laubenburger, G., "Toxicity Measurements in Activated
Sludge," Jour. San. Eng. Div., Proc. Amer. Soc. Civil Engr., 94, SA2,
247 (1968).
38. Gaudy, A.F., Jr., and Turner, B.C., "Effect of Air Flow Rate on Re-
sponse of Activated Sludge to Qualitative Shock Loading," Proc. 17th
Ind. Waste Conf., Purdue Univ., 136 (1962).
39. Arthur, R.M., "An Automated BOD Respirometer," Proc. 19th Ind. Waste
Conf., Purdue Univ., 628 (1964).
40. Simpson, J.R., and Nellist, G.R., "Development and Use of a Large-
Volume Automatic Respirometer," Waster Poll. Control, 69, 596 (1970).
41. Advertising Circular, Robertshaw Controls Co., Model 970, Richmond,
VA (1974).
56
-------
42. Eckenfelder, W.W., and Ford, D.L., Water Pollution Control, Pemberton
Press (1970).
43. Kalinske, A.A., "Effect of Dissolved Oxygen and Substrate Concentration
on the Uptake Rate of Microbial Suspensions," Jour. Water Poll. Control
Fed., 43, 73 (1971).
44- Duggan, J.B., and Cleasby, J.L., "Effect of Variable Loading on Oxygen
Uptake," JWPCF, Vol. 48, No. 3, pp 540-550 (1976).
57
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APPENDIX A
DEVELOPMENT OF A CONTINUOUS RESPIROMETER
As discussed in Section 5, DO/oxygen uptake was the parameter selected
for use in the biological simulation monitor. A preliminary system, a con-
tinuous oxygen uptake meter or continuous respirometer, was developed to test
preliminary concepts and evaluate the rapidity and reliability of response.
As reviewed in the introduction, several continuous and semi-continuous res-
pi rometers have been developed. Although some systems offer good sensitivi-
ty, other aspects render them unsuited for this project. Below is a descrip-
tion of the continuous respirometer developed for this work.
DESCRIPTION OF THE CONTINUOUS RESPIROMETER
The respirometer basically is a 10 liter plexiglas laboratory activated
sludge unit with a one-liter (adjustable volume), air tight side car (see1
Figure A-l). A variable speed pump brings mixed liquor from the aeration
basin to the side car. Retention time in the side car can be varied not only
by changing the pump delivery rate but also by adjusting the volume of the
side car. The 5-inch diameter plexiglas cylinder which constitutes the side
car is outfitted with exit ports at the 1, 1.5, 2 and 2.5 liter levels. The
side car is made air tight by a floating plexiglas disc cover. This disc is
fitted with a DO probe which extends approximately 4 cm into the liquor. A
probe continuously monitors the DO level in the side car. A magnetic stirr-
er, set to create minimal vortexing, maintains a completely mixed system in
the side car. The overflow returns to the aeration basin by gravity through
the selected port.
The feed enters directly into the activated sludge unit and is complete-
ly mixed. The aeration basin retention time can also be varied. Similarly,
the MLVSS, DO and temperature can be controlled to the desired conditions.
The laboratory operating parameters are listed in Table A-l.
After testing various aeration devices, we selected a commercially a-
vailable aerator sold to aerate fish tanks and aquaria. It is a permanent
(cf air stones) hollow tube of plastic material which is porous throughout
its length.*
*"Bubble Wand," Marine and Aquarium Products, Division of Aquaria, Inc.
15800 Armenta Street, Van Nuys, California 91406.
58
-------
10
DO
METER
AIR
SOURCE
:=Sf
AIR FLOW
REGULATOR
RECORDER
RECORDER
FEED
PUMP
ADJUSTABLE
BAFFLE
CLARIFIER
AERATION
DEVICE
EFFLUENT
FEED
Figure A-l. Schematic of the continuous respirometer.
-------
It did not exhibit the tendency towards rapid clogging as did sintered glass
spargers. The sintered glass also was difficult to clean. The tubing is
readily available, inexpensive and therefore disposable. However, the tubing
can be readily cleaned and reused. The tubing is cleaned by scraping the sur-
face with a razor edge followed by an aqueous rinse. The tubing can be cut
to any length. It can also be slightly formed to fit into curved spaces.
Bubble size was small and well patterned - to effect good mixing in the aera-
tion basin and rolling action for clarifier recycle. Figure A- 2 is a photo-
graph of the laboratory setup.
The oxygen source for the laboratory studies was compressed house air.
The flow was regulated by a hospital-type oxygen flow regulator with a back
pressure of 50 psi. The type employed ranged from 0-7 liters/minute. The
regulators gave very accurate results when checked against a wet test meter.
The oxygen flow meters also proved to be very durable and delivered a well
regulated flow. Such regulators are easily read, readily available and
comparatively inexpensive.
TABLE A-l. LABORATORY OPERATING PARAMETERS
Parameter Value
Retention time - side car 10 minutes
Retention volume -side car 1 liter
Retention time - aeration basin 6 hours
MLSS, aeration basin , 3000 mg/1
V
MLVSS, aeration basin 2500 mg/1
Temperature 20°C
pH 5 - 7
Feed flow 15 ml/min
The pumps employed were either laboratory solution metering or positive
displacement.
CHARACTERIZATION OF THE CONTINUOUS RESPIROMETER
Preliminary Work
Three continuous respirometers were set up. In a 5-day run, the F/M
ratio of the feed varied every 24 hours in units 1 and 3 according to the
pattern:
60
-------
Figure A-2. Photograph of Continuous Respirometer
-------
Day 1 2 3 4 5
F/M 0.3 + 0.6 -» 0.3 -* 0.1 + 0.3
(This 5-day test was repeated the following week.) F/M is the "food-to-micro-
organism" ratio. It is defined mathematically as follows in Equation (A-l):
F/M « 24 S /t Xv (A-l)
where:
SQ is the BOD concentration of the feed (substrate) in mg/1
t is the retention time in hours
Xy is the concentration'of biomass (MLVSS) in mg/1.
The factor of 24 (hours/day) converts hours into days so that F/M has units
of inverse days.
F/M change was effected by varying the concentration of commercial pow-
dered evaporated skim milk and dibasic ammonium phosphate (NH.)^ HPO^ Us an
an additional nitrogen and phosphorus source). The operating parameters em-
ployed are given in the previous section. The DO levels in the side-car and
basins were continuously monitored and recorded. The F/M ratio was maintain-
ed in unit 2 at 0.3 throughout the 5-day run as a control.
The DO levels-in both the aeration basins and side cars varied noticeably
within the first 60 minutes of the F/M change. As expected with healthy
biological systems the DO increased when the F/M ratio decreased and decreas-
ed when this ratio increased. A comparison of the sensitivity, i,.e.» rate of
change of DO in the side car and in the aeration basin, was made. Prelimi-
nary results indicated that changes in the side car DO level averaged 1 1/2
to 2 times more sensitive to changes in F/M during the first 60 minutes than
the DO level changes in the aeration basins. This was substantiated by 21
additional short-term runs where the F/M value in influent varied approxi-
mately every two hours. The sensitivities were evaluated according to
Equation (A-2). The time, t., was evaluated from 0 through 60 minutes at 5
minute intervals. .
s . (d[o2]/dt)tl., Slde car//(d[o2]/dt)tii aerat1on basin (fl.2)
The rate of change in DO was obtained by curve fitting the strip chart
graph (0-60 minutes) to a second order polynomial using a least squares anal-
ysis. Correlation coefficients for the resulting equation were greater than
0.9800. See Figure A-3 for representative curves of DO versus time for the
aeration basin and side car.
The DO meters and probes were YSI of Ohio instruments.
In this preliminary work additional parameters were run in an effort to
62
-------
F/M 0.3-** 0.6
DO,
mg/l
6.0
5.0
4.0
3.0
i
2.0
1.0
1
10 20 30 40 50
TIME, MINUTES
AERATION
BASIN
60
Figure A-3. Representative curves - DO vs time -
preliminary study.
63
-------
corroborate the results obtained from the continuous respirometer. These
analyses included: triphenyltetrazolium chloride (TTC); total organic car-
bon (TOC); and adenosine triphosphate (ATP)(blended samples). The TOC was
run according to Standard Methods (A-l) using acidification to eliminate in-
organic carbon. The TTC analysis was performed according to the test proce-
dure proposed by Lenhard et al. (A-2) and modified by Ford et al. (A-3).
The ATP analysis was performed according to the modified test procedure of
Upadhyaya (A-4).
The sampling program employed is listed in Table A-2. Samples were grab
samples from the aeration basin. System configuration precluded obtaining
meaningful samples from the side car.
TABLE A-2. SAMPLING ROUTING - PRELIMINARY WORK
Sample Time,
Number Minutes Comments
1 0 Before shock* was introduced-represen-
ted value of previous 24-hour period
2 15
3 30
4 45
5 60
6 90
7 120
After introduction of shock
After introduction of shock
After introduction of shock
After introduction of shock
After introduction of shock
After introduction of shock
*Controlled F/M change.
The continuous DO readings in both the side car and aeration basin ex-
hibited the correct changes for the variations in the feed. The sampling
did not interfere with these readings.
Results of TTC Analyses
The curves resulting from the daily analysis of the seven samples exhi-
bited similar but inconclusive behavior. Approximately forty-five to sixty
minutes after the shock was introduced a decrease in TTC was noted. This oc-
curred whether the F/M ratio was increased or decreased. Overall curve
shapes are similar. Figure A-4 shows representative TTC curves. By the
seventh sample, two hours after introduction of the shock, the TTC value is
approaching its initial value.
There was a correlation between the TTC value obtained from sample 1
(t * 0) and the ambient, steady state F/M level. See Table A-3 for the re-
sults.
64
-------
1.000
.900
.800
.700
o .600
h-
jB .500
o
.400
.300
.200
.100
(F/MO.6-^0.3)
(F/M 0.3-^0.6)
I
I
_L
I
L
I
20 40 60, 80 100 120 140
TIME, MINUTES
Figure A-4. Representative TTC curves.
65
-------
TABLE A-3.
Run No. Ambient F/M
I 0.3
0.1
0.3
0.6
II 0.3
0.1
0.3
0.6
RESULTS OF TTC
TTC, y moles
0.478
0.442
0.531
0.961
0.362
0.304
0.391
0.846
ANAI YSFS
/'TTC, u moles/ . ^
( mg/1 MLVSS x I0y
1.42
1.48
1.73
2.94
1.10
1.15*
1.45
3.00
*Wasted solids, 20% reduction MLVSS level.
Although these TTC analyses do reflect the difference in influent sub-
strate, the time of response appears to be on the order of 24 hours. The two-
hour sampling period following the introduction of the shock did not provide
sufficient differentiation.
Results of TOC Analyses
TOC analyses were performed on aliquots of the same sample's analyzed for
TTC and ATP. Again, no early differentiation of feed loading was seen with-
in the two-hour sampling period. The total influent at the new F/M loading
contributed a maximum 10% of the total volume of the system at the 2-hour
mark. Differences which correlated well with the steady state F/M level were
obtained 24 hours later from analysis sample 1. See Table A-4 for the resu-
lts of the TOC analyses.
TABLE A-4. RESULTS OF TOC ANALYSES
Run No. Ambient F/M
I 0.3
0.1
0.3
0.6
II 0.3
0.1
TOC, mg/1
77.3
58.7
63.0
80.6
68.1
60.4
(continued)
66
-------
TABLE A-4 (continued)
*»^^4lhi«MHMkM
0.3
0.6 71.2
results of ATP Analyses--
A third aliquot of the samples was analyzed for changes in ATP content.
Procedural problems precluded any meaningful data being obtained from this
analysis. In consideration of the conclusions of the literature review of
ATP, no additional effort was made to repeat the 5-day runs to obtain mean-
ingful ATP data.
At this juncture it was concluded that the continuous respirometer
equipped with DO probes provided a rapid and predictable indicator of micro-
organism activity. The next step was to specifically characterize the sy-
stem's response and reproducibility. This is discussed in detail in the
next section.
Characterization Study
The following experiment was designed to obtain the quantifying informa-
tion on the continuous respirometer:
Simultaneous data was obtained from both the side car and the
aeration basin.
All runs were performed at least twice.
The system was in a steady state at F/M - 0.3. The steady
state was evidenced by monitoring a steady DO level (£0.02
mg/1 average DO variation in a 12 minute period). Ambient DO
levels were maintained as similar as possible between systems
and within the same system from day to day.
[ A shock, changing the F/M, was applied for one hour, and the re-
sulting change in DO was monitored continuously.
The system was returned to an F/M of 0.3 and continuously moni-
tored for one hour.
A reading was taken two hours after the 0.3 F/M feed was re-
applied.
A period of not less than two additional hours was provided at
an F/M of 0.3 for system stabilization.
' A second run at a different F/M shock was then performed in a
similar manner. F/M levels used were 0.1, 0.2, 0.3, 0.4 and
0.5
' Simultaneously (and analogously) two other BioMonitor systems
were run at steady state F/M's of 0.1 and 0.5. Their responses
to the shock loads were monitored.
This experiment was designed to determine the reproducibility of the
systemic change to a repeated shock loading; correlation of response to
shock size; return to pre-shock stability after shock removal; and overall
reliability. Chemical oxygen demand (COD) analyses were performed along with
the DO monitoring. The COD tests were run according to Standard Methods (19),
67 '
-------
TABLE A-5. RESULTS OF INTER-SYSTEMS COMPARISONS
Aeration Basin Side Car
Baseline F/M JU JT3 JET 0.1 0.3 0.5
Average change in DO (ADO/
AT, mg/l/hr) for 0.1 change 0.54 0.37 0.16 0.68 0.49 0.12
in F/M
Average change in DO per
cone., MLVSS (ADO/AT/MLVSS, . n 97 nfi qq ?1 04
mg/1/hr/MLVSS/mg/l) for u ^J u<0
0.1 change in F/M x 10"
Average time to notice a
change of DO of 1.0 mg/1 3.8 5.4 7.6 3.7 7.7 7.9
in minutes
Average % return to
original DO level 2 hours 96 95 96 87 90 79
after removal of shock
Average absolute value of
difference from DO level Q 2 n A n 9 04 02 01
2 hours after removal
of shock, mg/1
TABLE A-6. CORRELATION COEFFICIENTS
Correlation Coefficients
Function for 1st order fit
ADO/At, mg/l/hr vs A F/M units
Aeration Basin 0.989
Side Car 0.995
ADO/At, mg/l/hr/mg/1 MLVSS vs
AF/M units
Aeration Basin 0.992
Side Car 0.995
68
-------
TABLE A-7. RESULTS FROM COD EXPERIMENTS*
Run
F/M Change
Before AM Shock
After AM Shock
End of AM Run
CT»
F/M Change
Before PM Shock
After PM Shock
End of PM Run
I
0.1+0.3
2117
2510
2448
0.1+0.5
2462
2266
2388
II
0.3+0.1
2422
2520
2492
0.3+0.5
2206
2794
2358
III
0.5+0.3
3457
3273
3572
0.5+0.1
3354
3244
3076
IV
0.1+0.2
2064
2198
2058
0.1+0.4
2396
2266
2325
V
0.3+0.2
2377
2319
2354
0.3+0.4
2289
2106
2144
VI
0.5+0.2
3596
3428
3362
0.5+0.4
3188
3134
3057
VII
0.1+0.2
2518
2408
2586
0.1+0.4
2235
2228
2202
VIII
0.3+0.2
2346
2541
2071
0.3+0.4
2230
2142
1958
IX
0.5+0.2
2912
3036
3256
0.5+0.4
3126
2888
2758
results reported as mg/1 COD
-------
TABLE A-8. RESULTS FROM COD EXPERIMENT - MINUS FEED*
Run
F/M Change
Before AM Shock
After AM Shock
End of AM Run
F/M Change
Before PM Shock
After PM Shock
End of PM Run
I
0.1-0.3
1977
2370
2308
0.1-0.5
2342
2099
2226
II
0.3-0.1
2099
2217
2189
0.3-0.5
1883
2446
2055
III
0.5-0.3
2909
2700
3046
0.5-0.1
2806
2743
2570
IV
0.1-0.2
1962
2084
1946
0.1-0.4
2294
2130
2193
v
0.3-0.2
2043
1996
2030
0.3-0.4
1955
1764
1803
VI
0.5-0.2
3044
2913
2843
0.5-0.4
2636
2598
2519
VII
0.1-0.2
2411
2290
2469
0.1-0.4
2128
2088
2066
VIII
0.3-0.2.
2025
2233
1747
0.3-0.4
1909
1811
1620
IX
0.5-0.2
2373
2527
2744
0.5-0.4
2587
2361
2230
results reported as mg/1 COD
-------
The results of these experiments are listed in Tables A-5, A-6, A-7,
and A-8 and Figures A-5 thru A-8. The following summarizations and conclu-
sions can be made:
(a) There is more sensitivity (larger ADO) to a change in F/M loading
in both the side car and aeration basin for the system at the steady state
F/M of 0.1; the least sensitivity at 0.5 F/M.
(b) The system operated at a steady state F/M - 0.1 results in a lin-
ear relationship (in the range studied) for ADO (mg/1) versus F/M and for
ADO [mg/l/hr)/(mg/l MLVSS)] in both the side car and the aeration basin
data. The correlation coefficient of the corresponding first order poly-
nomials are given in Table A-6.
(c) The system operated at a steady state F/M of 0.1 also yields, on
the average, the most rapid response in both the side car and aeration basin
compared to the systems operating at steady state F/M's of 0.5 and 0.3.
There appears to be no significant correlation between average response time
and magnitude of F/M change for any of the three cases.
(d) In the aeration basin, the percent return to original DO level,
that is prior to F/M shock, is 95% or better in all three cases after two
hours. The average percent return in the side car of 86% after two hours re-
flects the comparatively low levels of ambient DO. The DO level in the side
car returned to within an average of 0.2 mg/1 off its original DO value.
(e) The results of the COD experiment are seen in Tables A-7 and A-8.
Table A-7 lists the COD values determined from the aeration basin samples.
Table A-8 lists the COD values less the appropriate, weighted feed value.
The feed value is a function of F/M level in the aeration basin and shock
feed and the percent volume of shock added in two hours. Neither set of
data provides a predictable pattern. This is due, in part, to the problems
of obtaining a truly homogeneous sample from the mixed liquor for analysis.
Another aspect of the COD analysis is that the changes are too rapid to eli-
cit any significant (measurable) response within the organism. -Moreover, the
magnitude of the changes is small. The experiment yielded an average BOD/COD
ratio of 0.77 for the powdered skim milk used. The average ratio of mg
MLVSS/mg COD for the mixed liquor was 0.875 before shocking.
This information characterizes the continuous respirometer system. The
increased sensitivity and rapidity of response at the lowest level F/M in-
vestigated is easily explained: The impact of addition or removal of sub-
strate at the lower feed level is greater because any change represents a
larger percent variation from the steady state. The microorganisms are so
well fed at an F/M - 0.5, that a short change in feed (addition or removal)
has little effect. It is especially evident when comparing ADO/At's between
steady state F/M's of 0.1 and 0.5 (Table A-5). It should be noted, however,
that at a steady state F/M of 0.1, the MLVSS cannot be maintained at a 2500
mg/1 level. They do stabilize fairly well at slightly less than 2000 mg/1.
At this point actual industrial wastes were brought to the laboratory
and applied to the continuous respirometers. The details are given in the
next section.
71
-------
ro
ADO
3.0
2.0
1.0
SIDE CAR
BASELINE F/M = 0,1
BASELINE F/M = 0.3
BASELINE F/M = 0.5
O.I 0.2 0.3 0.4
CHANGE IN F/M
Figure A-5. F/M change vs ADO/At (mg/1-DO/hr) - side car.
-------
-J
CO
ADO
,0
1.0
AERATION BASIN
BASELINE F/M = 0.
BASELINE F/M = 0.3
BASELINE F/M = 0.5
0.2 0.3 0.4
CHANGE IN F/M
Figure A-6. F/M change vs ADO/At (mg/1-DO/hr) - aeration basin.
-------
mg
MLYSS
BASELINE
F/M=O.I
BASELINE F/M =0.3
I
I
I
BASELINE F/M=0.5
I
O.I 0.2 0.3 0.4 O.5
F/M CHANGE
Figure A-7.
F/M change vs ADO/At per MLVSS
(mg/1-DO/hr/mg/l-MLVSS) - side car.
74
-------
BASELINE F/M=0.1
BASELINE F/M=O.3
BASELINE F/M =0.5
L
O.I 0.2 0.3 0.4 0.5
F/M CHANGE
Figure A-8.
F/M change vs ADO/At per MLVSS
(mg/1-DO/hr/mg/l-MLVSS) - aeration basin.
75
-------
Industrial Wastes Study
Samples of two industrial wastes were tested in the laboratory - a dairy
waste and a meat packing waste. The former recycles whey for use in pig
farming while the latter does not retrieve the blood and fat for reuse in
feeds and tallow, etc. The dairy waste has a BOD of approximately 1200 mg/1
with a TSS of 300 mg/1. The meat packing waste has a BOD of approximately
900 mg/1.
Prior to the shockloading of the respirometer with an industrial waste,
the biosystem was acclimated to a low level of the waste for a period of five
days. The system was acclimated with a 3% (by volume with the standard solu-
tion of 0.3 F/M evaporated milk feed) dairy waste. The system was acclimat-
ed at a 1% level for the meat packing waste. Shocks (higher percents by
volume loadings of wastes) were applied for two hours. The system was re-
turned to the proper acclimation feed for 22 hours before the next shock was
applied. The DO levels in the side car were monitored and recorded. All
shock load sequences were performed at least twice.
The results of the industrial shocks are seen in Tables A-9 and A-10.
The results from the meat packing industry show that inhibition (DO increase)
could have been initially experienced. The variation in DO level however is
below the Winkler/DO probe sensitivity comparison. The 1% acclimation period
does not appear sufficient for this,waste which, though high in BOD, has a
large dissolved solids concentration due to the high blood content. The
biosystem appears acclimated after the second shock - a 5% by volume loading.
The decrease in DO (from the 10% shock on) indicates that the microorganisms
were able to utilize the waste substrate entering the system in the remain-
ing shock loadings. This result suggests that not acclimating the system
to the waste prior to a shock load would be preferable. This would result
in a response more indicative of the response observed on location at a
wastewater treatment plant.
The runs using the dairy waste as a shock performed analogously to the
F/M shocks using evaporated milk. This was as anticipated.
The continuous respirometer provides a rapid and predictable response
to controlled laboratory shock loadings. Additional work was undertaken to
fine tune the design and operating parameters of the respirometer. Special
consideration was given to developing a monitor with a more rapid response.
The results of this modification program are discussed in Section 6.
76.
-------
TABLE A-9. RESULTS OF MEAT PACKING INDUSTRIAL
WASTES RUN - SIDE CAR DATA*
Percent Shock,
cone, by vol. ADO, mg/1 PI, 0 16 min.
3 + 0.10
5 +0.09
10 - 0,04
20 - 0.08
33 1/3 - 0.30
*acclimation @ \%
TABLE A-10. RESULTS OF DAIRY INDUSTRIAL
WASTES RUN - SIDE CAR DATA*
Percent Shock,
cone, by vol.
10
20
33 1/3
50
ADO, mg/1 02, @ 16 min.
- 1.08
- 1.19
- 2.29
- 3.36
*acclimation @ 3%
77
-------
REFERENCES
1. "Standard Methods for the Examination of Water and Wastewater," 13th
Edition, Amer. Public Health Assn., Washington, D.C. (1971).
2. Lenhard, G.; Nourse, L.D.; and Schwartz, H.M. "The Measurement of
Dehydrogenase Activity of Activated Sludges," Proc. 2nd Int'l Conf.
Water Poll. Res., Tokyo, Japan (1964).
3. Ford, D.L.; Yang, J.T.; and Eckenfelder, W.W. "Dehydrogenase Enzyme as
a Parameter of Activated Sludge Activities," Proc., 21st Ind. Waste Conf.,
Purdue University, West Lafayette, Indiana (1966).
4. Upadhyaya, A.K., "Determination of Relationships Between Biodegradable
Fraction and Viable Mass in Activated Sludge Systems and Their Signifi-
cance in Design," Ph.D. Dissertation, Vanderbilt University, Nashville,
Tennessee (1973).
78
-------
APPENDIX B
DEVELOPMENT OF PROPOSED MATHEMATICAL MODELS FOR
BIOMONITOR RESPONSE
In general, the literature indicates that a lag in the response of
specific growth rate to changes in influent flow rate and substrate concen-
tration exists (B-l-B-3). The Monod model (B-4) is unable to predict the
dynamic behavior of microbial growth subject to the changes in dilution rate
and influent substrate concentration. More complicated models accounting for
physiological state of microorganisms are necessary to achieve even qualita-
tive agreement of model with experimental data.
BASIC CONCEPTS OF MICROBIAL GROWTH
In aerobic biological waste treatment systems, the influent organic sub-
strate is contacted with activated sludge of the mixed liquor in aeration
basins. The activated sludge reacts biochemically with the organic matter,
converting it to carbon dioxide, water, and additional sludge mass. Equation
(B-l) depicts the reaction and is the basis for the model developed in this
study.
Soluble Substrate + 0 Microorganisms , Active Cells
Soluble Substrate + 02 > Nonactive Cells
Biodegradable Residue
Nonbiodegradable Residue (B-l)
C02
H20
A serial conversion of soluble substrate to active mass and nonactive mass,
as depicted in Figure B-l, will be assumed. Total organic carbon (soluble)
concentrations in influent and effluent will be measured as organic substrate
and volatile suspended solids of mixed liquor as biomass concentration.
The basic relationships between the specific growth rate of microorgan-
isms and the concentration of soluble substrate are discussed below.
A variety of mathematical models have been proposed to describe the
basic kinetics of microbial growth and substrate removal in the activated
sludge system. In 1942, Monod (B-4) proposed a kinetic model of microbial
growth in pure culture which depends on the cell and substrate concentrations,
The growth rate of microorganisms may be expressed as follows:
dX/dt - UX (B-2)
79
-------
Nonactive
Mass
(SS and VSS)
Soluble
Residue
(TOG)
7\
Soluble
Substrate
(TOG)
**
Active
Mass
(SS and VSS)
Soluble
Residue
(TOG)
Soluble
Substrate
(TOG)
Soluble
Residue
(TOG)
Inert
Residue
(SS and VSS)
SYNTHESIS METABOLISM
ENDOGENOUS METABOLISM
* Noribiodegradable
** Biodegradable
Figure B-l. Microbial metabolism in soluble substrate.
-------
where y is the specific growth rate and X is the concentration of bacterial
cells. Monod found that the value of y is not constant, but depends on the
concentration of growth limiting substrate, S, according to the equation:
y - ym S/KS + S (B-3)
The maximum growth rate, y , and the saturation constant, K , are kinetic
parameters, and are assumed to be constant for a specific system. When the
substrate concentration is low with respect to the value of K , equation
(B-3) may be simplified into a first order equation in the manner of Garrett
and Sawyer (B-5)
y - ym/Ks S - KS (B-4)
Monod also suggested that the relationship between the growth of bac-
teria and utilization of substrate be represented by:
-dS/dt - 1/Y dX/dt (B-5)
where Y is referred to as the yield factor which he assumed to be constant.
This model has been widely used to predict steady state growth rate and to
design the CMAS process with some success (B-6). However, Storer and Gaudy
(B-l) and Sherrard (B-7) found the yield factor varies with growth rate ra-
ther than remaining constant.
Koga and Humphrey (B-2) discussed the dynamic response of a chemostat
as predicted by the Monod empirical model. They concluded that the Monod
model is inadequate to predict the dynamic behavior observed in chemostat
experiments. Kono and Asai (B-8) introduced physiological activity in
growth kinetics to account for lag phase and declining phase. According to
the studies on transient loadings Young et al. (B-3) also noted that the
Monod model is not satisfactory for predicting unsteady state microbial
growth.
Tebbutt and Christoulas (B-9) showed that a first order reaction with
retardation as proposed by Fair et al. (B-10) satisfactorily described
treatment kinetic with sewage.
-ds/dt - KX(S/S0)nS (B-6)
For n * 0, equation (B-6) describes a linear kinetic model of substrate re-
moval, it is the form as a first order reaction proposed by Tischler and
Eckenfelder (B-ll).
By integrating for the range 0 £ n <_ 2, Equation (B-6) may be express-
ed approximately as (B-l2):
So " S/So " AC0*0)6/1 + A(KX6)B (B-7)
where:
A - 0.585 + 0.415 exp (-1.4695n)
81
-------
B = 1/(1 - 0.2267n)
8 * hydraulic residence time in the system
Grau et al. (B-13, B-14), on the basis of numerous experiments and af-
ter thorough theoretical analysis, proposed the following differential equa-
tion for multi-component substrate removal kinetics:
-dS/dt - KnX(S/SQ)n (B-8)
where n is the formal order of reaction. For n = 1, Equation (B-8) may be
reduced to the Eckenfelder kinetic model (B-15) as:
-dS/dt - KX S/SQ (B-9)
Equation (B-9) logically states that the removal rate, dS/dt, decreases as
the fraction of substrate remaining, S/S , to be moved decreases. The ra-
tionale for this rests in the fact that as the more readily removable com-
pounds are exhausted, those yet to be removed result in a decreasing removal
rate.
It is assumed that within the mixed liquor of activated sludge there
exist active (or viable) cells of concentration X which increase in cellu-
lar mass at a rate directly proportional to their cellular mass at any time,
then:
(dXa/dt) synthesis - yxaXa (B-10)
By introducing the yield factor, Y, defined as units active mass synthesized
per unit soluble substrate utilized, it gives:
(dXa/dt) synthesis « -Y ds/dt (B-ll)
In accordance with the concept of Sinclair and Topiwala (B-16) active
mass is lost by endogenous metabolism (endogenous respiration and cellular
death) to provide maintenance energy for viable cells. The rate of endogen-
ous metabolism is assumed to be first order with respect to active cells
with a constant specific rate, b:
(dXa/dt)endogenous metabolism= -bXa (B-12)
Combining Equations (B-10) and (B-12) an expression for the net growth rate
of active cells is obtained:
(dXa/dt>net growth^xaXa ' bXa
During the endogenous metabolism some of the active cells are assumed
to die and release their contents back into the mixed liquor to serve again
as soluble substrate for the surviving microorganisms. However, some con-
stituents of the cell material are nonbiodegradable and remain as part of
the biomass (nonactive cells). Thus, the rate of production of nonactive,
but previously active, cells is proportional to the rate of breakdown of
active cells due to cell lysis and endogenous respiration:
82
-------
dXn/dt - a bXa (
According to Kountz and Forney (B-17), approximately 75-80% of the microbial
cells is biodegradable and remaining 20-25% is nonbiodegradable residue, i.e.,
a = 0.20 - 0.25 (B-15)
The total volatile suspended solids in the mixed liquor is defined as:
Xv - "a * "n '* "io
The inert organic matter, X. , in the system is so small with respect to
total biomass that it may be neglected and Equation (B-16) may be reduced
to:
Xv = Xa + Xn (B-17)
The net rate of biomass production in the system would then be expressed as:
dXv/dt = (yxa - b + ob) Xa (B-18)
In aerobic biological systems the dissolved oxygen will be consumed by
microorganisms for synthesis and endogenous metabolism. The oxygen required
for synthesis is proportional to the substrate utilized while the oxygen
consumed during endogenous metabolism is proportional to the endogenous rate.
The oxygen uptake rate is:
R = a'/Y u X, + b1 bX3 (B-19)
Xa a a
Then the specific oxygen uptake rate may be expressed as:
r=a'/Yu , + b'b (B-20)
A a
With material balance, mathematical relationships for each completely
mixed biological treatment system may be developed for soluble substrate,
active mass, and total mass. The general mass balance equation is:
Accumulation = Input - Output ± Conversion (B-21)
It is noted that the soluble substrate concentration released by cells
decomposition during endogenous metabolism is not taken into account for the
overall substrate balance. Although efforts have been made about such vari-
ous substrate sources (B-18, B-19) it is doubtful whether the present state
of knowledge and the difficulties inherent in parameter prediction justify
their use for design and operation practice.
STEADY STATE OF ACTIVATED SLUDGE UNIT
If the system shown in Figure B-2 is operated at steady state condition
and the sludge is wasted daily to remain specific volatile suspended solids
for various influent substrate concentrations; the mass balance equations
83
-------
Fo , so , co
Air
F S X C
e
, e ,
Figure B-2. Schematic of activated sludge unit.
Air
Fo
1
1
1
'
Ve,C2
f~
S2
x2
C2
V2
l_
itr
F-F0
S
X
C
V
t
\
1
1
1
1
t
i
^ F^, Sp> C/^>
0, 0, 0
Air
Figure B-3. Schematic of BioMonitor.
84
-------
for soluble substrate, active mass, and total mass are:
Soluble Substrate Balance
0 - FQ(S0 - S) - 1/Y yxaXaV (B-22)
Active Mass Balance
0 * ° - FoXae - Wa + ^xaXaV ' bXaV <
Total Mass Balance
0 = ° " FoXve " Wv + (yxa ' b + ab) XaV t
If all biomass are homogeneously mixed within the aeration basin and
the clarifier and the accumulation of biomass in the clarifier is negligible,
i.e.:
Xa/Xv * Xae/Xve = Wa/Wv <*-25>
Thus, the definition of mean cell residence time may be written as:
8c = XvV/FoXve + Wv - XaV/FoXae + Wa
Equation (B-23) can be rearranged and Equation (B-26) can be substituted in-
to the result to give:
yxa = 1/8C + b (B-27)
Substituting Equation (B-27) into Equation (B-22), it gives:
Xa = 6cY(So ' S)/e(1 + bec) (B'28)
where 6 is hydraulic residence time, V/F . Substituting Equations (B-26),
(B-27) and (B-28) into Equation (B-24) and solving for Xy, it yields:
,*v = Y(SQ - S) 9c/9 (1 + ab6c)(l + b6c) (B-29)
The activity of the mixed liquor in activated sludge system is defined
as the active cell fraction, i.e., the active mass divided by the total bio-
mass. Hence, the activity, x, may be shown:
x = Xa/Xv - 1/1 + ab8c (B-30)
STEADY STATE EVALUATION OF BIOMONITOR
Based on the schematic diagram of the BioMonitor shown in Figure B-3
at steady state the material balance on soluble substrate, active mass, to-
tal mass, and oxygen concentration will yield:
85
-------
Contact Chamber
Soluble Substrate Balance
° Vo +
Oxygen Concentration Balance
0 = FCr(F-F0)C2-F0C2-R2V2 + KLa2(C2*-C2)V2 (B-38)
At steady state the microorganisms both in contact chamber and the
aeration basin provide the same physiological state, i.e., same activity,
thus:
Xal/Xvl + Xa2/Xv2 = Xae/Xve = Wa/W
v
also b] = b2 = b, Y] = Y2 = Y
From Equations (B-32) and (B-33) and Equations (B-36) and (B-37), it is evi-
dent that:
Equations (B-31-33) and Equations (B-35-37) mav be rewritten as follows:
86
-------
Contact Chamber
0 ' FoSo + (F-Fo>S2 - FS1 '
0 - (F-F0)Xa2 - FXal + yxaXalVl - b X^ (B-42)
0 - (F-FQ)Xv2 - FXvl - (yxa - b + ab^ (B-43)
Aeration Basin
0 - FST - (F-FQ)S2 - FQS2 - 1/Y y^V,, (B-44)
0 - FXal - (F-FQ)Xa2 - FQXae - Wa + yxaXa2V2-bXa2V2 (B-45)
0 - FXvl - (F-Fo>Xv2 - FoXve-Wb + Ka-b+ab>Xa
Now the mean cell residence time may be defined as:
9cl = Xvl
9c2 * Xv2ov2 + FQXve + Wv -
Xa2V2/(F-F6>Xa2 + FoXae + Wa ' FXal
Substituting and rearranging Equations (B-41)-(B-46), it yields:
Contact Chamber
yxa - l/ecl + b (B-49)
xal = Y/V1[F0(S0-S2)+F(S2-S1)]/(l/9cl + b) ' (B-50)
Xvl ' YCFo
-------
DYNAMIC MODELS OF THE BIOMONITOR
At unsteady state conditions equations derived for steady state may be
modified and give:
Contact Chamber
Soluble Substrate Response
»1 d₯dt Foso * Xa2 - FXal + ^xalXa!Vl ' b XalVl {
Total Mass Response
V]dXvl/dt = (F-FQ)Xv2 - FXyl + (yxal-b+ab)XalV1 ' (B-58)
Oxygen Concentration Response
VI dtydt - FQC0 + (F-FQ)C2 - FC1 - R1V1
+ KLa1(C*-C1)V1 (B-59)
Aeration Basin
Soluble Substrate Response
V2 dS2/dt = FS1 - FS2 - 1/Y Pxa2Xa2V2 (B-60)
>
Active Mass Response
V., dXa2/dt - FXal -
-------
LIST OF ABBREVIATIONS AND SYMBOLS
ABBREVIATIONS
a1
b
b1
C
C*
K
r
S
V
w
a
SUBSCRIPTS
0
1
2
oxygen consumed per unit substrate utilized, dimensionless
endogenous metabolism rate, T"'
oxygen required per unit active biomass lost by endogenous
metabolism, dimensionless _3
dissolved oxygen concentration, ML _-
saturated dissolved oxygen concentration, ML _~
steady state dissolved oxygen concentration, ML
flow rate, L3r'
reaction rate constant, T~' or M~iL3T~'
overall oxygen transfer coefficient, T"'
nth order reaction rate constant, T~l
saturation constant, ML"3
oxygen uptake rate by microorganisms, ML"3T~'
specific oxygen uptake rate by microorganisms.
soluble substrate concentration, ML"3
reactor volume, L3
active biomass wasted per day, MT"1
volatile suspended solids wasted per day,
active biomass fraction in mixed liquor,
active biomass concentration, ML"3
r-1
MI'1
dimensionless
active biomass concentration in effluent, ML"3
inert organics concentration, ML"3
nonactive biomass concentration, ML"3
volatile suspended solids concentration, ML"3
yield factor, dimensionless
nonbiodegradable fraction of microbial cell materials,
dimensionless .
specific growth rate, T"1 _-|
maximum specific growth rate- T
microbial synthesis rate, T"1
hydraulic residence time, T
mean cell residence time, T
influent
contact chamber
aeration basin
89
-------
REFERENCES
B-l Storer, F.F., and Gaudy, A.F., Jr. "Computational Analysts of Trans-
ient Response to Quantitative Shock Loadings of Heterogeneous Popu-
lations in Continuous Culture," Enviro. Sci. Tech., 3, 143-149
(1969).
B-2 Koga, S. and Humphrey, A.E. "Study of the Dynamic Behavior of the
Chemostat System," Biotech. Bioeng., 9, 375-386 (1967).
B-3 Young, T.B.; Bruley, D.F.; and Bungay, H.R. III. "A Dynamic Mathemati-
cal Model of the Chemostat," Biotech. Bioeng., 12, 747-769 (1970).
B-4 Monod, J. "Recherches sur la Croissances des Cultures Bacteriennes,"
Hermann et Cie, Paris (1942).
B-5 Garrett, M.T., Jr. and Sawyer, C.N. "Kinetics of Removal of Soluble
BOD by Activated Sludge," Proc. 7th Ind. Waste Conf., Purdue Univ.,
West Lafayette, Indiana (1952).
B-6 Lawrence, A.W., and McCarty, P.L. "Unified Basis for Biological Treat-
ment Design and Operation," J. San. Eng. Div., ASCE, 96, 757-778
(1970).
B-7 Sherrard, J.H. Ph.D. Thesis, Univ. of California, Davis (1971).
B-8 Kono, T. and Asai, T. "Kinetics of Continuous Cultivation," Biotech.
Bioeng., 11, 19-36 (1969).
B-9 Tebbutt, T. H. Y., and Christoulas, D.G. "Performance Studies on a
Pilot-Scale Activated Sludge Plant," Water Poll. Cont., 74, 701-710
(1975).
B-10 Fair, G.M.; Geyer, J.C.; and Okun, D. "Water and Wastewater Engineer-
ing," Vol 2, John Wiley & Sons, Inc., New York (1968).
B-ll Tischler, L.F., and Eckenfelder, W.W., Jr. "Linear Substrate Removal
in the Activated Sludge Process," Proc. 4th Int'l. Water Poll. Res.
Conf., Prague (1969).
B-l2 Christoulas, D.G., and Tebbutt, T.H.Y. "Mathematical Model of a Com-
plete-Mix Activated Sludge Plant," Water Res., 10, 797-804, (1976).
B-13 Grau, P., and Dohanyos, M. "Substrate Removal Kinetics of Activated
Sludge," Vod. Hospod. B20, 298-305 (In Czech) (1970).
90
-------
B-14 Grau, P.; Dohanyos, M.; and Chudoba, J. "Kinetics of Multi-Component
Substrate Removal by Activated Sludge," Water Res., 9. 637-642
(1975).
B-15 Adams, C.E., Jr.; Eckenfelder, W.W.; and Hovious, J.C. "A Kinetic
Model for Design of Completely Mixed Activated Sludge Treating Vari-
able-Strength Industrial Wastewater," Water Res., 9, 37-42 (1975).
B-16 Sinclair, C.G., and Topiwala, H.H. "Model for Continuous Culture which
Considers the Viability Concept," Biotech. Bioeng., 12, 1069-1079
(1970).
B-17 Kountz, R.R. and Forney, C., Jr. "Metabolic Energy Balances in a
Total Oxidation Activated Sludge System," Sew, Ind. Wastes, 31,
819-826 (1959).
B-18 Martin, E.J., and Washington, D.R. "Kinetics of the Steady-State Bac-
terial Culture-I. Mathematical Model," Proc. 19th Ind. Waste Conf.,
Purdue Univ., West Lafayette, Indiana (1964).
B-19 Westberg, N. "A Study of the Activated Sludge Process as a Bacterial
Growth Process," Water Res., 1, 795-804 (1967).
91
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APPENDIX C
PILOT PLANT INVESTIGATIONS
DESCRIPTION OF PILOT PLANT
Figure C-l is a detailed schematic of the pilot plant system with the
various components defined. Actual pictures of the system are seen in Fig-
ures C- 2 and C- 3 . The trailer holding the components is40 feet long by
8 feet wide. The pilot plant consists of six plug flow aeration basins with
an approximate volume of 300 gallons (252 cubic feet) each. Each compart-
ment measures 3' x 2' x 7' deep. The total outside dimensions are 9' x 4' x
7.8' deep. The effective standing water depth is 7 feet. The effluent from
basin six enters a secondary clarifier set up for return sludge to basin one.
The biological clarifier is 7 feet in diameter at wier level with a surface
area of 38.5 square feet. The maximum flow through the system is 13.4 gal-
lons per minute.
Baseline feed to the system is the primary effluent from Metro's (Nash-
ville's) Central Sewage Treatment System. The average BOD for the primary
effluent during the test period was approximately 110 mg/1. Metro Central
Wastewater Treatment Plant has a capacity of 68 MGD. Feed is pumped in at
1.7 gallons per minute. The return sludge is pumped in at 3.5 gallons per
minute in an effort to maintain a solids level of 3500 mg/1 MLSS and 2500
mg/1 MLVSS. This combined flow of 5.2 gallons per minute effects a one hour
retention per basin for a total system retention time of six hours. Minimum
retention time for the system is 2.34 hours for 6 basins, of 0.39 hours per
basin. >
A dye study was performed to determine the flow pattern of the pilot
plant, i.e., breakthrough times of the individual basins. Three mis of
Rhodamine W.T. dye (concentration 21,000 ppm) was added to aeration basin I.
Percent transmission was read on an Aminco Fluoro-Micro Photometer set at a
meter multiplier of 0.3 and a sensitivity of 30%. Maximum percent transmis-
sion was set at 100% with tap water and dye. The zero percent transmission
blank was tap water. Influent flow during the study was 2.2 gpm and return
sludge was 3.2 gpm for a total of 5.4 gpm flow through the system. The av-
erage effective volume of each of the 6 basins is 314 gallons. Therefore,
the theoretical retention time at this flowwas58 minutes or 0.967 hours.
A problem seemed to occur with the fluorometer measurements approximate-
ly 2 hours into the proposed five hour study. There arose the possibility
that a local textile manufacturer was discharging (as it is known to do) some
of its red dye which was fluorescing and confusing the measurements. The
92
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Effluent from Pilot Plant Study
vo
CO
Primary Effluent Trench of .WTP
Code
Number
1
2
3
4
5
6
8
9
10
11
12
13
14
15
16
17
KEY
Component
Pressure filter
Splitter box
Aeration basin
Air compressor
Air system & flow meters
Secondary sludge return
pump
Biological claHfler
Chemical sludge thickener
Flocculation tank
Line tank
"to waste"
Chemical clarifler
Mixing tank - baffled
Flow splitter
Tank
Pump regulators
Electrical control box
Dimensions/description
3' diameter, 5.7' high
3' x 2", 7'swd*
overall dimensions
9' x 41 x 7.8'
5 hp, 3495 rpm
1.5 hp, 1725 rpm
variable speed
ID, 7.3'; 00, 8'
2' swd
3' x 4' x 4.5'
2.2' diameter; 5.9' deep
_ Influent for
Pilot Plant
Study
a)
b)
5' diameter; 2.5 swd
3' diameter1 4 ..5 swd
tank: 2' x 6' x 4' deep
mixers: % hp, 1725 rpm
lh hp, 1750 rpm
*swd « standing water depth
Figure C-1. Detailed schematic of pilot
plant.
-------
I
Figure C-2. Full View of Pilot Plant Facilities
-------
Figure C-3. Close-up of Pilot Plant
Aeration Basins
-------
study was continued through approximately 3 1/2 hours with plans to restudy
the problem at a later date.
A second dye study was performed 2 weeks later. This delay permitted the
system to flush itself of residual dye. Operating parameters at this time
were: same fluorometer as previously employed with the same meter multiplier
of 0.3 but a sensitivity of 37. Tap water and dye was again the blank used
to calibrate 100% transmission. The "zero" blank was tap water. There was
one major difference. Tap water at a rate of 5.4 gpm was pumped into the
system in place of the raw sewage feed and return sludge. This eliminated
not only the spurious readings from the industrial dye but also reduced the
possible errors due to dye adsorption onto the biofloc.
Theoretically the basin is a plug flow unit; therefore, the theoretical
breakthrough of dye in each compartment is a spike occurring in basin II one
hour after the dye is added to basin I; 1 hour after basin II in basin III,
etc. The breakthrough point in the clarifier was taken at the first signi-
ficant increase in the reading. The values listed for aeration basin I in-
dicate the time at which the dye reached the level initially monitored in
the clarifier. Background levels in the basins averaged about 12%. Mixed
liquor was in the basins before the introduction of the tap water. The
background level of fluorescence in the clarifier was around 3%.
The results of these two dye studies are seen in Table C-l. The results
indicate some short-circuiting in the system. Time from peak to peak should
be one hour. Our data reveal travel times (distance between peaks) of 1.42,
0.50, 0.83, 0.83 and 0.67 hours for an average value of 0.85 hours. This
information will be integrated in the analysis of results obtained during
the shocking procedures described below.
Industrial Wastes Shock Program
The following general experimental procedure was employed for each of the
three industrial wastes monitored. The system was stabilized with respect
to solids level and equipment performance. The WWTP primary effluent was
pumped to the splitter box. Adjustment in flow was made both at the pump
and by variation in the overflow gate position. The industrial waste used
to shock the system was also pumped into the flow at the splitter box. Ad-
justment in flow was made at the pump. An additional contact container be-
low the splitter box outfall was added to effect sufficient mixing between
the sewage and industrial waste. It was from this second contact container
that the sample was pumped to the BioMonitor. The additional mixing con-
tainer and longer connecting tubing caused a delay (increase cf laboratory
studies) in response time of the BioMonitor to about four minutes.
The BioMonitor, pumps, meter and recorder were set up in a weather sta-
tion box alongside the trailer. Figures C-4 and C-5 show the setup employed.
A second weather station box was set up on the trailer bed. This housed e-
quipment, additional supplementary tests, materials for oxygen uptakes,
maintenance paraphernalia, clean-up accessories, etc.
96
-------
-
Figure C-4. Close-up of BioMonitor at pilot plant
-------
.* I
Figure C-5. Close-up of auxiliary equipment at pilot plant
-------
TABLE C-1. RESULTS OF PILOT PLANT DYE STUDIES
Location,
Basin#
1**
2
3
4
5
6
clarifier
7/19 Study
not reached
@3.4 hr
1.27
1.74
1.74
1.96
1.96
2.8
Breakthrough
8/3 Study
3.67
1.42
1.92
2.75
3.58
4.25
Time, hours*
Theoretical
1.00
2.00
3.00
4.00
5.00
6.00
*After addition of dye to aeration basin I.
**Time at which aeration basin I is flushed to the fluorescence level
initially monitored in the clarifier.
The testing and sampling program set up at the pilot plant was as fol-
lows: the shock load applied for 15 minutes. The baseline feed flow was
reduced by the flow of waste to maintain the same retention time. A single
shock load was studied per day. Fresh industrial wastewater was brought in
daily. They were transported in plastic-lined 55 gallon drums. The wastes
studied in this part of the project were: (a) food (potato) processing;
(b) meat processing; and (c) electroplating. The schedule of the pilot
plant sampling program is given in Table C-2.
Potato Processing Waste
The potato processing waste had an average BOD of 256 mg/1 and a TOC of
230 mg/1. The waste was at a very high pH (=< 11) because of a caustic peel/
cleaning step in the process.
During the three days of testing the potato processing waste, the re-
turn sludge flow was maintained at 3.5 gpm. The sewage feed flow to the pi-
lot plant was controlled at 1.8 gpm for the one day and 1.65 gpm for two
days. The shock flows of potato processing wastes were: 1.8 gpm (or 100%
on day one) and 1.2 and 0.6 gpm on the two 1.65 gpm days (73% and 36, re-
spectively). Shock loading with potato waste was applied to a steady-state
system (with reference to the DO level in the BioMonitor) and lasted 15 min-
utes. The effect of the shock was then monitored through the pilot plant
system for 6 hours. The BioMonitor unit at the time of the tests had a
feed flow rate of 20 ml/min and an average return rate of - 70 ml/min.
Upon addition of the potato waste at the 36% and 100% contribution of
the total feed flow the change in DO was positive (i.e., DO increased).The
73% contribution caused a decline in DO level. Assuming minimum variability
in the waste as supported by individual TOC analyses on each day's
99
-------
TABLE C-2. PILOT PLANT SAMPLING PROGRAM
o
o
Time*
continuous
before
0
7 min
15 min
30 min
1 hr**
2 hr
3 hr
4 hr
5 hr
Biomonitor A.B. I
DO Solids TOC 02*** DO Solids TOC
X X
X XX
X
X
X
X
X
X
X
X
X
02
X
X
X
X
X
X
X
X
X
X
A.B. IV
DO Solids TOC
X
X
X
X
X
X
02
X
X
X
X
X
X
A.B. VI
DO Solids TOC
X
X
X
X
X
X
02
X
X
X
X
X
X
*With reference to shock period - "0" is beginning of shock
**TOC samples are collected at one time on the hour from all three basins.
02 uptake samples are on the hour, quarter hour and half hour for
aeration basins 1, 4, and 6, respectively.
***0xygen uptake
-------
waste and the simple nature of the industrial process involved, the following
explanation is submitted: one problem plagued both the reproducibility and
correlation of data throughout the pilot plant study. Specifically, this is
the inherent variability of the feed stream (raw sewage) at the large WWTP
A study was made to test the variation in the influent flow. TOC was the
monitoring parameter. The results are seen in Table C-3. A large variation
is seen in Aeration Basin I. The variations are less in later basins as an-
ticipated.
TABLE C-3. TOC ANALYSES - "STEADY STATE"*
Time into Shock A.B. I A.B. IV A.B. VI
0
7 min
15 min
30 min
1 hr
2 hr
3 hr
4 hr
5 hr
74.7
90.9
86.9
116.0
43.8
80.9
64.0
114.9
102.3
85.3
92.5
66.9
58.8
78.8
72.2
107.8
69.2
69.2
76.3
74.0
74,2
*No external shock applied; reflects natural variations.
Average TOC values, mg/1, including variances are: AB I 86.0 ± 28%; AB IV
75.8 ± 16%; and AB VI 78.5 ± 19%. Samples were obtained from the pilot plant
for this study when no external shock was applied. Therefore, the BioMonitor
is measuring not only the industrial "overlay" but also the natural week-day
variations.
To test the accuracy of our results, a split sample was run with
£PA's RSKERL Laboratory on the TOC analyses of filtered mixed liquor from
the pilot plant aeration basins. The results are seen in Table C-4.
It was possible, however, for the BioMonitor to exhibit relatively stable
periods. But again, such times were unpredictable. Preliminary work was
performed on DO changes in quiet times to later analyze the significant of
the change in DO in the BioMonitor during shock periods. The results are as
follows: over the five hour monitoring period the variation in DO level dur-
ing nonshock periods averaged ± 0.05 ppm 02 in a 15 minute time span. The
standard deviation (a) was ± 0.03 ppm (3a= ± 0.09 ppm 02). Again, this vari-
ability is neither predictable nor controllable. While this quality serves
the project well for the on-site location studies, it is not conducive to
good results when shocking in the "overlay" manner described. Similarly,
this problem was avoided in the laboratory by adding the shock to an inten-
101
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TABLE C-4. TOC ANALYSIS - SPLIT SAMPLE (MG/L)
Sample Kerr VU % difference*
A.B. 1
A.B. 2
Avg. filter
paper
leachate
35.5
36.5
8
37.8
39.0
5
3.1
3.3
*% difference - ((VU-Kerr)/(VU+Kerr)) x 100
tionally very reproducible and steady baseline feed. The laboratory results
were reproducible and able to be meaningfully correlated as discussed earli-
er. Fortunately, the pilot plant is an artificial, contrived situation and
as such not to be routinely encountered when the BioMonitor is in actual use.
Specifically, it appears that during the test at the 73% level some con-
stituent in the sewage caused the DO level to decrease or conversely - some-
thing else during the other two tests caused the DO to increase. Because of
the high pH of the waste the possibility of inhibition seems strong and so
that the former conjucture (a spurious DO decrease) seems the more probable.
Table C-5 lists the ADO values found for the three levels of shock load-
ing. Considering only the absolute magnitude of the change there is good
correlation between ADO with time into shock period for all 3 cases individ-
ually. However, the ADO does not correlate magnitude of shock applied for
the two positive ADO cases. This too could be a result of other components
in the feed working against the anticipated magnitude of change.
TABLE C-5. ADO, PPM, IN BIOMONITOR POTATO
PROCESSING WASTE-PILOT PLANT STUDY
Time into Shock, Percent Waste
minutes 36 73 100
0
2
4
8
12
15
0
-
0.02
0.57
0.80
1.00
0
-
-0.07
-0.25
-0.42
-0.50
0
0.04
0.12
0.14
0.19
0.24
Oxygen uptakes were performed on the aeration basin liquor of the pilot
102
-------
plant during these three shock runs. Samples were taken from aeration basins
I, IV, and VI. The results are seen in Tables C-6, C-7 and C-8. An oxygen
uptake should decrease to correlate correctly with an increase in DO, and,
conversely, increase to correlate correctly with a decrease in DO. The vol-
ume of the shock compared to the volume in the pilot plant's aeration basins
was small. As evidenced in the results of our oxygen uptake studies, so was
its effect. Variation in the oxygen uptake essentially reflectedthe changes
in raw sewage stream composition.
TABLE C-6. OXYGEN UPTAKE DATA (MG/L/HR)
POTATO PROCESSING WASTE - 36%
Time into
before
0
7 min
15 min
30 min
1 hr
2 hr
3 hr
4 hr
Shock A.B. I*
28.8
22.5
25.0
28.0
29.2
42.4
63.0
28.0
34.8
A.B. IV
21.6
21.0
20.0
16.0
15.6
A.B. VI
18.8
21.8
17.7
13.0
15.0
*A.B.
» aeration basin
TABLE C-7. OXYGEN UPTAKE DATA (MG/L/HR)
POTATO PROCESSING WASTE - 73%
Time into
before
0
7 min
shock A.B. I*
21.6
24.3
25.5
A.B. IV
19.2
A.B. VI
18.0
15 min 33.3
30 min
1 hr
2 hr
3 hr
4 hr
5 hr
23.4
29.7
51.0
63.8
68.4
63.9
19.8
24.3
21.0
19.8
20.2
19.2
21.3
19.2
22.5
19.2
*A.B. - aeration basin
103
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TABLE C-8. OXYGEN UPTAKE DATA (MG/L/HR)
POTATO PROCESSING WASTE - 100%
Time into Shock
before
0
7 min
15 min
30 min
1 hr
2 hr
3 hr
4 hr
5 hr
A.B. I*
19.8
48.0
41.6
39.0
30.0
30.0
34.5
36.9
34.5
, A.B. IV
23.1
21.6
21.6
19.2
21.0
22.2
A.B. VI
24.3
21.0
21.0
21.0
22.6
21.4
*A.B. » aeration basin
Table C-9 lists the results of TOC analyses during the three shock periods
and for 6 hours afterwards. All TOC analyses were performed on a Beckman 915
Total Carbon Analyzer. Again, the variation in results seemed to reflect
changes in the raw sewage composition rather than a meaningful correlation
with the shock application and diminution.
Later in an effort to obtain more meaningful data a series of short
shocks using the potato processing waste was performed. The oxygen uptake
was monitored. The data is given in Table C-10. While the oxygen uptakes of
the shock periods are uniformly higher than those values obtained for the
"normal" feed periods proceeding them, the difference is not significant.
The accuracy of an oxygen uptake test is probably on the order of ± 10%. As
such, this data also appears inconclusive.
104
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TABLE C-9. POTATO PROCESSING WASTE - PILOT PLANT STUDY
TOC VALUES (MG/L)
Time into Shock
0
7 min
15 min
30 min
1 hr
2 hr
3 hr
4 hr
5 hr
0
7 min
15 min
30 min
1 hr
2 hr
3 hr
4 hr
5 hr
0
7 min
15 min
30 min
1 hr
2 hr
3 hr
4 hr
5 hr
A.B. I
68.4
66.0
63.5
90.6
69.7
80.2
74.6
70.0
69.7
71.2
63.3
73.8
68.9
62.5
69.9
69.5
65.7
-
88.0
99.3
71.4
-
-
66.3
49.8
69.8
76.1
A.B. IV
73.4
67.4
70.1
67.8
63.7
63.4
57.9
79.0
68.8
67.8
53.3
55.8
65.3
A.B. VI % shock
66.0 36
51.8 73
73.9
-
74.3
61.4
59.6
52.9 100
57.3
62.3
52.7
-
48.8
105
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TABLE C-10. OXYGEN UPTAKE (A.B. I) - SERIES OF
SHORT SHOCKS - POTATO PROCESSING WASTE
Time Oxygen Uptake.. , Nature of Time
(mg/l/hr) Period Represented
10:25 a.m.
10:45
11:10
11:30
11:45
12:00 noon
12:18
12:34
12:58
1:15
52.0
68.5
75.0
67.5
68.1
64.2
66.6
67.2
67.5
67.0
normal feed
normal feed
normal feed
zero time
(normal feed)
shock I
normal feed
shock II
normal feed
shock III
normal feed
Meat Processing
Because of the large waste volumes required in this part of the project,
a different meat processing industry was used as a source of waste from that
employed in the laboratory shock tests. This plant reclaimed both blood and
fats. The representative BOD level in this waste was approximately 800 mg/1.
Shock load experiments were carried out in the same manner as those conduct-
ed with the potato processing waste. The operating parameters for the runs
are given in Table C-ll. Weather conditions precluded a third run. The re-
sultant changes in DO are given in Table C-12.
Tables C-13 and C-14 list the oxygen uptakes determined for the three
basins. The changes in the oxygen uptake in aeration basins da correspond
to the directions of the changes in DO in the BioMonitor. In the first run
(Table C-13), when the BioMonitor exhibited an increase in DO, the oxygen
rate accordingly decreased from zero time through two hours. This increase
in DO experienced a high BOD waste was attributed to the possibility of a
disinfectant (from washing the plant floors) in the waste. The A.B. IV oxy-
gen uptake exhibited a decrease from 2 through 4 hours. Peak time from the
dye studies in aeration basin IV is 2.75 hours.
In the second run (Table C-14), the BioMonitor exhibited a decrease in
DO as anticipated from the meat packing waste. The Aeration Basin I oxygen
uptake increased from 20 minutes through 2 hours as anticipated from the DO
change monitored both in the BioMonitor and in the basin itself.
A series of short shocks was again introduced using the meat packing
106
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TABLE C-ll. OPERATING PARAMETERS - MEAT
PACKING WASTE - PILOT PLANT STUDY
Meat Packing*
Flow, gal/min
Baseline FeecJ*
Flow, gal/min
Return Sludge
Flow, gal/min
Run I
6/14/76
0.65
1.1
3.5
Run II
6/15/76
1.2
0.5
3.5
Solids
A.B. I
Return Sludge
Biomonitor
MLSS
1938
2961
1496
MLVSS
1455
2016
1179
MLSS
2562
3459
1551
MLVSS
1635
2160
1030
*Feed to Biomonitor unit is 20 ml/min sampled from
the indicated combined Meat Packing waste and
Baseline Feed flows. Retention time in the
contact chamber is approximately 3 minutes.
TABLE C-12. ADO, MG/L IN BIOMONITOR,
MEAT PROCESSING WASTES -
PILOT PLANT STUDIES
Time into Shock,
minutes
4
8
10
12
15
ADO, mq/1
Run I
(6/14/76)
± 0.80
± 1.20
± 1.25
1
Run II
(6/15/76)
- 0.06
- 0.30
- 0.50
- 0.65
107
-------
TABLE C-13. OXYGEN UPTAKE RATES (MG/L 02/HR) -
MEAT PACKING WASTE - PILOT PLANT STUDIES
6/14/76
before
zero time
7 mln
15 min
30 min
1 hr
2 hr
3 hr
4 hr
5 hr
A.B. 1
21.0
26.0
26.2
22.5
21.2
19.8
20.6
25.5
19.8
20.0
A.B. 4
f
15.0
16.2
15.0
14.7
13.2
13.6
A.B. 6
12.3
15.0
15.0
14.2
14.8
13.6
TABLE C-14. OXYGEN UPTAKE RATES (MG/L 02/HR) -
MEAT PACKING WASTE - PILOT PLANT STUDIES
6/15/76
before
zero time
7 min
20 min
30 min
1 hr
2 hr
3 hr
4 hr
5 hr
A.B. 1
20.1
27.0
27-0
25.8
27.0
37.8
51.0
49.2
46.5
46.5
A.B. 4
15.0
18.0
19.0
19.5
19.2
A.B. 6
15.4
19.8
17.7
18.2
18.0
17.4
108
-------
waste in an effort to correlate oxygen uptake and change In DO in the Bio-
nnlnfin T*J reifi 3*h ^^ reSUl*S nn V* ^^ UPtakG t6StS
-------
TABLE C-15. OXYGEN UPTAKE - SERIES OF SHORT SHOCKS
MEAT PACKING WASTE - PILOT PLANT STUDIES
Description Oxygen Uptake (mg/l/hr)
normal feed 53.1
normal feed 56.4
normal feed 54.6
normal feed 60.6
Shock I 58.2
normal feed 58.2
Shock II 60.0
normal feed 61.8
Shock III 60.3
normal feed 63.6
Shock IV 59.4
normal feed 61.2
Shock V 41.4
110
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TABLE C-16. ADO, MG/L - SERIES OF SHORT SHOCKS
MEAT PACKING WASTE - PILOT PLANT STUDIES
Shock II ADO
Time into shock, min
4 -0.05
8 -0.08
12 -0.17
Time out of shock, min
4 +0.05
8 +0.14
12 +0.16
Shock IV
Time into shock, min
18 -0.20
Time out of shock, min
14 +0.10
111
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TABLE C-17. TOC VALUES (MG/L) - MEAT PROCESSING
WASTE - PILOT PLANT STUDIES
Time into Shock
0
7 min
15 min
30 min
1 hr
2 hr
3 hr
4 hr
5 hr
0
7 min
15 min
30 min
1 hr
2 hr
3 hr
4 hr
5 hr
A.B. I
58.0
54.9
52.7
71.2
62.4
81.0
85.7
52.2
52.9
56.9
81.2
52.2
48.8
99.4
99.4
103.1
110.4
110.4
A.B. IV
48.6
61.2
52.7
49.7
62.4
49.7
52.2
69.0
42.1
39.5
69.0
A.B. VI
56.1
49.5
43.3
54.9
48.6
47.6
36.1
74.4
82.7
75.6
61.5
47.6
% Shock
37.1
70.6
112
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TABLE C-18. ADO, MG/L, IN BIOMONITOR - ELECTROPLATING
WASTES - PILOT PLANT STUDY
Time into Shock
minutes
0
2
4
6
8
10
12
15
TABLE
Time into Shock
0
7 min
15 min
30 min
1 hr
2 hr
3 hr
4 hr
5 hr
0
7 min
15 min
30 min
1 hr
2 hr
3 hr
4 hr
5 hr
C-19. TOC
WASTE
A.B.
59.1
47.9
38.3
41.3
48.1
60.5
47.5
48.5
47.7
53.0
58.4
49.5
66.8
67.5
70.1
65.6
60.9
64.9
%
35.3%
0
+0.05
+0.15
+0.20
+0.05
-0.35
-0.40
-0.55
VALUES (MG/L)
- PILOT PLANT
I A.B. IV
56.5
46.2
45.4
42.2
27.5
-
50.2
58.4
58.1
60.0
60.5
50.2
_
Shock Load
97.2%
0
+0.10
+0.10
+0.05
-0.20
-0.40
-0.60
-0.65
- ELECTROPLATING
STUDY
A.V. VI % Shock
50.2 35.3
46.4
44.8
45.4
42.2
39.5
57.7 97.2
60.7
60.2
69.6
60.7
55.8
113
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TABLE C-20. OXYGEN UPTAKE DATA (MG/L/HR) - ELECTROPLATING
WASTE - PILOT PLANT STUDY
Time into Shock
before
0
7 min
15 min
30 min
1 hr
2 hr
3 hr
4 hr
5 hr
before
0
7 min
15 min
30 min
1 hr
2 hr
3 hr
4 hr
5 hr
A.B. I
25.5
26.7
26.1
27.8
25.5
28.2
36.8
50.4
79.0
63.8
54.3
57.3
51.0
33.0
29.4
28.0
42.6
25.5
36.8
A.B. IV
14.7
24.0
25.8
23.1
20.7
rained
27.2
25.0
21.4
21.9
20.4
19.5
A.B. VI
24.8
23.2
24.4
24.3
21.4
out
22.5
26.4
23.1
18.0
20.9
20.2
% Shock
35.3
97.2
114
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crease in oxygen uptake from the 7 minute to 15 minute sampling value. The
97.2% run shows an increase from 0 to 7 minutes in the oxygen uptake and a
decrease in the value from 7 to 15 minutes. Again, however, it is question-
able whether some of these differences are significant given the level of
precision of the test procedure.
Although the pilot plant studies produced sparse results which could not
be predicted or reproduced, the experience essentially began the on-site test-
ing. An idea for sensitivity of response to raw sewage, maintenance regimes,
operating problems, field needs, etc. was obtained. In Section 6 the results
of the on-site trials are presented. This represents BioMonitor response due
to inherent variability in the sewage - not industrial waste overlays.
115
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APPENDIX D
ON-SITE INFORMATION
MAINTENANCE PROCEDURES - INDUSTRIAL SITE
1) Upon arriving, note any peculiarities on strip chart (e.g., poor mixing
in main reactor, floating solids in clarifier).
2) Note time, date, and location on strip chart. Note temperature in moni-
tor tube.
3) Take solids sample from main reactor (contact chamber also as necessary).
4) Measure return flow from monitor tube and note on strip chart and daily
log.
5) Switch feed to waste position; measure total feed rate and raw feed
rate; note on strip chart and daily log.
6) Plug overflow tubing in clarifier; plug (or clamp) return tubing from
monitor tube; remove DO probe; quickly plug probe opening.
7) Clean DO probe membrane (replace if necessary) and begin calibration.
8) Remove strip chart from previous day's operation and check recorder for
ink supply, paper supply and pen operation.
9) Check pump head tubing; replace if necessary.
10) Clean feed tubing, if necessary, by backwashing with propanol followed
by plain water.
11) Check oil level in air compressor.
12) Skim solids from top of clarifier and stir if necessary.
13) Check air diffuser for clogging. Unclog if necessary.
14) Waste solids as needed.
15) Clean up BioMonitor and station.
16) Complete DO probe calibration; note temperature on strip chart; and re-
insert probe (replacing teflon tape as necessary); fill in data requir-
ed in log.
17) Remove plugs (clamp) from return tubing from monitor tube and from
overflow tubing in clarifier.
18) Measure total feed flow and raw feed flow and note on strip chart and
daily log.
19) Measure return flow and note on strip chart and daily log.
20) Note time, date, and location on strip chart.
21) Fill dilution water tank as needed.
MAINTENANCE PROCEDURES - WASTE TREATMENT SITE
1) Upon arriving, note any peculiarities on strip chart (e.g., poor mixing
in main reactor, floating solids in clarifier).
116
-------
2) Note time, date, and location on strip chart.
3) Take solids sample from main reactor (contact chamber also, if necessar-
y).
4) Measure return flow from monitor tube and note on strip chart and daily
log.
5) Switch feed to waste position; measure feed flow rate; and note on strip
chart and daily log.
6) Plug overflow tubing in clarifier; plug return tubing from monitor tube;
remove DO probe; plug probe opening.
7) Clean DO probe membrane (replace if necessary) and begin calibration.
8) Remove strip chart from previous day's operation and check recorder for
ink supply, paper supply and pen operation.
9) Check pump head tubing; replace if necessary.
10) Clean feed tubing, if necessary. Backwash with bleach followed by ex-
cess water.
11) Replace desiccant air supply. Save used desiccant for regeneration.
12) Skim solids from top of clarifier. Stir main reactor every 2 hours.
13) Check air diffuser for clogging. Unclog if necessary.
14) Waste solids as needed.
15) Clean up BioMonitor and station.
16) Complete DO probe calibration; note temperature on strip chart; reinsert
probe (replacing teflon tape as necessary in Monitor tube).
17) Remove plugs from return tubing from monitor tube and from overflow tub-
ing in clarifier.
18) Measure feed flow and note on strip chart and daily log.
19) Measure return flow and note on strip chart and daily log.
20) Note time, date, and location on strip chart.
117
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BIOMONITOR DAILY LOG
Location:
Date:
By:
Day
Time:
I. BioMonitor
A. Solids: MLSS
B. Clarification
MLVSS
% MLVSS:MLSS
C. Air Supply: Desiccant Replaced
Main Reactor Setting
Monitor Tube Setting
D. Flow Rates: Feed Return
E. Feed Tubing: Backwash
F. Mixed Liquor Wasted:
G. Temperature in Monitor Tube:
H. General Housekeeping:
Clean
Replace
Time:
II. D.O. Meter
A. Calibration: Adjustment (±)
B. Membrane: Replace
III. Chart Recorder
A. Ink: Refill
B. Pen: Clean
IV. Pumps
A. Replace Pump Head Tubing:
C. Paper: Refill
D. Calibration; Adjustment(±)
B. Approximate Van"-speed Seeting:
V. Other
118
-------
DATA SAMPLING ROUTINE - WASTE TREATMENT PLANT
I TOC Samples
1) Composite separately 50 ml grab samples of both Influent and effluent
every 20 minutes every hour.
2) Keep composite acidic from first grab sample on - check with pH paper.
3) At end of one hour, shake, and then filter composite into test tube.
4) Seal.
5) Label with date, time, the letter "C" (for composite), location and
source, e.g.,
10-4-76
3-4 pm C
Location
6) Store in refrigerator.
7) If recorder indicates a "shock" take an inf1uent grab sample - DO NOT
COMPOSITE - as often as warranted - e.g., every 15 minutes instead of a
composite.
8) Acidify, filter, seal, label (as shown) and store:
10-4-76 date
4:25 pm S time, "S" for shock
Influent location
Sharp Decrease nature of shock
9) This applies only to the influent during a shock. Plant effluent is
still composited.
II Pi Uptake
1) One analysis per hour from specified location in aeration basin.
2) Record temperature in bottle after 02 uptake is complete.
3) Label chart paper with data, time of sample withdrawn and temperature.
Indicate periodically the correct time on the chart paper by placing an
arrow on the line with the time next to it.
119
-------
DATA SAMPLING ROUTINE - INDUSTRIAL SITE
I TOC Samples
1) Take 50 ml grab samples of influent every 20 minutes. Composite 3
samples (150 mis ) every hour.
2) Keep composite acidic from first grab sample on - check with pH paper.
3) At end of one hour, shake composite, then filter composite into beaker.
4) Pipet 2 ml of filtrate into clean test tube.
5) Pipet 2 ml of water into the same test tube.
6) Seal .
Shake.
Label with date, time, the letter "C" (for composite), location, e.g.,:
7)
8)
10-4-76
LOCATION
3-4 pm C
9) Store in refrigerator.
10) If recorder indicates a "shock" take a grab sample - DO NOT COMPOSITE -
as often as warranted - e.g., every 15 minutes instead of a composite.
11) Acidify, filter, dilute, seal, label (as shown below) and store.
10-4-76 date
4:25 pm S time, "S" for shock
Industrial Site location
Sharp Decrease nature of shock
II Metals Samples (Site 2)
1) Fill two 30 ml test -tubes with an aliquot from the composite for metals
analyses.
Acidify.
Label as indicated in 1-8,
Seal.
Ill Recording pH Meter (Site 1)
1) Keep eye on recording pH meter.
2) Periodically record time on chart.
3) If rapid major change occurs, take a grab sample of influent for TOC
analysis as listed in Steps 1-10 and 1-11.
Indicate periodically the correct time on the chart paper by placing an
arrow on the line with the time next to it.
120
-------
RESULTS FROM BIOMONITOR flT JOINT W.T.P. 1
600
5MO
r\>
789 10 11 12 123HS67B9 10 11 13 1 2 3 4 S 6 7
CD
TO
m
m
i r> co
' om
\ i~=e
CD m5>
o 2-
- ae :z
Ooo
-
x
30 ;o
- mm
O t/>
o cr
m
n>
16.9 " C
.S " C
ZS.U " C
80.0 ' C
17.6 * C
7 fl.M. MONDflY OCT. 4. 1976 TO 7 fl.M. TUESDflY OCT. 5, 1976
-------
RESULTS FROM BIOMONITOR flT JOINT W.T.P. 1
ro
600
SHO
I 1 1 1 1 1 1 1 1 1 1 1 [
I 1 1 1 1
I I 1 I I 1 1 I I I I i
I I I 1 I
789 10 11 12 1 23<456783 10 11 12 1 231567
O
Q
18.2 ° C
2U.6 " C
19.0 C
7 Fl.M. TUE50RY OCT. 5, 1976 TO 7 fl.M. WEDNESDflT OCT. 6, 1976
-------
RESULTS FROM BIGMONITOR flT JOINT W.T.P. 1
ro
Cm)
600
S<40
480
360
300
Q 210
180
120
60
"1 T
T 1 1 1 1 1 1 1 1 1 1 1 1 1 r
1 - 1 - 1 - 1 - 1 - 1 - 1 - 1 - 1 - 1 - 1 - 1 - 1
789
fl.M.
17.S 8 C
tO 11 12 1
NOON
m.s ° c
2 3 .H S 6 7 8 9
13.3 " C
10 It \Z 1
HIO
13.S ° C
2 3
s _J
\
CD
g
S 6 7
13.0 " C
7 P.M. WEONESOflT OCT. 6, 1976 TO 7 fl.M. THURSDflY OCT. 7, 1976
-------
RESULTS FROM BIOMONITQR flT JOINT W.T.P. 1
500
ro
1 1 1 1 1 1 1 1 1
789
fl.M.
10 11 12 1
NOON
23
10 11 12 1
mo
2 3
6 7
fl.M.
13.4 " C
m.o " c
12.4 C
12.0 ° C
7 fl.M. THURSDAY OCT. 7, 1976 TO 7 ft.M. FRIDflY OCT. 8, 1976
-------
RESULTS FROM BIGMGNITGR flT JOINT W.T.P. 1
600
SUO
ro
en
1 1 , 1
783 10 It 12 1 231S67891QU131 2 3US67
l<4.3 " C
21.2 " C
23.9 " C
n.i ' c
12.2 " C
7 fl.M. WEONESOflT OCT. 13, 1976 TO 7 fl.M. THURSOflY OCT.
1976
-------
RESULTS FROM BIQMONITQi flT JOINT w.
T p
ro
600
540
480
430
3SO
300
340 f
180
120
50 h-
7 9
P.M.
12. J °
7 fl.M.
II ! 1 II 1 II 1 1 1 1
1 1 i 1
T r
r- f-
10 11 12 1
NOON
13.3 ° C
13.7 ° C
13.6 " C
11.S ° C
FRIDflY OCT. 8, 1976 TO 7 fl.M.= 5RT.UROflY OCT. 9, 1976
-------
RESULTS FROM BIGMONITOR flT JOINT W.T.P. 1
*» O 2UO -
789 tO 11 12 1 2 3 H S 6 7 8 9 10 H 12 1 23HS67
11.8 ° C
17.7 ' C
20.3 ° C
13.8 * C
7 fl.M. THURSDflT OCT. 14, 1976 TO 7 fl.M. FRIOflY OCT. 15. 1976
-------
RESULTS FROM BIQMQNITGR flT JOINT W.T.P. 1
t\>
0
600
SHO
480 -
430
f_j
o
I 1 1 1 1. f 1 1 1 1 1 1 1 1 1 i I I I I I I I
7 8 9 10 11 12 1 2 3 4 S 6 7 8 9 10 41 12 1 2 3
11.2 * C
19.0 " C
23.0 ° C
19.0 " C
16.1 ' C
7 fl.M. FRIDflY OCT. 15. 1976 TO 7 fl.M. SflTUROflY OCT. 16. 1976
-------
RESULTS FROM BIQMGNITOR fiT JOINT rt.T.P. 1
EDO
ro
1 I . L I _ I \ I I I I
1 1 I 1 1 1 L L I I I I
7 8 3 10 11 1Z I Z 3 «* S 6 7 8 9 10 11 IZ 1 234S67
5L3
CD
IS.8 ° C
IS.9 " C
13.0 " C
11.7 ' C
8.2 " C
7 P.M. SflTURDflY OCT. 16, 1976 TO 7 fl.M. SUNDRY OCT. 17, 1976
-------
RESULTS FnOM BIOMONJTOR RT JOINT W.T.P. 1
600
180
1£0
60
i i I i
j i
7
fl.n.
8 3 10
U 12
NOON
123US678910U
\Z
HJO
I 2 3
11.3 ° C
11
H 10
- 3
- 6
S 6 7
fl.rt.
13.0 ' C
8.2 ' C
7 fl.M. SUNDRY OCT. 17. 1976 TO 7 fl.M. MONOflT OCT. 18, 1976
-------
EFFLUENT CGNCENTRflTI ON flT JOINT W.T.P. 1
ISO
135
130
tos
CO
LJ
75
60
30
IS
, 1 , r
1 1 1 1 1 1 1 1 r
1 1 1
78910111212314567891011131
2314567
7 fl.M. MONOflY OCT. 4, 1976 TO 7 fl.M. TUESOflY OCT. 5. 1976
-------
EFFLUENT CGNCENTRHTI ON RT JOINT W.T.P. 1
to
ro
I 1 1 1
I 1 1 1 1 1 1 1 1 1 1 n 1 1 1 1 1 I
i i t i
789 10 11 12 123456789 10 11 12 123(tS07
7 fl.M. TUESDRY OCT. 5, 1976 TO 7 fl.M. WEDNE50RY OCT. 6, 1976
-------
EFFLUENT CONCENTRRTION flT JOINT W.T.P. i
iso
135 -
105
1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 ! 1 i 1 r
co
oa
I 1 1 I'll
7 8 9 10 11 12 1 2 3
567891011121234567
7 fl.M. WEDNESOflT OCT. 6, 1976 TO 7 fl.M. THUR5DRY OCT. 1, 1976
-------
EFFLUENT CONCENTRRTI ON RT JOINT W.T.P. 1
150
135
10S
CO
O 60
30
IS
_1_ 1 I I 1 1 1 1 1 1 1 1 1 I L 1 I I I 1 I I I
7 8
fl.M.
10 11 \2 1
NOON
231S67891Q
11 12
H10
1 2 3
H S 6 7
fl.M.
7 fl.M. THURSDflT OCT. 7, 1976 TO 7 fl.M. FRIORT OCT. 8, 1976
-------
EFFLUENT CONCENTRflTI ON flT JOINT W.T.P. 1
ISO
CO
en
7 fl.M. FRIDflY OCT. 8, 1976 TO 7 fl.M. SflTURDflT OCT. 9, 1976
-------
EFFLUENT CQNCENTRflTI ON flT JOINT W.T.P. 1
CO
ISO
135 -
7 8 9 10 11 IE 1
1 fl.M. HEONESDflY OCT. 13, 1976 TO 7 P.M. THURSDflY OCT. 14, 1976
-------
EFFLUENT CONCENTRflTI ON flT JOINT W.T.P. 1
ISO
CO
135 -
IDS
-I
7 fl.M. THUR5DRY OCT. 14, 1976 TO 7 fl.M. FRIOflY OCT. 15, 1976
-------
EFFLUENT CONCENTRATION PIT JOINT W.T.P. 1
ISO
13S -
120 -
I OS -
75 -
CO O 60
00 .
i - 1 - 1 - 1 -
1 - 1 - 1 - 1 - 1
1 - 1 - 1 - 1 - 1 - 1 - 1 - 1 - 1 - 1
1 1 1 1 i i i
S 6 7 8 9 10 11 13 1 2 3
30 -
IS -
7 8 9
A.M.
10 11 IZ I
NOON
7 fl.M. FRIDflT OCT. 15, 1976 TO 7 fl.M. SflTUROflY OCT. 16, 1976
-------
EFFLUENT CONCENTRflTI ON RT JOINT W.T.P. 1
ISO
CO
vo
CD
SI
13S -
iao
1QS
90
75
60
30 -
IS
1 - 1
i - 1 - 1 - 1 - 1 i r
J 1 1 1 1 1 1 1 1 1 1 1 1 1 1 ' t I i I I i [
789
fl.M.
10 11 12 1
NOON
2345678
9 10 11 12 1
MID
a 3 14
s 6 7
fl.M.
7 fl.M. SflTUROflY OCT. 16, 1976 TO 7 fl.M. SUNDRY OCT. 17. 1976
-------
EFFLUENT CONCENTRflTI ON flT JOINT N.T.P. 1
13S
O
s:
105
90
7S
0 O 60
30
IS
i
i l i i l i i
i i i i i i
7 8 3 10 11 12 1
P.M. NOON
231S678910U12123I4S67
HID fl.M.
7 fl.M. SUNDRY OCT. 17, 1976 TO 7 fl.M. MQNDflT OCT. 18, 1976
-------
RESULTS FROM BIOMONITOR flT INDUSTRIflL SITE 1
CD
3000
2700
2400
2100
1000
1SOO
1ZOO
900
600
300
.1 . I 1 1 1 1 L
1 1 1 1 1 1 1 1
§
769 10
R.H.
234S678
N80M
910U121
NIO
Z3HS6 7
fl.H.
»9.8 " C 80. S ' C 19.6 ' C
7 P.M. MONDR1T OCT. 4, 1976 TO 7 fl.M. TUESDflY OCT. 5, 1976
-------
RESULTS FROM BIOMONJTOR flT INDUSTRIflL SITE 1
3000
2700
2MOO
2100
1800
1500 -
1200 -
900 -
600 -
300 -
r r i i i r i i i i i i i
i i i r
-ee-
789 10 11 12 1 2 3 H S 6 I 8 9 10 11 12 1 2 3 M S 6 7
R.H. NOON ' NXO R.H.
19.7 * C 22.1 " C 21.7 * C
7 fl.M. TUESOflY OCT. 5. 1976 TO 7 fl.M. WEONESDflY OCT. 6, 1976
-------
RESULTS FROM BIOMONITOR RT JNDUSTRIflL SITE 1
o
o
3000
2700
2400
aioo
l»00 -
1500
1ZOO -
300 -
600
300 -
ri 1 1 1 1 1 1 1 1
i 1 1 1
I 1 1 1 1 » i 1 1 1 1 1 ' I I I II I
789 10 UIZ 123156789 VOU 12 J23HS67
GD
Q
21.0 * C
7 fl.M. WEDNESDflY OCT. 6, 1976 TO 7 fl.M. THURSOflY OCT. 1. 1976
-------
RESULTS FROM BIOMONITOR flT INDUSTRIflL SITE 1
3000
Z700 -
i 1 1 1 1 1
i 1 1 1 1 1 1 1 1 1
O
0
7 a 9 10 11 1Z 1
fl.M. NOON
3
-------
RESULTS FROM BIOMONITQR flT INDUSTRIflL SITE 1
LD
o
3000
3700
2400
£100
1800
ISOO
900
600
300
i 1 1 1 1 1 r
1 1 1 1 1 1 1 1 1 1 1 1 i
7 8 9 10 11 1? I
fl.M. NOON
1 - 1 - ' ' ' '
i i i i i
o
CD
3 M 5 6 7 8 9 10 11 12 1 234567
. MID fl.M
19.9 " C
7 fl.M. FRIDflT OCT. 8. 1976 TO 7 fl.M. SflTURDflY OCT. 9, 1976
-------
RESULTS FROM BIOMONITOR RT INDUSTRIRL SITE 1
3000
2700 -
01
7891011121234S0709101112123IIS07
20.2 ' C
20.0 ' C
19.9 " C
19.9 ' C
18.0 * C
7 fl.M. WEDNESDRY OCT. 13, 1976 TO 7 fl.M. THURSDRT OCT. U,1976
-------
RESULTS FROM BIOMONITOR flT INDUSTRIflL SITE 1
3000
8700
ZtOQ
2100
laoo -
1SOO -
1200 -
900 -
600 -
300 -
7 8 9 10 11 12 1 3 3 * S 6 78 9 10 11 12 1 Z 3 l| 5 6 7
CD
o
Q
18.0 " C 19.0 " C 19.3 ' C 18.8 " C 17.6 ' C
7 fl.M. THURSOflT OCT. 14, 1976 TO 7 fl.M. FRIDRY OCT. 15.1976
-------
RESULTS FROM BIOMONITOR flT INDUSTRIRL SITE 1
9000
2700
2*00
2100
1000
1SOO
00 O 1200
900
600
300
I i i
T I I i i i r t
til
to
o
o
o
I I I i
I I I I I I i i I I I I
7 S 10 It 12 1
A.M.
19 It 12 1 2 3 « S « 7
NIO A.M.
I7.i * C
19.1 ' C
ti.S * C
1S.2 " C
18.2 * C
7 fl.M. FRIDflY OCT. 15, 1976 TO 7 fl.M. SflTUROflY OCT. 16,1976
-------
RESULTS FROM BIOMONITGR flT INDUSTRIE SITE 1
IO
CD
3000
2700 -
2400 -
2100 -
1800 -
1500 -
1200 -
300 -
600 -
300 -
I I 1 1 1 1 1 1 1 1 1 1 1 1 1
I 1 1 I
I I I I
I I I I I I I I I I I I
7 89 10 11 12 1 231456789 10 11 12 I 23 4 5 6 7
CD
O
CD
18.0 ° C 18.3 " C 18.1 ° C 17.3 ° C 17.0 " C
7 fl.M. SflTURDflY OCT. 16, 1976 TO 7 R.M. SUNDRY OCT. 17,1976
-------
RESULTS FROM BIOMONITOR flT INOUSTRIflL SITE 1
3000
2700
2100
2100
1800
1500
o O 1200
900
600
300
I I T I I
I
10
6 _J
>s.
O
7 8 10 11 12 1 2 3 « S 0 7 8 9 10 11 12 I 2 3 « S 8 7
17.0 ' C
17.1 " C
18.0 * C
17.t " C
18.0 * C
7 R.M. SUNDRY OCT. 17, 1976 TO 7 ft.M. MONDflY OCT. 18,1976
-------
RESULTS FROM BIOMONITOR flT JOINT W.T.P. 2
500
ISO
, - , , ,
, - , - , - , - , - , - , - , - ,
i i i i i i i i i i i i i i i i i i i i i i i i
7 8 9 10 11 12 1 2 3 H 5 6 7 8 9 10 II 12 1 2 3 M S 6 7
7 fl.M. TUESDflT DEC. 1, 1976 TO 7 P.M. WEDNESDHT DEC. 8, 1976
-------
RESULTS FfiOM -6IOMONITQR flT JOINT W.T.P. 2
soo
450 -
O1
1 1 1 1 1 1 1 1 1
i I I I 1 I ._!_. 1 I 1
789 10 11 12 1 334567 8 9 10 11 13 1 2 3
O
a
7 fl.M. WEONESDflT DEC, 8, 1976 TO 7 fl.M. THURSDflY DEC. 9, 1976
-------
RESULTS FROM BIOMGNITOR flT JOINT W.T.P. 2
01
SOD
450
400
3SO
300
ZSQ -
O 200 -
I 1 1 1 1 1 1 1 1 1 I I I I 1
CD
7 P.M. THURSDflT DEC. 9, 1976 TO 7 fl.M. FRIDflY DEC. 10, 1976
-------
EFFLUENT CONCENTRRT I ON flT JOINT W.T.P. 2
soo
450 -
400 -
350 -
300 -
2so -
<£ O 200 -
150 -
100 -
50 -
7 8 9 10 11 12 1
Q.M. NOON
2 3 4 5 6 7 8 9 10 11 12 1
M10
234
567
fl.H.
7 fl.M. TUESDflT DEC. 7, 1976 TO 7 fl.M. WEDNESDflT DEC. 8. 1976
-------
EFFLUENT CONCENTRflTION flT JOINT W.T.P. 2
en
01
CJ
500
450
400
350
300
350
200
ISO
100
SO
i i r
I I T I I I I 1
1 -.1 I I I 1 1 1 1 1 I 1 III I I I I I I I I
7 8 9 10 U 12 1
fl.H. NOON
3 H 5 6 7 8 9 10 11
MID
2 3 it S 6 7
fl.M.
7 fl.M. WEDNESDflT DEC. 8, 1976 TO 7 fl.M. THURSDflT DEC. 9, 1976
-------
EFFLUENT CONCENTRRTI ON RT JOINT W.T.P. 2
soo
ISO -
1 1 1 1 1 1 1 1 1 1 T 1 1
7 8 9 10 11 12 I
2 3 1.5 6 7 8 9 10 11 12 I
231567
7 fl.M. THURSDflY DEC. 9, 1976 TO 7 fl.M. FRIDflT DEC. 10, 1976
-------
RESULTS FROM BIOMONITOR flT INDUSTRIflL SITE 2
tn
SCO
450
7 8 9 10 11 12 1
O
7 fl.M. TUESOflT DEC. 7. 1976 TO 7 fl.M. WEDNESDflT DEC. 8, 1976
-------
RESULTS FROM BIOMONITOR flT INDUSTRIflL SITE 2
soo
en
oo
I 1 1 1 1 1 1I 1 1 1 1 I
7 8
B.M.
10 11 12 1
NOON
7 fl.M. WEDNESDflY DEC. 8, 1976 TO 7 fl.M. THURSDAY DEC. 9. 1976
-------
RESULTS FROM BIGMONITGR flT INDU5TRIRL SITE 2
01
500
7 fl.M. THURSOflT DEC. 9, 1976 TO 7 fl.M. FRIDflT DEC. 10, 1976
-------
METflL CONCENTRflTION flT INDU5TRIRL SITE 2
O
a:
o
Z 3 "4 S 6 7
0.9
- 0.8
-0.7
- 0.6 __)
- o.s
- 0.1
- 0.3
- 0.2
- 0.1
0.0
O
7 R.M. TUESOflT DEC. 7, 1976 TO 7 fl.M. WEDNESOflY DEC. 8, 1976
-------
METflL CONCENTRRTION RT INDUSTRIRL SITE 2
i 1 1 1 1 1 1 1 1 1 1 1 Q-9
i 1 1 1
i 1 1 1 r~i
1C
LJ
- a.2
- o. i
0.0
7 8 9 10 11 12 1
fl.n. NOON
3456789
10 11 12 1
HID
2 3 <4
567
ft.M.
7 fl.M. WEDNESDflY DEC. 8, 1976 TO 7 fl.M. THUR5DRY DEC. 9, 1976
-------
METflL CQNCENTRflTIGN flT INDUSTRIflL SITE 2
cr>
PO
oc
o
rxj
0.9
- a.a
- 0.7
- 0.6 _J
- 0.5
- O.H
- 0.3
- 0.2
- 0.1
0.0
O
1C
o
789
10 n 12 i
NOON
7 fl.M. THURSORY DEC. 9, 1976 TO 7 fl.M. FRIDflT DEC. 10, 1976
-------
. REPORT NO.
EPA-600/2-79-180
TECHNICAL REPORT DATA
[1'lense read Instructions on the reverse before completing)
2.
..TITLE AND SUBTITLE
Development of a Biological Simulation Monitor
for Joint Municipal/Industrial Treatment Systems
3. RECIPIENT'S ACCESSION'NO.
5. REPORT DATE
August 1979 Issuing date
6. PERFORMING ORGANIZATION CODE
'. AUTHOR(S)
Ann N. Clarke, U. Wesley ECkenfelder, and John A. Roth
8. PERFORMING ORGANIZATION REPORT NO.
. PERFORMING ORGANIZATION NAME AND ADDRESS
Center for Environment Quality Management
Vanderbilt University
Nashville, TN 37235
10. PROGRAM ELEMENT NO.
1BB610
11. CONTRACT/GRANT NO.
R803740
12. SPONSORING AGENCY NAME AND ADDRESS
Robert S. Kerr Environmental Research Laboratory
U.S. Environmental Protection Agency
P.O. Box 1198
Ada, OK 74820
13. TYPE OF REPORT AND PERIOD COVERED
Final6/1/75-5/31/77
14. SPONSORING AGENCY CODE
EPA 600/15
15. SUPPLEMENTARY NOTES
16. ABSTRACT
Evaluation of existent monitoring hardware for the ultimate purpose of de-
tecting the industrial wastewater source causing chronic or acute inefficiency
in the performance of a joint biological treatment facility. The approach rep-
resents the first phase of the ultimate purpose; that phase being bench and
pilot scale bio-treatment studies of selected industrial wastes at various
loadings. Several monitoring techniques were applied to the treatment systems,
and the parameters identified in pretreatment guidelines were monitored as
measures of removal efficiencies.
17.
KEY WORDS AND DOCUMENT ANALYSIS
DESCRIPTORS
b.lDENTIFIERS/OPEN ENDED TERMS
Industrial Waste Treatment,
Measuring Instrument,
Monitoring,
Warning System,
Waste Treatment
Wastewater
18. DISTRIBUTION STATEMENT
Release to public
EPA Form 2220-1 (9-73)
c. COSATI Field/Group
BioMonitor,
Combined Industrial-
Municipal Treatment,
Treatment Efficiency
19. SECURITY CLASS (This Report)
Unclassified
20. SECURITY CLASS (Thispage)
Unclassified
68 D
173
163
-------