EPA/600/2-79/012
 o-EPA
               States
               imental Protection
            Municipal Environmental Research  I PA 6i,\  '-.'
            Laboratory         !>/,-!•. 197;.
            Cincinnati OH 45268
               oh and Development
Full-Scale
Demonstration of
Open Tank Oxygen
Activated  Sludge
Treatment

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                RESEARCH REPORTING SERIES

Research rep-jrts cf the Office of Research and Development, U G  Environmental
Protection Agency have been grouped into nine series These mre broad cate-
gories were established to facilitate further development and application of en-
vironmental technology Elimination of traditional grouping was  consciously
planned to foster technology transfer and a maximum interface in related fields
The nine series are

      1   Environmental Health  Effects Research
      2   Environmental Protection Technology
      3   Ecological Research
      4   Environmental Monitoring
      5   Socioeconomic Environmental Studies
      6   Scientific and Technical Assessment Reports (STAR)
      7   Interagency Energy-Environment Research and Development
      8   "Special' Reports
      9   Miscellaneous Reports

This report has been assigned  to the  ENVIRONMENTAL PROTECTION TECH-
NOLOGY series This series describes research  performed to develop and dem-
onstrate  instrumentation, equipment, and methodology to repair or prevent en-
vironmental degradation from point and non-point sources of pollution This work
provides the new or improved technology required for the control and treatment
of pollution sources to meet environmental quality standards
This document is available to the public through the National Technical Informa-
tion Service, Springfield, Virginia 22161

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                                         EPA-600/2-79-012
                                         May 1979
             FULL-SCALE DEMONSTRATION
  OF OPEN TANK OXYGEN ACTIVATED SLUDGE TREATMENT
                        by

               Stephen R.  Pearlman
Metropolitan Denver Sewage Disposal District No. 1
             Denver, Colorado  80229


                       and


               Donald G.  Fullerton
                 FMC Corporation
            Englewood, Colorado  80110
                Grant No. S803910
                  Project Officer

                Richard C. Brenner
           Wastewater Research Division
   Municipal Environmental Research Laboratory
             Cincinnati, Ohio  45268
   MUNICIPAL ENVIRONMENTAL RESEARCH LABORATORY
        OFFICE OF RESEARCH AND DEVELOPMENT
       U.S. ENVIRONMENTAL PROTECTION AGENCY
             CINCINNATI, OHIO  45268

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                                DISCLAIMER
This report has been reviewed by the Municipal Environmental Research Labo-
ratory, U. S. Environmental Protection Agency, and approved for publication.
Approval does not signify that the contents necessarily reflect the views
and polices of the U. S. Environmental Protection Agency, nor does mention
of trade names or commercial products constitute endorsement or recommenda-
tion for use.
                                     n

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                                 FOREWORD
The Environmental Protection Agency was created because of increasing public
and government concern about the dangers of pollution to the health and wel-
fare of the American people.  Noxious air, foul water, and spoiled land are
tragic testimony to the deterioration of our natural  environment.   The com-
plexity of that environment and the interplay between its components require
a concentrated and integrated attack on the problem.

Research and development is that necessary first step in problem solution
and it involves defining the problem, measuring its impact, and searching
for solutions.  The Municipal Environmental Research Laboratory develops
new and improved technology and systems for the prevention, treatment, and
management of wastewater and solid and hazardous waste pollutant discharges
from municipal and community sources, for the preservation and treatment of
public drinking water supplies, and to minimize the adverse economic, social,
health, and aesthetic effects of pollution.  This publication is one of the
products of that research; a most vital communications link between the re-
searcher and the user community.

This report presents design details, operating experiences, and all operat-
ing and performance data for the first full-scale demonstration of an open
tank pure oxygen activated sludge wastewater treatment system.   Considera-
tion of the oxygenation technology discussed herein is recommended for de-
sign engineers, facilities planners, and potential  municipal users.
                                     Francis T.  Mayo, Director
                                     Municipal  Environmental  Research
                                     Laboratory

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                                 ABSTRACT
This report presents an operating summary of a full-scale demonstration of
the FMC open tank pure oxygen (FMC 02) activated sludge system, conducted
at the facilities of the Metropolitan Denver Sewage Disposal  District No. 1
(Metro) in Denver, Colorado.   The system was operated over a  period of 15
mo at both steady state and diurnal flow rates ranging from 22,700 mVday
(6 mgd) to 53,000 m^/day (14 mgd), with average F/M loadings  varying between
0.49 and 1.14 kg BOD/day/kg MLVSS and clarifier overflow rates ranging from
16.5 to 32.2 m3/day/m2 (406 to 791 gpd/ft2).

The overall performance of the system was dictated in large part by the quan-
tity of filamentous organisms in the activated sludge, and the investigation
of these organisms, with attempts to control or eliminate them, was an ongo-
ing activity during much of the demonstration.

The system was evaluated as to oxygen transfer efficiency and oxygen consump-
tion.  Further, it was compared to the Metro diffused air system running in
parallel with the demonstration system on the-basis of sludge production and
power requirements.  Comparison of sludge settleabilities was made between
these two systems and a closed tank pure oxygen system (UNOX) also in opera-
tion at Metro.

In addition to allowing an evaluation of the FMC 02 system as a whole, the
demonstration provided an opportunity to evaluate various component equip-
ment items as to their reliability and performance.

This report was submitted in fulfillment of Grant No. S803910 by the Metro-
politan Denver Sewage Disposal District No. 1 under the partial sponsorship
of the U. S. Environmental Protection Agency.  This report covers the opera-
tional period of June 1, 1976, to September 7, 1977.
                                    IV

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                                 CONTENTS
Foreword	    iii
Abstract	     iv
Figures   	     vi
Tables	    vii
Abbreviations and Symbols 	  viii
Acknowledgements  	     x


   1.  Introduction   	     1
   2.  Conclusions    	     4
   3.  Recommendations  	     6
   4.  Facilities   	     7
   5.  Process Monitoring   	     16
   6.  Analytical Procedures  	     17
   7.  Process Operation and Performance  	     18
   8.  Comparative Sett!eabilities  	     36
   9.  Oxygen Transfer Efficiency 	     39
  10.  Solids Production  	     44
  11.  Oxygen Consumption 	     47
  12.  Power Requirements   	     49
  13.  Supplemental  Testing 	     52
  14.  Equipment Performance and Reliability  	     58


References	     61
Appendices

   A.  Daily Operating Data   	     62
   B.  Filamentous Investigations:  Reports of
         Dr. W.O. Pipes	     95

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                                  FIGURES

Number                                                                  Page
  1   Metro treatment facilities  	    8
  2   Demonstration site plan	    9
  3   Dimensional layout of mixed liquor basin and clarifier  	   10
  4   A typical FMC 02 installation	11
  5   Elevation view of rotating active diffuser (RAD)  and
        drive assembly	   12
  6   Section view of RAD diffusion media and impellers 	   13
  7   FMC 02 system in operation at the Metro plant	14
  8   Mixed liquor basin with RAD's installed 	   15
  9   Relationship of SVI to filamentous counts 	   22
 10   Photomicrograph of oxygen system mixed liquor, 8/17/76  	   23
 11   Mixed liquor basin overflow weir  	   29
 12   Diurnal flow patterns	30
 13   Photomicrograph of oxygen system mixed liquor, 7/26/77  	   33
 14   Comparison of SVI values (adjusted to 2000 mg/1  MLSS)
        for oxygen and air systems	37
 15   Schematic of off-gas test equipment	40
 16   Off-gas dome locations	42
 17   Oxygen transfer efficiency versus oxygen flow at various
        basin locations	43
 18   Total and soluble BOD	54
 19   Suspended solids profile of the mixed liquor basin  	   55
 20   Dissolved oxygen profile of mixed liquor basin  	   57
                                     VI

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                                  TABLES

Number                                                                 Page
  1   Phase Summary	18
  2   Performance Data   	20
  3   Operating Parameters 	   21
  4   Influent Wastewater Distribution 	   38
  5   Oxygen System Solids Production  	   45
  6   Solids Production - Air Versus Oxygen  	   46
  7   Oxygen Consumption 	   48
  8   System Power Requirements  	   50
  9   Nitrogen Forms, Alkalinity, and pH   	   53
 10   Gear Drive Power Requirements  	   59
                                     vii

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                         ABBREVIATIONS AND SYMBOLS
ABBREVIATIONS

BOD
BODA
BODR
cm
COD
CODR
D.O.
Eff
EPA
FAD
F/M
ft
g
gal
gpm
gpd
hp
hr
in.
Inf
kg
kgf
kWh
1
Ib
m
mA
mg
mgd
mil gal
min
MLSS
MLVSS
mo
No.
psig
RAD
rpm
SRT
biochemical oxygen demand, 5 day
BOD applied
BOD removed
centimeter
chemical oxygen demand
COD removed
dissolved oxygen
effluent
U. S. Environmental Protection Agency
fixed active diffuser
food/microorganism ratio
foot
gram
gallon
gallons per minute
gallons per day
horsepower
hour
inch
influent
kilogram
kilograms, force
kilowatt hour
1 i ter
pound
meter
mi 11i ampere
milligram
million gallons per day
million gallons
minute
mixed liquor suspended solids
mixed liquor volatile suspended solids
month
number
pounds per square inch, gauge
rotating active diffuser
revolutions per minute
solids retention time
                                    vm

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SS         -- suspended solids
SVI        -- sludge volume index
TKN        -- total Kjeldahl nitrogen
TOC        -- total organic carbon
TOCR       -- TOC removed
VSS        -- volatile suspended solids
SYMBOLS

CaCOs      — calcium carbonate
I-P        — current-to-pneumatic
NH4-N      -- ammonium nitrogen
N02-N      — nitrite nitrogen
N03-N      — nitrate nitrogen
02         -- oxygen
Q          -- influent wastewater flow
R          — return sludge flow

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                              ACKNOWLEDGEMENTS


The authors wish to acknowledge the assistance and direction  provided  by Mr.
Richard C.  Brenner, Project Officer, U.S.  Environmental  Protection  Agency,
and Mr. John L.  Puntenney,  Project Director and Director of Operations and
Maintenance at Metro.

Many members of the Metro staff made significant contributions  to the  success
of the project, but special recognition of the following individuals and their
supporting staffs Is warranted:

          Duane E.  Humble,  Microbiologist
          John K. Nelson, Superintendent of Operations
          Harry M.  Harada,  Jr., Director of Laboratory  Services
          Larry Pannell, Superintendent of Maintenance
          Pam Stover, Stenographies
          Carol Lee, Graphics


FMC personnel involved in the implementation of the project should  be  acknow-
ledged for their efforts:

          Richard B. Weber, Manager of Operations, Marox Systems
          Duane M.  Parker,  Manager of Engineering, Marox Systems
          Gordon Drew, Engineer
          Steve Potts, Engineer
          Tony Hlinak, Engineer

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                                 SECTION 1

                               INTRODUCTION
PROJECT BACKGROUND
The development of high efficiency open tank oxygenation systems for waste-
water treatment was begun in March 1971 with the establishment of a batch-
mode pilot plant at the facilities of the Metropolitan Denver Sewage Disposal
District No. 1 (Metro).  This first step in a joint research and development
effort between Metro and the Martin Marietta Corporation was followed in July
1971 by a 7.6-1/min (2-gpm) flow-through pilot system to monitor substrate
removal.  For oxygen transfer, the system employed a fixed active diffuser
(FAD), a device producing minute oxygen bubbles by the shearing action of a
high velocity stream of water directed across porous diffusion surfaces.  In
September 1972, based on the recommendation of several consulting engineers,
the system was scaled up to a 57-1/min (15-gpm) pilot plant, a size deter-
mined to be suitable for obtaining design data for existing plant expansion
or new plant construction.  In January 1973, 6 mo prior to completion of the
57-1/min (15-gpm) study, the oxygenation process was sold by the Martin Mari-
etta Corporation to FMC Corporation, which continued the research investiga-
tion with the Metro staff.  Results from the 57-1/min (15-gpm) pilot study
indicated the following:


     1.  Efficient oxygen mass transfer using the FAD,

     2.  Satisfactory treatment performance at nominal detention times of
         1 to 2 hr,

     3.  Effective system operation at a wide range of F/M ratios (0.2 to
         1.2 kg BOD/day/kg MLVSS), and

     4.  Efficient control of supplied oxygen through the use of D.O. sen-
         sors, analyzers, and controllers.


Concurrent with the above program, two EPA funded research and development
studies were being conducted on open tank oxygenation systems:  1)  a 114-1/
min (30-gpm) activated sludge pilot program, testing the FAD at the City of
Englewood, Colorado Wastewater Treatment Plant (October 1972 - July 1974) (1)
and  2) a comparison of pure oxygen versus diffused air for the aerobic sta-
bilization of waste activated sludge at Metro (November 1972 - May 1974) (2).

The success of the 57-1/min (15-gpm) pilot study at Metro resulted in a scale

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up of the system to a 1900-m3/day (0.5-mgd)  facility  to  verify  the  performance
of the FAD on a large scale.   A major objective of this  project was the inves-
tigation of a flotation phenomenon observed  in  all  previous  testing with the
FAD, a phenomenon wherein solids rose to the surface  of  the  mixed  liquor ba-
sin to produce a concentrated sludge layer (float).   This  study, from January
12 through April 16, 1974, indicated that float could be continuously genera-
ted in mixed liquors having both high (_> 4000 mg/1) and  low  (=2600  mg/1) con-
centrations of suspended solids.  It was also ascertained  that  removal  of the
float, which averaged 6.5 percent total  solids, could supply up to  50 percent
of the total system wasting requirements.

The development by FMC engineers of an improved device for achieving small
bubble diffusion led to the next phase of the research and development effort.
This device, a rotating active diffuser (RAD),  differed  from the FAD in that
oxygen bubble shear was produced by rotating the diffuser  through  the liquid
medium, rather than by pumping liquid across the diffusion surfaces.  Substi-
tution of the RAD for the FAD in the 57-1/min (15-gpm) pilot  system  indicated
that the RAD produced oxygen transfer efficiencies comparable to those ob-
tained with the FAD, but with lower power requirements for equivalent oxygen
transfer.  As a result, a full-scale RAD prototype unit  was  installed in an
aerobic digestion basin at Metro for further testing. This  study  verified
that high oxygen mass transfer and utilization  efficiencies  could  be realized,
and that the mixing characteristics of the RAD  were sufficient  to  keep sludge
solids uniformly mixed.  The prototype unit operated  continuously  for 3 mo in
unscreened waste activated sludge without any major problems or hardware fail-
ures.  The success of development efforts to this point  led  Metro  and the FMC
Corporation to submit a request to the EPA on March 19,  1975, for  a grant to
demonstrate the open tank oxygenation system in full-scale operation at the
Metro facilities.

PURPOSE OF THE PROJECT

As outlined to the EPA in the grant request, the objectives  of  the project
were as follows:


     1.  To convert a three-pass, diffused air  activated sludge system to a
         single-pass, open tank oxygenation system and evaluate the operation
         of this system at varying F/M ratios,  detention times, and ambient
         temperature conditions.

     2.  To provide the data base necessary for the design of either a par-
         tial or total conversion of the existing Metro  diffused air system
         to open tank oxygenation.  This data base would include oxygen uti-
         lization efficiency, solids settling characteristics,  power require-
         ments for oxygen dissolution, and the  reliability of diffusion and
         oxygen control equipment.

     3.  To provide EPA an opportunity to demonstrate on a large scale a
         pure oxygen open tank treatment system previously researched on a
         smaller scale.

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4.  To provide EPA with data for technology transfer purposes related
    to other activated sludge treatment systems that might benefit from
    the upgrading of an existing facility.

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                                  SECTION 2

                                 CONCLUSIONS
A three-pass, diffused air mixed liquor basin was modified for the installa-
tion of a single-pass FMC 02 system which employed RAD's for oxygen dissolu-
tion and dissolved oxygen sensors for control of oxygen flow to the basin.
In the absence of filamentous organisms, the system provided satisfactory
treatment performance at average oxygenation times of 1.2 to 1.9 hr based on
influent flow, at F/M ratios ranging from 0.7 to 1.1  kg BOD/day/kg MLVSS, and
with mixed liquor suspended solids (MLSS) concentrations between 2700 and 3940
mg/1.

Filamentous organisms in the activated sludge resulted in the deterioration of
the system performance with respect to sludge settleability during much of the
demonstration.  These organisms were also present in the parallel  operating
Metro diffused air system, though to a lesser degree, and may have been intro-
duced into both systems by one of the primary effluent streams feeding the
Metro secondary.  Oxygen system performance was excellent during the last 3^
mo of operation, with no adverse effects due to filamentous organisms.

Effluent soluble BOD values averaging 4 mg/1 throughout the demonstration in-
dicated efficient mixed liquor basin performance with respect to BOD removal.
Poor clarification was responsible for those high effluent BOD values encoun-
tered.

Adequate mixing of the mixed liquor basin contents was demonstrated by both
suspended solids and dissolved oxygen profiles of the basin.

The system evidenced minimal nitrification operating at oxygenation times of
1.2 to 2.7 hr based on influent flow and SRT's of 3.5 to 10 days based on to-
tal system inventory.

Tests conducted during the demonstration showed oxygen transfer efficiencies
in excess of 96 percent at or below the design oxygen flow rate.  Efficiencies
in excess of 92 percent were obtained at oxygen flow rates up to 25 percent
above design.

Solids production during the operation of the oxygen system was equivalent to
that obtained from the parallel operating air system, at comparable SRT's.

Oxygen consumption averaged 1.23 kg 02/kg BODR under what were considered nor-
mal operating conditions.  Periods of long SRT, low BOD removal, and oxygen
system equipment problems exhibited somewhat higher values for oxygen consump-

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tion.

The calculated power required for the operation of the oxygen system averaged
39 percent below that required for the parallel operating air system, based
on equivalent flow rates and BOD removals.

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                                  SECTION 3

                               RECOMMENDATIONS
The oxygen system was operated at average clarifier overflow rates up to 32.6
m3/day/m2 (800 gpd/ft^).  For most of the time, overflow rates were less than
24.4 m3/day/m2 (600 gpd/ft^).  The performance of the system should be evalu-
ated at higher clarifier overflow rates.

The maximum treatment capacity of the system was never determined because of
hydraulic limitations of the mixed liquor basin.  This capacity should be as-
certained in future studies.

Additional cold weather operating data would be desirable in future studies
to demonstrate the capability of the system.

Future studies, if possible, should investigate the difference in the growth
rates of filamentous organisms in the FMC 02 system as compared to a diffused
air system.

In future operations, where modification of process operating variables fails
to alleviate filamentous sludge conditions, consideration should be given to
the use of continuous low-dose chlorination for filamentous control (3).  The
reported chlorine dosage of 2 to 3 kg/1000 kg MLVSS/day equates, for an MLVSS
level of 3000 mg/1 and an oxygenation time of 1.5 hr based on influent flow,
to a chlorine dosage of 0.38 to 0.56 mg/1 (3.1 to 4.7 Ib/mil gal) of influent
flow.

During this demonstration, an accumulation of floating solids (float) concen-
trated on the surface of the mixed liquor.  Further studies should evaluate
the controlled removal of float to produce a waste sludge of high solids con-
centration.

The dewatering characteristics of oxygen activated sludge should be investi-
gated.

The use of FMC rotating active diffusers to provide oxygen where needed for
the maintenance of dissolved oxygen levels in existing diffused air activated
sludge systems should be studied.

The feasibility of single-stage nitrification using the FMC 02 system alone
or together with a diffused air system should be evaluated.

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                                  SECTION 4

                                 FACILITIES
TREATMENT PLANT DESCRIPTION

Completed in 1966, the original  Metro treatment complex consisted of a
106,000-m3/day (28-mgd) primary treatment facility and a 371,000-m3/day (98-
mgd) conventional aeration activated sludge system, the latter designed to
receive both the effluent from the Metro primary process and  265,000 nwday
(70 mgd) of primary treated sewage from the City of Denver's  North Side (DNS)
Wastewater Treatment Plant.  Solids processing facilities consisted of a dis-
solved air flotation system for activated sludge concentration and vacuum
filters for the dewatering of the concentrated waste activated sludge, Metro's
primary sludge, and anaerobically digested sludge from the DNS treatment
plant.

Rapid growth in the Metro area caused the plant to exceed design capacity by
1973.  Construction of additional primary and secondary treatment capacity
and sludge processing facilities began in 1974 and was completed in 1976.  The
additional treatment facilities included a 159,000-m3/day (42-mgd) primary
treatment system and a 273,000-m3/day (72-mgd) closed tank pure oxygen acti-
vated sludge facility (UNOX).   Anaerobic digesters were provided for sludge
stabilization.   With the facilities expansion, the treatment  plant has been
subdivided into two treatment complexes, North (original facilities) and
South (new facilities) (Figure 1).

OXYGEN SYSTEM INSTALLATION

The Metro North Complex secondary treatment facility consists of 12 three-
pass aeration basins and associated clarifiers.  The basins are grouped into
four quadrants, each containing three adjacent basins feeding, individually
or through a common channel, into three secondary clarifiers.   For reasons
of access it was decided to install the demonstration equipment in the first
pass ("A" pass) of aeration basin No. 11 and to use clarifier No.  11 for the
final settling tank in the initial phases of the project.  The general site
plan for the demonstration is shown in Figure 2.

Several  modifications of the existing facilities were required for the instal-
lation of the oxygen system.  First, since only the "A" pass  of the three-
pass aeration basin was to be used for the demonstration, it  was necessary to
install  a 137-cm (54-in.) bypass duct to allow for a direct connection from
the discharge end of "A" pass to the venturi outlet in "C" pass feeding the
clarifier.  Second, although a control gate was available to  isolate the feed

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                                             CHLORINE
                                             CONTACT
                                             CHAMBER
                    CONDARY
                      -~-
                              ADMINISTRAT
                                 BUILDING
       PROCESSING
        V ANAEROBIC J
        r DIGESTERS S
            ECONDARY  )Tl  CLATTERS  )
 ^^ v-^ v,    y v_x  V_^ \^_y \Lx
Figure  1.  Metro treatment  facilities.
                 8

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                                      54 in. DUCT
  — RETURN SLUDGE
   ® ROTATING /
      DIFFUSERS
   V. D.O. SENSC
   — CONTROL GATE
   / BAFFLE
NOTE: 1  in. = 2.54 cm
GE
TIVE
LOCATION
E
4 cm

SE
n
"C"
PASS
'.ijrt.iw

liMtr*
"B"
PASS

A
1


13
®
12 *
®
11
®
10
®
9

8 *
®
7
®
5 6
® S)
3 4*
S> ®
1 2
2> ®
" +
1
CONDARY INFLUENT
"A"
PASS
                              BASIN NO.  11
         Figure 2.   Demonstration site plan,

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from the mixed  liquor  basin  to  clarifier  No.  11,  the existing facility did
not allow segregation  of  the return  sludge  from that of the other clarifiers
operating in  the quadrant.   To  accomplish this, baffles were installed in the
return sludge wet well and pump line to prevent sludge interchange.

The mixed liquor basin and clarifier chosen for the demonstration are depic-
ted in Figure 3.  Fluctuating somewhat with the liquid .level in the secondary
influent channel, the  capacity  of  the mixed liquor basin was a nominal 2500
m3 (661,000 gal).  The clarifier was of the center-feed type with three rows
of overflow effluent weirs at the  periphery.
                                                          WATER LEVEL

1
>
INF. L
-i

, >
10 f

<
t
"•A
A>!
u-» A
M?XED LIQUOR BASIN n
T"
^
'SUB
                   20 ft
                                 'SUBMERGED MIXED
                                  LIQUOR TRANSFER
                                  PIPE
                                         -2 ft

                                         -5 ft
130 ft
                                                       SECONDARY ClARIFIER
                   30 ft
                                      00
                                               NOTE:  1 ft * 0.305 m
                                         2 ft
                 SECTION A-A
       Figure 3.  Dimensional  layout of mixed liquor basin and clarifier.
Ten bridges were installed spanning "A" pass to accommodate the  installation
of the 13 RAD's used for the demonstration.  Two RAD's were mounted  on  each
of the first three bridges at the influent end of the basin, with a  single
RAD on each of the other bridges.  The greater number of RAD's at the influ-
ent end of the basin were provided to meet the anticipated oxygen demand  in
this area.  A dissolved oxygen (D.O.) sensor located in the basin between
bridges 2 and 3 was used to regulate, through a control system,  the  flow  of
oxygen to the first six RAD's.  The next four RAD's were similarly controlled
                                      10

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by a D.O. sensor located between  bridges  5 and 6, and the last three RAD's by
a third D.O. sensor located  between  bridges 9 and 10.  Each D.O. sensor pro-
vided a 4-20 mA signal proportional  to the measured D.O. level; this signal
was coverted by an I-P transducer to a pneumatic signal in the control system.
The input signals from the three  D.O.  sensors were compared to individual set
points on a control panel, and  return  pneumatic signals were conveyed to flow
control valves which modulated  the oxygen flow to each of the three controlled
areas of the basin.

Liquid oxygen, supplied by an outside  vendor, was stored in a 42-m^ (11,000-
gal) dewar from which it was vaporized to a gas by ambient heat exchangers
for transmission to the system.   Signals  were transmitted to a control center
from an orifice plate and temperature  and pressure sensors installed down-
stream of the vaporizer.  These signals were translated in the control system
to both instantaneous and totalized  oxygen flow readings on the control panel.
Gauges on the panel also monitored oxygen temperature and pressure.  Dissolved
oxygen analyzers and recorders  were  provided to monitor D.O. levels at the
three sensor positions in the basin, with alarm systems installed to indicate
high or low D.O. conditions.  A schematic of a typical FMC 02 installation is
shown in Figure 4.
                        CONTROL
                        PANEL
                          MOTOR/GEAR
                          REDUCER
                          ASSEMBLY
                                                        D.O. ANALYZER
                                                             TYPICAL OPEN
                                                             BASIN
INFLUENT
WASTEWATER-r
                          ••• ••••••>-.•••-.•. •-».,••. -..-k.•>..
                          . ,-.».,-....••. y., ; ., -. . .^..', ... .-.' :
                                                                   MIXED
                                                                   LIQUOR
                                                                   SETTLING
      LOX  STORAGE
      (STAND-BY)
     -VAPORIZER
                 Figure 4.  A typical  FMC  02  installation.
Thirteen RAD's were used to provide efficient oxygen transfer in the mixed
liquor basin.  The equipment was sized  to  accommodate a nominal  flow of
46,900 m3/day (12.4 mgd) and a BOD loading of 7030 kg/day (15,500 Ib/day).
Principle elements of the RAD are shown in Figures 5 and 6.   The RAD con-

                                      11

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                                           HAND RAIL
                          MOTOR/
                      UilGEAR
                          REDUCER
                          ASSEMBLY
                                    CONCRETE
                                     BRIDGE
                                    [STRUCTURE
                             LIFTING  LUG
                           STAINLESS  STEEL
                            HOLLOW  SHAFT
                            ROTATING ACTIVE
                            DIFFUSER DISC
MIXING IMPELLERS
Figure 5.   Elevation  view of rotating  active  diffuser
           (RAD)  and  drive assembly.
                        12

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                                   0,  GAS
                       MIXING
                      IMPELLERS
                   (TOP AND BOTTOM)
 DIFFUSION
  MEDIUM
(TOP AND BOTTOM)
          Figure 6.  Section view of RAD diffusion media  and  impellers.
sists of a 2.1-m (7-ft)  diameter  submerged rotating disc, located approxi-
mately 0.9 m (3 ft)  above  the oxygenation tank floor and mounted to a 16.8-
cm (6.625-in.)  diameter  hollow  shaft.  Twelve diffusion assemblies, each
consisting of upper  and  lower ceramic plates epoxied into a plastic frame
20.3 cm (8 in.) wide,  are  installed  in sections near the periphery of the
disc forming circular  diffusion bands on both the upper and lower surfaces
adjacent to the tapered  edge of the  disc.  Radial impellers are mounted on
the top and bottom surfaces of  the disc to provide shear for small-bubble
formation, solids mixing,  and oxygen distribution into the mixed liquor.
The disc and shaft are rotated  by a  gear drive operating at an output speed
between 82 and 86 rpm.   Oxygen  is transferred from the supply line to the
hollow shaft via a rotating seal  and is distributed from the shaft at the
disc interface by radial  lines  leading to the diffusion assemblies.  Oxygen
gas from the supply  system is provided to the basin at pressures of 21,100 -
24,600 kgf/m2 (30 -  35 psig).   As the oxygen gas emerges from the ceramic
plates in the diffusion  assemblies,  the rotation of the disc and the radial
flow of mixed liquor shear the  oxygen bubbles to produce minute bubbles in
the 50 - 200 micron  range. The micron-size bubble is essential for the oxy-
gen absorption rate  required for  efficient oxygen transfer into the liquid
medium.  The tapered edge  of the  disc prevents turbulence which would cause
coalescence of the bubbles.

Modification of the  existing facility and installation of equipment was ac-
complished within a  2-mo period prior to startup of the project.  Figure 7
shows the demonstration  system  in operation at the Metro plant.  Figure 8 is
a view of the mixed  liquor basin  with RAD's installed prior to startup.
                                    13

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Figure 7.   FMC 02 system in  operation  at the  Metro plant.
                          14

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15

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                                  SECTION 5

                              PROCESS  MONITORING
Metering, recording, and totalizing devices  were  used  to monitor  the influ-
ent flow, return and waste sludge flows, and the  supply of oxygen fed to  the
aeration basin.   Dissolved oxygen levels in  the basin  were continuously moni-
tored at three Ipcations by installed D.O. sensors  checked daily, and cali-
brated as required, against a portable D.O.  meter.   pH values  were initially
obtained in the laboratory on daily composites  of the  influent and effluent
samples and weekly mixed liquor grab samples, but carbon dioxide  losses and
resultant pH changes during sample transportation and  storage  dictated the
advisability of making in situ pH determinations.  Beginning December 26,
1976, these measurements were made daily using  a  portable pH meter.   Mixed
liquor temperature readings were taken in situ  twice daily.  Clarifier sludge
blanket measurements were taken six times per day using a portable blanket
finder.  Initially, settling tests (unstirred SVI)  on  the mixed liquor were
performed daily.  This frequency was expanded to  twice per day on December 26,
1976, and expanded again to include twice per day stirred SVI  determinations
from March 8, 1977, onward.  Centrifuge spins of  the return sludge, checked
frequently against laboratory suspended solids  results, were used to facili-
tate real-time sludge wasting, and twice daily turbidity measurements of  the
final effluent provided immediate system performance evaluation.

Twenty-four hr composite samples of the influent, effluent, mixed liquor, and
return sludge (equivalent to waste sludge)  samples  were collected by refrige-
rated automatic samplers for laboratory analysis.  Samples making up the  com-
posites were taken at 20-min intervals and were not proportioned  for flow.
Because of biological growth fouling the inlet line of the effluent sampler,
automatic sampling at this location was discontinued on May 30, 1977, intfa-
vor of a manual sampling procedure, with grab samples  every 2  hr  making up
each daily composite.

Daily laboratory analyses included total and volatile  suspended solids on in-
fluent, effluent, mixed liquor, and return sludge samples, as  well as BOD and
TOC on the influent and effluent.  Influent  and effluent nitrogen forms,  as
well as influent and mixed liquor alkalinity levels, were determined weekly,
the latter on grab samples delivered to the  laboratory.  Initially, nitrate
nitrogen analysis of the effluent was performed on composite  samples, but the
procedure was changed to grab sample analysis after May 30, 1977, due to ele-
vated nitrate levels produced by a nitrifying bacteria culture in the efflu-
ent sampler inlet line.  Soluble BOD analyses were run on influent and efflu-
ent samples twice weekly until May 4, 1977,  and daily  thereafter.  Filamentous
counts and general microscopic examinations  of the mixed liquor were performed
at least twice per week over the course of the project.

                                     16

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                                 SECTION 6

                           ANALYTICAL PROCEDURES
Suspended solids analyses were performed in accordance with Standard Methods
(4), a fiberglass overlay atop the standard filter being employed as a modi-
fication to aid in filtration.  Five-day biochemical oxygen demand (BOD) was
determined by the membrane electrode method (4).  Samples analyzed for solu-
ble BOD were filtered through a 0.45 micron membrane filter prior to an-
alysis.  TOC determinations were made on a Dohrman Envirotech DC-50 carbon
analyzer (5).  COD determinations were made in accordance with Standard
Methods (4).  Nitrate-nitrite nitrogen was determined by the automated cad-
mium reduction technique (4).  Ammonia and total Kjeldahl nitrogen forms were
determined using the automated phenate method (5), samples for Kjeldahl
analysis being digested in a Technicon Block Digester prior to analysis.
Alkalinity was determined by potentiometric titration to pH 4.5 on a Brink-
mann Autotitrator (4).  Settling tests (SVI), both stirred and unstirred,
were determined in 2-liter Mallory Settleometers (6).  Stirred SVI tests were
performed using a device consisting of two opposed vertical rods moving
adjacent to the settleometer wall at a motor-driven speed of 1 rpm.  Counts
of filamentous organisms in the mixed liquor were made on Gram stain smears
of approximately diluted samples examined microscopically.
                                     17

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                                 SECTION 7

                     PROCESS OPERATION AND PERFORMANCE
The demonstration project began on March 30, 1976, and terminated on Septem-
ber 7, 1977.  The period from March 30 through the end of May 1976 was a
startup period during which personnel involved with the project were familiar-
izing themselves with the equipment and a general electrical, mechanical, and
pneumatic shakedown of the system was performed.  The balance of the project
has been divided into seven operating phases, summarized in Table 1.


                         TABLE 1.  PHASE SUMMARY
Phase
I


II


III

IV
V
VI

VII
Period*
6/1/76
7/1/76
8/1/76
9/1/76
10/7/76
11/1/76
12/26/76
3/8/77
3/29/77
5/5/77
6/7/77
7/5/77
8/5/77
- 6/30/76
- 7/31/76
- 8/31/76+
- 9/28/76
- 10/31/76
- 11/21/76
- 1/31/77°
- 3/28/77
- 5/4/77
- 6/6/77
- 7/4/77
- 8/4/77
- 9/7/77
No.
of
Days
30
31
26
28
25
21
36
21
37
33
28
31
34
Nominal
Influent
Flow
(mgd)
9


6


6

10
12
14

12
No. of
Flow Pattern Clarifiers
Steady State


Steady State


Steady State

Diurnal
Diurnal
Diurnal

Diurnal
1


1


1

2
2
2

2
* Division of phases  into  periods made on the basis of temporary
  shutdowns, or arbitrarily  to  create roughly 1-mo operating periods.
+ 8/25/76 - 8/29/76,  system  shutdown.
0 1/20/77, system shutdown.

                                     18

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Initially, the project outline called for division of the demonstration into
operating phases based upon both steady state and diurnal flow patterns at
different flow rates.  Although this regime has been adhered to in this re-
port, it is important to note that in Phases II and III, flow conditions,
rather than being planned, were dictated by operating difficulties as des-
cribed below.  These two phases show identical  operating parameters in Table
1; however, a division has been made because Phase III was actually an inves-
tigative phase instituted in an attempt to overcome operating difficulties
experienced in Phase II.

The various phases of operation and interim periods of project shutdown are
described in the following discussion.   A summary of operating performance
data is shown in Table 2, with the operating parameters in Table 3.  A com-
plete daily record of the operating performance of the system can be seen in
Appendix A.

PHASE I (JUNE 1 - AUGUST 31, 1976)

The flow during this phase was steady state, averaging 34,400 m^/day (9.1
mgd).  The first operating period, from June 1  to June 30, was characterized
by a sludge quality which yielded the best settling characteristics encoun-
tered over the course of the project, an average unstirred SVI of 79 ml/g.
Effluent quality during this period averaged 30 mg/1 suspended solids (SS).
This level of solids in the effluent was attributed to a failure of the rap-
idly settling sludge to sweep pin-point floe from suspension.  In mid-July,
SVI's began to increase, with values exceeding  100 ml/g for the first time.
As a result, the return sludge solids concentrations began to decrease and
sludge blanket levels in the clarifier began to rise.   By mid-August, SVI
values were averaging in excess of 200 ml/g and sludge bulking was a common
occurrence, the principle contributor to an average 60 mg/1 SS in the efflu-
ent for the month of August.  MLSS levels, which had averaged 3070 mg/1 dur-
ing the month of June, decreased to an average  of 2180 mg/1 in August.   Due
to poor effluent quality from August 11 through 13, the flow through the sys-
tem was reduced over the next 6 days from 35,200 nH/day (9.3 mgd) to 26,900
m3/day (7.1 mgd) in an effort to improve performance.   Although effluent qual-
ity did improve, sludge settling characteristics remained unchanged.

It was noted during this time that the high SVI values were very closely tied
to an increase in the population of filamentous organisms that were appearing
in the activated sludge.  Figure 9 illustrates  this relationship as observed
during the demonstration.  In brief, the filamentous organisms observed were
slender, straight to slightly curved filaments  generally ranging in length
between 30 and 200 microns and appeared to be outgrowths of sludge floe par-
ticles (Figure 10).  These organisms were gram-negative, unbranched and un-
sheathed, with individual cells approximately 0.5 microns in diameter by 1.0
- 1.5 microns in length.  Microbiologists from  both Metro and EPA concurred
on the morphological description of the organism as being of bacterial  rather
than fungal origin and on the fact that it was  not a Sphaerotilus type, al-
though no serious attempt was made to identify  it.

Over the next several months, a major effort was made  to investigate possible
causes of the filamentous growth and methods for controlling it.   The data

                                     19

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Figure 10.   Photomicrograph  of  oxygen  system mixed  liquor, 8/17/76.
                                23

-------
from the latter part of July indicated that high mixed liquor D.O.  levels
(> 10 mg/1), resulting from malfunctioning D.O.  sensors, coincided  with the
proliferation of filamentous organisms, a relationship previously reported
(7).  On August 18, the D.O. set point for the mixed liquor was reduced to 1
+_H mg/1 to evaluate the effects on the filamentous population.  This evalu-
ation continued until August 24 when it became apparent that the filamentous
situation was not improving.  As a result, a decision was made to empty the
basin for a new startup.

Over the course of Phase I, effluent quality averaged 38 mg/1 SS and 26 mg/1
BOD at an average F/M loading of 0.76 kg BOD/day/kg MLVSS.  Clarifier overflow
rates averaged 30.8 m3/day/m2 (756 gpd/ft^).

Float accumulation in the mixed liquor basin was in evidence during the first-
operating phase.   This float material, varying in depth up to 38 cm (15 in.),
averaging approximately 6 percent total solids and containing high  concentra-
tions of Nocardia, was first noted in the basin  on April 25 during  the startup
period.   Since no provision had been made for the removal  of float  from the
basin, attempts were made beginning in May to re-entrain the float  into the
mixed liquor.  A float screw*, water sprays, surface mixers, and an air-lift
pump were all unsuccessful  in re-entraining the  float.  On July 3,  a down-
draft pump** was installed near the outlet end of the basin, followed on Aug-
ust 4 by a second downdraft pump located near the center of the basin.  With
the two downdraft pumps in operation, re-entrainment was only partial and
float was still present on the surface of the mixed liquor.  It should be
noted that at no time during the demonstration was any float present on the
surface of the clarifier.

PHASE II (SEPTEMBER 1 - NOVEMBER 21, 1976)

After dumping the system at the conclusion of Phase I, it was decided to use
a seed sludge from aeration basin No. 12 for the next startup to accelerate
establishment of the system.  This sludge was chosen because it evidenced a
minimal population of filamentous organisms***.

Despite the reseeding of the system and the continuation of the low D.O.
level control begun in August, the filamentous sludge condition and resultant
high SVI values experienced in Phase I continued to persist.  Operating under
  * A helical screw mounted around a diffuser shaft to auger floating materi-
    als downward into the mixed liquor.

 ** A shrouded propeller mounted vertically in the mixed liquor basin designed
    to draw material from the liquid surface over the shroud and through the
    propeller to exit near the bottom of the basin.

*** Filamentous cultures similar to those observed in the oxygen basin were
    observed in all the operating air system basins at Metro, although to a
    considerably lesser degree.
                                     24

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steady state hydraulic conditions, the average flow of 22,300 m3/day (5.9 mgd)
reflected the inability of the system to sustain a higher hydraulic loading
without adversely affecting effluent quality.   In analyzing the Phase I data,
it was evident that periods of high F/M ratios occurred, with values up to
1.5 kg BOD/day/kg MLVSS being attained.  High  F/M ratios have been cited in
the literature as a possible cause contributing to filamentous conditions (3,
8, 9).  Flow rates, which started out greater  than 30,300 m3/day (8 mgd) at
the beginning of Phase II, were gradually decreased in an effort to reduce
the F/M loading to approximately 0.5 kg BOD/day/kg MLVSS.  No improvement in
sludge quality was observed, and further flow  reductions to 11,400 m3/day (3
mgd) by the end of the first operating period  of Phase II were necessary to
maintain effluent quality.  Unstirred SVI values averaged 242 ml/g for the
month of September, and the effluent quality of 26 mg/1 SS and 19 mg/1 BOD
for September was maintained by reducing influent flows in an attempt to off-
set the poor sludge settleability.

On September 28, the influent flow to the system was shut down in order to
evaluate a period of aerobic digestion for controlling filamentous prolifera-
tion, an approach suggested by a pilot study conducted at the City of Engle-
wood, Colorado Wastewater Treatment Plant.  After 42 hr of aerobic digestion
of the mixed liquor, during which an 11,400-m3/day (3-mgd) return sludge flow
was maintained, no improvement was seen in the filamentous condition.  On Sep-
tember 30, it was decided to dump the contents of the system, clean the mixed
liquor basin and clarifier, and restart the system.  Startup was begun by
seeding the mixed liquor basin with the Metro  air system sludge exhibiting
the best settling characteristics available on the plant site.  The fill ope-
ration commenced on October 4, the system was  stabilized by October 6, and
data collection began on October 7.  At this startup, mixed liquor D.O. le-
vels were raised to 3 mg/1 to investigate the  effect of a somewhat higher
D.O. concentration on filamentous control (3,  8).  The D.O. level was raised
again on October 22 to approximately 5 mg/1 and maintained at that level
through November.  In spite of the elevated D.O. levels, filamentous prolif-
eration began shortly after the October startup, with a resultant increase
in SVI's.  October effluent quality, averaging 16 mg/1 SS and 9 mg/1 BOD, was
achieved by holding flow rates at or below 22,700 m^/day (6 mgd) for the en-
tire period.

Much of November exhibited increasingly poor sludge settling characteristics,
with return sludge and MLSS concentrations continuing to decrease.  Effluent
quality remained generally acceptable until an attempt was made, shortly be-
fore the end of the operating period, to increase the flow through the system
from 22,700 m3/day (6 mgd') to 26,500 m3/day (7 mgd); this resulted in bulking
conditions, leading to an average effluent quality of 48 mg/1 SS and 18 mg/1
BOD for the month.  By November 21, filamentous counts and SVI values had
reached such high levels that a decision was made to temporarily halt opera-
tions pending a coordination meeting at Metro  with the EPA Project Officer
and representatives of Metro and the FMC Corporation.

Overall performance for Phase II showed an average effluent quality of 26 mg/1
SS and 15 mg/1 BOD, at an average F/M loading  of 0.51 kg BOD/day/kg MLVSS and
a clarifier overflow rate of 20.0 m3/day/m2 (491 gpd/ft2).


                                      25

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Float re-entrainment, unsuccessful  in Phase I  in  keeping the mixed liquor
basin surface free of float, was practiced intermittently during Phase II
with similar results.  However, re-entrainment began to come under increasing
suspicion as being a possible cause of filamentous proliferation for two reas-
ons:  1) The first occurrence of filamentous growth in the system came shortly
after the installation of the first downdraft  pump in July.   The second and
third system startups in late August and early October, in which re-entrain-
ment was practiced virtually from the start, exhibited filamentous from the
outset.   2) A brief interruption of the re-entrainment process  during October
appeared to result in an improvement in sludge floe characteristics.  This
was observed microscopically as a partial coating of the filaments with zoog-
leal mass.  After resumption of float re-entrainment, further deterioration
of the floe was noted.

INTERIM PERIOD (NOVEMBER 22 - DECEMBER 25, 1976)

In the coordination meeting of November 24, it was decided to investigate
possible methods of eliminating the filamentous organisms from the activated
sludge.   Although chemical treatment was considered, it was thought to offer
only a temporary remedy.  Emphasis was placed instead on operational changes
which might effect a lasting solution.  To conserve project resources, labor-
atory monitoring during this interim period was to be limited to sludge qual-
ity determinations and those analyses required for sludge wasting; as such,
this information has not been included in the data tables.

The prevailing hypothesis at this time was that the float material, still
abundant on the surface of the mixed liquor, was  responsible for causing the
growth of the filamentous population.  The coordination meeting outlined four
approaches for subsequent investigation:

     1.   100 percent skimming of float to waste,

     2.   100 percent float re-entrainment,

     3.   Partial float re-entrainment plus float skimming, and

     4.   No re-entrainment or float skimming.

The system was restarted on December 4 by again seeding the mixed liquor ba-
sin with return sludge from one of Metro's aeration systems exhibiting good
settling characteristics and relatively few filamentous organisms.  An im-
provised float skimmer* was installed at the north end of the basin between
bridges 9 and 10 in  an attempt to skim the float from the surface.  In addi-
* The float skimmer consisted of a funnel mounted in an assembly which al-
  lowed the rim of the funnel to float near the liquid surface.  The funnel
  was connected to a pump which in turn removed the floated solids that en-
  tered the skimmer system to waste.

                                     26

-------
tion, the two downdraft pumps previously installed continued to operate to-
wards the outlet end of the basin in an effort to re-entrain the surface
float.  Despite these efforts, float removal was again only partial over the
surface of the basin.  The system was drained on December 15 when SVI values
again rose into the 200 - 300 ml/g range.

PHASE III (DECEMBER 26, 1976 - MARCH 28, 1977)

The system was started up again on December 21 without sludge seeding in an
attempt to develop a sludge entirely free of filamentous organisms.  However,
as a result of leakage across the dividing baffles in the return sludge well,
cross seeding did occur between the oxygen system and the adjacent air basin.

Data acquisition, largely suspended during the previous period, was resumed
on December 26.  On December 30, two additional downdraft pumps became avail-
able and were installed in the basin to improve float re-entrainment.  At-
tempts at float removal using the float skimmer had proved ineffective, and
the device was removed from service.  Poor effluent quality and continued
high SVI's from the startup of Phase III through January 19 resulted in an-
other system shutdown on January 20.  The basin was emptied and re-seeded on
January 21 with the objective of leaving the float solids in place, with no
attempts to re-entrain or skim.  Although effluent quality was acceptable for
the remainder of January, filamentous counts again were high and influent
flow was limited to rates approximating 22,700 m^/day (6 mgd).

On January 10, a consultant was employed by the FMC Corporation to investi-
gate the filamentous conditions existing in the oxygen activated sludge; his
reports are presented in Appendix B.  While undertaking studies to determine
the types of filamentous organisms present in the sludge, the consultant in-
dicated that the organisms were common to both the open tank oxygen and air
activated sludge systems operating at Metro and that they may have been in-
troduced into the systems by the influent wastewater feeding the North Complex.
He further indicated that the character of the poorly settling sludge was that
of floe built upon a filament backbone, and that such character resulted from
a combination of filaments in the wastewater and the generally weak, thin na-
ture of the waste.  With a lack of substance in the influent on which to
build a compact floe, the floe was instead growing on the available filament
structure.  The filament thought to be responsible for the poor sludge set-
tling characteristics was believed to be an acid-producing relative of Sphae-
rotilus, a sheathed organism not previously described.

Following a recommendation of the consultant, a comparison of the settling
characteristics of the open tank oxygen and air activated sludge systems was
undertaken to determine if problems existed in the air system similar to
those observed in the oxygen system.  The closed tank oxygen system, treat-
ing different wastewater in the Metro South Complex, was included in this
study for comparison (see Section 8, Comparative Settleabilities).

Since all efforts directed towards removing or re-entraining float material
had proved largely unsuccessful, the system was drained again on January 31
to allow for the construction and installation of an overflow weir system


                                     27

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in the mixed liquor basin to facilitate float removal  (Figure 11).   Float
accumulation in the basin had been primarily a result of a submerged outlet
from the aeration basin which did not allow float solids to exit from the
system.  It was expected that the surface outlet provided by the overflow
weir would eliminate the float accumulation.   With a fixed overflow weir, it
was necessary to maintain a constant liquid level  in the aeration basin not
subject to diurnal level fluctuations in the influent channel.   To achieve
this, the normal sewage inlet to the mixed liquor basin was sealed and a
system of air-lift pumps, easily regulated for either steady state or diurnal
flow, was installed at the head end of the basin.   The pump system consisted
of three units, each capable of delivering approximately 189 I/sec (3000 gpm).

Installation of the overflow weir and air-lift pumps was completed on Febru-
ary 23, with the system restarted on February 24.   Data acquisition began on
March 8.  Following installation of the weir, float accumulation on the mixed
liquor surface was markedly reduced, but not eliminated.  Despite the float
reduction, no improvements were observed in the filamentous character of the
sludge or in the sludge settleability.

From March 8 until the end of Phase III on March 28, effluent quality, at a
flow rate of 23,500 m3/day (6.2 mgd), was generally good despite gradually in-
creasing SVI values for the mixed liquor.  Sludge return rates,  held at 88
percent (R/Q) for this period, may have aided in improving effluent quality
from the previous operating period by removing sludge rapidly from the clari-
fier.

Over the course of Phase III, effluent quality averaged 57 mg/1  SS and 33
mg/1 BOD at an average F/M loading of 0.64 kg BOD/day/kg MLVSS.   Clarifier
overflow rates averaged 21.3 m3/day/m2 (522 gpd/ft2).

PHASE IV (MARCH 29 - MAY 4, 1977)

At a project coordination meeting on March 24, it was noted that two objec-
tives of the project had not been met due to a preoccupation with sludge qual-
ity and attempts to improve it.   First, the system had not been operated in
any diurnal flow pattern; second, the system had not been tested at elevated
flow rates.  It had been clear for some time that, with poor sludge settlea-
bility, the system was clarifier limited.  With excess clarifier capacity re-
cently made available by Metro, a decision was made to use two clarifiers
for subsequent operations.  On March 29, clarifier No. 11 was removed from
the system and the mixed liquor was diverted to clarifiers No.  7 and 9 (Fig-
ure 2).  The flow rate was gradually increased to 37,800 m^/day (10 mgd) and
regulated to a diurnal pattern approximating that normally seen at Metro
(Figure 12).

Effluent quality, at an average flow of 37,100 m3/day (9.8 mgd)  for the phase,
remained relatively poor, with sludge bulking occurring rather consistently
during peak flow periods.  This bulking, at peak flow rates approximating
49,200 m3/day (13 mgd), was directly attributable to continuing problems with
sludge quality.  However, it did appear that sludge settleability was begin-
ning to improve to some extent and it was decided to "wait out" the process
in hopes of further improvement.

                                     28

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                                           30

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A problem occurring for the first time during Phase IV was the appearance of
algae in the final  effluent.   This algae,  which could be seen  growing in the
effluent launders and on the weirs of the  clarifiers, undoubtedly contributed
to the reported values for effluent SS and BOD.   On nine of the 37 operating
days in this phase, the laboratory reported the presence of varying amounts
of algae in the final effluent composite samples analyzed.  The cause of the
algal growth was not determined, but the growth was not unique to the open
tank oxygenation system.  A similar proliferation had occurred at varying
times in Metro's closed tank oxygenation system, though not to any appreci-
able extent in the air system.

Overall performance during Phase IV demonstrated an average effluent quality
of 41 mg/1 SS and 31 mg/1 BOD.  The F/M loading rate, reflecting increased
flow, rose to 1.14 kg BOD/day/kg MLVSS.   Clarifier overflow rates, with the
addition of a second clarifier to the system, decreased to an  average of 16.5
m3/day/m2 (406 gpd/ft2).

PHASE V (MAY 5 - JUNE 6, 1977)

Maintaining the diurnal flow pattern established during Phase  IV, influent
flow was increased to an average 45,800 nr/day (12.1  mgd) during Phase V.  It
can be seen in Table 3 that mixed liquor unstirred SVI values  decreased sig-
nificantly, averaging 150 ml/g for the phase.  Final  effluent  quality was gen-
erally superior to the 30 mg/1 SS and 23 mg/1 BOD reported for the phase, as
the averages contain several  anomalous data points.   Algae was noted, though
less frequently than in the previous phase, in three of the 33 final effluent
composite samples collected.  In addition,  2 day's data, shown  in Appendix A,
deserve special mention.  The unusually high values of 148 mg/1  SS and 49
mg/1 BOD for the effluent sample of May 11 resulted from an exceptionally
high influent SS loading of 257 mg/1*.  Although later in the  demonstration,
the system exhibited the ability to handle such loadings easily without ad-
verse effect, at this time sludge settleability had not improved sufficiently
to prevent bulking with the high influx of solids.   The effluent sample of May
28, with values of 83 mg/1 SS and 62 mg/1  BOD, contained clumps of a greyish
slime which, upon microscopic examination, consisted of colonies of Vorti-
cella sp., a growth of ciliated protozoans which had been observed growing
along with the algae in the clarifiers.   Elimination of these  two data points
from the phase averages would result in an effluent quality of 24 mg/1 SS and
20 mg/1 BOD, values more representative of the performance of  the system than
those shown in Table 2.

Although the algal  growth in the clarifiers was diminishing during this
phase, the continued presence of algae in  some of the effluent samples col-
* The elevated loading level  was traced to the air-lift pumping  arrangement
  used to supply influent to  the oxygen system basin;  at low flow in  the in-
  fluent channel, the pumps would actually draw mixed  liquor solids from ad-
  jacent air system basins to make up for the flow deficit.


                                     31

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lected prompted a decision to institute,  on  May 30,  a manual  sampling  pro-
gram to replace the automatic sampler used up to this time.   It was  theorized
that the automatic sampler influent line  might be located so  as to provide  a
sample containing debris not visibly apparent in the effluent leaving  the
clarifier.  Comparison data taken over several days  revealed  the  consistent
presence of algae and Vorticella slime in the automatically collected  samples
and only minimal amounts in the manual samples.  Following institution of the
manual sampling program, algal contamination of final effluent samples ceased
for all practical purposes.

Overall during Phase V, the effluent quality mentioned above  was  achieved at
a system F/M loading average of 1.10 kg BOD/day/kg MLVSS, with clarifier
overflow rates averaging 20.4 m3/day/m2 (501 gpm/ft2).

PHASE VI (JUNE 7 - AUGUST 4, 1977)

This phase was divided into the two operating periods shown  in the data
tables to produce approximately 1-mo operating periods.  There were  no signi-
ficant differences in operating parameters between the two periods other than
a decrease in F/M loadings resulting from a decline in influent wastewater
BOD during the second period.  The flow during this phase was increased to  an
average of 53,000 m3/day (14.0 mgd).  Although a diurnal  flow pattern  was
maintained, the nature of the pattern was changed on July 7  (Figure  12) due
to constraints in operating the Metro air system.  Unstirred  SVI  levels, as
a result of a diminishing filamentous population (Figures 9,  13), decreased
to an average of 107 ml/g.  As a result,  the system responded with the fi-
nest effluent quality of the demonstration, averaging 16 mg/1 SS  and 12 mg/1
BOD.  F/M loadings for the phase averaged 0.85 kg BOD/day/kg  MLVSS,  with
clarifier overflow rates averaging 23.7 m3/day/m2 (581 gpd/ft2).

Although the system showed no signs of being anywhere near its failure point
at 53,000 m3/day (14.0 mgd), a practical  hydraulic limit was  reached during
peak-flow (68,000 m3/day, 18 mgd +_) periods.  The installed overflow weir so
elevated the liquid level in the mixed liquor basin that the support bridges
for the diffuser drives became partially submerged.

PHASE VII (AUGUST 5 - SEPTEMBER 7, 1977)

The hydraulic limitations discussed above, coupled with the fact  that previ-
ous operation at 45,800 m^/day (12.1 mgd) during Phase V had yielded less
than desired results, prompted a decision to return to a nominal  45,400 m3/
day (12-mgd) diurnal operation in order to acquire additional performance
data at this flow rate.


 Unstirred SVI  values continued to decrease  and averaged  under 100 ml/g for
 the phase.   The influent flow rate averaged 46,600  nP/day (12.3  mgd),  result-
 ing in an F/M Ioading2of 0.75 kg BQD/day/kg MLVSS and a  clarifier overflow
 rate  of 20.8 m /day/m  (511  gpd/ft ). Effluent quality  remained excellent,
 averaging 17 mg/1  SS and 13 mg/1  BOD.
                                      32

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Figure 13.   Photomicrograph  of oxygen  system mixed  liquor,  7/26/77.
                                33

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OPERATION SUMMARY

An overview of the seven operating phases detailed above shows  that the ini-
tial performance of the system was satisfactory;  a proliferation  of filamen-
tous organisms then led to a marked deterioration of the system performance
extending over a period of several months, with subsequent recovery of the
system and excellent performance during the latter phases of operation.   At-
tempts at determining the causes of the filamentous proliferation met with no
success.   Investigations of float involvement,  the influence of both high and
low D.O.  levels in the mixed liquor, and the effect of high F/M loadings did
not provide an answer.  Filamentous conditions  at both high and low mixed li-
quor temperatures appeared to rule out a solely temperature related phenome-
non (10).

Also unexplained is the disappearance of the filamentous organisms from the
system.  Other than increasing the flow rate through the system,  with resul-
tant increases in system loadings, no operational changes were  made which
could explain the improvement in sludge quality and attempts to tie the im-
provement to the flow or loading changes would  be purely conjectural.

There is  a possibility that the filamentous appearance and disappearance may
have been related to changes in influent wastewater characteristics (see Sec-
tion 8, Comparative Settleabilities).   This, however, does not  explain the
rapid growth of the culture in the oxygen system as compared to the diffused
air system during several of the operating phases.   With the two  systems ope-
rating at different F/M loadings, detention times,  etc., any of a number of
factors may have been responsible for this disparity.

A hypothesis submitted by the system supplier to account for the  filamentous
growth experienced in the oxygen system is as follows:  At the  time of initial
startup of the system, the influent wastewater  may have had essentially non-
filamentous characteristics.  As a result, the  system developed a good settl-
ing sludge.  Float accumulation over a period of approximately  90 days contri-
buted to a sudden increase in and continuation  of filamentous growth during
July 1976, resulting in a system shutdown in August 1976.  Subsequent attempts
to restart during the fall of 1976 and the winter of 1976-77 occurred when the
influent wastewater was of a filamentous nature,  explaining the rapid growth
of filamentous organisms after these startups.   In each case, operation was
discontinued after a short period, with insufficient time allowed for the sys-
tem to stabilize.  Following installation of the overflow weir  in February
1977, the system was restarted, again with an influent wastewater having fila-
mentous characteristics.  Rapid filamentous growth occurred for a period of
approximately 6 weeks following startup, followed by a sudden reduction in
filamentous counts.  This significant improvement was caused by:   1) the over-
flow weir preventing excessive accumulation of floated solids on  the mixed li-
quor surface, 2) a change in basic influent wastewater characteristics
from filamentous to nonfilamentous,  3) a change in the mixed liquor tempera-
ture, or  4) a combination of any of these three factors.  Both 1) and 2) were
accompanied by operation for an adequate time to permit system  acclimation.
Continued operation resulted in the development of a sludge with  better
settling characteristics than those of the parallel operating air system.


                                     34

-------
In any case, the last 3% mo of operation with the FMC G£ system comprised a
period of excellent performance at relatively high F/M loadings, at mixed li-
quor temperatures comparable to those experienced in previous operating peri-
ods yielding poor performance, at mixed liquor D.O.  levels similar to those
maintained earlier, and with no basic alterations in the philosophy of opera-
tion of the system.  With two clarifiers in use during this time, overflow
rates were limited to those mentioned under the various operating phases.
However, sludge settleability and blanket levels were such that higher over-
flow rates might well have been achieved.
                                    35

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                                  SECTION 8

                         COMPARATIVE SETTLEABILITIES


Beginning in April  1977 and continuing until  the end  of the project,  a  com-
parison of mixed liquor SVI values was made on  samples  from both  the  open
(FMC 02) and closed (UNOX)  tank oxygen systems  and the  diffused air system.
The purpose of this study was to determine if the sludge settling difficul-
ties experienced with the open tank oxygen system were  unique  to  that system,
or were common to either or both of the other operating systems at the  plant.

For each settling test, stirred SVI's were run  on mixed liquor samples  as
collected and at 25 percent and 50 percent dilutions  (made with final efflu-
ent from the system being tested) so that the data could be plotted to  yield
SVI values for each system at equivalent solids concentrations.   The  data,
plotted as SVI adjusted to a mixed liquor suspended solids concentration of
2000 mg/1, are shown in Figure 14.

It is important to note that although the air and FMC 02 systems  operating
in Metro's North Complex were at all times treating the same influent waste-
water, the influent to the UNOX system in the South Complex was a separate
wastewater stream.   On several occasions during the course of  the project,
influent sources were switched so that the three systems were  treating  diffe-
rent wastewaters at various times.  Wastewater  "A" in Table 4  was the primary
effluent from the Denver North Side Sewage Treatment  Plant, a  waste from the
City of Denver proper containing packing house  and other industrial wastes,
the domestic waste from the city, and supernatant from  the Denver North Side
anaerobic digesters.  Wastewater "B" was a somewhat more domestic waste col-
lected from suburban Denver communities and given primary treatment at
Metro's primary facility; also included in this stream  were the Metro in-plant
wastes.  Table 4 depicts the pattern of differing wastewater distribution  to
the three treatment systems during the project.

Observations made earlier in the demonstration  indicated that  the FMC 02 sys-
tem sludge settleability had been more severely affected by filamentous orga-
nisms than that of the air system.  However, it is apparent in Figure 14 that
for the duration of the comparative test period the settleabilities of  the
two systems tracked closely with one another.  The UNOX system, treating dif-
ferent wastewater, exhibited a markedly different trend.  These observations
suggest the possibility that influent wastewater characteristics  may  have
played a significant role in determining sludge quality.  This hypothesis  is
further supported by the fact that each time the influent sources to  the
North and South Complexes were switched, on June 25 and again  on  August 23,
1977, the systems newly receiving the Denver North Side wastewater appeared


                                     36

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                                    37

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to be adversely affected.   While not  sufficient  to establish a relationship
between influent wastewater and  sludge  quality,  these observations do indi-
cate that such a relationship  may have  existed.
               TABLE  4.   INFLUENT WASTEWATER DISTRIBUTION

Period
6/1/76 - 1
11/15/76 - '
6/25/77 -
8/23/77 -

1/14/76
6/24/77
8/22/77
9/7/77
System
Air and FMC 02
UNOX
Air and FMC 02
UNOX
Air and FMC 02
UNOX
Air and FMC 02
UNOX
Wastewater*
A (62%) + B
Off Line
A (100%)
B (100%)
B (100%)
A (100%)
A (100%)
B (63%) + A
(38%)


(37%)

  * Wastewater "A" = Denver North Side primary effluent and digester
    supernatant.
    Wastewater "B" = Metro primary effluent and in-plant wastes.
                                     38

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                                  SECTION 9

                         OXYGEN TRANSFER EFFICIENCY
The method employed to evaluate the efficiency of oxygen transfer from spe-
cific diffusers into the mixed liquor required the capture of all gases
leaving a representative area of free liquid surface and the determination
of the oxygen fraction of those gases.   The total off-gas oxygen thus mea-
sured, extrapolated from the test area  to the total  area of influence for
the monitored diffuser, was compared to the total amount of oxygen flow to
the diffuser to yield the oxygen transfer efficiency.   As the off-gas capture
was made over a surface area representing only a part of the area of influ-
ence of the diffuser being tested, it was necessary to establish that differ-
ent test areas within an influence area would yield approximately equivalent
values for the transfer efficiency.

Due to the impossibility of isolating the diffuser under test from adjacent
diffusers in the basin, oxygen flow was set during each test so that the
target diffuser and all adjacent diffusers were receiving equivalent oxygen
flow rates.  The possibility of transient oxygen demand conditions in the ba-
sin influencing the measurements was reduced by conducting each test over a
period of several hours, monitoring for steady state conditions and using
the data obtained during such periods.

OFF-GAS TEST EQUIPMENT

The equipment used for off-gas collection and analysis is shown schematically
in Figure 15.  A floating dome captured the gas leaving a 3.7-m2 (40-ft^)
area of the basin surface.  A 17.8-cm (7-in.) diameter water filled tube was
attached around the periphery of the dome to provide stability and prevent
tiHing of the dome under conditions of increasing off-gas volume.

The captured off-gas was transferred from the dome through a flexible hose
to an oxygen gas analyzer (Biomarine Industries, Model OAR 602) and then to
a wet test meter (Precision Scientific  Company, Model  63126) before being
vented to atmosphere.  Revolutions of the wet test meter were detected and
counted by means of a proximity switch  (Electro-Corporation, Versa Switch
Model 50) which provided accurate accounting of off-gas displacement through
the meter.  A strip chart event marker  was used with the wet test meter to
measure the time per revolution of the  meter.  These recorded data, together
with the oxygen analyzer data, allowed  for a precise determination of steady
state conditions.  The wet test meter was equipped with a mercury thermometer
to allow for the conversion of measured gas volumes  to volumes at standard
temperature conditions.


                                     39

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A thermistor and strip chart recorder provided continuous temperature moni-
toring in the vicinity of the oxygen gas analyzer, and an inclined water
manometer tapping the off-gas line from the dome allowed monitoring of the
approximate gas pressure under the dome.  Data from these sensors was used
for test monitoring only, rather than for data evaluation.

For oxygen flow to the system, an orifice plate and needle  valve located in
the oxygen line to each diffuser allowed for adjustment and measurement of
differential and upstream pressure.  These parameters, combined with measure-
ments of oxygen temperature, allowed for the accurate determination of oxygen
flow.

Prior to the start of each test period, the Biomarine oxygen gas analyzer
was calibrated in air pursuant to the manufacturer's instructions, and addi-
tional checks were made at intervals with a second instrument (Taylor Indus-
ries, Model QA 250) to verify calibration of the Biomarine  unit.  Calibra-
tion of the wet test meter was performed prior to use by comparison with a
rotameter (Fischer Porter, Tube No. FP-1/8-20-G-5/840).

DATA REPRESENTATION

Figure 16 shows the locations of the off-gas dome during the oxygen transfer
test periods.  RAD's 1 through 4 were not tested because of severe surface
turbulence near the head end of the basin resulting from the surface dis-
charge of influent wastewater into the basin.   RAD's 9 and  11 were not tested
because of visually apparent diffuser leaks.

Test results are shown in Figure 17, with oxygen transfer efficiency depicted
as a function of oxygen flow rate to the diffusers under test.   The actual
data points shown represent the mean values of numerous determinations made
over the course of each test period.  The dashed boxes surrounding each data
point give an indication, horizontally, of the degree of accuracy estimated
for oxygen flow measurements and, vertically,  of the standard deviation of
the individual transfer efficiency measurements contributing to the mean.

Measured oxygen transfer efficiencies were consistently in  excess of 96 per-
cent at gas flow rates at or below design flow for the diffusers.  Even at
gas flows more than 25 percent higher than design, transfer efficiencies ex-
ceeded 92 percent with the exception of efficiencies measured downstream of
RAD 7.  This RAD was equipped with an experimental diffusion medium for eval-
uation purposes, a medium incapable of producing as fine an oxygen bubble as
the other RAD's in the system.

The data from three of the test locations shown in Figure 16 are not shown
in Figure 17.  Low transfer efficiencies were  found at the  dome locations up-
stream of RAD 6, downstream of RAD 12, and upstream of RAD  13.   The poor per-
formance at RAD 6 was traced to leaks in RAD's 5 and 6, both repaired prior
to acquiring data shown for the test downstream of RAD 6.   After completion
of the off-gas testing, RAD 12 was also found  to be leaking, and this was be-
lieved responsible for the poor transfer efficiencies measured  at both RAD's
12 and 13.   The leaks were traced to a process problem in the manufacture of
the diffuser tile assemblies, and this problem has since been corrected.

                                     41

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RAD 13-
RAD 12-
RAD 11-
RAD 10-
RAD 9
RAD 8-
RAD 7
RAD 5
RAD 3
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                         42

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                                 SECTION 10

                              SOLIDS PRODUCTION
Oxygen system solids accumulation,  expressed as  a  function  of both  BOD re-
moved (BODp) and BOD applied (BODA),  is summarized in Table 5.   BODA data
have been presented along with the  more conventional  BODR relationship be-
cause the latter results in misleading interpretations under sludge bulking
conditions, where effluent BOD does not reflect  mixed liquor basin  perfor-
mance.  Both gross and net solids accumulation values are presented, with
the net figure discounting influent solids to give an approximation of so-
lids accumulation resulting from BOD oxidation.  The  low sludge yields shown
for the first two periods of Phase  II can be attributed to  the relatively
long SRT of 9 to 10 days (based on  total  system  inventory)  maintained during
these periods, as compared to a 3-to  6-day SRT for the balance of the demon-
stration.

Table 6 shows a comparison of solids  accumulation  data between the  oxygen
system and Metro's diffused air system.  As seen in the gross solids accumu-
lation figures, the air system exhibited an overall solids  accumulation of
0.99 kg SS/kg BODR, as compared to  1.12 kg SS/kg BODR for the oxygen system,
at comparable SRT's.  Although these figures appear to indicate that sludge
production in the air system was lower than in the oxygen system, they do
not take into account differences in  influent solids  concentrations.  The
influent BOD concentrations were virtually identical  for the two systems dur-
ing the course of the demonstration,  but the oxygen system  influent SS concen-
tration was significantly higher than that of the  air system much of the time.
Through the second operating period of Phase II, the  concentration  of SS in
the influent to the oxygen system was equivalent to that of the air system.
However, the startup of the South Complex treatment facility in November 1976
and the resultant flow reduction to the North Complex produced an uneven dis-
tribution of solids in the North Complex secondary influent channel.  From
the third operating period of Phase II through the remainder of the demonstra-
tion, the oxygen system influent averaged 29 percent  higher in SS concentra-
tion than the air system influent.   This is accounted for in the net solids
accumulation figures in Table 6, which show virtually equivalent overall
sludge production for the two systems.
                                     44

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-------
                                  SECTION 11

                              OXYGEN CONSUMPTION
Oxygen consumption as a function of several  parameters is presented in
Table 7.  This discussion focuses on the relationship between oxygen sup-
plied and BODR, but is generally applicable  to the other relationships
presented as well.  The underlined data, with a mass weighted average of
1.23 kg 02/kg BODR, is considered representative of system performance
under normal operating conditions.  The relatively high oxygen consumption
experienced in the second period of Phase I  was attributed to malfunctions
of the dissolved oxygen sensing system which caused excess oxygen to be
supplied to the basin.  Poor BOD removal resulting from sludge bulking
produced the high consumption figures shown  for the third operating period
of Phase I and the first operating period of Phase III.  Evidence of this
can be seen in the disparity between BODA and BODR figures for these two
periods.  Phase II was characterized by both high SRT's and long mixed
liquor basin detention times, a combination  favoring endogenous respira-
tion and requiring additional oxygen.  Leaking diffusers (see Section 9,
Oxygen Transfer Efficiency)  were responsible for the anomalous oxygen con-
sumption values shown for the last two operating periods of the demonstra-
tion.
                                     47

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-------
                                 SECTION  12

                              POWER  REQUIREMENTS


 Power requirements  for  operation of the FMC 02 system are shown in Table 8,
 with  the  air  system data, where available, shown for comparison.  It should
 be emphasized that  actual oxygen generation power requirements for the oxy-
 gen system were  not available, as all of  the oxygen used was purchased from
 an outside vendor.   The oxygen generation power requirement data shown in
 the table was derived from  power requirements experienced during March 1978
 in the operation of the cryogenic oxygen  plant serving Metro's South Complex*.
 Power required for  oxygen compression is  shown in the table for installations
 in which  the  cryogenic  plant  output pressure is insufficient for the require-
 ments of  the  open tank  oxygen dissolution system.  A cryogenic plant capable
 of output pressures of  21,100 to 24,600 kgf/m2 (30 to 35 psig) would elimi-
 nate  this power  requirement.

 The overall power requirement differences among the various operating periods
 resulted  from the fact  that the power required for oxygen dissolution was a
 constant, independent of flow rate  and organic loading.  During Phases II and
 III,  with average flow  rates  at 49  percent and BOD loadings at 46 percent of
 design, power requirements  (flow or mass weighted, as appropriate) averaged
 151 kWh/1000  m3  (571 kWh/mil  gal) treated and 1.28 kWh/kg BODR (0.58 kWh/lb
 BODR).  During Phases I  and IV, where flow rates averaged 75 percent and BOD
 loadings  66 percent of  design, power requirements averaged only 111 kWh/1000
 m3 (422 kwh/mil  gal) treated  and 1.13 kWh/kg BODR (0.51 kWh/lb BODR).  In
 Phases V, VI,  and VII,  with flow rates averaging 105 percent and BOD loadings
 92 percent of design, the power required decreased to 109 kWh/1000 m3 (411
 kWh/mil gal)  treated and 0.93 kWh/kg BODR (0.42 kWh/lb BODR).  These latter
 figures would have  been reduced even further, were it not for diffuser leaks
 and resultant excess oxygen consumption (see Section 9, Oxygen Transfer Effi-
 ciency).

 A  comparison  of  FMC 02  system versus air system power requirements, for
 those periods  where the air system  data were available, shows a significant
 power savings  in  favor  of the oxygen system.  Overall averages for the air
* During March 1978,  the cryogenic plant produced  an  average  35.4 metric tons
  OJday (39.0 tons/day) at a power requirement of 392  kWh/metric ton  (356
  kwh/ton).   This figure is a conservative  estimate of  the  power required for
  oxygen generation,  as it represents  the highest  value attained for cryo-
  genic plant operation in the first 4 mo of 1978.

                                     49

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system were 189 kWh/1000 m3 (716 kWh/mil  gal)  treated and 1.52 kWh/kg BODR
(0.69 kWh/lb BODR), while the corresponding averages for the FMC 02 system
were 114 kWh/1000 m3 (431 kWh/mil  gal)  treated and 0.95 kWh/kg BODR (0.43 kWh
/lb BODR).   Based on the air system power requirement, these figures repre-
sent a 40 percent reduction based  on flow and  a 38 percent reduction based
on BODR for the oxygen system.
                                    51

-------
                                  SECTION 13

                             SUPPLEMENTAL TESTING
NITROGEN FORMS, ALKALINITY, AND pH

Nitrogen forms, alkalinity, and pH data are presented in Table 9.   These data
were collected mainly for the purpose of monitoring any nitrification that
might occur during the demonstration.   As the data indicate, nitrification
did not occur to any measurable extent except during July and August of the
first operating phase, when effluent nitrate nitrogen levels averaged 1 to
2 mg/1.  Alkalinity comparisons between the oxygen system and Metro's non-
nitrifying air system revealed no significant variations.   The pH  reduction
from influent to effluent of the oxygen system over the course of  the project
resulted from C02 production as a function of BOD oxidation, rather than from
any reduction in the system alkalinity.

SOLUBLE BOD

Soluble BOD determinations on the oxygen system were run in conjunction with
total BOD analyses on both influent and effluent samples to monitor mixed
liquor performance independent of clarification.  As seen in Figure 18, total
and soluble BOD values for the influent wastewater tracked closely over the
entire course of the demonstration, while effluent total BOD showed signifi-
cant fluctuations only minimally reflected in the soluble BOD.  The high ef-
fluent total BOD values shown were the result of poor clarification, rather
than poor mixed liquor basin performance, and the overall  average  of 4 mg/1
soluble BOD in the effluent indicates efficient biological treatment.

SUSPENDED SOLIDS PROFILE

A suspended solids profile of the mixed liquor basin was run on July 13,
1976, to verify that the mixing provided by the RAD's was sufficient to main-
tain a uniform concentration of suspended solids at varying depths of the ba-
sin.  The data are presented in Figure 19.  With the exception of  location
"A", the suspended solids variation at any depth for a particular  location
did not exceed 7 percent of the mean value for samples taken at that location.
Location "A" was situated directly across the basin from the return sludge
inlet, explaining the disparity in the measured solids levels at that loca-
tion.

DISSOLVED OXYGEN PROFILE

A comprehensive D.O. profile of the mixed liquor basin was run on  December 15,
                                     52

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                                    54

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1976, to verify that aerobic conditions existed throughout the basin under
normal operating conditions.  The data presented in Figure 20 show the D.O.
levels found at various locations in the basin.  At the time of the profile,
the D.O.  set points in the basin ranged from 3 to 5 mg/1.   Although notably
high D.O. levels were recorded at locations "G" and "H", the result of a mis-
calibrated experimental D.O. control sensor, zero D.O.  levels were not found
anywhere in the basin.  The lowest values noted, averaging approximately 0.7
mg/1, were found at location "A", the head end of the basin receiving both
the influent wastewater and return sludge streams.
                                      56

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                                           57

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                                  SECTION 14

                    EQUIPMENT PERFORMANCE AND RELIABILITY


As the first full-scale application of the FMC 02 system, this demonstration
provided an opportunity to evaluate various equipment items used in the open
tank pure oxygen system.   Where practicable, items from more than one supplier
were tested to 'determine their reliability and performance.

ROTATING ACTIVE DIFFUSERS

A malfunctioning automatic epoxy dispenser used in the manufacture of the dif-
fuser tile assemblies produced an epoxy mix that softened upon prolonged expo-
sure to water.  This resulted in leaks around the diffuser tile (2 percent of
all tile installed) and, in some cases, actual displacement of tile sections
from their holders (0.5 percent of all tile installed).  The manufacturing
process was subsequently amended, and 30 diffusers in operation at the Engle-
wood-Littleton Wastewater Treatment Plant in Englewood, Colorado, have exper-
ienced no leaks in 15 mo of continuous operation.

ROTATING SEALS

The rotating seals used to connect the oxygen supply lines to the diffuser
shafts were manufactured by Deublin Company.  Failure of the seals caused by
problems in material compatibility necessitated the replacement of all the
seals with modified units prior to the completion of the demonstration.  The
original units used Buna-N "0" rings which tended to swell in the pure oxy-
gen environment.  In addition, the graphite-to-tool steel rotating surface
used was not durable enough for the pure oxygen exposure, the graphite deter-
iorating into a lubricant that opened a leak path.  The final configuration
replaced the Buna-N "0" ring with a Viton seal, and changed the rotating sur-
faces to provide a copper-impregnated teflon surface to rotate against the
tool steel.  No failures occurred with the modified seals, and 30 of these
seals have been in use at the Englewood-Littleton plant for a period of 15
mo without failure.

GEAR DRIVE UNITS

Five different gear drive units were employed to drive the RAD's used in the
demonstration.  Evaluation of these units included assessments of maintenance
requirements, overall reliability, and measured horsepower.  Units from three
manufacturers (Chemineer, ProQuip and Morse Chain) were installed for the en-
tire course of the demonstration, with an FMC unit evaluated for 13 mo and a
U.S. Motors unit evaluated for only 1% mo.  Of all the units tested, only the


                                     58

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Morse Chain drive required no lubrication or oil change during the course
of the demonstration; it also demonstrated superior overall reliability.  The
ProQuip drive suffered only a minor oil leak around one of the bearings, a
problem which was readily corrected.  The FMC drive, located in an area sub-
ject to considerable splashing from the influent sewage pumps, experienced a.
lip seal failure at the top bearing resulting from the abrasive materials in
the influent.  This failure could have been avoided through the use of a
double lip seal to protect against the abnormal environment.  The Chemineer
drives had problems attributed to an undersizing of the output shaft bearings
in the gear box.  Near the end of the demonstration, these units were modified
on site by replacing the upper drive bearings to increase the load carrying
capacity of the drives.  Thirty Chemineer units with the larger bearings are
presently operating at the Englewood-Littleton plant, and after 15 mo of con-
tinuous operation have experienced no failures.

On two occasions, measurements were made of the power requirements for each of
the installed drives to determine actual draw horsepower.  Since not all drive
units were running at the same rpm, a correction factor was applied to convert
the measured horsepower for all units to 82.6 rpm*.  Table 10 summarizes the
information obtained for the drive units used during the demonstration.

                 TABLE 10.  GEAR DRIVE POWER REQUIREMENTS
On ve
Location
1
2
2
3
4
5
6
7
8
9
10
11
12
13
Manufacturer
Chemineer
FMC
U.S. Motors
Chemineer
Chemineer
Chemineer
Chemineer
Chemineer
Chemineer
Chemineer
Chemineer
Chemineer
ProQuip
Morse Chain
rpm
85.5
82.6
84.0
85.5
85.5
85.5
85.5
85.5
85.5
85.5
85.5
85.5
84.4
74.0
Correction
Factor
to 82.6 rpm
0.9066
1 . 0000
0.9534
0.9066
0.9066
0.9066
0.9066
0.9066
0.9066
0.9066
0.9066
0.9066
0.9406
1 . 3665
Measured
hp°
8.06
6.84
+
7.94
7.80
7.90
7.94
7.98
7.80
8.02
7.55
7.83
6.84
7.54
Corrected
hp°
7.31
6.84
+
7.20
7.07
7.16
7.20
7.24
7.07
7.27
6.84
7.09
6.44
10.30
        • 1 hp - 0.746 kW
        + hot available
* Arbitrarily standardized at the rpm of the FMC drive.
                                     59

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DISSOLVED OXYGEN SENSORS

Five D.O. sensors supplied by different manufacturers were evaluated during
the demonstration.   Four were polarographic types employing a teflon membrane
and electrolyte in the sensor element.   Of these, three were equipped with
mechanical agitators to provide the mixed liquor velocity required for accu-
rate measurement and cleansing of the membrane.

It was apparent in mid-July 1976 that the polarographic sensors were causing
operational problems.   Agitator failure caused by debris clogging the mecha-
nisms resulted in membrane fouling.   This caused the sensors to show lower
D.O. levels than were actually present in the basin and resulted in excess
oxygen usage and high basin D.O. levels.  The problem was corrected by an
FMC modification using an air-lift mechanism to induce a mixed liquor stream
past the membrane face in lieu of the mechanical agitator previously used.
This modification decreased the maintenance requirements considerably and in-
creased the reliability of the sensors.  Of the polarographic sensors used,
one unit, manufactured by Weston and Stack, was judged superior to the others
in this demonstration on the basis of large membrane surface exposure, suffi-
cient reservoir of electrolyte, and adaptability to the air-lift mechanism
used in the modified configuration.

The fifth sensor tested was a unit using bi-metallic surfaces to produce a
current flow dependent upon the D.O. level, with an abrasive rotating arm
used to continually clean the active surfaces.  The principal advantage of
this unit was the elimination of the membrane and electrolyte, the most com-
mon maintenance items of polarographic sensors.   The performance of the unit,
however, was not sufficiently good to recommend it in future applications.
Metal from the sensor clogged the abrasive surface of the cleaning bar, ren-
dering it ineffective.  This allowed deposits to form on the bi-metallic sur-
faces and resulted in erroneous readings.  Two sensor assemblies with diffe-
rent metals were used, but neither provided the reliability needed.
                                     60

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                                  REFERENCES
 1.  Rakness, K.R.  Open Tank Oxygen Activated Sludge Wastewater Treatment.
     EPA Project No. S801790, U.S.  Environmental  Protection Agency,  Cincin-
     nati, Ohio, Publication Pending.

 2.  Cohen, D.B. and D.G. Fullerton.  Aerobic Stabilization of Waste Activated
     Sludge - An Experimental Investigation.   EPA-600/2-75-035, U.S. Environ-
     mental Protection Agency, Cincinnati,  Ohio,  1975.   175 pp.

 3.  Sezgin, M., D.  Jenkins, and D.S. Parker.  A  Unified Theory of Filamentous
     Activated Sludge Bulking.  J.  Water Pollution Control  Federation,  50(2):
     362-381, 1978.

 4.  Standard Methods for the Examination of  Water and  Wastewater.   14th  Ed.,
     American Public Health Association, Washington,  D.C.,  1976.   1193  pp.

 5.  Methods for Chemical Analysis  of Water and Wastes.   EPA-625/6-74-003a,
     U.S.  Environmental  Protection  Agency,  Cincinnati,  Ohio,  1974.   298 pp.

 6.  West, A.W.   Operational Control Procedures for the Activated Sludge  Pro-
     cess.  Part II, Control Tests.   EPA-330/9-74-OOOb,  U.S.  Environmental
     Protection  Agency,  Cincinnati,  Ohio, 1973.  22 pp.

 7.  Ryder, R.A.   Dissolved Oxygen  Control  of Activated Sludge Aeration.  Wa-
     ter Research, 6:441-445, 1972.

 8.  Rensink, J.H.  New Approach to  Preventing Bulking  Sludge.   J. Water  Pollu-
     tion  Control  Federation, 46(8):1888-1894, 1974.

 9.  Pipes, W.O.   Bulking of Activated Sludge. Adv.  Appl.  Microbiol.,  9:185-
     234,  1967.

10.  Nash, N., P.O.  Krasnoff, W.B.  Pressman,  and  R.C. Brenner.   Oxygen  Aera-
     tion  at Newtown Creek, March 1977, J.  Water  Pollution  Control Federation,
     49(3):388-400,  1977.
                                      61

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                                 APPENDIX A

                            DAILY OPERATING DATA
Appendix A is a computerized daily operating record of the demonstration
project and shows those analyses used for process  control  and  as  indicators
of process performance.  The data are grouped by calendar  months,  rather
than by phases and periods as in the body of this  report.   Due to  altera-
tions in the computer program necessitated by dual  clarifier operation  be-
gun in March 1977, two sets of data sheets are shown for this  month.

Entries of "-1" in the data tables indicate the absence of data,  due  either
to sampler malfunction or personnel error.  Data have been edited  only  where
necessary to correct for the miscalibration of metering devices.

Caution should be observed in interpreting average results shown  in the
tables.  The averages given are simple numeric means of the tabulated daily
data, and these may not equate with overall performance for certain calcu-
lated quantities.  As an example, consider 2 day's data for calculating
Ib Oz/lb BODR:


           Day 1:  10,000 Ib 02/5,000 Ib BODR  =  2 Ib 02/lb BODR

           Day 2:  10,000 Ib 02/10,000 Ib BODR =  1 Ib 02/lb BODR


The average of the above values on the right side of the equations would be
1.5 Ib 02/lb BODo, while on an overall  consumption basis,  the  average value
would be 20,000 Ib 02/15,000 Ib BODR  =  1.33 Ib 02/lb BODR.
The trade name MAROX is used throughout Appendices A and B to denote the
open tank pure oxygen activated sludge system discussed in this report.
                                     62

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10/18/77 METROPOLITAN DENVER SEWAGE DISPOSAL DISTRICT NO. 1 PERIOD: APRIL 1977
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18/18/77 METROPOLIAN DENVER SEWAGE DISPOSAL DISTRICT NO. 1 PERIOD: JUNE 1977
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IB/13/77 METROPOLITAN DENVER SEWAGE DISPOSAL DISTRICT NO. 1 PERIOD: JUNE 1977
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10/18/77 METROPOLITAN DENVER SEWAGE DISPOSAL DISTRICT NO. 1 PERIOD: AUGUST 1977
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                                 APPENDIX B

           FILAMENTOUS INVESTIGATIONS:  REPORTS OF DR. W. 0. PIPES
Appendix B is a collection of correspondence from Dr. Wesley 0. Pipes to the
FMC Corporation concerning the investigation and attempts at identification
and control of filamentous organisms in the oxygen system activated sludge.
                                     95

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                         WESUEY O. PIPES. PH.D.
                            S7 8HADY HILL. ROAD
                         MEDIA. PENNSYLVANIA 1&O63

                               
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                                  - 2 -
              from the Unox system does contain many actinomycete colonies.

          2.  The Marox system mixed liquor contains two types of filamen-
              tous microorganisms.  One. type appears as a series of rod-
              shaped cells about 1.5 um in diameter.  It was present in
              the Marox mixed liquor during May and June 1976 and is still
              present.  The other type is more slender and appears as a
              continuous filament.

          3.  Both types are also present in the air system mixed liquor.

          4.  Both types are also present in the influent,  Actinomycete
              colonies were also seen in the influent, but they were
              judged to be derived from the filtrate from the. Unox sludge.

          5.  The activated sludges in both the Marox and air systems appear
              to be poorly flocculated.

     I prepared streak plates on corn meal agar and glucose-peptone-yeast
extract agar of the secondary influent, air mixed liquor., and Marox mixed
liquor.  I also brought back samples of these materials for further examin-
ation.  My laboratory results, so far, are as follows:

          1.  Filamentous bacteria did not develop on the streak plates.
              However, I have the filamentous bacteria growing in a liquid
              enrichment culture.  I may be able to Isolate them in the
              next few weeks.

          2.  The streak plates did develop unusually large numbers of
              fungi.   The dominant types are those which produce arthrospores
              (Geotrichun,  Oidiodendron, and Trtchosporon).  I do have
              these organisms in pure culture.

          3.  The arthrosporic fungi could give the appearance of chains of
              rod-shaped cells in liquid culture; thus, these fungi could
              account for the filamentous organisms which have been present
              in the mixed luqour since last May.

          4.  The arthrosporic fungi are also present in the secondary
              influent.

     I have encountered arthrosporic fungi as nuisance organisms in activated
sludge twice before.   They are extremely difficult to get rid of, but the
activated sludge system can be operated to give satisfactory performance
even when they are present.  The other filamentous organism may be even more
of a problem, but I don't want to speculate further until I can find out
more about it.

     I recommend that we undertake a program to accomplish the following
objectives:

          1.  Operate the system to give satisfactory performance in spite
              of the high SVI and in spite of the poor flocculation.
                                      97

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                                   - 3 -
          2.  Determine If the same problem exists in the air system as in
              the Marox system.

          3.  Determine if the secondary influent is the primary source of
              filamentous organisms.

          4.  Find a technique for improving the flocculation of the activated
              sludge.

          5.  Find a method of reducing the SVI.

     The first thing we need is a method of measuring SVI which gives repro-
ducible results and which gives an SVI value independent of the mixed liquor
suspended solids concentration.  I recommend using a one liter cylinder with
a stirrer operated at one rpm or less.  1 also recommend that you acquire
equipment so that four settled volume tests can be run simultaneously and
that SVI versus suspended solids concentration curves be developed for both
the Marox and air sludges.  I discussed this test procedure with Dr. Rise
and Mr. Parker vhen T. was out there last Monday.  If it can be shown that
the SVI versus suspended solids concentration curves are the same for both
th& Marox and air systems, this would go a long way toward demonstrating
that the problems are the same.  In any case we need to get consistant SVI
values to deal with (-he problem in the Marox system.

     We need to have a measure of how well flocculated the sludges are.  The
only reasonable measure of flocculation that anyone has come up with so far
is the supernatant suspended solids from the settled volume test.  However,
mixed liquor suspended solids concentration has an influent on the super-
natent suspended solids.  After the SVI versus suspended solids curve has
been determined, pick a solids concentration (about 3000 mg/1) which gives
2 consistant settled volume and use it as a standard solids concentration
for determining both settled volume and supernatent suspended solids.  After
several days of supernatent suspended solids data have been collected plot
these values versus the respective effluent suspended solids.  There should
be a linear proportionality between the two values if the secondary settling
tank is being operated properly.

     In order to stabilize operation of the system I recommend that the
secondary influent be introduced at a constant rate (the large daily fluctu-
ations in the aeration tank suspended solids may be part of the problem).
If it is impossible to obtain a constant influent rate, adjust the return
sludge flow rate in proportion to the influent flow rate.  The mixed liquor
suspended solids should be

                         MLSS =  Q ^ R   (RAS)

     Have your operator make this calculation each day and check it against
the measured MLSS.  It will help him understand your operational objectives.

     I recommend that the return sludge flow rate be made equal to the
influent flow rate (R=Q).  Have the operator calculate a solids balance on
the secondary settling tank each day (pounds of solids in •* pounds of solids
out) and measure the height of the sludge blanket each day.  Once the sludge
                                      98

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                                    - 4 -
blanket is gone and the solids balance works (within 10%) reduce the return
sludge rate slowly.  I recommend operating at R = 0.9 Q for a few days to
see how the system responds, then going to R «= 0.8 Q for a few days, etc.
When the sludge blanket starts to build up again do not reduce R aj^V further.
Try to hold the sludge blanket at least two feet below the overflow'weirs.

     I recommend that you allow the solids to build up in the system and try
to operate between 5000 and 6000 mg/1 in the aeration tank.  This will re-
duce the F/M ratio which should improve flocculation.  It will also increase
the SRT which could encourage the growth of actinoitycetes in your sludge.
Continue the periodic microscopic examination of your sludge.  If the
actinomycetes show up reduce the SRT even if it requires increasing the
F/M ratio.

     I suggest that you send me weekly data summaries for my review.  If
an operating problem arises suddenly, you can call me and I will respond as
best I can on the telephone.

     I believe that we need to isolate and identify the other filamentous
organism from your sludge in order to determine if the air system has the
same problem and if the source of the organism is the'secondary influent.
I will be working with my enrichment cultures for the next couple of weeks
to see what 1 can isolate.  If I am able to isolate the organism, I will
need to get additional samples to demonstrate that it really is the
organism in your system.  If I don't isolate the organism, I will need
additional samples for trying different isolation techniques.

     The arthrosporic fungi need to be investigated further.  There are
techniques tor obtaining reasonably precise counts of these organisms in
wastewater and iii sludge.  However, this would require a significant amount
of laboratory time.  I could get a student here and train him for that type
of work, but, if'the laboratory work were done here, the expense of trans-
porting the samples would be rather large.  It might be more reasonable for
you to get a laboratory technician whom I could train to work out there.

     These recommendations and suggestions should give you a good deal to
think about and I expect that you will have several questions.  I will be
expecting a response from you after you have had time to consider all these
points.  Looking ahead, it occurs to me that Monday, Jan.  31, might be a
suitable date for me to make another visit to Denver so that we could
review the progress and I could obtain additional samples.

                                      Sincerely,
                                      V. 0. Pipes
                                      Beta Professor of Ecology
                                      Department of Biological Sciences
WOP/sls
                                     99

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                         WEBUEY O. PIPES. PH.D.-

                           »7 SHADY HILL. ROAD

                         MEDIA, PENNSYLVANIA IOOO3


                              (»IB) l_O •-**«•
                                                   February 1, 1977
Mr. Richard B. Weber
3999 South Kariposa Street
Englewood, Colorado  80110

Dear Mr. Weber:

    Enclosed is ray report on examination of the samples which were sent
to me during January.  The fungus counts in the system are high but
apparently not high enough to indicate that fungi are a major part of
the problem.  The filamentous bacteria grow very slowly or not at all.
in the enrichment cultures T have tried so far.  It'appears that they
will be difficult to isolate and identify them but 1 believe that we
should continue to try in order to show that the same problems exist
in both the air and Marox systems and to devise a ready-made solution
in case this probleia ever occurs in another Marox system.

    In thie type of situation it is important to be able to correlate
the laboratory observations with the operating data and with experiments
with sludge samples.  I would like to have the opportunity to analyze
the operating data for January for both the air and Marox systems.
Once your laboratory personnel arc set up to run settling tests at dif-
ferent solids concentrations, as I recommended Jn my letter of Jan." 17, 1977,
and we can get some data to determine the similarity of settling character-
istics of the air and Marox sludges, I will be able to recommend some
laboratory experiments which can be used to test some possible solutions
to the bulking problem.  I have always found it expedient to try out ideas
in laboratory tests before trying them in the plant because a variety of
ideas can be tried out at the same time without running the risk of
upsetting plant performance.

    There are no obvious simple solutions to this problem and it may take
Borne time and effort to find and demonstrate a solution.  It is possible
that we may stumble across a simple solution such as just reducing the
tine the sludge is out of th? aeration tank; however, at this point we
can'/count on that.  We really need operating data foi eoir.e extended period
when the operating conditions .ire not changed frequently and then a care-
ful trial of possible solutions suggested by knowledge of the nature of
the filamentous organisms .".r.d/or by laboratory tests with sludga samples.

                                   Sincerely,


                                    M o. /y'«*
                                   W.  0. Vipes, Ph.D.
                                   Bets Vxoffssor of Ecology
                                   100

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                                                           W. 0. Pipes
                                                           Jan. 31, 1977

                           FMC-DENVER PROJECT

        Examination of Samples for Filamentous Microorganisms

Introduction

    This report covers the examination of samples collected from the
Metro Denver North plant on Jan. 10, Jan. 19, Jan. 25, and Jan. 27, 1977.
There is a demonstration Marox oxygen activated sludge system operating
at this plant.  Both the air and the Marox systems have had operational
difficulties over the past six months apparently due to poorly floccu-
lated activated sludge and a growth of excessive numbers of filamentous
microorganisms which causes high SVI values.  Ths objectives of these
examinations were to determine the indentities of the filamentous micro-
organisms and obtain some clues to the nature of the problem so that po-
tential solutions can be developed.

Samples

    Jan. 10, 1977   Microscopic examination of the air and Marox mixed
liquor samples showed that the floe particles in both systems were loose
and open textured.  Two types of filamentous microorganisms were seen in
both mixed liquor samples.  Some filamentous microorganisms were seen in
the secondary influent sample.

    Both mixed liquor samples and the secondary influent sample were
streaked on glucose-peptone-yeast extract agar (GPY) and on corn meal agar.
Filamentous bacteria did not grow on these plates; however, several fungus
colonies developed.   Many of the fungi produced arthrospores or blasto-
spores or' both.  On the four secondary influent streak plates a total of
15 fungus colonies developed of which 8 produced arthrospores, 3 produced
blastospores, and 2 developed both arthrospores and blastospores.  On the
                                   101

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                                                                         2.
four air mixed liquor streak plates a total of 25 fungus colonies developed
of which 6 produced arthrospores, 12 pTeoduced blastospores and 2 produced
both.  On the four Marox mixed liquor streak plates a total of—19 fungus
colonies developed of which 4 produced arthrospores, A produced blastospores,
and 2 produced both.  Although these fungus counts can not be related to
the volume of liquid which contained them, they are unusually high numbers
of fungus colonies for streak plates.  Arthrosporic fungi can sometimes
look very much like filamentous bacteria when growing in a liquid.  Thus,
it was decided that future samples should be examined for fungus colony
counts.

    The two types of filamentous bacteria from the mixed liquor samples were
observed to be growing on GPY plates which were flooded with 4 ml of mixed
liquor each.  Many other microorganisms were also growing in these cultures.

    Jan. 19, 1977  Samples of air mixed liquor and Marox mixed liquor col-
lected on Jan. 19 were received that evening and examined the following day.
The floe particles were still loose and open textured.  Both types of
filamentous microorganisms were still present.  A few short chains of what
could be arthrospores were seen in the Marox mixed liquor but not in the
air system mixed liquor.  Clumps of cells which could be blastospores were
seen in both mixed liquor samples.

    Pour plates of serial dilutions; 0.1, 0.01, 0.001, and 0.0001 ml per
plate; were made of the two mixed liquor samples on CPY agar.  Microscopic
counts of floe particles in the agar and of floe particles developing
fungus mycelia were made on random fields after four days of incubation
et 20 C.  The purpose of these counts was to determine the faction of the
floe particles which developed mycelia and thus to test the hypothesis
that most of the floe particles were developing around fungus mycelia.
In the Marox mixed liquor 1.3% of the floe particles developed mycelia and
5j> the air system mixed liquor 0.4% of the floe particles developed mycelia.
From this,, the hypothesis was rejected.

    Total counts of fungus colonies developing on the pour plates were made.
                                    102

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                                                                        3.
In the air system mixed liquor, the fungus colony count was 1500 per ml
of which 500 had^arthrospores and 900 had blastospores.  In the Marox
nixed liquor, the funcus colony count wivs 900 per ml of which 300 had
arthrospores and 600 had blastospores.  Four plates using GPY agar is
not the best method of obtaining fungus colony counts, so any conclusions
about the numbers and role of the fungi in the systems were deferred
until after examination of additional samples.

    Liquid enrichment cultures were made up in GPY broth and lactate-
glycerol broth and intioculatcd with mixed liquor from the Marox and air
systems.  These enrichment cultures were aerated and incubated at 20 C.
Microscopic examination after four days of incubation showed that the
filamentous bacteria were not growing in these cultures.

    Hicroscopic examination of the mixed liquor samples on Jan. 24, after
they had been sitting at room temperature for five days without aeration
showed that the two types of filamentous microorganisms were growing more
than the other sludge, organisms.  The larger organism had formed filaments
up to 300 uro long.  This organism is greater than 1 urn in diameter and
forms a continuous tube, not divided into cells, having occasional dark
inclusions.  The other filamentous organism is less than 1 \im in diameter,
has many dark inclusions, and forms short filaments (about 40 pro long)
sometimes in a rosette formation.  From the observation that these orga-
nisms are growing in the anaerated mixed liquor samples, it was hypothesized
that they are microaerophylic.  The dark inclusions could be sulfur deposits.

    Jan. 25, 1977  Samples of air mixed liquor,.Marox mixed liquor, and
raw sewage collected around noon were received at 7:00 p.m. and examined
that evening.  Three samples of raw sewage were received; labeled Delganey
structure, Gibville Main, and Broadway Relief Main.  The sample from the
Delganey structure is a mixture of sewage from four Interceptors two of
which are the Gibville Main and the Broadway Relief Main.

    Microscopic examination of the mixed liquor showed that both types of
filamentous organisms were still present in both samples.  The Marox mixed
                                    103

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                                                                        4.
liqu-ir appeared to be more poorly flocculated and the air mixed liquor
better flocculated than previous samples.

    Spread plates were made of serial dilutions; 0.1, 0.01, 0.001,  and
0.0001 ml per plate; 'on Cooke's Rose Bengal Agar with chlorotetrocycline.
This medium is the best known for Isolation of fungi from water and waste-
water.  The fungus colony counts at four days of incubation at 20 C are
presented in Table I.

                               TABLE I
           Fungus Colony Counts (per ml) on .Jan. 25  Samples

Sample                                      Counts
             Total         Colonies         Colonies         Other
                           with             with             Fungus
                           Arttvrospores     Blastospores     Colonies
Air ML       2100                              1300            800
Marox ML     1600             400               600            600
Delganey     1000                               800            200
Gibville      300             100               200
Broadway      700             100               400            200

    These counts are somewhat higher than are usually found in raw sewage
and mixed liquor samples.  The question of their significance in the
system is deferred for the discussion below.

    In an attempt to find a suitable enrichment techniques for the filamen-
tous orgeniGir.p seen in the mixed liquor samples, liquid cultures were made
up using 1) sodium acetate, 2) sodium acetate plus sodium sulfide, 3) sodium
acetate plus peptone, and 4) glucose, peptone, and sodium sulfide.  The
cultures were incubated at 20°C and not aerated.  The two types of filamen-
tous micro.organisms grew in all four enrichment media but only in the
cultures with glucose, peptone, and sulfide did they grow more than in the
unenriched, unaerated mixed liquor.
                                      104

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                                                                        5.
    Heavy streaks of mixed liquor were placed on acetate-sulfide agar and
these plates were Incubated in air at 20°C.  The filamentous microorganisms
grew for two days on these plates but other microorganisms prew wore
vigorously and after four days the filaments were breaking up.

    Two hundred ml of sewage was placed in the bottom of a desslcator and
1 gm of dextrose, 1 gm of peptone, and 500 mg of M  SO,  were added to
stimulate the production of H~ S.  Heavy streaks of mixed liquor were
placed on GPY agar and on acetate sulfide agar and these plates were incu-
bated in the dessicator for four days.  The filamentous microorganisms
grew more vigorously on these plates than on the acetate-sulfide plates
Incubated in air.  However, several protozoans developed on these plates
and spread the other bacteria to the extent that the isolation of the
filamentous microorganisms is impossible.

    Jan. 27. 1977  Samples collected in the morning were received at
5:30 p.m. and examined that evening.  The samples were air mixed liquor,
Marox mixed liquor, secondary influent and raw sewage.

    The microscopic examination showed the mixed liquor samples to be
quite similar to those of Jan. 25.  Both types of filamentous microorganisms
were still present.

    Spread plates were made of serial dilutions; 0.1, 0.01, 0.001, and
0.0001 ml per plate; on Cooke's Rose Bengal Agar with chlorotetracycline.
The fungus colony counts at four days of incubation are presented in
Table II.
                                   105

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                               TABLE II
           Fungus Colony Counts (per ml) on Jan.  27  Samples
 Sample                                        Counts
             Total         Colonies           Colonies        Other
                           with               with            Fungus
                           Arthrospores       Blastospores     Colonies

Air ML       4300             400                2700           1200
Marox ML     5200             300                3100           1800
Secondary
 Influent    1200             100                 400            700
Raw
 Sewage       300             100                                200
 Discussion

    'Fungi  The loose, open texture of the floe particles suggested that
 the floe might be fromed by bacterial cells adhering to the outside of
 fungus mycelia.  The counts made on the pour plates of the Jan. 19 samples
 shows that this  is not  the case.  The vast majority of the floe particles
 do  not contain fungi.   Some other explanation must be sought for the poor
 flocculation.

     The usual range for fungus colony counts both on raw sewage and on
 mixed liquor samples is 10 to 100 colonies per ml.  I have previously seen
 mixed liquor samples which had obvious fungus myeella1 mats and in which
 the fungus colony counts were in the range of 10,000 to 100,000 per ml.
 In  those cases the fungi clearly were associated with poor flocculation
 and a high SVI.

     In this case the fungus colony counts in the raw wastewater are in
 the range of 100 to 1,000 per ml and in the mixed liquor samples are in
 the range of 1,000 to 10,000 per ml.  The only count made on the secondary
 influent showed  more fungus colonies than the influent.  Except for the
 samples of Jan.  27 the  majority of the fungi are those which produce
 blastospores.  The blastosporic fungi are commonly called yeast and,
                                    106

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                                                                         7.
although they are not uncommon In sewage, It is a bit unusual to find them
making up over half of the fungi present.

    Whether the fungi are growing in the aeration tank or not is .not clear
from these data.  The fungus colony counts in the mixed liquor are almost
10 times higher than those of the raw sewage but the solids in the mixed
liquor should be about 10 times higher than in the raw sewage.  Although
only one fungus colony count was made on the secondary influent the results
are suggestive of some source of fungus growth within the plant.  There
is no other apparent reason tor a higher fungus count in the secondary
influent than in the raw wastewater.

    At this point, it is apparent that the filamentous microorganisms in
the mixed liquor are not fungi.  Further investigation of fungi in the
activated sludge system does not seem warranted except for investigation
of a possible source of fungi somewhere between the raw sewage and the
secondary influent.

    Bacteria  The two types of filamentous microorganisms in the mixed
liquor are bacteria.  They do not grow on an agar medium with a simple
'substrate and the usual   array of growth factors.  They are not
Sphaerotilus natans. Bacillus cereus, Vitreoscilla, or Cytophaga.  They
do not form true branches; thus, they are not any of the actinomycetes.
They seem to be stimulated by sulfide ion and thus could belong in the
Begglatoa - Thiothrix group.  However, this awaits further confirmation.

    The filamentous organisms appear to be microaerophylic because they
grow more vigorously in unaerated cultures.  Why microaerophylic organisms
should be growing in an oxygen activated sludge system is rather puzzellng.
The only apparent reason is that there must be periods of anaerobic
conditions in the secondary settling tank and the return  sludge lines
where they have an opportunity to grow.

Recommendations

    1.  In seeking a solution to a case of filamentous bulking when

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the causative organisms can not be isolated immediately,  it is
very important to analyze the operating data to determine how
the activated sludge reacts under different conditions.  I
recommend that the operating data for the month of January
for both the Marox and air systems be supplied to me for  my
analysis.

2.  It appears that the sludges in both the air system and the
Marox system are similar.  The tests to demonstrate that  they
do have stellar settling and flocculation characteristics should
be carried out as soon as possible.  Please refer to my letter
of Jan. 17.

3.  The entire flow diagram for the Metro Denver North Plant
should be analyzed to determine if there is a potential source
of fungi between the raw sewage and secondary influent.

A.  From the information gleaned about the filamentous micro-
organisms in the nixed liquor, it appears that one possible
solution to the high sludge volume index could be to reduce
the amount of time that the sludge is held in the secondary
settling tank and the return sludge lines.

5.  The efforts to isolate and identify the filamentous
microorganisms in the sludge should continue.  Identification
of these organisms is essential for demonstrating thut the
problem in the Marox system is the same as in the air  system
and for development of a ready-made solution for the problem if
it ever is encountered In other Marox systems.
                               108

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                                                    v-.l
                                                        torch 16, 1977


Mr. Richard B. Weber
Operations Manager
Havox Diffusion Systems
FMC Corporation
3999 South Marlposa Street
Enplewood, Colorado   80110

Dear Mr. Weber:

     Enclosed Is a report on try exanlnatlon of the samples of March 10, 1977.
It Is claar that the filamentous organisms present now are different from
those present In January.  The air systems are growing an organism tentatively
identified as Sph&erotiluE natans which does not appear to be growing In the
Mevox system.  The fact that Sphaerotilus Is growing in the air eyatta but
not in the parallel Karox system could be quite significant if It continues.

     The Marox mixed liquor contains large numbers of short, Irregularly
bent filaments.  I have had no success In trying to prow this organism,  It
could bo the sane organism which was present in the 1 farox nixed liquor during
June last year if I remember the stained slides from that period properly.
The filaments are ehort enough that they nay not interfer very much with
settling and compaction.
                                    Sincerely,
                                    W. 0. Pipes, Ph.D.
                                    Bet* Professor of Ecology
WOP/fllB
enclosure

tic!  Dr. Ratph His*
                                     109

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                              FMC - DKNVER PROJECT

                        EXAMINATION OF MARCH 10 SAMPLES
     Four samples were received on the evening of March 10, 1977; namely,  Marox
mixed liquor, air mixed liquor from area 2, air mixed liquor from area 4,  and
secondary influent.

Microscopic Exarnination

     The Marox mixed liquor was poorly flocculated with many free bacterial cells
and the floe particles were loose, network-like structures.  Many free swimming
and stalked ciliates were present.  These protozoc are usually associated  with
a well flocculated sludge and probably indicate that the flocculation will
improve.  One filamentous organisra was present in large numbers.  It is greater
than 1 urn in diameter and forms short, irregularly bent filaraents with dark
inclusions.  It is an organism which was not present in any of the samples
examined during January.  No other filamentous organisms.were observed.

     The Marox nixed liquor was reexamined after sitting underated for four days.
The. short irregularly bent filaments were still present but gave no appearance
of having grown.  A much longer, more slender filamentous organism had appeared.
It appeared to be a sheathed bacterium.

     The air mixed liquor from area 2 was somewhat'better flocculated than the
Marox mixed liquor but not well flocculated.  A variety of protozoa were seen
but noue in large numbers.  Two filamentous organisms were seen.  The short,
irregularly bent filaments seen in the llarox mixed liquor were present in  small
numbers.  The dominant filamentous organism was less than 1 vim in diameter and
appeared to be a sheathed bacterium.  Reexamination of the sample after four
days without aeration showed that the longer, more slender, filamentous organism
had grown and many more filaments were present.

     The air mixed liquor from area 4 was better flocculated than the other two
samples.  However, it had many free swimming flagellated organisms which are
usually indicative of poor flocculation and low dissolved oxygen concentration.
Both types of filamentous organisms were present.  After the sample had been
left four days without aeration the longer, more slender filamentous organism
had grown and many more filaments were present.  Shorter filaments of the  raore
slender organism showed motility.

     The secondary influent sample showed both types of organisms present  in
good numbers.  This is probably due to some recirculation of material from the
activated sludge.

Sludge Test

     The lysozyrae - detergent test was performed on all three sludge samples on
March 11, 1977.  The longer, more slender organism is definately a sheathed
bacterium, probably Sphacrotilus natans.  The irregularly bent filaments were
dissolved completely.
                                       110

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                                                                             2.
 Cultures

      Spread  plates were made of serial dilutions  (0.1, 0.01, vnd 0.001 ml per
 plate)  on Cooke's rose bengal agar, GPY agar, AcS agar, and tryptacase soy
 agar  (TSA).   The fungus colony counts were in the same range ac the January
 counts.   It  was not possible to obtain counts of filamentous bacterial colonies
 due to  overgrowth of the plates by fungi and protozoa.

      Streak  pJates were made on GPY, AcS, and TSA media.  The short, irregularly
 bent  fil?ments started to grow on the AcS plates but were overgrown by other
 bacteria  in  four days.  Colonies of the sheathed bacterium were isolated from
 TSA plates.

 Summary

      In terms of operational effect, the most disturbing feature of .the Marox
 mixed liquor is the poor floccvlation.  This tray be a feature of the start-up
 process and  the flocculation could improve greatly.  However, if the floccula-
 tion  does not improve the F:M ratio should be reduced.

      The  sheathed filamentous bacterium in the air mixed liquor is tentatively
 identified as Sphaerotilus natans.  It definately was not present in the samples
 examined  during January.  The fact that it is growing in the air systems but
 not in  the Marox system could be extremely significant.  This needs more
.documentation.

      The  irregularly bent, filamentous organism which dominates the Marox mixed
 liquor  appears to be different from the two organisms which were present in
 January.   It could correspond to one of the filamentous organisms seen on the
 stained slides from last summer.  I have no information as to why it would be
 showing up again at this time.
                                      ni

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Department of Biological Sciences
(215) 895-2624
drexel  university • Philadelphia 19104 • 215-895-2000
                                                     March 24, 1977
Mr. Richard B.  Weber
Operations Manager
Marox Diffusion Systems
FMC Corporation
3999 South Mariposa Street
Englewood, Colorado  80110

Dear Mr. Weber:

    This will complete my report on the examination of  the  samples received
on February 23, 1977.  You may recall that in my report of  March 2, 1977
I mentioned that I had made pour plates with nutrient agar  to obtain actin-
omycete counts but that it would take four weeks for the colonies to develop.

    The Englevood sewage had an actinomycete count of 10 per ml.  Of the
two samples from the Metro Denver North Plant, the air  mixed liquor had a
count of 300 per ml and the Marox Pilot Plant had a count of 3000 per ml.
These counts are- not high enough to indicate an operational problem, .how-
ever, they do indicate the potential for developing an  actinomycete problem.
Keeping the sludge residence time in the activated sludge systems to less
than 12 days should prevent the problem from developing.

                                   Sincerely,
                                   W. 0. Pipes,  Ph.D.
                                   Betz Professor of Ecology
WOP/sls

cc:  Dr.  Ralph E. Rise
                                      112

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Department of Biological Sciences
(215) 895-2624
drexel university • Philadelphia 19104 • 215-395-2000

                                                      July 19,  1977
Mr. Richard B. Weber
Operations Manager
Marox Diffusion Systems
KSC Corporation
3999 South Mariposa Street
Englewood, Colorado  80110

Dear Mr. Weber:

    Enclosed is a report on my examination of the samples which were  sent
to me on June 16, 1977.  The Marox mixed liquor at that time was in better
condition than the air mixed liquor but 1 did not find anything unusual
about the microbiology of either sample.

    I am also enclosing a summary of my findings on all the samples for
the January-June period. The summary describes some culture work which we
did during March and April  and which had not been previously reported to
you.  I believe that the filamentous bacterium which was causing the
problem last winter is an acid-producing, sheathed organism which has not
previously been described.   However, there is another filamentous bacterium
which is still present in both systems and we never have been able to do
any culture work with it.  Thus, I am not able to reach any firm conclusions.
                                  Sincerely,
                                  Wesley 0. Pipes, Ph.D.
                                  Betz Professor of Ecology
WOP/sls
enclosure
cc:  Dr. Ralph E.  Hise
                                    113

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                         FMC - DENVER PROJECT

                       Samples of .June 16, 1977


    On  June 16, samples from the Metro Denver North plant were received.
The samples were from the Marox system basin 11, the air system basin 10,
and the secondary influent flowing into basin 11.  Spread plates of serial
dilutions (0.1, 0.01, 0.001, and 0.0001 ml per plate) were made on Cooke's
Rose Bengal agar, on glucose-peptone-yeast extract (GPY) agar, on acetate-
sulfide (AcS), and on trypticase soy (TS) agar.  Heavy streaks of mixed
liquor samples were made on GPY agar and AcS agar.  All plates were incu-
bated at 20°C.

    An extra sample consisting of algae from the secondary settling tank
was also received.  This sample was examined microscopically and then
streaked on GPY and AcS agar plates.

Microscopic Fxamination

    The Marox mixed liquor sample showed a well flocculated sludge but the
particles were sir^all and stringy .(tassel-like).  Many free swimming and
stalked ciliates were seen indicating a "well-oxidized" sludge.  Only one
type of filamentous organise was seen.  It was apparent as the short,
irregularly bent filament with dark inclusions which is more than one
micrometer in diaoieter and which has been seen in all the mixed liquor
samples from this plant.  It apparently does not interfere with the settling
characteristics of the sludge.

    The mixed liquor from the air system showed a loose textured sludge with
very small, stringy particles.  The sludge was highly filamentous and the
filaments appear to be the same type as seen in the Marox system.  Only a
few ciliated protozoa were seen.

    The secondary influent samples had only a small amount of suspended
material in it.  A few filair-uitous bacteria of the same type seen in the
mixed liquor were present.   .he filaments in the secondary infJuent are
much, much longer than those in the njixed liquor.

    The algap. from the secondary settling tank consisted of very long
filaments of Ulothrix, many green flogellated algae of the genus Euglena,
and many desmids    of the genus Closterium.  These are common types of
algae often found around sewage outfalls.  Ulothrix grows attached to
surfaces and forms a microhabitat which provides conditions suitable for
the other algae.  Many protozoa were also associated with the algne as
were filamentous bacteria of the type seen in the mixed liquor.  A few large
filaments showed numerous dark inclusions and a definate gliding motility.
They are definately Eeggiatoa but they were not found in the mixed liquor
camples.  Streak plates were made on GPY agar and AcS agar in an attempt
to isolate the Beggiatoa.
                                   114

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                                                                         2.
Streak Plates

    The filamentous bacterium seen in the two mixed liquor samples and in
the secondary influent did not grow on any of the streak pistes.  This is
consistant with previous results.  One filamentous bacterium was isolated
from the Marcx mixed liquor.  It was found to be a gram negative spore-
former and its morphology is consistant with that of Bacillus cereus.  It
is clearly not the filamentous organism growing in the sludge.

    The Beggiatoa. from -the sample of algae from the surface of the secondary
settling tank grew slowly on AcS agar.  However, it was not isolated.
    The fungus colony counts on Cooke's Rose Bengal Agar made after four
days of incubation are givaa in Table I.  These counts are quite comparable
with the fungus found on samples obtained during the winter.  They are
somewhat higher than normal for sewaee and mixed liquor samples but apparently
the fungi in this case are not associated with deterioration of the settling
properties of the sludge.

                               TABLE I

            Fungus Colony Counts (per ml) on June 16 Samples

Sample       Total    Colonies         Colonies          Other
                      with             with              Fungus
                      Arthrospores     Blastospores      Colonies


Air ML       3,700       700              200             2,800
Marox ML     2,400     1,200              200             1,000
Secondary
 Influent      300                        100               200
Actinomycete Counts

    Actinomycete counts were made on the TS plates after 28 days of incu-
bation.  The actinomycete count on the secondary influent was 70 per ml,
on the air mixed liquor 580 per ml and on the Marox mixed liquor 1,100 per
ml.  These counts are not high enough to indicate an operating problem.

Summary

    The June 16, 1977 samples showed a well flocculated sludge in the Marox
system but a poorly flocculated, filamentous sludge in the air system.  The
filamentous bacterium in both systems is the short, irregularly branched
organism which has been seen in all samples examined from this plant.
Fungi and actinomycetes are also present but in relatively small numbers.
                                     115

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                         FMC - DENVER PROJECT


                     Summary of Samples Examined

                         January - June 1977
Introduction
    This report summarizes the information obtained about the microbiology
of the air activated sludge and Marox systems at the Metro Denver North
plant for the period January through June 1977.   Both systems have had
operation difficulties from time to time due to  poor flocculation- and a
growth  of excessive numbers of filamentous organisms which cause exces-
sively high SVI values.  The Marox system is a demonstration project
operating in one basin of the activated sludge plant in parallel with the
air system.  A pilot plant Marox system was also operated to provide
additional information for comparison purposes.

Samples

    Samples of mixed liquor from the air activated sludge system and the
Marox system were obtained on January 10, 19, 25, and 27, February 23,
March 10, aiid June 16.  The Marox sample on February 23 was from the
pilot plant.  Secondary influent samples were examined on January 27 and
June 16.  Raw sewage samples were examined on January 25 and January 27.
Kaw Englracod sewage samples were examined on February 23.

Filamentous Bacteria

    One type of filamentous bacterium was seen In all mixed liquor samples.
It is a short, irregularly bent organism with dark inclusions.  It is
between one and two micrometers in diameter and  is not divided into cells.
We had no success attempting to grow this organism in the laboratory dispite
trying several different wet' a and a variety of  cultural conditions.  When
the mixed liquor samples art left unaerated for  several days it grows form-
ing longer filaments.  A lysozyme-detcrgent test failed to reveal the pres-
ence of a sheath and it reacted negatively to a  sulfur deposition test.
Thus, it is neither Sphjaerocilus nor Bepgiatoa.   It is present in the raw
sewage and secondary influent.  Since it was present in samples with good
settling characteristics as well as in samples with poor settling character-
istics it apparently does not form filaments long enough to interfere with
the settling of the sludge.

    A second filamentous bacterium was observed  in both the air and Marox
mixed liquor samples during January and in the air mixed liquor but not
the Marox mixed liquor samples in February and March.  It was not seen in
the June samples.  It is less than one micrometer in diameter and forms
very long, straight filaments.  It gave a negative sulfur deposition test
but a lypozyme-detergent test showed some sheath material.  It would grow
some on GPY agar but died out after about one week.  Good growth was ob-
tained on initial isolation plates by adding calcium carbonate to the
medium.  In a GPY broth it lowered the pH to 3.0 in less than one day and
                                     116

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                                                                         2.
then died off.  It appears to be an acid producing relative of Sphaerotilus.
It also appears to be the filamentous organism responsible for the high SVI
values found in the mixed liquor samples last winter.
    The fungus colony counts on the raw sewage, secondary influent, and
mixed liquor samples were higher than is usual for sewage and activated
sludge.  Also, an unusua!3y high proportion of fungi which produce either
arthrospores or blastospores were found.  Howevei, the fungus counts were
approximately one tenth of the fungus counts I h.ive found in mixed liquor
when it was clear that the' fungi were growing in the system and interfering
with the settling characteristics of the sludge.

Actinomycetes

    Actinoinycete colony counts were in the normal range for sewage and
mixed liquor samples except for the Marox pilot plant sample of February
23.  That sample showed a mixed liquor consisting largely of actinouiycetes.
Otherwise there was no indication that the actinoiaycetes were causing a
continuing problem in either system.

Conclusion

    A variety of different types of filamentous organisns are present in
both activated sludge systems.  Most of the filamentous organisms are
present in the raw sewage and in the secondary influent as we.ll as in the
mixed liquoi".  The funpi may be partially responsible for the poor flcc-
culation observed but are not present in high enough numbers to interfere
with the settling characteristics of the sludge.  Actinomycetes could
cause settling problems if a long sludge residence time were used but
this is not usually the case.  The filamentous bacteria present appear to
be microaerophylic and appear to grow more vigorously in the air system
than in the oxygen system.  The filamentous bacterium which appears to
be the most likely cause of high SVI values 'is an acin-producing, sheathed
organism  which has not been previously described.
                                    117

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                                  TECHNICAL REPORT DATA
                           (Please read Instructions on the reverse before completing)
1. REPORT NO.
  EPA-600/2-79-012
                             2.
                                                          3. RECIPIENT'S ACCESSIOI*NO.
4. TITLE AND SUBTITLE
                                                          5. REPORT DATE
  FULL-SCALE DEMONSTRATION  OF OPEN TANK OXYGEN
  ACTIVATED SLUDGE TREATMENT
               May  1979  (Issing Date)
              6. PERFORMING ORGANIZATION CODE
7. AUTHOR(S)
  Stephen R. Pearlman
  Donald G. Fullerton
                                                          8. PERFORMING ORGANIZATION REPORT NO.
9. PERFORMING ORGANIZATION NAME AND ADDRESS
  Metropolitan Denver  Sewage  Disposal  District No. 1
  6450 York Street
  Denver, Colorado  80229
              10. PROGRAM ELEMENT NO.

               1BC822, SQS#3.  Task D-l/27
              11. CONTRACT/GRANT NO.
                                                            Grant No.  S803910
12. SPONSORING AGENCY NAME AND ADDRESS
  Municipal Environmental  Research Laboratory--Cin.,OH
  Office of Research and  Development
  U.S. Environmental Protection Agency
  Cincinnati, Ohio  45268	
              13. TYPE OF REPORT AND PERIOD COVERED
               Final. June  1976-Sept.  1977
              14. SPONSORING AGENCY CODE

               EPA/600/14
15. SUPPLEMENTARY NOTES
      Project  Officer:   Richard C. Brenner  (513)-684-7657
16. ABSTRACT
    This  report presents an operating  summary of a full-scale demonstration of the FMC
open  tank pure oxygen (FMC 02) activated  sludge system, conducted  at  the facilities of
the Metropolitan Denver Sewage Disposal District No. 1 (Metro) in  Denver, Colorado.
The system was operated over a period of  15  mo at both steady state and diurnal flow
rates  ranging from 22,700 m3/day  (6 mgd)  to  53,000 m3/day (14 mgd), with average F/M
loadings varying between 0.49 and  1.14 kg BOD/day/kg MLVSS and clarifier overflow rates
ranging  from 16.5 to 32.2 mj/day/m2 (406  to  791 gpd/ft2).
    The overall performance of the  system  was dictated in large part by  the quantity of
filamentous organisms in the activated sludge, and the investigation  of these organ-
isms,  with attempts to control or  eliminate  them, was an ongoing activity during much
of the demonstration.
    The system was evaluated as to  oxygen  transfer efficiency and oxygen consumption.
Further, it was compared to the Metro diffused air system running  in  parallel with the
demonstration system on the basis  of  sludge  production and power requirements.   Com-
parison  of sludge settleabilities  was made between these two systems  and a closed tank
pure oxygen system (UNOX) also in  operation  at Metro.
    In  addition to allowing an evaluation  of  the FMC 02 system as a whole, the demon-
stration provided an opportunity to evaluate various component equipment items  as to
their  reliability and performance.	
17.
                               KEY WORDS AND DOCUMENT ANALYSIS
                  DESCRIPTORS
 b.IDENTIFIERS/OPEN ENDED TERMS  C. COSATI Field/Group
  Sewage treatment, *Activated sludge pro-
  cess, *0xygenation, Aeration tanks, Sedi-
  mentation tanks, *Liquid  oxygen,  Upgrading
  *0xygen activated sludge
   system, *Rotating active
   diffuser, *0pen tank,
   Dissolution
13B
18. DISTRIBUTION STATEMENT
  Release to Public
                                              19. SECURITY CLASS (This Report)
                                               Unclassified
                            21. NO. OF PAGES

                               128
 20. SECURITY CLASS (Thispage)
   Unclassified
                                                                        22. PRICE
EPA Form 2220-1 (9-73)
118
                                                                  v LI S GOVERNMENT PRINTING OFFICE 1979-657-060/1640

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