United States .
Environmental Protection
Agency
Office Of Water
(WH-595)
EPA430/W-90-013
September 1990
-EPA
Assessment Of The
Biolac Technology
Printed on Recycled Paper
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United States Environmental Protection Agency
Office of Municipal Pollution Control
ASSESSMENT OF THE BIOLACR TECHNOLOGY
Contract No. 68-C8-0023
September 1990
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ACKNOWLEDGEMENT
The report was prepared by Hydroqual, Inc. in fulfillment of
Contract 68-C8-0023. It was prepared by O. Karl Scheible, Dennis
E. Scannell and Eugene J. Donovan, Jr. of Hydroqual, Inc. Irene
Horner and Wendy Bell, OMPC, Washington, D.C. were Environmental
Protection Agency Project Officers. The assistance provided by
the plant operators and owners, as summarized in the report, is
acknowledged with appreciation. The cooperation and assistance
provided by Mr. Charles R. Morgan of Parkson Corporation was
helpful and appreciated.
NOTICE
This document has been reviewed in accordance with U.S.
Environmental Protection Agency policy and approved for
publication. Mention of trade names or commercial products does
not constitute endorsement or recommendation for use.
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CONTENTS
Section Page
FIGURES iii
TABLES iv
1 INTRODUCTION 1- 1
SCOPE OF WORK 1 - 2
2 SUMMARY AND CONCLUSIONS 2 - 1
3 RECOMMENDATIONS 3- 1
A DESCRIPTION OF THE BIOLAC SYSTEM 4- 1
INTRODUCTION 4- 1
SYSTEM CONFIGURATIONS 4- 2
Biolac-R System 4- 2
Biolac-L System 4- 5
Wave Oxidation Modification 4- 5
OTHER APPLICATIONS OF BIOLAC FLOATING AERATION CHAINS 4-5
UNIT OPERATIONS 4- 7
Aeration System 4- 7
Aeration Chains and Diffuser Assemblies 4-7
Blowers and Air Manifold 4-10
Clarification and Solids Removal 4-10
Integral Clarifier 4-11
Biolac-L Settling Basin 4-11
STATUS OF THE BIOLAC SYSTEM 4-13
Municipal Biolac Treatment Systems 4-13
Unit Operations Associated with the Biolac System 4-18
5 ASSESSMENT OF THE BIOLAC SYSTEM 5 - l
PROCESS DESIGN CONSIDERATIONS 5- 1
BIOLAC SYSTEM TREATMENT PERFORMANCE 5 - 6
EQUIPMENT 5. 8
Aeration System 5- g
Sludge/Solids Removal Systems 5-13
Polishing Basins 5-17
BIOLAC COSTS ' ' 5.17
6 SITE OBSERVATIONS 6- 1
INTRODUCTION ' g. l
LIVINGSTON MANOR WWTP, ROCKLAND, NEW YORK '...'.'.'.'.'.'.'.'.'. 6-1
Livingston Manor STP Photograph Descriptions 6-3
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BAY WWTP 6 - 3
Bay WWTP Photograph Descriptions 6-4
PIGGOT WWTP, PIGGOT, ARKANSAS 6- 5
Piggot WWTP Photograph Descriptions 6- 6
BLYTHEVILLE WEST, NORTH AND SOUTH WWTPS, BLYTHEVILLE,
ARKANSAS 6-7
Blythville WWTPS Photograph Descriptions (North, South
and West Plants) 6- 8
REFERENCES 6 - 9
APPENDIX A - DESCRIPTION OF BIOLAC TREATMENT SYSTEMS
APPENDIX B - PERFORMANCE DATA SUMMARY TABLES FOR SELECTED
BIOLAC PLANTS
ii
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FIGURES
Figure Page
1 TYPICAL BIOLAC-R FLOW DIAGRAM 4- 3
2 WAVE OXIDATION MODIFICATION OF THE BIOLAC-R SYSTEM 4-6
3 BIOLAC AERATION CHAIN DETAIL 4- 8
4 SCHEMATIC INTEGRAL BIOLAC-R SYSTEM CLARIFIER 4-12
5 BIOLAC TREATMENT SYSTEM - U.S. INSTALLATIONS (MUNICIPAL
WWTP'S ONLY) 4-14
6 BIOLAC-R PLANT DESIGN - AERATION BASIN LOADING 5-3
7 BIOLAC-R PLANT DESIGN - DIFFUSERS/AIR FLOW 5-5
8 OPERATING BIOLAC-R PLANTS POWER USAGE 5-7
9 INTEGRAL CLARIFIER RAKE MOTOR AND CONTROL SWITCHES 5-14
10 LIVINGSTON MANOR PHOTOS A AND B 6-4
11 LIVINGSTON MANOR PHOTOS C AND D 6- 5
12 BAY, ARKANSAS PHOTOS A AND B 6- 7
13 BAY, ARKANSAS PHOTOS C AND D 6- 8
14 BAY, ARKANSAS PHOTO E 6- 9
15 BAY, ARKANSAS PHOTO F 6-10
16 PIGGOTT, ARKANSAS PHOTOS A AND B 6-13
17 PIGGOTT, ARKANSAS PHOTOS C AND D 6-14
18 BLYTHEVILLE, ARKANSAS PHOTOS A AND B 6-17
19 BLYTHEVILLE, ARKANSAS PHOTOS C AND D 6-18
20 BLYTHEVILLE, ARKANSAS PHOTOS E AND F 6-19
21 BLYTHEVILLE, ARKANSAS PHOTO G 6-20
iii
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TABLES
Table Page
1 SUMMARY LISTING OF MUNICIPAL WASTEWATER PLANTS WITH BIOLAC 4-15
2 SUMMARY OF UNIT OPERATIONS WITH BIOLAC SYSTEMS (MUNICIPAL
BIOLAC PLANTS 4-19
3 MANUFACTURER'S RECOMMENDED DESIGN CRITERIA FOR BIOLAC R
SYSTEMS IN COMPARISON TO CONVENTIONAL EXTENDED AERATION
SYSTEMS 5. 2
4 SUMMARY OF AVERAGE PERFORMANCE DATA FROM SEVERAL BIOLAC
SYSTEMS 5. 9
5 PROBLEMS IDENTIFIED AT VARIOUS BIOLAC PLANTS 5-10
6 BIOLAC SYSTEM CONSTRUCTION COSTS 5-18
iv
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SECTION 1
INTRODUCTION
The Environmental Protection Agency (EPA) has supported the application of
new technologies to municipal wastewater treatment in order to encourage the
development of better and more efficient treatment technologies. This often
involves support of the full scale application of a technology on a widespread
scale without the benefit of long term field demonstration and evaluation, with
acceptance of the potential risk of O&M and/or process problems due to the lack
of experience.
The Office of Municipal Pollution Control (OMPC) evaluates specific
technologies to determine performance capabilities and to identify weaknesses,
limitations in terms of use, maintenance shortcomings and cost effectiveness.
Where an evaluation addresses a technology with which there have been problems,
they need to be defined in order to correct them or to clearly indicate the
limitation of a technology for further consideration and support. Where
technologies are successful and show beneficial applications, the EPA is
interested in providing current information to encourage their use.
This report addresses the BiolacR Wastewater Treatment System. Biolac,
which stands for BIOLogical Aeration Chains is a registered trademark of the
Parkson Corporation, Fort Lauderdale, Florida manufacturers of the system. It
utilizes oscillating, diffused air aeration chains in extended aeration and
aerated lagoon treatment processes.
The first full scale installation in the United States was at Fincastle,
Virginia in 1986. Little information has been available regarding system
operation and experience, except for an assessment report(l) prepared for the
EPA in 1986 that relied primarily on the manufacturer's literature. With the
startup of several plants since then, an evaluation of the system was
recommended in order to investigate any problems that may have been identified
with the process, and to determine if the technology was appropriate for
application to municipal wastewater treatment.
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Page 1-2
SCOPE OF WORK
The overall objective of this evaluation was to determine the status of
Biolac systems within the United States with regard to equipment
configurations, process design and performance, operation and maintenance
experiences, equipment and process related problems, and problem resolutions.
Based on this evaluation, the USEPA would assess if the technology is
appropriate for continued application to municipal wastewater treatment and
would define system limitations, if any, that may need to be addressed with new
systems.
The scope of work relied on the collection of existing data and contact
with operating plants. Information was received from the EPA, the Regional
offices, the manufacturer and treatment plant operators through telephone
interviews and several site visits. Data regarding the Biolac equipment,
treatment system design parameters, and operating conditions were compiled, and
problems that were identified with the operation, maintenance and process
performance of the systems were defined. Modifications that have been made to
the equipment in existing systems or are planned for new plants were reviewed
with the plant operators and the manufacturer, particularly as they relate to
reported problems.
This report describes the Biolac treatment system and presents information
on the present status of installations. The current approach to the design of
the treatment system and an evaluation of the equipment and associated problems
are included, as well as plant performance and cost information.
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Page 2-1
SECTION 2
SUMMARY AND CONCLUSIONS
The Biolac Treatment System uses the process technology of either extended
aeration or flow-through lagoons for the treatment of wastewaters. The key
component is the aeration device, which is assembled as a floating aeration
chain. A series of diffuser assemblies are suspended from a "chain" of floats
stretched across the basin surface. Located near the basin bottom, the rising
air bubbles from the diffusers cause the aeration chains to oscillate across
the surface. These moving fine bubble diffusers provide sufficient oxygen and
keep the mixed liquor solids in suspension. The Biolac-R configuration
incorporates an integral clarifier and sludge return and the Biolac-L is a
simple flow-through lagoon and polishing basin.
The Biolac System was developed in Europe during the mid 1970s with the
manufacturer reporting over 200 installations worldwide. By late 1989, there
were greater than 50 Biolac systems operating or in the design/construct stage
in the United States. Forty-five of these are municipal facilities, of which
32 are Biolac-R and 10 are Biolac-L configurations (the other three are
modified systems). Most operating plants are the R configuration (19 of 27
operating plants). These also have longer operating histories, with the first
facility going on-line in 1986.
Operating experience is limited because the technology is relatively new to
the United States and most plants have only recently come on-line. The long
term reliability of system components and performance could not be fully
evaluated within the context of this report.
The systems are sized conservatively relative to conventional extended
aeration and flow-through lagoons. Loadings to the Biolac-R extended aeration
system are typically 7 to 8 Ibs BOD/d-1,000 ft^, with an F/M ratio of 0.03 to
0.1 Ibs BOD/lb MLVSS; the hydraulic residence time is typically 24 to 48 hours.
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Page 2-2
The flow-through Biolac-L lagoon systems are designed for a hydraulic residence
time of 6 to 20 days.
Greater than half the plants have design flows between 0.5 and 2.0 mgd.
Only two plants have a design flow greater than 2 mgd (both are 4.0 mgd). The
remaining are less than 0.5 mgd design capacity. Most plants are located in
the South, with 14 of the 27 operating in Arkansas and Alabama.
Operating plants are consistently meeting permit requirements. Of 13
plants for which performance data were available, average effluent BOD ranged
between 5.1 and 20.8 mg/L. , representing removals of 91 to 98 percent. The
TSS effluent levels ranged between 6.7 and 34.8 mg/L, with removals of 86 to 96
percent. Most plants were accomplishing full nitrification.
A major claimed advantage of the systems, low cost operation due to low
power requirements for mixing, appears to be realized based on an average
reported horsepower for aeration of 45 HP/million gallons of basin volume.
This is significantly less than required by conventional fixed aeration
systems. Whereby aeration horsepower in extended aeration systems is generally
set by mixing requirements for fixed aeration systems, the Biolac aeration
system sizing is set by oxygen requirements, resulting in significantly less
power input than conventional systems.
Problems that have been encountered with the Biolac system have related
primarily to equipment materials, installation and maintenance. Various
problems which centered on materials of construction and hardware design
resulted in corrosion failures, excessive wear, and clarifier return sludge
clogging problems. These appear to have been adequately addressed and solved
by replacement, repair, and/or redesign.
The fine bubble diffusers have operated well. Where problems have been
noted, these were limited and generally due to improper installation (clamp
materials and adequate fastening), and clogging/failure of the diffuser sheath.
Proper, routine flexing of the diffusers appears to be an essential maintenance
task to assure the performance and life of the diffusers.
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Page 2-3
Total capital construction costs, based on data (received from the
manufacturer) for 13 plants averaged approximately $1.30/gpd design capacity
with a range of $0.84 to $2.11/gpd for plants greater than 0.5 mgd. This
excluded the cost of land.
Overall, the Biolac system, installed in the Biolac R and L configurations,
is a reliable, effective wastewater treatment process. The aeration chain
system and integral clarifiers are cost effective because of low power and
operation and maintenance requirements, and are appropriate to the application
of extended aeration process technology.
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Page 3-1
SECTION 3
RECOMMENDATIONS
The Biolac Wastewater Treatment system should be considered a viable, cost
effective, alternative extended aeration or flow-through lagoon process for
application to municipal wastewaters.
Application of the Biolac technology should incorporate several elements
that affect its performance and O&M requirements. These include effective
screening of coarse solids, routine flexing of the diffusers, skimming devices
in the integral clarifier (although the need for this may be influenced by the
size of the plant and the acceptable level of operator attention), use of
corrosion resistant materials (coal tar epoxy painted steel or stainless steel)
for appropriate metallic parts that contact the water, sludge withdrawal
systems to minimize the potential for clogging (addressing air lift pipe
sizing, suction line hole sizes and spacing), and effective design of the
blower systems for noise control and air filtration.
Continued evaluation of O&M requirements and experience is recommended.
Current experience is limited because most plants are only recently installed.
Attention should be paid to the long-term operation and the demonstrated unit
life of the Wyss diffusers in the Biolac treatment system applications. The
overall operation and maintenance costs for the system, and winter operational
reliability should be assessed as experience is gained with the systems.
An evaluation of one modified Biolac system, the wave oxidation
modification for biological nutrient removal, is recommended. The apparent low
power requirements for the system suggests that it may be a viable alternative
nitrogen removal system. Particular attention should be paid to system control
and process stability.
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Page 4-1
SECTION 4
DESCRIPTION OF THE BIOLAC SYSTEM
INTRODUCTION
Biolac stands for Biological Aeration Chain systems. Manufactured by the
Parkson Corporation of Fort Lauderdale, Florida, the system utilizes a moving
fine bubble aeration device and earthen basin construction, in the application
of low loaded extended aeration and aerated lagoon process technologies. There
are more than 200 systems reported in operation, primarily in the United States
and Europe.
The basic Biolac process layout consists of a basin or lagoon equipped with
floating aeration chains. A polishing basin following the aeration basin is
optional, but is generally recommended by Parkson when designing a new facility
and assuming land is available. This may reduce operator requirements and will
provide greater process stability, particularly in cases where stringent
effluent limits are imposed. The polishing basin may be aerated, unaerated or
split into aerated and unaerated zones. The process goal is direct discharge
of clarified effluent of secondary quality or better. Nitrification can be
accomplished and a process option is available for nitrification-
denitrification.
The innovative aspects of the Biolac system lie in the approach to aeration
and mixing. The key component is the floating aeration chain. This is a
series of diffuser assemblies that are suspended from a "chain" of floats
stretched across the basin surface. The chains oscillate across the basin
surface, propelled by the rising bubbles from the diffusers; this moves the
diffusers through the liquid, thereby mixing and aerating the wastewater
simultaneously. When the chain moves to full tension in one direction, the
diffuser assemblies swing slightly and cause the chain to move in the opposite
direction, repeating the oscillation cycle. The chains typically move
laterally 8 to 30 feet (for activated sludge applications) under normal
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Page 4-2
operating conditions, mixing the volume of water in the traversed path and
maintaining the mixed liquor solids in suspension. In cases where less mixing
is required (e.g. flow-through lagoons) the chain spacing will be wider, with
greater lateral movement.
The reported advantages of the system lie primarily in the lower energy
requirement, when compared to conventional extended aeration systems, to
maintain mixing. Additionally, the systems are relatively stable due to low
organic loadings and long hydraulic retention times. Long solids retention
times in the extended aeration system will require smaller quantities of well
digested sludge to be handled, simplifying this part of the plant. Low
maintenance is also suggested for the blowers, diffuser assemblies, and
integral clarifier components.
This section presents a description of the system configurations, and the
elements of the unit operations that comprise the system. A discussion of the
status of Biolac facilities in the United States is presented, addressing the
types and size of facilities currently in operation.
SYSTEM CONFIGURATIONS
Alternate configurations of the Biolac system are applied, dependent upon
the site requirements. The Biolac-R system is an extended aeration/activated
sludge process, and the Biolac-L system configuration is an aerated flow-
through lagoon system. A third configuration that has very recently been
developed is known as the Wave Oxidation Modification; it operates under a
modified aeration pattern to achieve anoxic zones for denitrification.
Floating aeration chains have also been installed in existing lagoon systems as
a retrofit, replacing existing fixed aeration equipment.
Biolac-R System
Figure 1 illustrates the typical Biolac-R arrangement. It is an extended
aeration activated sludge process, generally designed more conservatively than
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Influent
WAS
(Optional)
1
Sludge
Pond
Polishing
Basin (Optional)
Flow
Ifeaaurin
Device
1
Effluent
Aerated Unaerated
FIGURE 1. TYPICAL BIOLAC-R FLOW DIAGRAM.
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Page 4-4
a conventional extended aeration system. Preliminary and primary treatment are
not components of the system, although, as will be discussed later, effective
screening can contribute to successful operation and lower maintenance of the
Biolac system, as with any secondary treatment plant. It is generally
recommended by the manufacturer.
Lagoon/basin depths range from 8 to 20 feet. Depths on the lower end of
the range are generally designed in cases where deep basin construction is
impractical for hydraulic, geologic, or cost reasons. Depths on the higher end
of the range are typically used, since oxygen transfer efficiency by fine
bubble aeration is greater with the increased diffuser submergence. Basin side
slopes are engineered based upon soils and construction considerations. For
the Biolac-R basin, in which high mixed liquor solids are maintained, sidewall
slopes in the order of 1.5 to 1 (horizontal to vertical) are optimum to
minimize the required mixing energy.
Clarification and sludge return are provided to maintain appropriate mixed
liquor solids levels. Integral clarifiers are used in most systems, although
existing external clarifiers may be used with older systems where lagoons were
retrofitted with the Biolac aeration systems. A waste sludge pond is also
provided with the Biolac-R system; this is generally small because of the
limited sludge production in these low loaded systems. Digesters, or other
sludge conditioning processes, would generally not be needed due to the
stability of the waste sludge.
A polishing basin is optional, but would be located after the aeration
basin. Although not required, it is recommended by the manufacturer for
additional stability affecting effluent polishing and additional solids
settling. This is particularly the case when there is little operator
attention, restrictive effluent standards, and/or high hydraulic variability
that may influence the integral clarifier performance. The polishing basin is
usually divided by a floating curtain wall, with aeration in the first section
and quiescent settling in the second section.
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Biolac-L System
The Biolac-L system operates as an aerated flow-through lagoon. Its
configuration is as shown on Figure 1, except that it does not have
clarification and sludge return, and a waste sludge pond is not needed. A
polishing basin is required for the Biolac-L, with two to four days HRT (based
on average flow) and storage capacity for sludge. As with the Biolac-R system,
the polishing basin can be divided into aerated and unaerated sections.
Wave Oxidation Modification
The Wave Oxidation Modification is a combined carbon oxidation,
nitrification-denitrification process. The process employs a Biolac-R system
operated at low (0.5 mg/L or less) dissolved oxygen levels (0.5 mg/L or less
through the entire basin) and automatic control of each aeration chain's air
flow. Air is throttled back to progressively alternating groups of aeration
chains. This sets up a situation in which several oxic and anoxic zones
alternate in the aeration basin as illustrated on Figure 2. After a period of
time (approximately 15 minutes), the air flow is redistributed and the low air
flow chains receive high air flow, maintaining the mixing requirement for the
mixed liquor solids. A dynamic moving "wave" of alternating oxic and anoxic
zones is formed.
The Wave Oxidation Modification has been employed in more than a half dozen
wastewater treatment facilities in Europe. There is one plant operating in the
United States, located in Decatur, Arkansas. It handles a combined domestic
and poultry waste high in organic nitrogen. The plant has been operating since
mid 1989 and has reported good performance.
OTHER APPLICATIONS OF BIOLAC FLOATING AERATION CHAINS
The Biolac floating aeration chains have also been used outside the
application of a specifically designed R or L system, primarily in retrofitting
existing aeration systems. In Ellsworth, Kansas, for example, floating chains
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Influent
TIME: t = 0 minutes
Ianoxici oxic lanoxic! oxic Ianoxici
Effluent
c
Influent
HAS
TIME: t - 15 minutes
\
WAS
Effluent
1 oxic Ianoxici oxic ianoxici oxic 1
FIGURE 2. WAVE OXIDATION MODIFICATION OF THE BIOLAC-R SYSTEM.
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Page 4-7
have been used in an aeration basin prior to stabilization pond treatment.
Aeration chains have also been retrofitted to an existing aerated lagoon
treatment facility in Excelsior Springs, Missouri, where the aerated lagoon is
followed by an overland flow treatment system. The Biolac aeration chains have
been in operation in a previously existing plant at Durant, Oklahoma for over a
year and a half; the aeration chains replaced the fixed aeration equipment in
the first one-third section of two basins operated in parallel. A polishing
basin with aeration chains was also added to the system. These changes allowed
this plant to meet discharge permit limits. Several Biolac equipped aeration
basins are currently being planned to provide nitrification of a trickling
filter plant effluent at the 55 mgd wastewater plant in Witchita, Kansas.
UNIT OPERATIONS
The major components of the Biolac systems are the aeration equipment and
the clarification/solids handling elements. The following discussions present
a description of these unit operations.
Aeration System
The aeration system consists of the floating aeration chains and diffuser
assemblies and the blowers and air piping manifold.
Aeration Chains and Diffuser Assemblies
The heart of the Biolac system is the floating aeration chain assembly. A
schematic of this assembly is shown on Figure 3. A restraining chain connects
the end floats of the aeration chain with a hook to an anchor post mounted on
the basin bank. Tension adjustment is made by simply increasing or decreasing
the length of chain between the last float and the anchor post. Flexible hose
connects the air header to the air pipe of the float assemblies. The hose is a
multi-layered construction with inner and outer layers made of PVC, with fiber
reinforcement for strength. The outer layer is also impregnated with
plasticizers and U.V. inhibitors.
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Float Assembly
Flexible Hose
Down Coming
Flexible
Air Hose
WyssDiffusers
Counterweight
7///X
PVC
Diffuser Assembly
Concrete skirt/apron—J
FIGURE 3. BIOLAC AERATION CHAIN DETAIL.
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Page 4-9
The float assembly consists of the float, air pipe, two downcoming air
tubes and a fine bubble diffuser/counterweight assembly. The float is a
polyethylene shell filled with closed-cell polyurethane foam. The float is
designed to remain buoyant, even in the event that the entire chain becomes
filled with water. The float shell material contains inhibitors to resist
ultraviolet deterioration.
The air pipe runs through the center and extends out of the ends of each
float. Hose connection points are located at both ends of the float for
joining the air pipe to the downcoming air tubes. The air pipe and connections
for new systems are made of polyethylene and fastened with stainless steel
clamps.
The downcoming air pipes are connected to the diffuser/counterweight
assembly; clearance between the basin bottom and the diffuser centerline is
typically one foot. The diffuser/counterweight assembly is constructed of PVC,
and supports either two, four or six diffusers. The counterweight keeps the
assembly submerged when the diffusers are charged with air.
WyssR Flex-A-TubeR diffusers (manufactured by Parkson) are used, consisting
of a plastic frame, diffuser sheath, retainer pad, backflow check valve and
stainless steel fastening hardware. The diffuser sheath is composed of
modified PVC soft plastic material. When air is introduced to the diffuser,
the flexible sheath expands and thousands of tiny aperatures open, each
releasing a jet of fine bubbles. When air flow to the diffuser is disrupted,
the liquid head collapses the sheath and closes the apertures, preventing
fouling from backflow of solids. When air flow to the diffusers is re-
established, any solids, slime or carbonate build-up on the surface are
displaced by the flexing action of the sheath.
The EPA has studied(2) the WyssR diffusers and classified them as fine
bubble diffusers. However, the manufacturer notes that the air bubbles can
approach medium size when the diffusers are fully charged with air. The
operating range for each diffuser is from 1 to 5 scfm with a typical operating
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Page 4-10
air flow of 3 scfm. Parkson estimates a diffuser life expectancy of five years
under normal conditions with recommended maintenance. Maintenance consists of
weekly to bi-weekly diffuser flexing, a procedure by which the aeration chain
air flow is shut off, the air remaining in the chain is bled off (by opening a
ball relief valve on the air header), and the chain is then recharged with air.
Blowers and Air Manifold
Positive displacement rotary type blowers, designed for continuous service,
are generally supplied. For larger systems, multistage centrifugal machines
may be economical and are considered. In most designs, three blowers, each
capable of handling 50 percent of the air requirement, are provided; thus, two
blowers will be in service at capacity, with one on standby. The blowers are
fitted with an inlet filter and silencer, a discharge silencer, a pressure
relief valve, a discharge check valve, an isolation butterfly valve and a
discharge pressure gauge.
Connection between blower discharge and the aeration chains is through the
air piping manifold. The pipe is normally laid adjacent to the basin, running
perpendicular to the aeration chains. A header pipe off the manifold is
located at the point of connection to each aeration chain. Each header
contains a butterfly valve to isolate each aeration chain on the air piping
manifold for maintenance and a pressure relief valve for depressurization of
the aeration chains. Each header pipe is supported by a concrete thrust block
and a flexible hose is used for header to float connections.
Clarification and Solids Removal
The Biolac-R and Biolac-L systems provide for solids/liquid separation. An
integral clarifier is typically incorporated with the R system, while a
quiescent zone is provided in the polishing basin of the L system.
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Page 4-11
Integral Clarifier
The integral clarifier section is defined by two concrete walls, and a
floating partition wall which separates the clarification zone from the
aeration zone. Figure 4 presents a cross-sectional view of the clarifier. The
rear wall of the aeration basin serves as the back wall, and the two parallel
concrete walls extend out into the basin. The floating partition wall which
separates the aeration basin and the clarification zone, is fixed across the
open end between the two sidewalls.
The partition wall is fixed to the sidewalls to permit flow to enter the
clarifier only under the length of the partition, minimizing short- circuiting.
A flocculating rake, which moves along the length of the clarifier sludge
trough, is provided for sludge concentration and distribution. Sludge is
withdrawn by an air lift pump. Overflow weirs are provided for effluent
discharge to the polishing basin. The weir design loading rate is typically
less than 10,000 gpd/lineal foot of weir length at average flow.
The air lift sludge removal system consists of an air blower (or air from
the main aeration blowers is used), air piping, sludge suction piping, gravity
flow sludge trough, and an RAS/WAS sludge control valve or gate. A positive
displacement blower supplies the required air to lift sludge from the hopper
bottom to a concrete gravity flow sludge trough into a sludge flow control box.
The suction pipe, typically made from PVC, has holes spaced appropriately along
its length for removal of the sludge. Two gravity flow pipes from the sludge
control box convey the settled sludge to either the sludge pond or back to the
head of the plant to be mixed with the plant influent. An electrically
activated and time controlled sludge gate directs sludge flow to either the RAS
or WAS pipe.
Biolac-L Settling Basin
A minimum of one day detention time in the unaerated section of the
polishing basin is typically provided. The volatile solids (about one-half the
-------
Waste
Activated
Sludge
Effluent
Return Activoted Sludge
S
Rear Wall of
Aeration Basin
Floating Partition Wall
for Aeration Basin/Clarification
Zont Separation
Flocculation Rake Mechanism for
Sludge Distribution and Concentration
Clarifier Influent
Sludgt Hopper
Sludge Suction Pipe- PVC pipe located along the length
of the Clarifier Hopper Bottom
FIGURE 4. SCHEMATIC INTEGRAL BIOLAC-R SYSTEM CLARIFIER.
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Page 4-13
total solids) settling in the basin are further degraded by about 40 to 60
percent under anaerobic conditions that develop in the settled sludge zone at
the bottom of the basin. The polishing basin is sized to provide up to one to
two decades of sludge storage within this zone. At the time when it becomes
necessary to remove the sludge, one of various methods can be selected to
remove sludge, including a floating dredge, dewatering and bulldozing, etc.
STATUS OF THE BIOLAC SYSTEM
The Biolac Treatment System was developed in Europe in the mid-1970s; by
1985, there were approximately 100 installations throughout Europe and around
the world. The Biolac system was first introduced to the United States in 1985
with a pilot test at the Miami Conservancy District located in Franklin, Ohio.
The first full-scale floating aeration chain system was started in January 1986
for the treatment of a dairy waste; approximately one month later the first
Biolac domestic wastewater treatment plant was put into service at Fincastle,
Virginia. These two installations, as well as many other early U.S.
installations, were retrofits of existing plants.
Recent Parkson information^) lists approximately 200 Biolac installations
operating in the U.S., Europe and other parts of the world. There were 59
domestic and industrial U.S. installations either on-line, under construction
or in the design phase as of September 1989. Recently (March 1990), Parkson
has reported selling an additional 12 systems for domestic applications and two
for industrial clients. The 59 installations are spread among 20 states, with
most located in the eastern half of the U.S. Figure 5 locates the U.S.
municipal installations.
Municipal Biolac Treatment Systems
A listing of municipal plants is presented in Appendix A. A description of
the system and a discussion of the operations and performance of each plant is
included. This list is based on information compiled from telephone
interviews, site visits, or discussions with the manufacturer. Table 1
-------
• Plants On Line
A Plants In Design
Or Construction Phase
FIGURE 5. BIOLAC TREATMENT SYSTEM - U.S. INSTALLATIONS (MUNICIPAL WWTP'S ONLY)
-------
TABLE 1. SUMMARY LISTING OF MUNICIPAL
WASTEWATER PLANTS WITH BIOLAC
Plant
Alabama (10)
Ardmore
Berry
Camden, North
Cedar Bluff
Clayton
Columbiana
Hanceville
New Brockton
Oxford
Stevenson
Arkansas (7)
Bay
Blytheville, North
Blytheville, West
Blytheville, South
Decatur
Maynard
Piggott
Colorado (2)
Colorado Springs
Monument
Georgia (1)
Quitman
Indiana (4)
Ferdinand
Remington
Rensselaer
Cambridge City
Kansas (3)
Ellsworth
Wellsville
Witchita
Kentucky (3)
Edmonton
Greenville
Morgantown
Minnesota (2)
LeSueur
Wells
Design Flow
(mgd)
0.35
0.15
0.22
0.30
0.40
0.75
0.57
0.18
1.0
0.75
0.15
0.80
1.50
1.40
1.35
0.06
0.60
0.9
1.3
1.3
0.47
0.28
1.2
0.8
0.5
0.18
54.4
0.51
0.75
0.50
0.9
0.55
Plant
Type
R
R
R
R
R
R
R
R
R
R
R
R
R
R
W
R
R
L
L
L
R
R
R
R
L*
L
**
R
R
R
R
L
Status
D/C
0
0
0
0
0
0
0
D/C
0
0
0
0
0
0
D/C
0
0
D/C
D/C
D/C
D/C
D/C
D/C
0
D/C
D/C
0
0
0
D/C
D/C
Startup
March 1990
August 1989
August 1990
April 1990
May 1990
April 1989
March 1989
Summer 1987
June 1990
Summer 1987
March 1989
April 1989
April 1989
April 1989
Summer 1989
February 1990
April 1989
March 1989
July 1990
January 1990
Spring 1990
Spring 1990
Summer 1990
Summer 1990
April 1988
Spring 1990
Summer 1990
April 1989
April 1988
Summer 1988
May 1990
November 1989
-------
TABLE 1. SUMMARY LISTING OF MUNICIPAL
WASTEWATER PLANTS WITH BIOLAC
(Continued)
Plant
Missouri (2)
St. Louis
Excelsior Springs
New York (2)
Livingston Manor
Rock Hill
Ohio (4)
Coalton
Miami Conservancy
Frazeysburg
Lowell
Design Flow
(mgd)
4.0
2.4
0.8
0.22
0.046
4.0
0.18
0.054
Plant
Type
L
+
R
R
R
R
R
R
Status
D/C
0
0
D/C
D/C
0
D/C
0
Startup
November 1989
1985
1986
Fall 1990
Fall 1990
October 1989
Fall 1990
January 1989
Oklahoma (1)
Durant
Oregon (1)
Canby
Virginia (3)
Chase City
Fincastle
Winchester
1.7
1.15
0.6
0.08
0.28
R
L
L
D/C
0
0
April 1988
1986
Fall 1990
1986
1988
Biolac-R
Biolac-L
Biolac-R - Wave Oxidation Modification
Stabilization Ponds
Nitrification of Trickling Filter
+ Pre-aeration
0 Operating
D/C Design Construct
R
L
W
*
**
-------
Page 4-17
presents a summary listing of municipal Biolac wastewater plants, current
through December 1989. A total of 45 plants are listed, of which 42 are R or L
configurations. The first of the three other plants (Decatur, Arkansas) is a
Biolac-R plant with the Wave Oxidation Modification for nitrogen removal. The
second (Excelsior Springs, Missouri), uses the Biolac aeration chains for
preaeration prior to an overland flow wastewater treatment system. The third
(Witchita, Kansas), will use the aeration chains for second stage nitrification
of a trickling filter effluent.
Of the 42 Biolac plants, 10 are L configurations, and 32 use the R
arrangement. Only 5 of the Biolac L systems are currently in operation, with
the earliest startup in April 1988; the remaining are in the design/construct
stage. Thirteen of the 32 R plants are in the design/construct stage. Of the
19 operating plants, most have been brought on-line in the past two years, with
the earliest startup in 1986 (Livingston Manor).
Most plants are relatively small, based on the design flow. This is
summarized as follows for the 42 (operating and in the design/construct phase)
Biolac R and Biolac L plants.
Design Flow
(mgd)
< 0.1
0.1 - 0.5
0.5 - 1.0
1.0 - 2.0
2.0 - 5.0
Number
Biolac R
3
11
12
5
1
of Plants
Biolac L
1
2
3
3
1
As shown, greater than 50 percent of either R (53 percent) or L (60 percent)
plants have design capacities within the range of 0.5 to 2 mgd. Only one of
each has a design flow greater than 2 mgd (both are 4.0 mgd). The remaining
are less than 0.5 mgd design capacity.
Geographically, most plants are located in the south and midwest,
distributed among 14 states. Alabama and Arkansas have 17 of the 45 listed
plants, all of which are Biolac-R configurations. Of the 27 operating plants,
-------
Page 4-18
14 are in Arkansas and Alabama. Six of the remaining 12 are located in
moderate climate states (Kentucky, Oklahoma and Virginia). Six plants are
operational in winter climate conditions (Colorado, Kansas, Missouri, New York
and Ohio), and only three (Livingston Manor, New York; Excelsior Springs,
Missouri; and Ellsworth, Kansas) have experienced more than one winter
operation. Thus severe winter operating experience is limited at this time.
Unit Operations Associated with the Biolac System
A review of the plant descriptions listed in Appendix A indicates the range
of unit operations included in the process trains of Biolac treatment plants.
Parkson recommends influent screening, which is normally included as part of
the Biolac System scope. Grit removal systems are optional and can be included
if a large quantity of grit is anticipated. Both unit operations are shown in
the "typical" system flow schemes (see Figure 1).
A summary of unit operations associated with the Biolac system is presented
in Table 2 (based on municipal plants only). Four plants have no preliminary
treatment, while thirty-eight plants provide some form of pretreatment;
Bar Rack Only 2 piants
Bar Rack/Screening/Grit Removal 1 plant
Bar Rack/Comminution/Grit Removal 2 plants
Bar Rack/Comminution/Grit Removal 1 plant
and Primary Clarification
Screening Only 15 piants
Screening/Comminution 5 plants
Screening/Grit Removal 4 plants
Screening/Primary Clarifiers 2 plants
Comminution/Grit Removal 1 plant
Grit Removal 1 plant
Twenty-seven of the plants have screening, eleven of which are traveling
screens. Nine plants practice some type of comminution/grinding. Ten plants
-------
TABLE 2. SUMMARY OF UNIT OPERATIONS WITH BIOLAC SYSTEMS
(MUNICIPAL BIOLAC PLANTS)
Plant
Ardmore, AL
Berry, AL
Camden, AL
Cedar Bluff, AL
Clayton, AL
Columbians, AL
Hancevllle, AL
New Brockton, AL<1>
Oxford, AL
Stevenson, AL
Bay, AR
Blythevllle, AR-N
Blytheville, AR-W
Blytheville, AR-S
Maynard, AR
Piggott, AR
Colorado Springs, CO
Monument , CO
Quitman, GA
Ferdinand, IN
Remington, IN
Rensselear, IN
Cambridge, IN
Ellsworth, KS
Wellsvllle. KS
Edmonton, KY<2>
Greenville, KY
Morgantown, KY
LeSuer, MN
Hells, MN
St. Louis, MO
Fretreatment
Bar Bar Traveling Static Grit Primary
Type Rack Screen Screen Screen Grinders Chamber Clarlfier None
R X
R X
R X
R X
R X
R X X
R X
R X
R X X X
R X
R X
R XX
R XX
R XX
R X
R X
L X
L X X
L X
R XX
R X X
R X
R X
L X X
L X
R X X
R XX
R X
R X X
L X
L X
Post-Treatment
Clarification
Integral External None Aerated
X X
X
X X
X
X X
X X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X X
X
X
X
X
X X
Pollshin*
Aerated/
Non-Aerated Non-Aerated
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
Mono
X
X
X
X
X
X
X
X
X
Livingston Manor, NY R
Rock Hill, NY* R
Coalton, OH R
Miami, OH R
Frazeysburg, OH* R
Lowell, OH R
-------
TABLE 2. SUMMARY OF UNIT OPERATIONS WITH BIOLAC SYSTEMS
(MUNICIPAL BIOLAC PLANTS)
(Continued)
Plant
Durant, OK
Canby, OR*
Chase City, VA*
Fincastle, VA*
Winchester, VA
Bar Bar Traveling
Type Rack Screen Screen
L X
R
R
L
L X
Pretreatment Post-Treatment
_ Clarification Polishing
Static Grit Primary Aerated/
Screen Grinders Chamber Clarifier None Integral External None Aerated Non-Aerated Non-Aerated
XXX XX
X
X X
d'Wetland treatment follows aeration basin.
discharge to aquaculture pond.
-------
Page 4-21
have grit removal, with two primary clarification plants (these were retrofits
of existing plants).
None of the ten L systems have separate mechanical clarif iers. Two R
plants have external clarification; the remaining have integral clarifiers.
Nine Biolac-R plants do not have polishing lagoons. Of those that do, six use
fully aerated basins, while the remaining polishing basins are split into
aerated and non-aerated sections. When the polishing basin is used, the trend
is to have this aerated/non-aerated configuration with new Biolac-R systems
(with integral clarifiers), unless they are to be followed by a land treatment
process (wetlands, overland flow, etc.).
-------
Page 5-1
SECTION 5
ASSESSMENT OF THE BIOLAC SYSTEM
This section presents an evaluation of the Biolac wastewater treatment
system. The discussion focuses on the process design considerations for the
system based on in-field observations; performance data for selected plants; an
assessment of the system components and related Operation and Maintenance (0
and M); and the costs associated with the installation of the system.
Note that the system is relatively new; earlier discussions indicated that
the majority of facilities have come on-line in only the last one to three
years. As such, there is limited experience, particularly with respect to 0
and M and hardware reliability aspects that are influenced by long-term
operations. This also applies to operating costs, which were not estimated
within the context of this report. The principal focus is on the Biolac-R
configuration since this system is most common and is typically the preferred
system for new installations.
PROCESS DESIGN CONSIDERATIONS
As discussed earlier, the approach to sizing the extended aeration or flow-
through lagoon system is somewhat conservative when compared to conventional
systems. Table 3 compares the design parameters generally found for extended
aeration systems and the Biolac-R process.
The aeration basin for the Biolac-R system is sized to yield an average
Hydraulic Retention Time (HRT) of 24 to 48 hours and a Solids Retention Time
(SRT) of 30 to 70 days. These are greater than conventional design, in
particular with regard to the SRT. Food to microorganisms ratios are low,
ranging between 0.03 and 0.1, somewhat lower than typically used. The
volumetric BOD loading is 6 to 18 Ibs BODs/d- 1,000 ft3, with a typical loading
of 7 to 8 Ibs BOD/d- 1,000 ft3. Figure 6 presents actual design loading data
-------
TABLE 3. MANUFACTURER'S RECOMMENDED DESIGN CRITERIA
FOR BIOLAC-R SYSTEM IN COMPARISON TO CONVENTIONAL
EXTENDED AERATION SYSTEMS
Extended(fl)
Parameter Aeration Biolac-R(k)
Hydraulic Residence 18 to 36 24 to 48
Time (HRT), hours
Solids Retention Time 20 to 30 30 to 70
(SRT), days
F/M, (Ibs BOD5/d-lb MLVSS 0.05 to 0.15 0.03 to 0.1
Volumetric Loading 10 to 25 6 to 18
(Ibs BOD5/d - 1,000 ft3
MLSS (mg/L) 3,000 to 6,000 1,500 to 5,000
Basin Mixing 80 to 150(c) 12 to 15(d)
(HP/MG of Basin Volume)
(a)Reference 3
Reference 4
(c)Mechanical aeration
(d)Manufacturers data for mixing only
-------
n
4.5
4 -
3.5 -
3 -
2.5 -
2 -
1.6 -
I -
0.5 J
0
D
o
DESIGN LOAD
975 #BOD/MG
I 2
(Thou* and*)
BOD LOAD (THOUSAND POUNDS /DAY)
-r
3
FIGURE 6. BIOLAC-R PLANT DESIGN - AERATION BASIN LOADING.
-------
Page 5-4
for 25 Biolac-R plants; the mean design loading was 975 Ibs BOD/d-MG equivalent
to 7.3 Ibs BOD/d - 1,000 ft3. The polishing basin of the R system is typically
sized for an HRT of 12 to 24 hours.
Design sizing for the flow-through lagoon system (Biolac-L) is typically
based on hydraulic residence time. An HRT of 6 to 20 days is used, whereas
conventional design sizing would use a 3 to 10 day HRT. The Biolac-L polishing
basin is typically designed to provide an equivalent loading of 0.5 to 1.8 Ibs
BOD/d - 1,000 ft3, which generally results in an average HRT of one to two
days, and greater than 10 years capacity for sludge.
The Biolac aeration system sizing is based on the assumption that full
nitrification will be accomplished. The manufacturer recommends 1.5 Ibs oxygen
per pound of BOD5 removed and 4.6 Ibs of oxygen per pound of available
nitrogen. The rated transfer capacity for the Wyss diffusers under standard
conditions, in clean water is between 4 and 5 Ibs 02/hp-hr.
At the typical design loading, the air required to satisfy oxygen
requirements is higher than that required for mixing. Thus the aeration system
can be turned down during nightime, weekends, and/or the initial years of
operation at lower loadings, while still maintaining mixing. This provides a
large degree of flexibility and energy savings with this type of system when
compared to conventional fixed aeration equipment.
The total number of diffusers is determined by dividing the required air
flow by the normal design air flow per diffuser. This is typically 2 to 4
scfm/diffuser for the Wyss units. The number of aeration chains, floats per
chain, diffusers/float are then determined for the specific application. A
typical aeration chain spacing of 8 to 30 feet for Biolac-R plants and up to 30
to 50 feet for Biolac-L plants is used, above an unsloped basin bottom.
Parkson recommends keeping all diffusers at the same elevation for the simplest
installation and operation. Figure 7 presents a summary of the actual number
of diffusers used for the design of 25 Biolac-R plants. The mean was 385
diffusers per million gallons basin volume. This is equivalent to an air flow
of 1,350 scfm/MG at 3.5 scfm per diffuser.
-------
4.B
I
n
o
P
3.8 -
3 -
2.8 -
2 -
1.8 -
1 -
0.8 -
O
0.2
D
DIFFUSERS
385 /MG
AIR FLOW
1350 scfm/MG
@ 3.5 scfm/DIFFUSER
D
0.4 0.6 0.6
(Thousand*)
NUMBER OF DIFFUSERS
1.2
1.4
FIGURE 7. BIOLAC-R PLANT DESIGN - DIFFUSERS/AIR FLOW.
-------
Page 5-6
The minimal requirement for mixing and effective solids suspension is
approximately 3 to 4 scfm/1,000 ft^ of basin volume using the Biolac aeration
chains. This is equivalent to approximately 12 to 15 HP/million gallons.
Figure 8 presents data showing actual operating HP at 25 Biolac-R plants. The
mean was approximately 45 HP/MG; note that these plants were typically at 50 to
70 percent of their design loading. This still compares favorably with
conventional fixed aeration systems which require up to 100 HP/MG basin volume.
Thus, whereby aeration HP in extended air systems is generally set by mixing
requirements for fixed aeration systems, the Biolac aeration system sizing is
typically set by oxygen requirements, resulting in significantly less power
input than required for conventional systems.
For the R system, an integral clarifier is normally provided to effect
solids settling, and an optional aerated/unaerated polishing basin can be
provided. The polishing basin is not considered a requirement to achieve
secondary effluent limits, but can provide additional polishing for solids
removal. Clarifier design rise rates (overflow) range between 200 and 800
gpd/ft2, with 400 gpd/ft2 being used most often. For the L system, solids
settling is accomplished in the quiescent settling zone established in the
unaerated section of the polishing basin. The design is typically for a 24
hour detention time in this zone. This is common for the aerated lagoon
process.
BIOLAC SYSTEM TREATMENT PERFORMANCE
Most Biolac plants have been operating a relatively short time and as yet
have not reached design flows or loads. Additionally, many plants are small
and permit sampling requirement are not extensive, thus minimal data has been
collected. The response to a request for data was good; approximately 75
percent of the domestic plants on-line responded with information. In many
instances, however, the data were limited, often representing monthly or
twice/month sampling. Additionally, several plants do not monitor the
influent, and the 24 domestic plants that were on-line, only 9 were on-line
longer than one year.
-------
s
2
*
a
I
4.5
4 -
a.5-
8-
2.5-
2-
U-
1-
0.5-
B
POWER USAGE
45 HP/MG
-i—i—\—i—i—i—i—i—i—i—i—i—i—i—i—i—r-
20 40 60 ft) 100 120 140 ISO IftO
OPDUTINGHP
200
FIGURE 8. OPERATING BIOLAC-R PLANTS-POWER USAGE.
-------
Page 5-8
Performance data summaries for 13 plants are presented in Appendix B. All
but one (Fincastle, Virginia) are R plants. In all cases, and in discussions
with other Biolac plants, the facilities were in full compliance with their
permit requirements. Table 4 summarizes these data, presenting the averages
for the different performance periods at each plant. Note that the initial
months of start-up data were excluded from these averages. The average
effluent BOD ranges from 5.1 to 20.8 mg/L; the average removal (for those
plants for which influent data were available) ranged between 91.1 and 97.9
percent.
The average effluent TSS concentrations ranged between 6.7 and 34.8 mg/L;
the average removal ranged between 86.3 and 95.7 percent. Ammonia levels were
typically less than 7 mg/L in the effluent, except for higher levels in the
Bay, Arkansas and two Blytheville, Arkansas plants. It is suggested that these
were influenced by high incoming ammonia concentrations due to farm
fertilization and high infiltration into the sewer collection system.
EQUIPMENT
Since the initial installations in 1985, design and materials modifications
have been made on a continuing basis, reflecting operating experience at an
increasing number of plants. Problems that were identified related to hardware
components and materials of construction, ineffective maintenance, and
inefficiencies in operation. The following discussions summarize the problems
noted by the operators and present how they have or are being addressed.
Table 5 summarizes the types of problems encountered by the various plants
that were interviewed and/or visited. Plants that reported the problems are
also shown, if possible. Finally, resolution of the problem, if there is one,
is also discussed.
Aeration System
The floating chain system is assembled in the field. Problems were
reported primarily by early Biolac plants, and related to the diffusers,
-------
TABLE *. SUMMARY OF AVERAGE PERFORMANCE DATA FROM SEVERAL BIOLAC SYSTEMS
Plant
Name
Morgantown HWTP
Morgantown , KY
Greenville WHIP
Greenville, KY
Hew Brockton WHIP
New Brockton, AL
Edmonton, WWTP
Edmonton, KY
Fincastle WWTP
Fincastle, VA
Lowell WWTP
Lowell, OH
Hanceville WWTP
Hancevilla, AL
Livlnston Manor HWTP
Rock land, NY
Blythville Heat WWTP
Blytheville, AR
Blrthevlll* North WWTP
Blytheville, AR
Blytheville South WWTP
Blytheville. AR
Bay WWTP
Bay, AR
Plggot WWTP
Flggot, AR
Influent Effluent I
Period of Flow BOD BOD BOD Loading
Performance Type (MOD) X Design (mg/1) (ma/1) Removal (Ibs BOD/dayJ
4/89 to 9/89 R 0.29 58.0 243 12.7 92.3 575
5/88 to 8/89 R 0.40 55.3 178 6.2 96.5 528
6/89 to 8/89 R 0.05 27.8 233 8.7 95.5 111.5
7/89 to 11/89 R 0.2 39.2 203 11.6 91.1 185
9/88 to 8/89 L 0.05 62.5 218 18.6 91.2 86.9
7/89 to 9/89 R 0.11 20*. 186 13.3 91.8 167.0
6/89 to 9/89 R 0.5 87.8 134 9.7 92.0 514.0
6/86 to 8/89 R 0.5 62.5 260 5.1 97.9 1,062.0
7/89 to 10/89 R 0.39 26.0 ND 7.6
4/89 to 10/89 R 0.39 48.8 ND 13.8
4/89 to 10/89 R 0.60 42.8 ND 15.1
6/89 to 9/89 R 0.27 180. ND 10.4
6/89 to 9/89 R 0.35 58.0 ND 20.8
Influent Effluent X Effluen'
TSS TSS TSS NH3-N
(mjt/1) (nut/1) Removal (mg/1)
188 11.7 95.7 0.1
213 12.4 94.7 0.5
257 10.7 94.4 1.9
266 18.4 89.5 3.2
190 21.5 89.7 ND
172.0 26.0 86.3 6.7
97.8 9.0 92.0 0.8
217.0 8.7 95.3 1.9
ND 14.9 - 2.2
ND 26.3 - 26.0
ND 18.1 - 30.9
ND 6.7 - 11.3
ND 34.8 - ND
ND: No data provided
-------
TABLE 5. PROBLEMS IDENTIFIED AT VARIOUS BIOLAC PLANTS
Problem
Hardware/Materials Related
Wear on chain restraining cables
and rake cable
Plants Reporting Problem
Excelsior Springs; Livingston Manor;
Ellsworth; Morgantown
Corrosion of hardware pieces Livingston Manor; Durant; Excelsior
(bolts, clamps, cable, connecting pieces) Springs; New Brockton
Loosening of diffusers, other parts
Livingston Manor; New Brockton
Comments
Chain material changed to stainless
steel or chrome plated steel; replacement
Materials changed from galvanized to
stainless steel; replacement
Diffuser/Aeration System
Diffusers blowing off frame
Diffusers clogging
Reduced diffuser life
Excessive blower noise
Blower Filters
Livingston Manor; Morgantown Installation; replace clips
Livingston Manor; Durant Loosening diffusers; improve clip, increase
flexing maintenance
Livingston Manor; Morgantown; Ellsworth Installation; improves flexing maintenance
Blythville; Bay; Columbians
Blythville
Install in separate buildings; improve
silencer design
Excessive dust; Install screens; frequent
replacement
Clarifiers
Rake motor
Rake limit switches and float overtravel
Ranceville; Hew Brockton; Decatur
Berry; Hanceville; Edmonton;
Morgantown; Lowell
Undersizing and problems relating to float
over travel; replace
Modify/replace switch with Improved design
Sludge Withdrawal
Air lift pump clogging
Lowell; Greenville; Bay
Improve solids removal (screening) upstream;
increase maintenance of lift line; improve
suction line design; increase opening sice
Process Related
Excessive debris/clogging and
floating sludge
Air distribution
Lowell; Greenville; Bay; Morgantown
Excelsior Spring; Morgantown;
Livingston Manor
Improve prescreening; sludge suction line;
rake cable and limit switches
Relocate aeration chains; increase density of
diffusers; Increase maintenance (flexing);
move aeration chain away from clarifier
curtain
Excessive Oil/Grease in Clarifier
Berry; Columbiana; Hanceville; Piggot Vacuum surface; install skimmers
-------
Page 5-11
diffuser/counterweight assembly and air distribution. These centered on the
corrosion of floats and anchoring cables. The floats were initially
manufactured with integral galvanized air pipe and eye bolts on the end floats
for cable connections. These problems have been corrected by utilizing an all
polyethylene float construction.
The limited number of plants which reported float corrosion problems also
commented on corrosion problems with the anchoring cables. Originally, the
aeration chain was 304 stainless steel, 3/32 inch diameter, wire cable, with 6
to 8 feet of link chain at the end to allow for tension adjustment. The cables
had shown excessive wear in the area where the cable dipped into the
wastewater. The restraining chain has since been changed to an all link chain
design of 3/16 inch diameter plated steel. Surface rusting of the new
restraining chain still occurs, however, although this does not effect the
structural integrity of the restraining chain. The manufacturer is considering
a change to all stainless steel. The Livingston Manor WWTP has had success
using nylon rope for restraining the floating aeration chains. The nylon rope
is lightweight and has the ability to stretch, therefore it stays out of the
wastewater. The rope remains dry and ice-free in winter.
There were relatively few diffuser problems, and overall, there was a high
degree of satisfaction with the Wyss diffusers. Problems included diffuser
sheaths blowing off their frames and shorter than expected diffuser life. A
diffuser can come off entirely; more often it would become unseated at one end
due to clamp failure, when either the clamp was improperly installed and/or
tightened or the clamp corroded. Both conditions have been resolved. The
clamp material must be stainless steel (which is the manufacturer's standard)
and should be tightened thoroughly during installation. If the clamp is
allowed too much freedom of movement it can slip as a result of diffuser
flexing, causing the diffuser to unseat.
Shortened diffuser life has been reported by a few plants. The cause is
not immediately apparent at each, but it can be due to several factors. If the
clamps are not properly tightened, sludge can enter the diffuser and be forced
-------
Page 5-12
into the aeration aperture, causing the sheath to clog. A diffuser will also
gradually lose its effectiveness if the apertures remain enlarged for extended
periods of time to the point where they can not return to their normal size
when uncharged. This is due to overcharging the diffusers (i.e. operating
above recommended air flow range) and can result in uneven air distribution
across the diffuser. The large bubbles that result from the enlarged holes
reduce overall aeration transfer efficiency. If the diffuser holes become
enlarged from extended stretching of the diffuser sheaths, an additional
problem can occur. When the system is not charged with air the normally closed
apertures can remain open and wastewater/sludge can enter the diffuser by the
pressure exerted from the liquid head.
The manufacturer suggests that a diffuser life of five years can be
expected under normal conditions. The key to achieving this is regular
diffuser flexing, as described in the operations manual provided for the
aeration chain system. This involves shutting the air off in a chain,
depressurizing the diffusers by bleeding the air and causing the diffusers to
collapse. The air is then turned back on, expanding the diffuser sheaths. A
one week frequency is recommended for flexing. A review of operating plant
data indicates that the procedure varied, with only a third following a routine
schedule.
An equally important point is that the diffusers not be overcharged.
Normal operating air flow is between one and five scfm/diffuser. Increasing
the air supply pressure and operating above the upper boundary continuously
will likely result in enlarged apertures, if not torn diffuser sheathes.
Pressure settings and relief valves on the air system can help minimize this
type of problem.
Two plants reported air distribution problems unrelated to faulty
diffusers. They have been noted near the clarifier and also along the diffuser
chains themselves. Solutions have included utilizing side chain floats in the
basin corners and locating air headers at both ends of the aeration chains. A
six inch diameter aeration chain option has recently been developed. This
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Page 5-13
enables a greater volume of air to be delivered at a lower pressure loss,
reducing the potential for uneven air distribution to the individual chains.
Few problems were reported concerning the blowers. Excessive noise was a
primary complaint. The manufacturer has addressed this by providing silencers
with improved noise attenuation. Several plants do not house their blower
equipment within fully enclosed structures to contain the noise. Plants in
Piggot and Bay, Arkansas housed the blowers in structures which had one or more
open sides. The plants are located in areas where the surrounding land is flat
and largely unwooded; thus the noise is not readily contained by either the
structure, or absorbed by hills and/or forested land.
Another problem was identified with regard to the silencers, and
difficulties in keeping the silencer filters clean. The problem was especially
difficult for plants located in farming regions. Bugs, dust and other debris
from planting and harvesting operations (large quantities of cotton fiber were
observed in Arkansas) clog the silencer air filters quickly. At the
Blythville, Arkansas plants (North, South and West) the silencer housings were
fitted with fine screens around their peripheries, resulting in greatly reduced
maintenance needs for the silencer filters.
Sludge/Solids Removal Systems
Several problems were noted with the clarification and sludge removal
systems in the Biolac R plants. A number of problems with the clarifiers
centered on the mechanical operation of the rake drive motor, limit switches
and the air lift sludge pumping system. The L systems provided sludge storage
times of 10 to 20 years in the polishing basin; with only 3 plants in operation
for less than 4 years, problems have not been encountered.
Figure 9 illustrates the limit switch/drive cable assembly for the integral
clarifiers. A two limit switch assembly which allows the motor to slow down
before starting off in the opposite direction is shown. The flocculating rake
mechanism, used for sludge distribution and concentrations, is suspended from a
-------
Poke Motor
Drive
Torgct ( 1 eoch top £ bottom coble)
Motor Control Switches
FIGURE 9. INTEGRAL CLARIFIER RAKE MOTOR AND CONTROL SWITCHES.
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Page 5-15
float similar to the floats used to support the diffuser/counterweight
assembly. The rake float is attached to a drive cable which is pulled back and
forth across the clarifier by the rake drive motor. Directional control of the
motor is accomplished through the use of a limit switch which is tripped by a
target attached to the drive cable.
Plant operators have reported difficulties due to the improper engagement
of the target and the switch. When this occurs, the rake is not stopped nor
sent back in the opposite direction, and the rake float eventually runs into
the limit switch and drive unit, sometimes resulting in the destruction of the
floats. A redesigned limit switch with modified upper and lower cable trip
arms eliminates improper switch engagements; an evaluation of their use was not
possible. Plant operators had reported successfully modifying the old
switches; one added a PVC collar to increase the target size, while another
modified the trigger arm by simply bending the trigger wire.
Another clarifier system problem was identified with the performance of the
air lift sludge pumping system. This centered on clogging of the piping,
resulting in a reduced sludge return rate and a solids buildup in the
clarifier, with subsequent downtime for unclogging the system. Several
contributing factors were identified including the lack of effective
pretreatment screening at the head of the plant, lack of maintenance of the air
lift system, and the air lift suction line design. The Biolac system does not
include primary clarification as a standard unit operation. Without this, the
plant must rely on the effectiveness of its pretreatment operation for large,
potentially clogging solids removal.
Communition is not recommended because of the tendency for comminuted
materials to mat together in the aeration basin, resulting in clogging
problems. Nine of the plants use some form of comminution. Screening is
recommended as a necessary pretreatment for most domestic applications.
Screening can be accomplished by either racks or screens. The size and amount
of coarse solids removed by each varies greatly. A simple bar or travelling
screen can retain particles four times smaller than the typical bar rack with
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Page 5-16
one inch clear openings. Generally, a review of the plants indicated that
those plants without or with minimal screening encountered difficulties with
clogging.
While there is no recommended approach to sludge suction line maintenance,
one operator reported a program that involved flushing the line monthly to
remove any debris that may have accumulated.
The manufacturer has been investigating suction line design modifications
for improved sludge removal. The utilization of tapered suction line, and/or
varying hole size and spacing has been studied to equalize velocities along the
length of the sludge hopper. Increasing the hole size (1.5 inch is standard)
would reduce clogging and with improved hole spacing would minimize dead spots
where sludge can accumulate, gasify and float. A pipe is now included that
extends from one end of the suction line to the surface, providing cleanout
capability.
The fraying of the rake drive cables and floating sludge are two problems
that can occur as a result of a malfunctioning limit switch or a clogged air-
lift sludge system. The rake drive cable material has been changed from
stainless steel to plastic impregnated galvanized steel to reduce cable
fraying.
Floating sludge in the clarifier may be attributed to inadequate sludge
removal or air leaking into the clarifier from the aeration chain closest to
the integral clarifier. Breakdown of the flocculating rake or sludge removal
operation will allow sludge to remain in the clarifier for an extended period
of time, resulting in gasification and subsequent floating sludge. Sludge will
also float to the surface if air from the aeration basin enters the clarifier.
This is prevented by locating the last aeration chain a sufficient distance
from the clarifier curtain wall and limiting the chain oscillation range. Air
flow to this chain may also be throttled back.
Operators have reported the need to manually skim floating sludge and
greases in the integral clarifiers. The manufacturer is currently designing a
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Page 5-17
mechanical skimmer and incorporating scum baffles for most new Biolac systems.
Better platform access across the clarifier is also being provided.
Rake drive motor troubles resulted from undersized motors or the lack of
delay timers. Larger motors have replaced undersized units and delay timers
have been installed on the rake drive motor which allows the motor to slow down
before changing its direction of rotation, and reduces the strain on the motor.
Polishing Basins
The polishing basin provides additional BOD and TSS removal, and acts as a
backup for additional solids removal when high hydraulic variability is
encountered, reducing the efficiency of the integral clarifiers. Plant
operators have reported significant algae growth in the basins, resulting in
large swings in polishing basin dissolved oxygen, poor basin appearance, excess
effluent suspended solids and reduced performance of the disinfection
operation. One plant reduced the algal discharge by submerging the effluent
intake pipe two to three feet below the water surface. In response to these
concerns, the hydraulic retention time in the polishing basins has also been
reduced from 36 to 48 hours to 12 to 24 hours so that proper operation will be
maintained, even at lower than designed flow rates.
System staging has recently been utilized by Parkson, in which two or more
smaller sized aeration basins are installed, as opposed to one large basin.
This can be beneficial in cases in which the initial flow or loading will not
approach design capacity for some time. The second basin can be by-passed or
operated at a low aeration rate, thus reducing the operating costs.
BIOLAC COSTS
Data received from the manufacturer on total capital construction cost for
several Biolac plants are presented on Table 6. Cost of land, which can vary
considerably and is a key consideration in selecting the aerated
lagoon/extended aeration treatment technology, is not included. Equipment
-------
TABLE 6. BIOLAC SYSTEM CONSTRUCTION COSTS
Proiect
Stevenson, AL
Blytheville , AR
(3 Plants 1.5,
Greenville, KY
Columbiana, AL
Camden, AL
Hanceville, AL
Oxford, AL
Camden , AL
LeSeur, MN
Goodwater , AL
Cedar Bluff, AL
Bid Date
September 1986
November 1987
1.4, 0.8 mgd)
July 1987
November 1987
June 1988
February 1988
July 1988
July 1989
October 1989
November 1989
December 1988
Design
Flow (gpdl
750,000
3,700,000
740,000
750,000
220,000
570,000
2,000,000
540,000
900,000
150,000
500,000
Design
BOD (mg/L1)
400
250
350
200
225
175
225
225
440
200
220
Contract Price
$680,000
3,048,000
977,000
1,100,000
355,000
1,019,000
2,193,000
799,000
1,900,000
640,000
695,000
$/gpd
0.90
0.84
1.32
1.46
1.61
1.78
1.10
1.48
2.11
4.25
1.39
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Page 5-19
costs, including the Biolac aeration chains, integral clarifier and air blowers
and piping are approximately 20 percent of the total cost for plants greater
than 0.5 mgd, and up to 30 percent or more for smaller plants. An average
estimated capital cost for plants greater than 0.5 mgd is in the range of $1 to
$1.5 per gallon per day of design flow for a typical municipal wastewater. The
smaller plants have a somewhat higher cost rate, as do plants with higher
concentrations of BOD (due to industrial wastes). Reported costs are
contractors bid prices to build the complete plant and also include
pretreatment facilities, pump stations, sewers, roads and buildings which are
variable with specific projects.
Operating expenses include labor, power and maintenance supplies, and will
vary with prevailing rates in the plant location. As discussed earlier,
aeration power can be controlled through the operation of the blowers; since
basin mixing is achieved at power levels generally less than required for
adequate oxygenation, basin dissolved oxygen levels can be used as a control
parameter, and power usage kept to a minimum. Operation of these plants is not
highly labor intensive. Depending upon plant size and monitoring requirements,
it was reported that only one to two full time or part-time personnel are
typically required for operation and maintenance. At this time, there is
minimal data available on actual operating costs and estimates have not been
made within the context of this report.
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Page 6-1
SECTION 6
SITE OBSERVATIONS
INTRODUCTION
Six plants were visited to observe operations. The Livingston Manor WWTP,
located in Rockland, New York was visited September 25, 1989, and five plants
located in the northeast corner of Arkansas were visited November 15 and 16,
1989. These site visits provided the opportunity to inspect both old and new
equipment, in retrofit and non-retrofit plants. The following discussion
summarizes observations made at the plants, and includes photos appropriate to
this assessment. Note that plant performance data for each facility may be
found in Appendix B.
LIVINGSTON MANOR WWTP, ROCKLAND, NEW YORK
The Livingston Manor WWTP serves a rural community located approximately
100 miles northwest of New York City. The plant treats an influent flow of 0.5
mgd. One-third of the total flow is a pretreated poultry processing waste and
the remaining two-thirds is municipal waste. It was among the first plants in
the United States to employ the Biolac system.
The influent flow passes through a comminutor or a set of bar racks. After
screening, grit is removed prior to biological treatment. The biological
treatment of the waste is accomplished in two aeration basins in series. The
basins are lined earthen pits and are followed by two 40-foot circular
clarifiers which provide clarification prior to discharge. Lime addition is
provided at the head of the plant to maintain the alkalinity level in the
biological processes.
The plant was retrofitted with the Biolac floating aeration chains in
November 1986. The plant had previously used coarse bubble static tube
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Page 6-2
•i
aerators since upgrading to an activated sludge plant in 1977. The static
tubes were replaced because of hardware failures which had necessitated
rebuilding the aeration system in 1981, and finally replacing it with the
Biolac system in 1986. The retrofit was completed in approximately one month,
while the plant continued to operate as a secondary treatment facility.
The plant staff consists of the superintendent, two assistants and an
administrative secretary, responsible for both the water and sewer departments.
Process monitoring is performed daily. Other 0 & M includes routine blower
maintenance/cycling and visual inspection of the aeration basins.
The retrofit of Livingston Manor WWTP proved beneficial. All effluent
characteristics showed modest improvements while 60 percent less horsepower was
needed. More complete nitrification was achieved after the retrofit. Studies
were conducted by Parkson, which confirmed that the system, at 6000 mg/L mixed
liquor suspended solids was completely mixed, at an air flow of 3 to 4 scfm per
1,000 cu ft. of basin volume. This is roughly one-fifth to one-eighth the air
required with fixed diffused air systems to achieve adequate mixing. Operation
at the high MLSS level causes some floating sludge in the aeration basin,
although this has apparently not caused process related problems.
At the time of the site visit some of the original Biolac equipment was
being replaced. These included deteriorated restraining cables and badly
corroded galvanized air pipes and eye bolts. Loose and corroded clamps
(stainless steel clamps had not been supplied) were responsible for improperly
functioning diffuser sheathes, many of which were filled with sludge. Some of
the restraining cables had been replaced by nylon rope, which appeared to
function adequately. The nylon rope's ability to stretch kept it from dipping
down into the wastewater during the chain's oscillation. Despite the equipment
problems the system has performed well, as evidenced by the performance data
presented in Appendix B. Removals have averaged 87.9 percent for BODs, 94.5
percent for TSS, 91.9 percent for TKN, and 84.5 percent for NH3-N.
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Page 6-3
Livingston Manor STP/Photograph Description
Refer to Figures 10 and 11:
A. Lined earthen basin equipped with Biolac floating aeration chains. Middle
aeration chain which is suspected to have diffuser problems due to uneven
air distribution, as evidenced by the large areas of bubbling around the
2nd and 9th floats.
B. Two diffuser assemblies with loose air clamps. Clamp in the middle of the
picture was missing its screw while clamp in the upper left hand corner was
severely corroded.
C. A diffuser which was sliced open lengthwise revealed a significant
accumulation of sludge within the diffuser.
D. Picture illustrates the benefit of the nylon anchoring line. Nylon
(foreground) stays out of water; therefore, does not accumulate debris.
BAY WWTP, Bay Arkansas
The Bay WWTP serves the rural community of Bay, Arkansas, receiving 100
percent domestic waste flow. This is a new Biolac-R type plant. Although the
design average flow is 0.15 mgd, the actual flow since start-up has been 0.27
MGD. The plant was installed adjacent to the original plant and was put on-
line in March 1989 after about a one year construction period. The original
plant was an unaerated flow-through lagoon, which now serves as the new plant's
sludge storage pond.
At the head of the plant, influent screening is provided by a pair of bar
racks with 0.5 inch openings. After screening, the influent is brought into
the aeration basin via two influent pipes to affect better inlet flow
distribution. The waste is then treated biologically in a 0.3 million gallon
aeration basin equipped with Biolac floating aeration chains. The solids are
settled in an integral clarifier. The clarified effluent is treated further in
a polishing basin, with a detention time of one day at the average design flow.
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FIGURE 10. LIVINGSTON MANOR PHOTOS A AND B.
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FIGURE 11. LIVINGSTON MANOR PHOTOS C AND D.
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Page 6-6
The basin is divided roughly in half by a floating curtain. The first section
of the basin is aerated while the second section is unaerated. After effluent
polishing, the waste is disinfected by chlorination. The plant staff consists
of the plant superintendent and one assistant, while three other town employees
are made available to the plant as needed.
The original plant interview revealed few problems, and all of them had
been resolved satisfactorily. Problems with the rake drive motor had been
resolved by the installation of an additional limit switch, which acts as a
delay, allowing the motor to slow down prior to changing its direction of
rotation. The plant also had floats containing galvanized air pipe. There was
no visible evidence of corrosion, although the plant was on-line for only six
months. The restraining chains showed signs of slight surface corrosion. Due
to economic considerations, the blower assembly was not contained within a
fully enclosed structure nor was a spare purchased.
Plant maintenance consists of regular blower maintenance as per
specifications; bar rack cleaning twice daily; daily floatable skimming of
basins and clarifiers; routine diffuser flexing; (rake) and air lift sludge
system cleaning using the town sewer cleaning truck approximately every three
weeks. Daily process monitoring includes dissolved oxygen, pH, chlorine
residual and clarifier sludge level. August and September, 1989 effluent
results show the plant to be performing very well (see Appendix B).
Bay WWTP Photograph Descriptions
Refer to Figures 12, 13, 14 and 15:
A. Influent to effluent view of the Biolac System. Aeration basin foreground,
integral clarifier in back of the aeration basin and the polishing basin in
the background.
B. Closeup of the anchoring system and header assembly. Chain length controls
the aeration chain tension and subsequently the aeration chains lateral
range of motion. Air header assembly includes a butterfly valve (large
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FIGURE 12. BAY, ARKANSAS PHOTOS A AND B
-------
FIGURE 13. BAY, ARKANSAS PHOTOS C AND D
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-It*
FIGURE 14. BAY, ARKANSAS PHOTO E
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FIGURE 15. BAY, ARKANSAS PHOTO F
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Page 6-11
handle) for air flow control and an air bleed valve (smaller handle) for
unchaining the aeration chain.
C. Side view of the integral clarifier consisting of 2 concrete sidewalls,
concrete backwall (basin backwall) and a floating curtain on the influent
side. Also note the corner float which is typical of the later designs.
D. Picture looking across the integral clarifier: baffle wall on the left;
float and drive cable supporting the flocculating rake in the middle and
the effluent weir on the right.
E. Picture of the airlift sludge system consisting of: air compressor (middle
foreground) ; air lift sludge pipe (vertical pipe just to the left of the
rake drive motor); gravity flow sludge line (pipe running back along the
concrete walkway) and the sludge control box.
F. Picture looking across the length of the floating curtain wall in the
polishing basin.
PIGGOT WWTP, PIGGOT, ARKANSAS
The Piggot WWTP in Piggot, Arkansas was designed to handle an average daily
flow of 0.6 mgd. The influent is 100 percent domestic wastewater, and the flow
to the plant is currently about 0.35 mgd. The plant was put on-line in April
1989 after about six months of plant construction. An unaerated flow through
lagoon was previously used for treatment of the town's wastewater; this now
serves as a storage lagoon for storm flow.
At the head of the plant, screening is provided by an Aquaguard^M traveling
screen, manufactured by Parkson. The influent flow is then measured by a
Parshall flume prior to biological treatment. Biological treatment is
accomplished in a 0.95 million gallon aeration basin, followed by solids
clarification in two integral clarifiers. Clarified effluent then flows into
the polishing basin, with subsequent disinfection by by ultra-violet light.
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Page 6-12
The plant supervisor/operator performs essentially all plant operations and
maintenance. One helper is available about one-third of the month to assist
with plant chores, and an additional town employee is provided to perform
weekend systems checks. A visual inspection of all systems is performed daily.
The screening device is cleaned automatically and the screenings are disposed
of as needed. The clarifiers are skimmed daily of floatables and blowers are
checked twice per week. The UV system is cleaned weekly while other
miscellaneous maintenance (i.e. spraying down equipment) is performed as
needed. Diffuser flexing has been performed on a weekly basis. Process
monitoring is performed three times per week and includes basin MLSS and SVI,
effluent TSS, basin and effluent pH. Basin and effluent dissolved oxygen is
measured daily.
The plant has had problems maintaining the mixed liquor suspended solids at
the recommended operating level. The plant effluent is meeting permit
requirements. Effluent concentrations are at or a bit above 20 mg/1 for BOD
and TSS (See Appendix B), which will likely improve results with increased
MLSS. A rake drive cable had frayed but was replaced with a plastic
impregnated cable. Blower equipment is protected by a roofed three sided
structure made of corrugated aluminum panels. It offers weather protection but
does little for noise reduction. Otherwise the plant has experienced few
problems.
Piggot WWTP/Photograph Descriptions
Refer to Figures 16 and 17:
A. Blower setup consisting of 3 to 20 HP blowers, two of which are on full-
time. Blowers are housed in a lightweight aluminum structure with one open
side which provides some noise reduction.
B. Flocculating rake drive control system equipped with dual limit switches.
First switch slows down the motor while the second reverses the motor
collation and returns it to correct operating speed.
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^^^H
m
FIGURE 16. PIGGOTT, ARKANSAS PHOTOS A AND B
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FIGURE 17. PIGGOTT, ARKANSAS PHOTOS C AND D
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Page 6-15
C. Effluent trough equipped with scum baffles.
D. Effluent weir from polishing basin. Discharges to the U.V. disinfection
channe1.
BLYTHEV1LLE WEST, NORTH AND SOUTH WWTPS, BLYTHEVILLE, ARKANSAS
The City of Blytheville, with a population of 25,000, is one of the larger
cities in Mississippi County, Arkansas. It is located approximately 185 miles
northeast of Little Rock and 70 miles north of Memphis, Tennessee. Blytheville
is primarily a farming community, growing cotton and winter wheat. The
majority of the wastewater flow is domestic. The Blytheville plants are
identical in design, differing in size only. The North plant is the smallest,
and is designed to handle an average flow of 0.8 mgd. The South plant is
designed for 1.4 mgd and the West plant for 1.5 mgd. Each plant was built
adjacent to former unaerated flow-through lagoons. Although the City's
original goal was to build one large plant to handle all the flow, this concept
was dismissed because of the major sewer system re-routing and renovation which
would be required. The plants were started in April 1989.
Each plant provides influent screening using an Aquaguard^M traveling
screen. Grinder pumps are used for volume reduction of the screenings prior to
disposal. The wastewater is biologically treated in the aeration basins which
incorporate solids settling in integral clarifiers. Clarified effluent is
treated further in polishing basins which have both aerated and unaerated
sections. The effluent is disinfected using an ultra-violet light system.
The combined staff for the three plants consists of the superintendent,
maintenance supervisor, a plant operations supervisor, three operators and an
administrative assistant.
Visual inspections of all equipment is performed daily. The clarifiers and
weirs are sprayed down weekly and the aeration basins and clarifiers are
skimmed as needed. Blower inlet and noise filters are cleaned weekly. The two
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Page 6-16
larger plants are sampled for permit requirements three times per week while
the other plant is sampled for permit requirements three times per month.
Additionally, process monitoring is performed daily.
The South plant has had trouble maintaining the desired operating mixed
liquor suspended solids level due to a significant underloading at the plant.
A two sided cinder block enclosure has been installed around the air lift
sludge blower to minimize the noise. The West plant developed a crack in the
concrete sludge trough due to soil settlement. The three plants had installed
screening around all noise filter housings to minimize silencer maintenance due
to debris accumulation. The three plants experienced high effluent ammonia
levels during the start up spring months which may have been caused by farm
fertilization operations and/or limited nitrification development. All these
plants were performing well, in subsequent months through October 1989, as
shown in the data in Appendix B.
Blytheville WWTPS Photograph Descriptions (North. South and West Plants)
Refer to Figures 18, 19, 20 and 21:
A. Blower silencers. Screens were installed to reduce filter clogging. Metal
mesh filters are used; these are brushed and washed regularly (North).
B. Integral clarifier. Note the curtain and rake drive cable (North).
C. Effluent trough and rake drive enclosure (installed by plant) (North).
D. Last aeration chain in basin; closest to 3 integral clarifiers (West).
E. One of three integral clarifiers at the West plant. Steel angle bracing
was installed to minimize lateral movement of the long effluent trough.
F. Aeration chain. Localized boiling indicated diffuser problem (West).
G. Structure used for air lift pump blower noise control at the South Plant.
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FIGURE 18. BLYTHEVILLE, ARKANSAS PHOTOS A AND B
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FIGURE 20. BLYTHEVILLE, ARKANSAS PHOTOS E AND F
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FIGURE 21. BLYTHEVILLE, ARKANSAS PHOTO G
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Page 7-1
SECTION 7
REFERENCES
1. Biological Wastes Treatment Using the Biolac System, A Technical Note. U.S.
Environmental Protection Agency Office of Municipal Pollution Control, EPA
625/8-85-010. Environmental Resources Management, Inc., West Chester, PA,
1986.
2. Fine Pore (Fine Bubble) Aeration Systems. Summary Report. U.S.
Environmental Protection Agency, Water Engineering Research Laboratory,
EPA/625/8-85/010, Cincinnati, OH 45268, October 1985.
3. Personal Communication, Charles Morgan, Parkson Corporation
4. Metcalf and Eddy, Inc., Wastewater Engineering. 1979.
5. Design Brochure, Parkson Corporation.
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APPENDIX A
DESCRIPTION OF BIOLAC
TREATMENT SYSTEMS
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TABLE A-l. DESCRIPTION OF BIOLACR TREATMENT SYSTEMS
Facility Kama
Location
Contact
Size
Design
Ardmore MWTP
Ardmore, Alabama
Bill Brakefield
Engineer
(615) 824-7980
Berry WHTP
Berry, Alabama
Mike Swindle
(Superintendent)
(205) 669-4786
Camden North HWTP
Caroden, Alabama
G.E. Jones - Engineer
Jones Engineering
(205) 872-7618
Cedar Bluff MWTP
Cedar Bluff, Alabama
Keith Davis - engineer
Lad Environmental
(205) 845-5315
Clayton WWTP
Clayton, Alabama
Bob Carter
Engineer
(205) 222-9431
Flow BOD
(mud) (»/day)
0.35 730
Current
Flow BOD
(nwd) (»/day)
Process Train
Bar rack
Biolac R
Chlorlnation
0.15 275
0.04
30
Aquaguard traveling screen
Biolac R
Chlorination/dechlorination
Post aeration (Cascade)
0.22 413
Bar screen
Biolac R
UV disinfection
0.30
550
Aquaguard traveling screen
Biolac R
Chlorination/dechlorination
0.40 512
Static screen
Biolac R
disinfection
Biolac Description
- Aeration Basin Volume, 0.70 MG
- 7 chains; 8 floats/chain;
4 diffusers/float
- Integral clarifier
- Polishing basin
Aerated zones
- 2 chains; 3 floats/chain;
2 diffusers/float
- Blowers: 3-15 hp (1 standby)
- Aeration basin Volume, 0.264 MG
- 5 Chains; 5 floats/chain;
4 diffusers/float
- Integral clarifier
- Polishing basin
Aerated and nonaerated zones
- 1 chain; 4 floats/chain
2 diffusers/float
- Blowers: 3-7.5 hp (1 on fulltitne)
- Aeration basin volume, 0.33 MG
- 6 chains; 6 floats/chain;
4 diffusers/float
- Integral Clarifier
- Polishing basin
Aerated and nonaerated cones
- 2 chains; 4 floats/chain;
2 diffusers/float
- Blowers: 2-7.5 hp (no standby)
- Aeration basin volume 0.53MG
- 7 chains; 8 floats/chain;
4 diffusers/float
- Integral clarifier
- Polishing basins
aerated and nonaerated zones
- 2 chains; 4 floats/chain;
2 diffusers/float
- Blowers: 3-15 hp (1 standby)
- Aeration basin volume, 0.45 MG
- 6 chains; 8 floats/chain;
4 diffusers/float
- Integral clarlfiers
- Polishing basin
Aerated zones
- 1 chain; 5 floats/chain;
2 diffusers/float
Conments/Problems
Plant not yet on line
Plant on line August 1989.
Good system, expect even
better effluent when MLSS gets
to design MLSS(2500 mg/L).
Rake drive cable frayed (re-
placed), float destroyed from
rake overtravel no longer a
problem now. Skim grease/oil
once/week.
Plant not yet on line
Plant not yet on line
Plant not yet on line
-------
TABLE A-l. DESCRIPTION OF BIOLAC1* TREATMENT SYSTEMS
(Continued)
Facility Name
Location
Contact
Size
PeaInn
Current
Columblana WWTP
Columbiana, Alabama
James Palmer
(Operator)
(205) 669-76*5
HancevlUe WWTP
Rancevllle, Alabama
Bill Hicks
(Operator)
(205) 352-6177
Flow BOD Flow BOD
(mgd) (»/day) (mud) (f/dav)
Process Train
0.75 1,251
0.5
- Bar acraen
- grit chamber
- Biolac R
0.57 632
0.25
365
Hew Brockton WWTP
New Brockton, Alabama
James Harrison
(Superintendent)
(205) 894-5550
0.176 300
0.05
98
Oxford HWTP
Oxford, Alabama
Ronald Windham
Engineer
(205) 271-3200
1.00 1,877
- Schrlber screen
- Biolac R
- UV disinfection
- Post aeration (Cascade)
Bar Rack
Biolac R
Nutrient removal
2 ponds with aquatic
plants
Post aeration
(effluent flume)
Manual bar rack
Aquaguard traveling screen
Grit removal
Biolac R
Chiorlnation/dechiorlnatlon
Post aeration (cascade)
Biolae Description
- Aeratln basin
- 6 chains; 8 floats/chain;
2 dlffusers/float
- Integral clarifier
- Polishing basin
aerated zones
- 3 chains; * floats/chain;
2 dlffusers/float
- Blowers: 3-20 hp (1 standby)
- Aeration basin
- 7 chains; 10 floats/chain
* diffusers/float
- Integral clarifier
- Polishing volume
aerated and nonaerated cones
- 2 chains; * floats/chain;
2 dlffusers/float
- Blowers: 3-16 hp (1 on full time)
- Aeratin basin volume, 0.2 MG
- 5 chains; 5 floats/chain;
2 dlffusers/float
- Integral clarifier
- Blowers: 3 to 5 - 5 hp
Aeration basin volume, 1.5 MG
11 chains; 13 floats/chain;
6 diffusers/float
Integral clarlfar
Polishing basin
aerated and non aerated zones
3 chains; 8 floats/chain;
2 dlffusers/float
Blowers: 2-60 hp (1 standby)
Comments/Problems
Plant on line December 1989.
Needed silencers for blowers,
system running well, skim oil/
grease every other day main-
tenance free otherwise.
On line March 1989. Very
pleased w/ system esp. compared
to mech. aerators which oper-
ator previously used. Rake
motor burned out (water dara.-
due to improper seal Installa-
tion). Rake overtraveled,
operator bent trigger forward
rake fine now. Rake floats
hang up on other hardware at
HWL. Skim oil/grease every 2
ks
Plant on line summer 1987. Very
dissatisfied originally due to
equipment problems. Clarifier rake
motor was under sized (would kick
out often in warm weather).
Floating curtain cable and
eyebolts rotted out. Dlffuser
clamps needed to be tightened.
Auto valves on waste pump not
working, must be switched manually.
Meeting designed effluent BOD and
NH3 but monitoring reports show
lower limits that are not always
met.
Plant not yet on Una
-------
TABLE A-l. DESCRIPTION OF BIOLACR TREATMENT SYSTEMS
(Continued)
Facility Name
Location
Contact
Stevenson WWTP
Stevenson, Alabama
J.M. Garner
(Operator)
(205) 437-2490
Bay WWTP
Bay, Arkansas
Crawford Holmes
(Superintendent)
(501) 781-3386
(City Hall #)
Blythevllle North WHTP
Blythevllle, Arkansas
Jimmy Gee
(Superintendent)
(501) 763-4961
Site
Design
Current
Flow BOD Flow BOD
(mud) (»/day) (mtd) (»/day)
Process Train
0.75 2,502
0.15
0.15 313
0.1
175
0.80 1,134
0.39
Blythevllle West WWTP
BLytheville, Arkansas
Jinnry Gee
(Superintendent)
(501) 763-4961
Blythevllle South WHTP
Blytheville, Arkansas
Jinny Gee
(Superintendent)
(501) 763-4961
1.50 3,253
0.77
1.40 3,562
Aquaguard traveling screen
Biolac R
Bar screen
Biolac R
Chlorination
Aquaguard traveling screen
Grinders
Biolac R
UV disinfection
Aquaguard traveling screen
Grinders
Biolac R
UV disinfection
Aquaguard traveling screen
Grinders
Biolac R
l/V disinfection
Biolac Description
- Aeration basin
- 12 chains; 10 floats/chain;
4 dlffusers/float
- Integral Clarifier
- Polishing basin
aerated and nonaerated zones
- 3 chains; 4 floats/chain;
2 dlffusers/float
- Blowers: 3-40 hp (1 standby)
- Aerated basin
- 6 chains; 5 floats/chain;
4 dlffusers/float
- Polishing basin
aerated and nonaerated
- 2 chains; 3 floats/chain;
2 diffusars/float
- Blowers: 2-7.5 hp / 5 cfra
- Aeratin basin volume, 1.09 MG
- 8 chains; 13 floats/screen;
4 dlffusers/float
- Integral clarifer
- Polishing basin
aerated and nonaerated zones
- 2 chains; 6 floats/chain;
2 diffusers/float
- Blowers: 3-25 hp (1 standby)
Aerated Basin Volume. 3.12 MG
11 chains; 24 floats/chain;
4 diffusers/float
Integral clarlfiers
Polishing basin
aerated and nonaerated zones
2 chains; 13 floats/chain;
2 diffusers/float
Blowers: 3-60 hp (1 standby)
Aeration basin volume, 3.12 MG
11 chains; 24 floats/chain;
4 diffusers/float
Integral clarifier
Polishing basin
Aerated and nonaerated zones
2 chains; 13 floats/chain;
2 diffusers/float
Blowers: 3-60 hp (1 standby)
Comments/Problems
Experiencing problems unre-
lated to Biolac system. A
Industry has left the area re-
sulting in greatly reduced
flow & BOD loading. This makes
supporting design MLSS levels
Impossible.
Plant on line March 1989. Good
system, lowmaint., flex dlffuser
every 2 weeks, clean air lift
sludge pump w/ sewer cleaning
equip, every 3-4 weeks, no
clogging problems.
Plant on line April 1989. Happy
w/system. Problems keeping blower
filters clean during summer,
planting and harvesting seasons.
Reduced substantially by screening
off Intake access pts. Still
clean once/week. Plant very well
maintained. Some high BOD, TSS &
NH3 numbers during initial months
after startup.
Plant on line April 1989. Con-
crete sludge trough cracked soil
settlement. Some high TSS & NB3
numbers during Initial months
after startup.
Plant on line April 1989. Trouble
maintaining MLSS.
-------
TABLE A-l. DESCRIPTION OF BIOLACR TREATMENT SYSTEMS
(Continued)
Size
Facility Ran
Location
Contact
Desinn
Currant
Decatur WWTP
Decatur, Arkansas
Rick McClean
(Superintendent)
(501) 752-3769
Flow BOD Flow
(mad) (»/day) (mud)
1.35 5,630
1.1
BOD
(»/day)
5500
Process Train
Maynard WWTP
Maynard, Arkansas
Paul Mitchell
(Operator)
(501) 6*7-2701
Piggot WWTP
Piggot, Arkansas
Bradley Schaffler
(Superintendent)
(501) 598-2946
0.06 110
0.60 1,000
0.3
450
Paint Brush Hills WWTP
Colorado Springs, CO
Kevin Smith
(Operator)
(719) 473-8600
Tri-Lakes WWTP
Monument, Colorado
0.90 1,350
1.30 2,168
Bar screen
Primary Clarlfier
Blolac R
Sand filters
Post aeration
(surface aerators)
Dechlorination
Bar screen
Biolac R
Chlorlnatlon
Aquaguard traveling screen
Biolac R
UV disinfection
Bar screen
Biolac L
Bar screen
Grit removal
Biolac R
Chlorination/dechlorinatlon
Biolac Description
- Aeration basin
- 15 chains; 25 floats/chain;
6 diffusers/float
- Integral clarifier
- Polishing basin
aerated and nonaerated zones
- 3 chains; 12 floats/chain;
4 diffusers/float
- Blowers: 4-50 hp (3 standby)
Comments/Problems
Aerated basin volume,0.104 MG
3 chains; 3 floats/chain;
4 diffusers/float
Polishing basin
Aerated and nonaerated zones
1 chain; 2 floats/chain;
4 diffusers/float
Blowers: 2-5 hp (no standby)
Aeration basin volume, 0.952 MG
6 chains; 13 floats/chain;
4 diffusers/float
plus 1 float at each corner at
effluent end with 4 diffusers/float
Integral clarifier
Polishing basin
aerated and nonaerated zones
2 chains; 8 floats/chain;
2 diffusers/float
Blowers: 3-20 hp (1 standby and 1
runs 25X of time)
Aeration basin
5 chains; IS floats/chain;
4 diffusers/float
No clarifier
Polishing lagoon
aerated and nonaerated zones
2 chains; 13 floats/chain;
4 diffusers/float
Blowers: 2-30 hp
2 Aeration basins at 2.1 MG each
11 chains/basin; 15 floats/chain;
4 diffusers/float
External clarifier
No polishing basin
Blowers: 2-125 and 1-75 hp
Meeting all eff. limits.
Wave oxidation plant. Took
some time to achieve denltri-
fication. Replaced 3 of 4
rake drive motors. 751 of
float assemblies were defective
(FVC const, came unglued). 40Z
of dlff will be replcd.(expo-
sure to severe weather & hand-
ling may be cause). Add lime
to maintain pB.
Plant not yet on line.
Plant on line April, 1989.
Had trouble getting up to
operating MLSS, some high BOD
& TSS #'s as a result. Rake
drive cable needed replacement.
Low maintenance, flex diffusers
occasionally & skim oil/grease
daily.
Plant on line March, 1989.
Plant waa built to serve a
growing community but currently
only serves a high school & 4
houses. Adequate evaluation
can not be made yet.
Plant not yet on line.
-------
TABLE A-l. DESCRIPTION OF BIOLACR TREATMENT SYSTEMS
(Continued)
Facility Nan*
Location
Contact
Size
Deslnn
Quitman WHIP
Quitman, Georgia
Flow BOD
(nutd) (*/day)
1.30 1,952
Current
Flow
(nutd)
BOD
(*/day)
Ferdinand WWTP 0.47 698
Ferdinand, Indiana
Rusty Groeschen
(Operator)
(812) 367-2617
Remington WWTP 0.28 271
Remington, Indiana
Marvin Sutter
(Operator)
(219) 261-2389
Renssalaer WWTP 1.20 1,942
Rensaelaer, Indiana
Lawrence Swartz
(Operator)
(219) 866-5530
Western Wayne STF 0.80 1,341
Cambridge City, Indiana
Dan Bine
(Operator)
(317) 478-3788
Ellsworth WWTP
Ellsworth, Kansas
John Kerschner
(Supt.- Water & Sewer)
(913) 472-3941
0.50 1,250
0.28
550
Process Train
- Biolac L
- Disinfection
- Grinders
- Grit removal
- Biolac R
- Chlorination/dechlorination
- Post aeration
- Bar screen
- Grinders
- Biolac R
- Chlorination/dachlorination
- Aerated grit chamber
- Biolac R
- Chlorination/dechlorination
- Post aeration
(Wyss diffusers)
- Bar screen
- Biolac R
- Disinfection
- Bar screen
- Grit chamber
- Biolac L
- Stablization pond
Biolac Description
- Aeration basin
- 11 chains; 31 floats,
17 floats, 14 floats,
and 10 floats/chain in each
of 4 cells; 4 diffusers/float
- No clarifler
- Polishing lagoon
nonaerated zone
- Blowers: 3-30 hp (1 standby)
- Aeration basin volume, 0.672 MG
- 7 chains; 9 floats/chain;
4 diffusers/float
- Integral clarifier
- Polishing basin
aerated and nonaerated zones
- 2 chains; 7 floats/chain;
2 diffusers/float
- Blowers: 3-20 hp (1 standby)
- Aeration basin volume, 0.45 MG
- 5 chains; 6 floats/chain;
4 dlffusers/float
- Integral clarifier
- No polishing basin
- Blowers:3-40 hp (1 standby)
- 2 Aeration basins at 0.95 MG each
- 8 chains/basin; 10 floats/chain;
4 diffusers/float
- Integral clarifier
- No polishing basin
- Blowers: 3-50 hp (1 standby)
- Aeration basin volume 1.3 MG
- 10 chains; 12 floats/chain;
4 diffusers/float
- No polishing basin
- Blowers: 3-20 hp
- Aeration basin
- 10 chains; 10 floats/chain;
4 diffusers/float
- No clarifier
- No polishing pond
(effluent not continuous,
mostly used for irrigation)
- Blowers: 3-20 hp
Comments/Problems
Plant not yet on line.
Plant not yet on line.
Plant not yet on line.
Plant not yet on line.
Start up spring/summer 1990.
Plant not yet on line.
On line April, 1988. Biolac
is used to supplement stabili-
zation ponds. Very happy w/
system. Changed check valves
on blowers(water check valves
were installed originally in-
stead of air check valves).
0 & M -only routine blower
malnt. Some freezing in winter
resulting in some restriction
of chain/float movement.
-------
TABLE A-l. DESCRIPTION OF BIOLACR TREATMENT SYSTEMS
(Continued)
Size
Facility Hame
Location
Contact
Wells vi lie WWTP
Desinn
Flow
(mgd)
0.18
BOD
(»/day)
300
Current
Flow
(mud)
*
BOD
(t/day) Process Train Biolac Description
* - Biolac L -2 Aeration basins
Comments/Problems
Plant not yet on line.
Wellsville, Kansas
Wichita WWTP
Wichita, Kansas
James Tush
(Superintendent)
(316) 522-9307
Edmonton WWTP
Edmonton, Kentucky
Halcom England
(Operator)
(502) 432-4844
34.4 18,148
0.51 851
0.2
310
Greenville WWTP
Greenville, Kentucky
Roy McDonald
(Operator)
(502) 338-5260
0.75 2,160
0.57
1,110
Morgantown WWTP
Morgantown, Kentucky
Randall Gaskey
(Operator)
(502) 526-5949
0.50 1,043
0.28
350
Primary clarifiers
Trickling filters
Biolac L
(for nitrification)
Chlorlnatlon
Post aeration
Bar screen and/or
conralnutor
Biolac R
aquaculture pond
chlorlnatlon
Post aeration
Aqua-guard traveling screen
Bar screen
Biolac R
Chlorination
Aquaguard traveling screen
Biolac R
Chlorination
2 chains/basin; 12 floats/chain;
2 diffusers/float
Ho clarifier
Polishing basin
aerated and nonaerated zones
2 chains; 12 floats/chain;
2 diffusers/float
Blowers: 2-20 hp (no standby)
6 Aeration basins,
volume 2.26 MG each
25 chains/basin; 16 floats/chain;
4 diffusers/float
External clarifier
Ho polishing pond
Blowers: 9-300 hp (3 standby)
Aeratln basin volume, 0.89 MG
10 chains; 10 floats/chain;
2 diffusers/float
Integral clarifier
Polishing basin
aerated zone
2 chains; 1st chain - 5 floats/
chain. 2nd chain 3 floats/chain;
2 diffusers/float
Blowers: 3-20 hp (2 standby)
Aeration basin volume 1.37 MG
10 chains; 11 floats/chain;
4 diffusers/float
Integral clarifier
No polishing basin
Blowers: 3-40 hp (2 standby)
Aeration basin
10 chains; 8 floats/chain;
2 diffusers/float
Integral clarifier
No polishing basin
Blowers: 3-25 hp (1 standby,
1-30 min. on / 30 min. off)
Plant not yet on line.
Startup - March 1990
On line April, 1989. Signif-
icant hydraulic design problems.
Rake limit switch problems &
drive cable frayed. Cable was
replaced w/new design. Ho prob-
lems w/alr lift sludge pump
but running continuously. Per-
formance can not be evaluated
due to hydraulics problems.
Plant on line April 1988.
Very good performance. Air lift
sludge system doesn't perform as
claimed. Floating sludge causes
solids to settle out in chlorine
out in chlorine contact chamber
(happens more frequently in rainy
weather ). Solids washout at
high flows (rsin). Rake cable
needed replacement.
On line March, 1989. Getting
good removals. Some dead spots
in basin (problem corrected by
blower operation described at
floats due to limit switch
Destroyed two rake
problems. Operator Installed
a PVC collar which has prevented
rake overtravel. Floating sludge
in clarifier when rake and/or
air lift sludge pump are down.
-------
TABLE A-l. DESCRIPTION OF BIOLACR TREATMENT SYSTEMS
(Continued)
Facility Name
Location
Contact
Site
Design
Current
LeSueur WWTP
LaSuaur, Minnesota
Brad Bjarka
(Project Engineer)
(507) 625-4171
Walla WWTP
Walls, Minnesota
Brad Bjarka
(Project Engineer)
(507) 625-4171
Baumgartner WWTP
St. Loula MSD
St. Louis, Missouri
PRC Engineering
(314) 832-0400
Excelsior Springs WWTP
Excelsior Springs, MO
Rex Brinker
Dir. of Utilities
(816) 637-1415
Flow BOD Flow BOD
(mgd) (»/day) (nmd) (f/day)
0.90 3,314 * *
0.55 1,147
Process Train
4.00 4,670
2.40 3,980
1.3
2100
Livingston Manor WWTP
Livingston Manor, NY
Bob Walco
(Superintendent)
(914) 439-4910
0.80 1,668
0.51 1,170
Rock Hill WWTP
Rock Hill, New York
0.22 367
Mech. bar screen
Grit removal
Biolac R
- Biolac R
Aerated lagoon
Biolac L
Chlorination
Pre-aeration using Biolac
Discharge to overland
flow area (April - Oct.)
or further treatment
in facultative lagoons.
pH adjustment
Bar rack comninuter
grit chamber
Biolac R
No information available
Biolac Description
- Aeration basin volume 3.2 MG
- 12 chains; 27 floats/chain;
1480 diffusers total
- No polishing basin
- Blowers: 4-60 hp (1 standby)
- 2 Aeration basins volume 1.75 MG
per basin
- 8 chains; 10 floats/chain;
4 diffusers/float
- No clarifier
- No polishing basin
- No information available on blowers
- Aeration basin
- 10 chains; 30 floats/chain
4 diffusers/float
- No clarifiar
- Polishing basin
aerated zone
- 9 chains; 35 floats/chain;
4 diffusers/float
- No information available on blowers
- Pre-aeration basin
- 12 chains; 10 floats/chain;
4 diffusers/chain
- No clariflers
- No polishing basin
- Blowers: 3-800 cfm (1 standby)
2 Aeration basins at 1.05 MS each
7 chains; 12 floats/chain;
4 diffusars/float
2 External clarifier
No polishing basin
Blowers: 3-40 hp (1 standby)
No information available
Comments/Problems
Plant not yet on line.
Plant not yet on line.
Plant not yet on line.
Biolac has been used for pre-
aeration here for over 4 years.
During original startup problems
getting chains moving was exp-
erienced (due to poor air dis-
tribution). A 1 in 5 year storm
resulted in chain & anchor prob-
lems w/4 of the 12 air lines.
No problems w/new chain & anchor
system. Low maintenance.
Retrofit. Plant on line 1986. One
of original biolac U.S. Installa-
tions. More than share of prob-
lems. Rotted Cables, aye bolts
and end caps on floats and
dlffuaar clamps. Have had quite
a bit of success using nylon rope
or anchorlina especially because
rope stays out of MLSS. Despite
cosmetic/equipment problems, plant
gets excellent removal of BOD &
TSS, generally 951 removal. TKN &
NH3 generally 90Z removal.
Plant not yet on line.
-------
TABLE A-l. DESCRIPTION OF BIOLAC>* TREATMENT SYSTEMS
(Continued)
Facility Name
Location
Contact
Coalton WWTP
Coalton, Ohio
Rackoff Engineers
(614) 464-3575
Size
Desixn Current
Flow BOD Flow BOD
(mgd) (*/day) (mgdj (*/day)
0.046 61 * *
q
Process Train
- Bar screen
- Blolac R
- Chlorination
Biolac Description
- Aeration basin
- 2 chains; 3 floats/chain;
4 dlffusers/float
- Integral clarifier
Comments/Problems
Plant not yet on line.
Franklin WWTP
Miami Conservancy Dist.
Nick Brookhart
(Wastewater Engineer)
1(800) *51-*932
4.00 18,000 4.5
29275
Frazeysburg WWTP
Frazeysburg, Ohio
Mona Miller
(City Clerk)
(614) 828-2564
Lowell WWTP
Lowell, Ohio
Paul Kullsek
(Operator)
(614) 896-3086
0.18 390
0.054 70
0.11
141
- Bar screen
- Primary clarifier
- Blolac R
- Chlorlnation/dechlorination
Ho information available
- Bar racks
- Grinder pumps
- Grit chamber
- Blolac R
- UV disinfection
Durant WWTP
Durant, Oklahoma
C.O. Reese
(Superintendent)
(405) 920-0364
1.70 2,400
2.10 3,173
- Bar rack
- Banninutor
- Biolac R
- Cascade post aeration
- Polishing basin
Aerated zone
- 1 chain; 2 floats/chain;
2 diffusers/float
- Blowers: 3-2 hp (1 standby)
- Aeration basin volume 9 MG
- 34 chains; 26 floats/chain;
6 diffusers/float
- 2 external clariflers
- No polishing basin
- Blowers: 3-300 hp/6000 cfm
blowers (1 standby)
No information available
Aeration basin
2 chains; 3 floats/chain;
4 dlffusers/float
Integral clarifier
Polishing basin
aerated and nonaerated zones
1 chain; 3 floats/chain;
4 diffusars/float
Blowers: 3-3 hp
(designed to have 2 running,
3 needed)
Aeration basin volume 5.3 MS
1st lagoon - 8 chains; 20 floats/
chain; 2 dlffusers/float;
2nd lagoon - 4 different chains;
19 floats/chain,
17 floats/chain,
15 floats/chain,
13 floats/chain;
all with 2 diffusers/float.
Polishing basin area 11 acres.
aerated zone
15 chains; 30 floats/chain;
2 diffusers/float
Blowers: 8-75 hp - 5 for lagoon
Retrofit-
Plant on line October 1989.
Plant not yet on line.
Plant on line Jan., 1989. Plant
underdeslgned hydraullcally.
Problems w/llmit switches on
rake system, operator fixed
problem himself. Air lift sludge
pumps clog w/ fine particles.
Cracked elbow on one float
assembly delivered. Solids
settling in polishing basin.
Generally reliable performance.
Partial retrofit ft added polishing
in April 1988 to help meet permit.
Operator doesn't think they would
be meeting permit now without
Blolac. Slime accumulation on
sleeves. Metal air line fati-
gue 3 or 4 holes developed. Need
to reduce effluent toxiclty.
Ciarlfiers overloaded.
-------
TABLE A-l. DESCRIPTIOH OF BIOLAC1* TREATMENT SYSTEMS
(Continued)
Slat*
Facility Hame
Location
Contact
Peatun
City of Canby WWTP
Canby, Oregon
Steve Hanson
(Superintendent)
(503) 266-4021
Ext. 248
Chase City WWTP
Chase City, Virginia
Flow BOD
(mud) (»/day)
1.15 2,160
Current
Flow BOD
(nmd)
0.76 1,270
0.60 1,201
Fincastle HWTP 0.08 150
Flncaatle, Virginia
Wayne Heikel
(Director)
(703) 473-3065
Lakeside HWTP 0.275 459
Winchester, Virginia
Hank Sliwinski
(Supt.- Several Plants)
(703) 722-2402
(Parkins Hill Plant *)
0.04
67
Process Train
Bar screen
Grit removal
Primary clariflers
Blolac R
External clarlfiers
Chlorlnation
Grit chamber
Biolac R
Sand filter
UV disinfection and
reaeration
Bar screen
Blolac L
Chlorinatlon
Post aeration
Bar screen
Biolac L
Disinfection
Blolac Description
- Aeration basin
- 8 chains; 4 floats/chain;
4 diffusers/blower
- External clarifier
- No polishing basin
- Blowers: 1-50 hp, 1-30 hp, 2-20 hp
Comments/Problems
Plant on line in 1886.
Control air in basin to produce
anoxic zone to achieve nitrification
denitrification. Older generation
equipment - corrosion problems.
2 aeration basins at .765 M3 each Plant not yet on line.
7 chains; 7 floats;
4 diffusers/float
External clarifier
aerated and nonaerated zones
3 chains; 3 floats/chain;
4 diffusers/float
Blowers: 4-25 hp (1 standby)
Aeration basin
2 chains; 7 floats/chain;
2 diffusers/float
External clarifier
Polishing basin
aerated and nonaerated zones
2 chains; 8 floats/chain;
2 diffusers/float
Blowers: 2-10 hp (1 standby)
Aerated basin volume 2.23 MG
4 chains; 14 floats/chain;
2 diffusers/float
No clarifier
Polishing basin
3 chains; 8 floats/chain;
2 diffusers/float
Blowers: 3-10 hp (1 standby)
Plant on line September 1986.
Good performance. Corrosion of
metal hardware. Basin froze to
within a 3 foot diameter around
floats for as long as 1 week
with no decrease in treatment.
Hot able to contact operator.
Equipment on line in 1988.
-------
APPENDIX B
PERFORMANCE DATA SUMMARY TABLES FOR
SELECTED BIOLAC PLANTS
-------
TABLE B-l. PERFORMANCE DATA SUMMARY
CITY OF MORGANTOWN, KENTUCKY - BIOLAC R PLANT
Month
January 1989
February 1989
March 1989
April 1989
May 1989
June 1989
July 1989
August 1989
September 1989
Mean:
Mean: April to
September
Design
X of Design
Flow
(MGD)
.322
.388
.425
.345
.247
.278
.285
.270
.316
0.320
1989 0.290
0.5
58X
Influent
BOD
(me/L)
95.
136.
61.5
138.
194.
106.
151.5
608.
258.
194.2
242.7
_
-
Effluent
BOD
(mz/L)
59.1
57.5
31.4
19.3
10.5
21.3
11.9
6.9
6.4
24.9
12.7
_
-
X
BOD
Removal
37.8
57.7
48.9
86.
94.6
84.7
92.1
98.9
97.5
77.6
92.3
_
-
Loading
Ibs BOD/d
255.
440.
218.
397.
399.
246.
360.
1369.
680.
484.9
575.2
1045
55X
Influent
TSS
(mc/L)
150.
120.
100.
184.
222.
168.
86.
77.
392.
166.6
188.2
.
Effluent
TSS
(me/L)
29.
16.5
6.4
7.2
20.
14.
24.
<0.4
4.4
13.5
11.7
.
X
TSS
Removal
80.6
86.3
93.6
96.1
91.
91.7
97.2
99.5
98.9
170.5
95.7
_
NH3-N
(mp/'L)
^\ lllf^f JLtJ^
7.7
7.6
5.4
<0.01
<0.01
0.1
0.3
2.4
0.1
_
Startup January 1989 to March 1989
Sampling Program: 1 sample per month
-------
TABLE B-2. PERFORMANCE DATA SUMMARY
CITY OF GREENVILLE, KENTUCKY - BIOLAC-R PLANT
Month
May 1988
June 1988
July 1988
August 1988
September 1988
October 1988
November 1988
December 1988
January 1989
February 1989
March 1989
April 1989
May 1989
June 1989
July 1989
August 1989
Mean:
Design
X Design
Flow
(MGD)
.580
.260
.360
.270
.280
.270
.480
.490
.680
.530
.740
.580
.290
.350
.330
.336
0.4
0.73
55X
Influent
BOD
(me./L)
198.
405.
225.
170.
320.
278.
140.
150.
125.
123.
129.
105.
85.
85.
123.
184.
177.8
Effluent
BOD
(mg/L}
23.
20.
10.
2.
4.
4.
4.
3.
2.
6.
5.
6.
2.6
2.6
2.6
2.0
6.2
X
BOD
Removal
88.4
95.1
95.6
98.8
98.75
98.6
97.1
98.0
98.4
95.1
96.1
94.3
96.4
96.4
97.9
98.
96.5
Loading
Ibs BOD/d
97.
878.
675.
382.
747.
626.
560.
613.
709.
543.
796.
508.
206
248.
338.
515.
527.6
1293
41X
Influent
TSS
(rag/D
166.
625.
180.
142.
174.
202.
162.
300.
137.
157.
122.
370.
182.
80.
250.
156.
212.8
Effluent
TSS
(me/L)
25.
81.
22.
6.
2.
4.
3.
7.
7.
12.
8.
7.
6.2
5.6
1.2
2.0
12.4
X
TSS
Removal
85.
87.0
87.8
95.8
98.9
98.0
98.2
97.7
94.9
92.4
93.4
98.1
96.6
93.0
99.5
98.7
94.7
NH3-N
(mg/L)
.30
.60
.40
.75
.70
.54
.46
.45
.20
.20
.30
.25
2.9
.20
.35
.15
0.5
MLSS
(mg/L)
1856.
1736.
1278.
1392.
2019.
2178.
3532.
3700.
3400.
3704.
2648.
2494.8
Sampling program: 1 day per month
-------
TABLE B-3. PERFORMANCE DATA SUMMARY
CITY OF NEW BROCKTON, ALABAMA - BIOLAC-R PLANT
Flow
Month WGD)
February 1988
March 1988
April 1988
April 1988
May 1988
June 1988
July 1988
July 1988
July 1988
July 1988
August 1988
August 1988
September 1988
September 1988
September 1988
September 1988
September 1988
October 1988
December 1988
February 1989
Mean:
June 1989 0.05
July 1989 0.06
August 1989 0.05
Mean: June to 0.053
August 1989
Design 0.175
X Design 30X
Influent
BOD
(me/L)
182.
280.
184.
173.
70.
283.
250.
290.
250.
190.
450.
234.
600.
270.
108.
225.
79.
113.
218.
175.
231.2
167
368
194
243
Effluent
BOD
fme/L)
19.
9.
6.
4.
18.
19.
7.
6.
3.
5.
8.
6.
8.
2.
7.
21.
15.
20.
2.
6.
9.6
3
3
2
2.7
Z
BOD
Removal
89.6
96.8
96.7
97.7
97.4
93.3
97.3
98.0
98.8
97.4
98.23
97.44
98.7
99.
93.5
90.7
81.0
82.3
99.1
96.6
95.0
98.2
99.2
98.9
98.8
Influent
Loading TSS
Ibs BOD/d (me/L)
105.
300.
218.
218.
47.
234.
201.
258.
300.
118.
505.
248.
658.
380.
185.
329.
163.
200.
222.
145.
251.7
69.6 153
184.1 547
80.9 176
111.5 292.0
Effluent
TSS
(me/L)
11.
22.
11.
11.
10.
17.
15.
12.
6.
3.
8.
6.
13.
6.
16.
20.
17.
18.
1.
14.
11.9
4
2
2
2.7
X
TSS
Removal
89.6
92.7
94.9
94.9
78.8
92.7
92.5
95.4
980.
97.5
98.4
97.6
98.02
98.4
91.35
93.9
89.6
91.0
99.6
90.4
93.8
97.4
99.6
98.9
98.6
NH3-N
(mg/L)
.7
.9
1.3
4.5
.8
.8
1.6
2.2
2.2
1.6
2.2
2.2
2.4
2.4
1.4
2.8
1.9
2.4
4.0
0.2
2.2
Sampling program monthly
-------
TABLE B-4. PERFORMANCE DATA SUMMARY
CITY OF EDMONTON, KENTUCKY - BIOLAC-R PLANT
Month
May 1989
June 1989
July 1989
August 1989
September 1989
October 1989
November 1989
Mean:
Mean: September
Flow
(MGD)
ND
ND
ND
ND
ND
ND
ND
0.2(D
Influent
BOD
fme/L)
100.
80.
110.
291.
396.
114.
102.
170.4
202.6
Effluent
BOD
31.
33.
18.
3.
12.
14.
11.
17.4
11.6
X
BOD
Removal
69.
58.75
83.6
99.0
95.9
87.7
89.2
83.3
9.1
Loading
Ibs BOD/d
ND
ND
ND
ND
ND
ND
ND
185(D
Influent
TSS
(me/L)
106.
26.
64.
513.
453.
102.
197.
208.7
265.8
Effluent
TSS
(me/L)
26.
22.
4.
11.
29.
29.
19.
20.0
18.4
X
TSS
Removal
75.5
15.4
93.75
97.9
93.6
71.6
90.36
76.9
89.5
NH3-N
(mg/L)
<1.00
<1.00
<1.00
7.50
<1.00
5.30
<1.00
2.5
3.2
to November 1989
Design 0.51
XDesign 39X
Startup April to
June 1989
Sampling program 1 day per month
(l)From operator
850
22X
-------
TABLE B-5. PERFORMANCE DATA SUMMARY
CITY OF FINCASTLE, VIRGINIA - BIOLAC-L PLANT
Month
September 1988
October 1988
November 1988
December 1988
January 1989
February 1989
March 1989
April 1989
May 1989
June 1989
July 1989
August 1989
Mean:
Flow
(MGD)
•ks__««JU
.044
.048
.050
.042
.049
.048
.052
.049
.069
.036
.057
.031
0.048
Influent
BOD
(me/L)
230.
200.
239.
215.
227.5
222.
229.6
217.
181.6
189.
235.
229.
217.9
Effluent
BOD
fme/L)
15.21
14.25
12.93
14.1
19.05
21.96
29.40
29.34
26.96
14.9
10.31
14.63
18.6
X
BOD
Removal
93.4
92.9
94.6
93.4
91.6
90.1
87.2
86.5
83.5
92.12
95.6
93.63
91.2
Loading
Ibs BOD/d
84.4
80.1
99.7
75.3
93.
89.
99.6
89.2
104.5
56.7
111.7
59.4
86.9
Influent
TSS
fme/L)
217.6
222.1
250.4
246.
242.5
255.
252.8
205.8
152.
155.5
131.
155.0
207
Effluent
TSS
(me/L)
8.
13.1
11.
14.5
27.63
49.87
45.2
21.3
29.4
15.5
7.25
14.8
21.5
X
TSS
Removal
96.3
94.1
95.6
94.1
88.6
80.45
82.1
89.7
80.7
90.03
94.5
90.5
89.7
Design
X Design
0.075
64X
Sampling program one day per month
-------
TABLE B-6. PERFORMANCE DATA SUMMARY
CITY OF LOWELL, OHIO - BIOLAC-R PLANT
Month
July 1989
August 1989
September 1989
Mean:
Design
X Design
Flow
(MGD)
0.120
0.122
0.092
0.111
0.18
62X
Influent
BOD
fme/L)
168
130
260
185.9
Effluent
BOD
frae/L)
29.0
7.5
3.5
13.3
X
BOD
Removal
82.6
94.2
98.6
91.8
Loading
Ibs BOD/d
167.7
132.3
199.5
166.5
Influent
TSS
fme/L)
214.5
93.3
208.5
172.1
Effluent
TSS
(me/L)
57.0
8.0
12.5
25,8
X
TSS
Removal
73.4
91.4
94.0
86.3
NH3-N
fmg/L)
17
3
0
6.7
MLSS
(mg/L)
763
3517
5412
3230
Sampling program weekly
-------
TABLE B-7. PERFORMANCE DATA SUMMARY
CITY OF HANCEVILLE, KENTUCKY - BIOLAC-R PLANT
Month
March 1989
April 1989
May 1989
June 1989
July 1989
August 1989
September 1989
Mean:
Mean: June to
September
Design
X Design
Flow
(MGD)
0.500
0.605
0.497
0.666
0.728
0.274
0.300
0.5
0.5
1989
0.57
88X
Influent
BOD
(me/L)
59.2
54.0
39.9
137.0
90.8
113.0
194.0
98.3
133.7
Effluent
BOD
(me/L)
12.4
9.8
12.8
15.8
10.5
7.5
5.1
10.6
9.7
X
BOD
Removal
79.0
81.9
67.9
88.5
88.4
93.4
98.0
85.3
92.0
Loading
Ibs BOD/d
247
272
165
761
551
258
485
391.
514.
832
62X
Influent
TSS
(me/L)
76
64
44
119
51
79
142
482.0
97.8
Effluent
TSS
(me/L)
6.5
11.0
7.0
9.0
2.7
7.3
17.0
8.6
9.0
X
TSS
Removal
91.4
82.8
84.0
92.4
94.8
90.7
90.0
89.4
92.
NH3-N
(me/L)
21.
2.1
15.7
1.0
1.0
1.0
0.1
3.3
0.8
-------
TABLE B-8. LIVINGSTON MANOR, NEW YORK
Date
June 1986
June 1986
June 1986
July 1986
July 1986
July 1986
July 1986
June 1987
June 1987
June 1987
July 1987
July 1987
July 1987
June 1988
June 1988
June 1988
July 1988
July 1988
July 1988
January 1989
January 1989
February 1989
February 1989
March 1989
March 1989
April 1989
April 1989
May 1989
May 1989
June 1989
June 1989
July 1989
July 1989
August 1989
August 1989
Average
Flow
0.530
0.616
0.5*0
0.611
0.569
0.548
0.621
0.677
0.661
0.692
0.638
0.801
0.725
0.526
0.488
0.451
0.489
0.452
0.748
0.480
0.248
0.222
0.606
0.515
0.491
0.578
0.334
0.921
0.365
0.404
0.624
0.593
0.507
0.277
0.488
0.544
±0.150
Influent
BOD
210.
268.
376.
241.
211.
168.
199.
141.
184.
243.
208.
254.
180.
261.
375.
320.
275.
284.
227.
305.
492.
330.
175.
227.
254.
311.
148.
166.
222.
359.
250.
254.
384.
228.
385.
260.
±79.6
Effluent
BOD
9.3
5.6
16.0
16.5
14.3
8.8
21.0
3.1
3.0
2.7
0.3
1.0
1.2
1.
1.
2.
2.
3.
2.
2.
4.
2.
6.
1.
3.
2.
4.
4.
4.
4.
5.
6.
11.
2.
4.
51.
±5.0
X Removal
BOD
95.6
97.9
95.7
93.1
93.2
94.8
89.4
97.8
98.3
98.9
99.8
99.6
99.3
99.6
99.7
99.3
99.3
98.9
99.1
98.3
99.2
99.4
96.6
99.6
98.8
99.4
97.3
97.6
98.2
98.9
98.0
97.6
97.1
99.1
99.0
97.9
±2.3
Loading
lb» BOD/Day
928.
1,377.
1,693.
1,228.
1,001.
768.
1,031.
796.
1,014.
1,402.
1,007.
1,697.
1,088.
1,145.
1,526.
1,204.
1,122.
1,071.
1,416.
1,221.
1,018.
611.
884.
975.
1,040.
1,499.
412.
1,275.
676.
1,210.
1,301.
1,256.
1,624.
527.
1,567.
1,132
±320.
Influent
TSS
187.
246.
650.
236.
106.
302.
84.
184.
160.
604.
240.
140.
140.
96.
164.
204.
184.
104.
206.
146.
300.
798.
58.
194.
128.
224.
192.
78.
100.
166.
120.
152.
364.
172.
178.
217.
±161.
Effluent
TSS
18.5
9.5
21.
17.
4.5
24.
8.
5.8
6.0
10.8
35.
4.
17.
2.
1.
2.
3.
2.
5.
1.
10.
5.
4.
9.
8.
1.
9.
3.
7.
5.
14.
10.
10.
3.
8.
8.7
±7.4
X TSS
Removal
90.1
96.0
96.7
92.8
95.8
92.1
90.5
96.8
96.3
98.2
85.4
97.1
87.9
97.9
99.3
99.0
98.4
98.1
97.6
99.3
96.7
99.4
93.1
95.4
93.8
99.6
95.3
96.2
93.0
97.0
88.3
93.4
97.3
98.3
95.5
95.4
±3.6
Influent
TKN
_
-
-
-
-
-
-
38.9
52.7
44.0
43.1
52.1
45.4
53.2
42.6
41.2
45.9
43.4
50.4
59.4
66.1
63.3
21.6
61.6
46.8
38.6
29.12
21.84
36.4
47.6
42.84
31.08
57.68
40.04
52.08
45.3
±11.3
Effluent
TKN
_
-
-
-
-
-
-
1.12
5.3
1.7
1.7
3.8
0.7
2.5
2.5
0.4
0.6
0.3
0.8
4.5
7.3
0.56
1.7
1.4
2.0
1.4
0.84
10.64
5.04
1.12
9.52
5.88
16.8
0.84
1.96
3.3
±3.8
X TNK
Removal
_
-
-
-
-
-
-
97.1
89.9
96.1
96.1
92.7
98.5
95.3
94.1
99.0
98.7
99.3
98.4
92.4
89.0
99.1
92.2
97.7
95.7
96.4
97.1
51.3
86.2
97.6
77.7
81.1
70.9
97.9
96.2
91.9
±10.6
Influent
HH3-N
„
-
-
-
-
-
-
12.6
17.6
14.3
13.2
14.8
13.2
20.1
16.2
37.7
33.6
13.4
29.7
4.5
17.6
12.9
11.7
12.3
11.2
10.6
14.8
14.56
22.12
13.1
13.44
13.8
11.48
16.43
17.5
16.2
±7.0
Effluent
NH3-N
„
-
-
-
-
-
-
0.1
2.5
0.1
0.1
0.1
0.1
1.1
0.8
0.3
0.3
0.1
0.6
3.7
5.3
0.1
0.28
0.3
0.28
0.84
0.28
1.68
3.92
1.12
8.96
4.48
14.48
0.28
0.89
1.9
±3.2
X NH3-N
Removal
_
-
-
-
-
-
-
99.2
85.8
99.3
99.2
99.3
99.4
94.5
95.1
99.2
99.1
99.3
98.
17.8
69.9
99.2
97.6
97.6
97.5
92.1
98.1
88.5
82.3
91.5
33.3
67.5
-26.1
98.3
94.9
84.5
±29.4
-------
TABLE B-9. PERFORMANCE DATA SUMMARY
CITY OF BLYTHEVILLE, ARKANSAS WEST
BIOLAC-R PLANT
Effluent
Month
April 1989
May 1989
June 1989
July 1989
August 1989
September 1989
October 1989
Mean:
Mean: June to
October 1989
Design:
Z of Design:
Startup April 1989 to
Flow
(MGD)
0.920
0.832
0.740
0.814
0.556
0.649
0.848
0.766
0.717
1.50
48
June 1989
BOD
(mg/L")
12.3
10.2
13.4
8.1
4.6
9.9
7.9
9.5
7.6
_
TSS
(mg/L)
43.5
12.8
14.2
5.5
36.0
10.4
7.8
18.6
14.9
_
NH3-N
(mg/L^
47.8
31.8
50.0
6.8
1.4
0.2
0.4
19.8
2.2
_
TABLE B-10. PERFORMANCE DATA SUMMARY
CITY OF BLYTHEVILLE, ARKANSAS NORTH
BIOLAC-R PLANT
Effluent
Month
April 1989
May 1989
June 1989
July 1989
August 1989
September 1989
October 1989
Mean:
Mean: August to
October 1989
Design
X of Design
Flow
(MOD)
0.462
0.338
0.345
0.403
0.474
0.263
0.446
0.39
0.39
0.8
49
BOD
(me/L)
4.1
7.1
12.8
21.5
11.9
5.9
23.6
13.8
13.8
TSS
fmg/L)
4.0
5.3
53.0
22.0
13.0
12.5
14.6
26.3
13.3
NH3-N
(mg/L)
39.2
4.3
51.0
85.2
1.2
0.7
0.5
26.0
1.0
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TABLE B-ll. PERFORMANCE DATA SUMMARY
CITY OF BLYTHEVILLE, ARKANSAS - SOUTH PLANT
BIOLAC-R PLANT
Effluent
Month
April 1989
May 1989
June 1989
July 1989
August 1989
September 1989
October 1989
Mean:
Design:
X Design:
Flow
(MGD)
0.676
0.620
0.673
0.645
0.519
0.543
0.538
0.602
1.40
43X
BOD
(mg/L)
6.9
12.4
16.5
25.2
33.8
11.0
0.2
15.1
TSS
(mg/L)
13.0
18.7
9.5
19.5
38.2
9.6
18.5
18.1
NH3-N
(mg/L)
38.7
7.9
70.4
95.3
3.3
0.2
0.4
30.9
TABLE B-12. PERFORMANCE DATA SUMMARY
CITY OF BAY, ARKANSAS - SOUTH PLANT
BIOLAC R PLANT
Effluent
Month
May 1988
December 1988
January 1989
February 1989
March 1989*
April 1989
May 1989
June 1989
July 1989
August 1989
September 1989
Mean: June to
September 1989
Design:
X Design
Flow
(MGD)
0.120
0.275
0.136
0.211
0.067
0.049
0.055
0.118
0.287
0.557
0.100
0.266
0.15
177X
BOD
(mg/L)
20.4
36.3
39.1
33.7
30.0
21.7
14.9
24.9
10.1
3.7
2.7
10.4
TSS
frng/L)
34.0
93.0
87.1
75.0
41.4
24.8
28.3
12.4
11.2
2.0
1.2
6.7
NH3-N
(ing/D
2.0
5.0
4.5
18.9
26.0
19.3
22.4
21.5
1.1
0.2
11.3
Sampling program two grab samples per month
*Biolac system on line; startup March 1989 to May 1989
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TABLE B-13. PERFORMANCE DATA SUMMARY
CITY OF PIGGOTT, ARIZONA
BIOLAC R PLANT
Month
June 1989
July 1989
August 1989
September 1989
Mean:
Design:
X Design:
Flow
(MGD)
0.561
0.194
0.382
0.249
0.35
0.60
58X
BOD
fmg/L)
19
17
28
19
20.8
Effluent
TSS
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