WQ0033455_WWTP_O&M_20081023

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AQUEONICS, INC
(Preliminary)
Wastewater Treatment Plant (W WTP)
Operation & Maintenance Manual
for
The Cliffs at High Carolina
Asheville, NC
With -Nature

TABLE OF CONTENTS
RtGEIVED I DENR I M
pQUIFFP PROTECTION SECTO
OCT 2 3 2008

OPERATIONS AND MAINTENANCE MANUAL
FOR
THE CLIFFS AT HIGH CAROLINA SEWAGE TREATMENT PLANT
THE CLIFFS COMMUNITIES
ASHEVILLE BUNCOMBE COUNTY, NORTH CAROLINA
INTRODUCTION
This site is served by municipal water supply and on-site wastewater treatment system. The
wastewater collection system consists of a gravity sanitary sewage collection system, with
lift stations, leading to an Aqueonics on-site tertiary sewage treatment facility. The treatment
facility proposes to discharge treated effluent to on-site disposal system, which are fed by dosing
force mains designed by others from a dosing storage tank attached to the treatment system. The
sewerage system will ultimately be designed, treat and discharge to service the anticipated
discharge from future dwelling units and commercial development and will be constructed in
two phases, of which initial construction will be for Phase I, serving Villages 1-5, 7, 9, 10, and
13. This phase will include, besides the residences, an Inn, Restaurant, Market, Banquet facility,
3 spas, and a clubhouse with an anticipated 98,410 gallons per day (gpd) total flow. Phase II will
comprise villages 6, 8, 11, 12, and 14. The full descriptions and associated flows are tabulated in
Figure 1.
_Water Consumption Treatment and Discharge Considerations
Estimates of Water discharge are based upon North Carolina Standards to be found in NCDENR
DWQ 2T. Total estimated flow based on this calculation is 98,410 gpd for Phase I. Phase II is
estimated to comprise 101,280 gpd. Treatment facilities have been designed to treat 100,000 gpd
for Phase 1, and 200,000 gpd for Phase II.
Nitrogen content of the influent wastewater is expected to be typical of a mixture of domestic
sewage values of mixed residential and commercial sources.
This project is subject to discharge criteria established by the NCDENR for nitrogen and
Phosphorus -limited discharge. The treatment facility has therefore been designed for nitrogen
and Phosphorus removal to comply with applicable standards for pretreatment.
Inasmuch as nitrogen removal in the treatment process of this plant provides for an effluent with
total ammonia plus nitrate nitrogen at less than 5 mg/l, it is clear that the criteria for adequate
pretreatment to meet groundwater standards, which call for groundwater nitrate levels at all
points to meet federal EPA drinking water standards for nitrates (less than 10 mg/1), will be
satisfied at all points around the discharge.
The effluent disposal delivery and distribution system will be described by others in a separate
report.

The Cls at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 2 of 24
The Cliffs at High Carolina
Design Flow calculations
PVi
Phllage 2 a 1 Buildi Floors Uni�lFldor Brfillnits FIawIBr F€ Unit Notes
10
2
5
2
1 120
1 24 M0
god
50
Village 4
Phase C VIil a 44`etiness & Poa S . F7. Flow3t . fL F ow Unit N
5.000 50 2
village -6
S . Ft Fiowtf100 . ft. F ow Unit Notes
Phase i Talla Wellness Roo
8,000 1 50 11, � - I -I 1 1 4,TM I g F - I I i
Village & - isenglass
Phase 11 Buildi Units+itld BrlUnd lo r- F ow Unit Notes
1 1 14 8 3 120 4^,320 gPd
Villa 7
Phase l Clubhouse I Sq- Ft. Fiaulli€ll W. ft. Row Unit Notes
15.000
50
4
7 c
1 2D,160
god
Village 8
Phase Il ##14 SF Units Br.Nnit ;!Iml&- Fow Unit Notes
42
4
1 120
1 2D,160
god
Village 4
Phase II Strauss Lake SF Ung11, Sr tUnit Flow/Br- Fa w Unit Notes
1,g 3 1, S 780
Village 10
Phase ll Practice Golf SF Units Br1Unft FlowlBr. Frew Unit Notes
8 1 4 120 13,840 Igpd
Village 11
Phase IIClubhouse Cottage SF Units Br./Unit Flo;tra'Br. Fow Unit Notes
24 4 1120 11,520 lood
Ylia 12
Phase ll SF Rrd Ltns SF Units Br1unit FiovrlBI Fotw Unit Notes
401 41 1201 IqaL-Ojgcd
Village 13
Phase I Gdf Maintenance I SC3. Ft. F =1100 . ft Flow Unit Notes
7.500 50 3,7501god
Village 14
Phase 11 V€11a a lake Lnert�ok Bui`d s Units Br./Unit Flaw r. Faw knit Notes
7 4 3 1201 lu,um 9csd
Figure 1

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 3 of 24
This project is located in Asheville, Buncombe County, North Carolina, which is subject to
discharge criteria established by the NCDENR for nitrogen limited discharge to groundwater.
The soils beneath each disposal site have been determined to be suited for spray application, and
approved for that purpose. The site and soils are judged to be suited to effluent disposal with the
disposal system as designed.
TREATMENT PLANT DESIGN
GENERAL CONSIDERATIONS
The selection of a treatment technology and disposal strategy at this site is governed by the
recent concern for dwindling groundwater resources and desire not to increase groundwater
pollution with nitrogen discharged in treated wastewater. Discharge criteria are imposed by The
State of North Carolina, Department of Environment and Natural Resources (NCDENR). The
NCDENR limits the concentration of nitrate -nitrogen (further presuming that ammonia
discharged is converted to nitrate) in a groundwater plume as it leaves the site to 5 mg/l, with
additional hydraulic loading limitations on subsurface distribution beds as determined by the
soils and groundwater.
The available processes which are economically and operationally capable of eliminating large
amounts of nitrogen from domestic -type wastewaters are limited. The selection of technology is
especially limited when one compares the nature of operator skill and level of maintenance
generally available to a small municipal or privately operated plant to those plants operated by
industry or a large utility for the removal of nitrogen. The basic process proposed to treat
domestic wastewater and remove nitrogen at this facility is a continuous sequential Carbon
Oxidation - Nitrification - Denitrification system using endogenous carbon for denitrification.
Sequential aerobic/anaerobic (anoxic) conditions with recycle of nitrified wastewater for BOD
enrichment to accomplish denitrification using fixed -film media reactors is employed.
The specific process design selected for this project is a biological process, which makes use of
concepts that have generally been known for more than 25 years to the technical community
interested in advanced technology for removal of nitrogen compounds. Pilot systems using this
process were first installed in the mid -1970's, with full scale installations occurring in 1979.
Nitrogen Loading and Unit Processes Descriptions
Typical design nitrogen content of domestic wastewater recommends that a value of 40 mg/l as
N be used. Organic nitrogen is both soluble and particulate with the soluble organic nitrogen
mainly in the form of urea and amino acids. Primary sedimentation acts to remove a portion of
the particulate organic matter. This removal generally will allow 80% or less of the total
nitrogen entering the plant reaching the biological treatment process. Ordinary secondary
biological treatment will remove most particulate organic nitrogen and transform some to
ammonium and other inorganic forms. Soluble organic nitrogen is partially transformed to
ammonium by microorganisms, but concentrations of 1 to 3 mg/l are usually found in biological

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 4 of 24
treatment effluents.
Because of the cost and inconvenience of most organic carbon sources used in denitrification
processes, a number of processes have been developed or are currently under development in
which the carbon oxidation -nitrification -denitrification processes are combined into a coherent
operational plan. The advantage of such processes for effective nitrogen removal, of which this
is an example, include: (1) reduction in the volume of air applied to suspended solids (or
pumping energy to a trickling filter) to achieve nitrification and BODS removal; (2) elimination
of the supplemental organic carbon sources (e.g., methanol) required to complete denitrification;
(3) stability of operations over long time periods.
In these combined processes, either the endogenous decay of the organisms or the carbon in the
wastewater is used to achieve denitrification. In addition to the Aqueonics process, other
examples include oxidation ditches where rotor oxygenation levels are controlled as in the
"Bardenpho" process. The reader is invited to review the 1975 USEPA Process Design Manual
for Nitrogen Control, Section 5.5 where combined Carbon Oxidation - Nitrification -
Denitrification System using endogenous carbon and Sequential Operations developments are
reviewed and commented upon. Most of these processes, however, utilize suspended growth
rather than fixed -film growth, which is a serious disadvantage to stable operation in small
facilities such as this one.
As early as 1975 a Danish plant of 1.5 million gallons per day (mgd) using the "alternating
contact" process was able to achieve nitrate levels of 2.0 to 5,0 mg/l. The "Bardenpho" process
of South African development was also able to achieve 5 to 7 mg/l of total nitrogen under long
term performance at 26,000 gpd. Problems with the larger EPA Blue Plains pilot plant of the
same time period point out the specific advantage of the Aqueonics process over the early work
in this field which was associated with suspended growth reactors to accomplish oxidation and
denitrification.
Operation of suspended growth reactors in the alternating aerobic/anaerobic (anoxic) mode
requires an F/M ratio sufficiently low to permit the development of a mixed culture of organisms
for carbon oxidation, nitrification, and denitrification; and severe filamentous bulking conditions
are also developed sometimes in the sludge as a result of this low F/M ratio. Maintenance of this
proper ratio is a sophisticated operational problem. Fixed -film reactors by their inherent nature
require no F/M ratio, since fixed bacteria automatically adjust their growth rate to the food
source, and there is, of course, no suspended sludge to bulk. Fixed -film designs, therefore serve
to avoid these problems, give greater stability to the process, and greatly reduce the risk of
sludge loading of the subsurface distribution beds.
The Blue Plains work did serve to establish several benchmarks with respect to criteria used in
the design of alternating systems. They are as follows: (1) To evaluate nitrification limitations
on a system, both nitrogen loads and nitrification rates must be taken into account, and, (2) there
is general agreement that the design of the combined carbon oxidation -nitrification functions of
the aerobic phase(s) can be separated from the anoxic phase(s). Therefore, the carbon oxidation

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 5 of 24
and nitrification calculations for the aerobic periods can be virtually identical to those advanced
for ordinary carbon oxidation -nitrification processes (See same USEPA document Section 4.4.1).
The Blue Plains work also supports a rational approach to sizing of the denitrification steps and
presents measured denitrification rates in systems using wastewater as the organic carbon source.
The relatively modern concept of the coupling of an anaerobic (anoxic) residence period with an
aerobic residence period in these systems is based on the recognition that dissimilatory
denitrification is accomplished by facultative bacteria using biochemical pathways that are
almost identical to aerobic biochemical pathways. These facultative bacteria can shift readily
from using nitrate to using oxygen and vice versa. In the aerobic towers, the carbon and
ammonia are oxidized and nitrogen gas stripped from solution so that nitrogen gas bubbles will
not form in the next packed -reactor or in the sedimentation process.
Aqueonics' use of fixed -film reactors with stable operational characteristics is a considerable
advancement over other aerobic/anaerobic (anoxic) processes, and provides a more easily
operated, more reliable, less maintenance intensive, and less costly system to operate than
denitrification processes using either methanol -based systems or suspended growth alternating
systems. Systems such as air -stripping and selective ion exchange have not been considered to
be appropriate for this application.
In addition to alternating aerobic/anaerobic (anoxic) fixed -film reactors, this system also
incorporates a primary clarifier to take advantage of its large removal rate of particulate organic
nitrogen and BOD. Careful attention has been given to integrating hydraulic loadings, recycle
capability, the ability of the operator to divide and redirect flow through the facility, and sludge
handling and solids separation in this facility to provide a plant with proper balance and
flexibility in operation. Aqueonics has conducted extensive full scale testing at Castlewood,
California to verify kinetic design parameters for this process and the results of that work are
incorporated in this design. Aqueonics full scale denitrifying plants utilizing the proposed
process have been in operation in California since 1979, Pennsylvania since 1983, South
Carolina since 1981, and in New Jersey since 1985. We therefore conclude this process to be the
most appropriate technology for use at this site. For this facility, alum addition for
physical/chemical removal of Phosphorus has been integrated into the process.
In order to obtain the benefits of the above-described system we have selected the Aqueonics K -
Series design (Figure 2). The process provides screening, maceration, fill flow equalization,
primary sedimentation, and a series of three alternating aerobic and (anaerobic) anoxic reactors
which are designed for carbon oxidation - nitrification and denitrification using influent sewage
as a carbon source for denitrification. Sand filtration and ultraviolet disinfection to permit limit
system follows tertiary treatment for further assurance of water quality. The tankage is of
reinforced concrete construction, totally enclosed, and the aerobic reactors are of the fixed -film
PVC media type, totally enclosed within an insulated shelter which is placed atop the tankage. A
controlled forced air supply is provided for purging of gases in tanks and for air flow in the
towers utilized in the process. All process air is pre -scrubbed in the trickling filters, then purified
of odors, moisture, and contamination through a combination potassium permanganate /

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 6 of 24
*4-0/ activated carbon filter before being exhausted from the building. All machinery and equipment
are located inside the insulated building, so that the Only sound external to the enclosure should
be a minimal hum of the blowers.
Clearly, sound exterior to the building is dependent upon sound containment by closed doors and
windows. See Figure 3 for an example of the containment building.

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 7 of 24
Figure 3
Design Calculations and Specifications
1.0 Design Conditions
The wastewater treatment plant has daily capacity of 200,000 gallons per day based upon
influent from the facilities listed on page one. The plant is designed to be utilized for
treatment of domestic sewage having a maximum daily average concentration of:

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 8 of 24
Biochemical Oxygen Demand (5 day) (BOD)
350 mg/l
Total Suspended Solids (SS)
250 mg/l
Total Nitrogen (N)
60 mg/l
Total Phosphorus (P)
20 mg/l
2.0 Effluent Requirements
Effluent quality from this plant is designed to have a maximum 30 day average
concentration of:
Biochemical Oxygen Demand (5 day) (BOD)
10.0 mg/l
Total Suspended Solids (SS)
5.0 mg/l
Ammonia Nitrogen + Nitrate Nitrogen
<6 mg/l
Dissolved Oxygen (DO)
>6.0 mg/l
Total Phosphorus (P)
1 mg/l
pH
6.5-8.5 S.U.
Fecal Coliform
14 MPN/100 ml
The achievement of the specified effluent quality is contingent upon sufficient nutrient
levels being present in the process waters, including sufficient alkalinity, and the
exclusion of any biologically inhibitory constituents. Effluent problems most frequently
reflect influent problems, so one of the first things to be done when problems are
encountered is to check the influent quantity and quality. Periodic baseline samples
should be taken regularly to assess the status of influent compared to design and to
effluent performance. A disinfection to permit limit standard suitable for recreational use
has been applied at , as it is believed that with pretreatment, including disinfection
to permit limit, monitoring for disinfection at surrounding monitoring wells will show a
negative result. Additionally, recontamination from natural sources, most particularly
from birds, is anticipated.
3.0 General Description
The wastewater treatment plant design is that of the Aqueonics Inc. Model K-200-3 as
manufactured by Aqueonics Inc., 4115 East North Street, Suite 202, Greenville, SC
29615-6212. The wastewater treatment system incorporates the concept of alternating
aerobic and anaerobic (anoxic) treatment. The complete system includes all necessary
equipment for efficient plant operation and utilizes a process composed of an influent
trash basket, an equalization basin with grinder pumps and forward flow control device, a
primary sedimentation basin, three pairs of alternating aerobic and anaerobic (anoxic)
fixed -film media reactors, sand filtration, ultraviolet disinfection to permit limit, an
effluent dosing tank with delivery system, and sludge holding and sludge thickening

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 9 of 24
M
5.0
tanks. The wastewater treatment plant is operationally flexible and capable of handling
loading variations. The equalization tank is capable of storing at least % of the
average daily flow. It is possible to suspend treatment while removing process elements
from service during periods of low loadings or in the event that maintenance is required,
although treatment may be negatively affected by operation with process elements out of
service.
An emergency power system is provided to
Valving has been provided to enable the a
event that process units require mainten
piping provide flexibility of operation and
Plant Aesthetics
The wastewater treatment plant will be locate
and golf course. Therefore, consideration ha
and odor control of the wastewater treatment
and contained within or beneath a locked
compatible with its surroundings. All mech,
the service building to minimize noise. 1
chemically scrubbed and filtered to remove oi
Description of Process
The treatment process includes the process
discussed below:
the treatment plant.
for to redirect flow within the plant in the
or cleaning. This valving and auxiliary
of maintenance.
1, in proximity to the dwellings, clubhouse
been given to the aesthetics, noise, safety
►lant. The entire treatment plant is secured
service building which is architecturally
tical equipment has been contained within
11 air discharged from the plant will be
as shown in the following list and
• Flow Equalization
• Primary Sedimentation
• Alternating Aerobic/Anaerobic (Anoxic) Treatment — Three Stages
• Up -Flow Sand Filtration
• Redundant Ultra Violet Disinfection System
• Effluent Discharge Works
• Sludge Holding Tank
• Sludge Thickening Tank
• Odor Control and Positive Treatment of all Process Gases
The process wastewater flows sequentially through the following chambers: (Figure 2)
1.
Flow Equalization
2.
Primary Clarification
3.
Aerobic #1
4.
Anaerobic # 1
5.
Aerobic #2
6.
Anaerobic #2
7.
Aerobic #3
8.
Anaerobic #3

The Cliffs at High. Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 10 of 24
9. Up -Flow Sand Filtration System
10. Redundant Ultra Violet Disinfection System
11. Effluent Pumping Station
12. Sludge Holding Tank
13. Sludge Thickening Tank
5.1 Screening
All raw waste entering the plant enters through a trash basket located in the flow
equalization tank and described in the information provided for this project.
5.2 Equalization and Flow Control
Raw wastewater is lifted from the flow equalization tank by one of two installed grinder
pumps (Manufacturer , Model hp, rpm, volt,
phase, 60 cycle). Either one will be able to handle average daily flow of gpm.
The alternate duty cycle of the pumps will facilitate equal wear on both pumps.
In sizing the grinder pumps, the following factors were considered. Average daily flow
at design capacity is gpd equalized at gpm. Total Dynamic Head ("TDH")
is determined as follows:
Top of plant = nominal elevation
Bottom of flow eq.
Top of head box '
Static Head
Losses in pipes and plumbing:
" - 90 deg. ell
- " - 90 deg. ell
pipe length = ' -ifdiameter and ' - " diameter
At gpm, " pipe loss is
it pipe loss is '/ '
Ell loss, " _ ' x =
it _ _
x
Total frictional loss:
" pipe: [ ' + ] _
'
if pipe: [ + ] —
Total Frictional Losses '
TDH = Static + frictional loss = +
or approximately ' TDH for pump sizing
Inasmuch as daily flow is fully equalized, peak flows are not a factor. Selection of the

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 11 of 24
(Figure ) with " impeller provides gpm (each) at
TDH (alternating simplex operation).
5.3 Head Box to Control Constant Forward Flow
Raw wastewater is pumped from the equalization basin to the head box, a tank having
chambers. Flow enters chamber No. , where inlet turbulence is reduced,
chamber no. contains a float switch control for sensing failure of the filling pumps
when activated (but not pumping) and providing switchover and alarm. Flow from
chamber no. flows under a baffle to chamber no. , a stilling chamber where
forward flow is divided between chamber no. and no. . Entry to chamber
no. is through a V -notch weir at the water surface. Water flowing into chamber
no. is ducted from the bottom of the chamber and becomes the forward flow
through the process. Water level in chamber no. and no. is controlled by a
variable rectangular weir between chambers no. and no. Varying the weir
level controls the rate of flow over the V -notch, and hence the rate of flow through the
plant. Water flowing over the variable weir enters chamber no. and is discharged
through the bottom to flow equalization.
5.4 Flow Equalization
Head box overflow returns to the flow equalization tank which has a working capacity of
gallons. This size provides working capacity to accept total daily flow in less than
16 hours, with capacity to continue treatment for more than 8 hours once incoming flow
ceases. This tank fills so long as raw influent flow exceeds the process forward flow rate
set by the head box. The grinder pumps located in the equalization tank operate in an
alternating simplex mode by a 4 float control system where the bottom float serves as a
pump protection kill switch and low level alarm, the second switch is the arm/off level,
switch no. 3 is the turn -on lead pump level, and switch no. 4 is the switchover-to-lag
pump and high level alarm switch.
The flow equalization basin is aerated and mixed by air supplied by a blower located in
the building. Air is supplied at a nominal rate of cfnVIin ft. to provide adequate
water velocity to maintain suspension of solids, or x cfin = cfin.
This amount of air is sufficient to maintain aerobic conditions which require about
cfin/1000 gal. or cfin at maximum capacity for this tank.
5.5 Primary Sedimentation
Screened and macerated influent is supplied at a constant rate via the head tank to a
primary sedimentation tank with overall plan dimension of ' x 'and effective
settling area of square feet with effective sidewater depth of Surface
overflow rates of gpd per square foot at average daily capacity produce settling of
solids in the gallon capacity tank. Precast 60 degree slope hoppers having a
bottom area of F square are utilized to concentrate solids which are subsequently air
lifted to a sludge digestion and holding chamber.

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 12 of 24
Details of the aerobic treatment computations are as follows:
Primary Treatment yields:
Raw influent= mg/1 BOD, mg/l N
Removal in primary clarifier = % BOD, % N
Influent to aerobic Tower I = . x = mg/1 BOD
x = mg/l NH3-N
5.6 Aerobic Treatment
Three trickling filter towers operating in series are designed to achieve removal of
ammonia and carbonaceous BOD to design specifications. The first tower utilizes plastic
media which has square feet of surface area per cubic foot. The second and third
use ft2/ft3 media. Each tower contains cubic feet of media with a
configuration of ' x ' x 'high. Solids sloughing off the media settle to
the bottom of the hoppers beneath the columns and are discharged to the subsequent
anaerobic reactor. Solids are collected in the bottom of the anaerobic reactor for
discharge to sludge holding via air lift pumps.
Each tower is provided one circulation pump, ( Model hp,
gpm, volt, phase, 60 cycle) (Figure ). One stand-by pump is
provided. Discharge from the pump is directed to a flow -dividing header which splits
flow equally between spray nozzles.
TDH has been computed as follows for the aerobic distributor for each tower:
Hydraulic loading of each tower is on the basis of a nominal gpm per square foot,
hence for a ' x 'tower, gpm is to be provided.
Piping Losses are:
Flow Friction Loss " diameter gpm
Static Head Losses:
Maximum Suction Head =
' to top of slab
Maximum Lift =
'to top of header
'Total Static Head
Dynamic Losses:
" diameter @ gpm
' pipe & side entry tee & x 900 ell
" (full)[ + +
x ]
Pressure Head loss through spray nozzle = '
Dynamic Head Loss = '
Static Head Loss = '
TDH '

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 13 of 24
5.7 Nitrogen Loading and Unit Processes
Organic nitrogen is both soluble and particulate with the soluble organic nitrogen mainly
in the form of urea and amino acids. Primary sedimentation acts to remove a portion of
the particulate organic matter. This generally will amount to approximately % of
the total nitrogen entering the plant. Ordinary secondary biological treatment will
remove more particulate organic nitrogen and transform some to ammonium and other
inorganic forms. Soluble organic nitrogen is partially transformed to ammonium by
microorganisms, but concentrations of - mg/1 are usually found in biological
treatment effluents. Browns l reports data to indicate this soluble organic nitrogen is fixed
within the crusted zone at the soil/bed interface once it reaches soil.
Stage I BOD and ammonia reduction
Use minimum water effluent temperature = degrees C
Raw flow through plant = gpm
Surface area of tower = ' x ' = square feet
Therefore, raw flow = / or gpm per square foot
Determination of the BOD removal fraction is performed, using B.F. Goodrich
Information Bulletin VC -5.0-477-1, by application of the Schultze Equation:
Ln (L./Lo) _ ' OD
Where Le is the effluent BOD
Lo is the influent BOD
K is the treatability factor, for domestic sewage
8 is the thermal factor, at degrees C
D is the height of the column in feet, feet
Q is the raw flow distributed on the top surface of the filter, gpm/square foot
Results of the analysis are contained in Table VC -5.0-477-1 of the BF Goodrich
Information Bulletin (Figure 7).
From Figure 7, % removal of BOD per stage is accomplished. BOD of effluent of
Tower I = % x mg/l = mg/l.
Minimal nitrification in Tower I will occur because of the presence of a large BOD
concentration (loading) of the tower. Heterotrophic bacteria are a dominant species in
comparison to the autotrophic nitrifiers, and their rapid growth will inhibit the
nitrification process.
1 Brown, K.W. & Associates, 1980. An Assessment of the Impact of Septic Leach Fields, Home Lawn Fertilization
and Agriculture Activities on Groundwater.

The Cliffs at High Carolina
Wastewater Treatment Plant
O&MManual, Section I
Page 14 of 24
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INFORMATION
General Products Division
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Figure 7

The Cliffs at High Carolina
Wastewater Treatment Plant O&MManual, Section I
Page 15 of 24
To determine the degree of inhibition we must first compute the biological BOD loading.
The biological loading is:
g/106 g x gal/day x lbs/gal #/day
There are 'x ox ' = cubic feet of media in the tower therefore the
loading is / — #/day/ W. The loading per thousand cubic feet is
important for computing the conversion of Ammonia -Nitrogen to Nitrate -Nitrogen in
each aerobic tower, since presence of DOD interferes with the Nitrification efficiency as
shown in Process Design Manual for Nitrogen Control. U.S. EPA Technology Transfer.
October 1975. (Figure ).
Ammonia conversion to nitrate is obtained by first using Figure (from the above
reference) which applies for minimal interference from DOD. Using the curve for
Midland, MI 13-19° C, we see that for ammonia -nitrogen concentrations above 2.5 mg/l,
3,800 A2 of surface area is required for conversion of one lb. of ammonia -nitrogen to one
pound of nitrate -nitrogen.
If we have fl of surface area per cubic foot of media, we would have:
ft, X W/fi3
f2/lb converted/day
#/day removed if DOD were not also present in the influent
To obtain the actual conversion, we must multiply by the nitrification efficiency, using
the most conservative value, in Figure , which is %.
Therefore, a conservative view would credit no nitrification in Tower I, which we assume
for purposes of this computation. Actual conversion of ammonia -nitrogen to nitrate -
nitrogen in Stage I does occur from our experience, and as shown in Figure , when
other than the most conservative data are selected, otherwise use of the first anaerobic
reactor would be moot.
Since Stage I influent nitrogen is
X 10-6 x x = #/day
Therefore, effluent from Stage I aerobic treatment will be:
DOD = mg/1, #/day
Ammonia -nitrogen = 1119/11 #/day
Nitrate -nitrogen =
Removal of nitrate -nitrogen in the subsequent anaerobic reactor is nearly complete, since
concentrations of DOD and bacteria are high; but we assume conservatively that no
further oxidation of DOD or ammonia -nitrogen occurs in any of the anaerobic reactors.

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 16 of 24
Stage II:
Influent = mg/1 BOD, Nday
mg/1 ammonia -nitrogen, Nday
BOD reduction will be, using Figure
% x mg/1= mg/1 effluent
The presence of BOD which survives the aerobic process is essential to the final
denitrification process in anaerobic reactor III, and is an essential feature of the
Aqueonics process. That is a key reason in the Aqueonics process for use of fixed film,
as it places a limit on polishing of BOD through surface and contact time limitations.
Nitrification in Tower II
The desired ammonia effluent is mg/1 or less in order to achieve the plant's goal of
mg/1 of total nitrogen. Therefore from Figure ft2 of surface is
required per pound nitrified per day. As in the calculation for Stage I, the BOD loading
is found to be / — #/day/1,000 ft2. From Figure the efficiency
will be 100%, as the loading is within the range at which the data were obtained.
We find conversion of: ft' x 30 Oft'
fi2/lb converted
lbs/day converted
Discharge from Aerobic I1 will therefore be:
BOD = mg/l, Nday
Ammonia -nitrogen = - = Nday
Nitrate -nitrogen = Nday
The nitrate is consumed in the second anaerobic reactor.
Stage III:
With minimal influent BOD, (the data of Figure were taken with BOD = -
mg/1) there will be no inhibition of the nitrification process by presence of BOD.
Tower III contains W of media which has ft IW. There is, therefore, a total
of ft2 of surface area. Since lbs. remain we have available ft2 per lb.
of influent ammonia. On first iteration, therefore, Figure tells us that an
approximate mg/l effluent ammonia concentration could be predicted, which is
less than the mg/1 goal and indicates acceptable aerobic tower capacity.
Anticipated Tower III discharge of BOD and ammonia will therefore be:
BOD < x % = mg/l, or Nday
Ammonia -nitrogen < mg/l, . #/day

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 17 of 24
Nitrate -nitrogen = mg/l, #/day
In the third anoxic reactor, the nitrate is consumed by facultative denitrifiers down to a
practical limit of mg/l, at which point the solution strength of both BOD residue
and nitrate are so low as to provide inefficient contact conversion. The same effect is
noted in Figure for the nitrification process.
Anticipated discharge from Anaerobic III will therefore be:
BOD < mg/1, or #/day
Ammonia Nitrogen < mg/l, #/day
Nitrate Nitrogen < mg/l, #/day
5.8 Phosphorus Removal
Phosphorus removal through alum addition is provided to meet an anticipated
specification of mg/l. Alum is provided through a solution feed apparatus for
alkalinity adjustment. The point of injection is to the suction side of the feed pump for
Tower III recirculation. The pump provides for thorough mixing of the alum with
forward flow. To provide flocculation, a fine -bubble diffuser is provided in the influent
chamber to Anaerobic III. Nucleation of floc is provided by the biological solids exiting
Tower III, and sedimentation is efficiently provided by Anaerobic III, the media of which
functions as a tube settler.
5.9 Sand Filtration
To meet the anticipated requirement of mg/1 Suspended Solids, sand filtration is
provided in the use of a Model filter. This square foot
continuous backwash upflow unit will be used at an overflow rate of less than
gpm/sf, but is rated at gpm/sf. To satisfy redundancy requirements, a dual air
supply unit for operation of the air lift shall be provided, with automatic switchover in the
event of failure of the lead unit. The unit is to be located in a chamber provided for the
purpose. Covered by the building, it is protected from the elements..
The predominating feature of this upwelling-flow rapid sand filter is its provision for
continuous backwash of the filter medium which continuously recycles from bottom to
top of the filter media bed. Experience has shown the filter to have rated capacity
well in excess of the gpm/sgft standard applied by Ten -States standards to rapid
sand filters, and we have elected an even more conservative application rate.
Recycle of sand is provided by an air lift which removes sand containing entrapped
filtered particles and deposits it (after light particles have been scrubbed from the sand
surface by agitation in the air lift) back on the top of the filter media bed. A depth of
" of filter media has been employed and is maintained continuously.
The light particles which have been filtered by the media and scrubbed from the sand
during airlift are returned to flow equalization. The manufacturers' specifications provide

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 18 of 24
that filter backwash is rated at 3-6% of forward flow. No additional mud wells, feed
reservoirs, surge protection, return pumps, or backwash pumps are required.
Discharge of the filtered effluent is directly to the ultraviolet disinfection unit, thence to
the flow measuring device, and to the effluent dosing tankage.
5.10 Supplemental Air
A total of three motor -blower sets shall be installed to meet supplemental air
requirements of the plant for the following purposes. The third motor -blower set has
been provided for stand-by purposes, and alternates with the supplemental air blower to
maintain it in operating condition.
Unit Process Reauired Air Suppl
Flow equalization aeration: cfin/lf x if cfin @ psi
Sludge holding: cfm/lf x if cfm @ psi
Air lifts: cfin (max) per lift cfm @ psi
(No more than 1 lift operates at one time) cfin @ psi
Air provided
cfin @ psi
Supplemental air shall be supplied at all times via ) blowers. The blowers
supply air for the purposes of sludge and equalization aeration and air lift pump
operation. blowers together will be of sufficient capacity to handle total plant
requirements. It is anticipated that in normal operation, blower will be dedicated
to flow equalization, and the other to sludge holding and the air lift pumps. In the
event that should fail; the stand-by unit(s) is available for either service.
The blowers are of the rotary, positive displacement type, ( Model ) each
supplying cfm of air at psi (Figure ). Open drip -proof motors,
hp, volt, phase, RPM shall also be supplied with each blower. Each
motorlblower assembly is mounted on a common steel base with a guarded V -belt drive
and pulley arrangement. Also included with each unit will be an air intake muffler filter,
an adjustable pressure relief valve, check valve, shut-off valve, and pressure gauge on the
air supply line.
5.11 Anaerobic Treatments
The "anaerobic" reactors are designed to achieve three functions. First, to function as a
tube settler for solids removal, second, to create an anoxic environment to accomplish
denitrification utilizing sewage as the organic carbon source and, thirdly, to achieve
permit limit "anaerobic" digestion of biomass.
Each of the "anaerobic" reactors contain plastic media having a surface area of
ft2/W placed atop precast concrete hoppers on fiberglass beams within the tankage.

The Cliffs at High Carolina
Wastewater Treatment Plant O&MManual, Section I
Page 19 of 24
Influent enters each "anaerobic" unit beneath the media and flows in a serpentine fashion
through the media (Figure ). A hydraulic retention time of 2 hours is maintained in
contact with the biota growing on the media for completion of the anoxic denitrification
reaction. A surface overflow rate of gpd/ft2 or less and tube settler effect of the
media makes these reactors extremely efficient clarifiers in addition to their primary
function in biological denitrification.
Denitrification conversion efficiency has been shown to be limited only by minimal
concentration of the nitrate substrate with which the colonies of facultative anaerobe
denitrifiers can be maintained. An effluent consistently less than mg/1 nitrate -
nitrogen has been achieved in similar facilities.
The process of anoxic denitrification is confirmed by EPA design data from the above
referenced handbook. Figure from that text shows that submerged hi&h-porosity
media reactors remove, at ° C, approximately pounds N/ /day. The
fixed media described in the EPA work where denitrification occurred was in a fluidized
bed of mm sand particles on which the denitrifiers grow. The biological coating of
denitrifiers caused the particles to grow to 3-4 mm in diameter, and occupy 50% of the
volume of the reactor. The media Aqueonics utilizes has less surface Denitrification -
Submerged Media area per unit volume, but the detention time for contact with biomass
is in excess of 2 hours instead of 6-1/2 minutes as in the fluidized bed, and adjustments
are made to increase the total volume thereby increasing surface area. To demonstrate
the Aqueonics process removal efficiency, one first finds the surface area per cubic foot
in the EPA reference system, and then compares it with that available in the plastic media
used in this system.
Using an average sand particle size of 3.5 mm, and assuming it to be spherical, we have,
computing the volume of a single particle
V = 4/3 pi (3.5 mm/2)3 = 22.44 mm3 =.02244 cm3
If the bed, by volume, is half -full of spheres, then
.02244 cm3/sphere x N spheres/cm3 = .5 cm3, or N = 22.28 spheres/cm3.
But 1 W = 28,317 cm3, so 1 ft3 will contain 630,949 spheres
To obtain the surface area within one cubic foot of sand media, As, it is only
necessary to multiply the number of spheres/ft3 by the surface area of the sphere,
which is
A/sphere = pi D2 = 38.46 mm2 =38 cm2 =.000409 ft2
Thus AS =.000409 x 630,949 = 258 fie/ft3 To compare this then to our fixed media
which has a surface area of ft2/ft3, we have
ft2/ft3 = of the specific reaction area.
ft2/ft3
But since the rate of removal is proportional to biomass contact (the reaction area),
and lb N/ ft3/day has been shown to be removed in the fluidized bed,
we can expect a proportionate plastic media removal rate of:

The Cliffs at High Carolina
Wastewater Treatment Plant O&MManual, Section I
Page 20 of 24
Volume Denitrification Rate (fixed media)
X
lbs/N/ ft3/day
lbs N per ft3 of fixed -film media/day
= lbs N/ft3 media
ft2/ft3 media
= lbs N/ft2 media/day
In the present design, each anaerobic reactor has sufficient media to provide 2 hours of
detention time. Thus, we have a design capacity in each reactor of ft2 of surface
per gpd, which is the nitrogen removal capacity of:
lbs N/ft2/day x ft2/gpd = lbs N per gallon per day
However, the influent N concentration, at mg/l, contains only lb/gallon x
X 10-6 = lbs N per gallon. Therefore more than sufficient denitrification
capacity exists within each reactor to complete the process: i.e., there is no process
limitation anticipated as a result of available surface area.
Solids which settle to the hopper bottom of the anaerobic reactors are periodically
removed via air lift pumps to the sludge holding chamber. The trickling filter towers
provide a release for nitrogen gas from solution so that solids are not lifted by entrained
gas after settling.
5.12 Alkalinity Control
Alkalinity in the form of carbonate is required by the autotrophic bacteria Nitrosomonas
and Nitrobacter in the aerobic conversion of ammonium to nitrate. Often, sufficient
alkalinity is present in the water supply to permit completion of the reaction for domestic
sewage treatment facilities. In cases where naturally acidic water sources are
encountered, insufficient alkalinity may be anticipated. You, as operator, should
periodically check alkalinity remaining in the effluent. This quantity should ideally
exceed mg/l, or you risk an inability to complete the nitrification process. The
alkalinity consumed in nitrate conversion is found experimentally to be approximately
mg/1 for each mg/1 of ammonia oxidized. However, the denitrification process and
respiration processes of the heterotrophic bacteria in BOD consumption replenish much
of the alkalinity by CO2 discharge, which goes into solution where it is utilized by the
autotrophs. In normal domestic sewage this quantity is usually sufficient to meet the
nitrifier's metabolic needs when acidity is sufficiently neutralized to prevent consumption
of alkalinity by the excess hydronium ion.
Additionally, data has shown that optimum nitrifier kinetics occur in the pH range of 7.5,
which is consistent with the optimum range for the denitrification process as well. It is
therefore clearly useful to the process to maintain pH in the slightly basic range up to 7.5
as a means to prevent consumption of alkalinity, as well as a means to achieve optimum
nitrifer and denitrifier kinetics. This is conventionally done through addition of hydrated

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 21 of 24
lime (Ca(OH)2), which is often added to the water supply for other reasons. If sufficient
quantities are provided to achieve the proper pH for the treatment process, then further
additions are not required at the sewage treatment plant. If, however, influent pH is low,
equipment has been provided in the form of a solution feeder to add a hydrated lime
solution to flow equalization, where it is stirred and mixed, using safety precautions as
described in subsequent sections of this manual. With the assumption the influent water
may have a pH as low as 6, or 1 ppm H+ ion, and we wish to go to a hydroxyl ion
concentration (pH = 7.5) or .5 ppm OH, we would have to be prepared to add 1.5 ppm of
OH, or .75 ppm of Ca(OH)2, which converts, roughly to
.75 ppm x 8.34 lbs/gal x MGD x 74/18 (AMU Ratio) = lbs/day
A solution containing lime can be provided by a Model solution feed pump,
with gallon solution tank, with mixer and low solution level alarm. Since the
solution could be fed as a 10% solution (solubility of Ca(OH)2 at 200 C is 160/0),
approximately /.l = gallons/day might be required to properly control pH.
The meeting of the needs for pH control still does not address the issue of alkalinity
requirement (as CO3), except peripherally in that natural alkalinity will not be consumed
in pH neutralization. Since residual alkalinity cannot be assured in a fundamentally
acidic water supply, we should be prepared to make up for lack of CaCO3 by adding
alkalinity. This is customarily done with the addition of soda ash (sodium carbonate,
Na2CO2) because of the relative insolubility of calcium carbonate. Since soda ash and
lime are complimentary, both materials can be added as required, or only soda ash need
be used. If pH adjustment is not required then alkalinity adjustment alone can be
accommodated by the solution feeder. Control of effluent pH and alkalinity, which
should be, respectively, 7.3-7.5 and 60 mg/1 or more for optimum nutrient removal, can
be confirmed through periodic analysis of effluent samples.
5.13 Effluent Pumping Chamber
Two effluent dosing pumps located atop the dosing tank alternately feed the discharge
drip system. Each dosing pump, Model Hp, volt,
phase, gpm at TDH) (Figure ) shall be connected to one discharge
piping as designed by others. The alternating simplex control system shall be operated
by four float switches in the dosing tank and shall control the dose, alternate the pumps
and provide for automatic switchover and alarm as in the flow equalization control
system described in section . The volume available in the dosing tank,
gallons, provides control over dosing volume, frequency, and duration.
5.14 Ultraviolet Disinfection Dual Units)
The proposed system incorporates 4 lamps in two Model Idisinfection units
which are required to provide for disinfection needs, and including the redundancy
requirement as stated in . There are two intensity monitors and two power
distribution centers. The UV system uses low pressure mercury vapor Slimline lamps
producing 7,500 u. watts/cm2 of 254 nm UV at 100 hours and have an expected lifetime

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 22 of 24
of 8,860 hours at which time the output will be 65% of lamp output at 100 hours. Lamp
power requirement is 85 watts per lamp, including power supply. A dose of 11w-
sec/cm2 is provided. Units are operated alternately, and each unit is fed by sand filter
with crossover connections to allow one unit to be removed from service for cleaning or
repair.
5.15 Sludge Holding Chambers
Sludge is pumped to the chamber, having a capacity of gallons, from the primary
clarifier and anaerobic reactor units by means of timed air lift pumps. Experience has
shown process biological sludge production to be at a rate of <.15 lb/lb of influent BOD,
or approximately the same as extended aeration designs. With an influent loading of
gpd @ mg/1 BOD, up to lbs/day of BOD is present, for a sludge
production of lb/lb x lb/day = lbs/day at 4-1/2% solids. This
produces lbs/day/( lb/gal x .045) = gallons/day biological sludge. In
addition, influent suspended solids contribute up to lbs/day, of which 60% are
removed in primary clarification as primary sludge. This contribution of .60 x
lb/day = lbs/day at 2.5% solids provides for an anticipated sludge volume of
lb/day/( gal/lb x .025) = gallons per day of primary sludge. Total sludge
production is up to gpd from both sources. This sludge is further stabilized and
concentrated. After settling and concentrating the sludge, the supernatant liquid is
removed by decanting with an hp Model decanting pump suspended
on a cable in the tank and raised and lowered by a winch. This process allows the plant
to produce sludge which has 4-1/2 - 7-1/2% solids for disposal at a projected rate. of
approximately gallons/day or less, depending particularly upon the influent
suspended solids concentration.
Normal sludge holding capacity objective is days. At this plant's rate of
production, capacity is provided for more than days of aerated detention/digestion
which provides a stabilized sludge discharge to be disposed by licensed hauler to an
approved facility for disposal. Aeration of sludge holding for aerobic digestion, odor
prevention, and suspension of solids is provided at cfiin/lf x If, or cfm
for gallons, or cf n/ gallons of sludge ( cfiin/ cubic feet).
Sludge will be periodically removed by licensed hauler for transportation to
facility or other licensed recipient with which the hauler has a contractual agreement.
6.0 Air and Gases
Air is required for operation of the aerobic biological processes. As the plant is totally
enclosed, process air must be drawn through the system. It is first drawn through the
tankage air space and then through the trickling filters sequentially to scrub the air of
odors and gases produced by the process and to provide oxygen for the aerobic biological
process. An exhaust fan is located above trickling filter III. In cold weather this pathway
also warms the air prior to contact with biological surfaces in the trickling filters, which
permits high rates to be maintained even in coldest weather. A granulated activated

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section I
Page 23 of 24
carbon and potassium permanganate air filter system is used for final air polishing prior
to discharge from the building.
7.0 Process Controls
Flow through the plant is controlled and protected by high and low level control mercury
float switches. A sensor in the head box provides protection against pump failure and
activates an alarm indicator. A high level process alarm float switch in the primary
clarifier indicates blockage or flooding of the process chain and activates an alarm
indicator. Sensors in the lines to the aerobic reactor sprayheads indicate pump failure or
line clogging and activate alarm indicators. Automatic controls all have Hand/Off/Auto
override switches for testing and emergency override. In normal operation the status
display shows which devices are on. If there is a malfunction in the plant, the red alarm
light will come on, the alarm will be transmitted on the phone line, and the alarm signal
in question will be indicated on the Panelview status display. This alarm indication will
remain until proper function of that device has been re-established. The alarm light can
then be reset.
An important feature of the Aqueonics Plant Controller is its ability to communicate via
telephone. When an alarm condition arises, the unit can automatically dial up to three
telephone numbers. One of the numbers is that of the local plant operator or maintenance
agency. A voice message will indicate the nature of an alarm requiring immediate
attention.
An ultrasonic recording and totalizing flow meter and primary V -notch flume device is
installed. The device may be downloaded to the printer, or to magnetic disk media on
demand. It stores data for up to days.
A sampling port, , is located in the
8.0 Concrete
Tankage is constructed of reinforced precast Portland Cement ASTM Type VII concrete
with compression strength of 4,000 psi @ 28 days and is adequately reinforced to
withstand normal soils and hydraulic forces imposed on the structures. Groundwater is,
and should be maintained below the plant footings.
9.0 Emergency Power System
Determination of the size of the generator unit required during emergency operations is
as follows:

The Cliffs at High Carolina
Wastewater Treatment Plant O&MManual, Section I
Page 24 of 24
User HP No. of Operating KW
Units Units Total
House Circuits
Simplex Grinder Pumps
Recirculation Pumps
Plant Air Blower
Effluent Lift Pumps
Control Panel & Lights
Chemical Feed
Total Load
The Programmable Logic Controller (PLC) and control panel provides automatically
phased start-up on timed delays when operating on the emergency generation system,
thereby limiting peak starting loads.
Sizing of the automatic transfer switch is determined by the larger of the above loads, or
the normal load. When on normal operation the load schedule will be:
Transfer Switch Design:
User HP
No. In Amperes Total KW
Service PI Hl P2 Total
Lift Station
House Circuit
Grinder Pumps
Recirculation Pumps
Bio Blower
Effluent Dosing Pumps
Control Panel
Sludge Pum
Blowers
Sand Filter
UV Disinfection Unit
Maximum Current Leg
Emergency generation equipment output has been sized to include those
anticipated loads of the sewage treatment facility. The emergency generator is a
KW -powered unit with integral and matching
automatic transfer switch Model , with automatic exerciser.

Operation and Maintenance
The routine operation of the plant will consist of inspection of plant processes and equipment,
solids handling when needed, replenishing of chemicals, wastewater sampling, housekeeping and
maintenance, and recordkeeping.
Even more important to successful operation of the plant is an understanding for and empathy
with what is going on in the system of which your plant is a part, and why as licensed operator,
this must be your responsibility. Crucial to you successful operation will be a continuing
observation of your influent and dialogue with Clubhouse management regarding their effluent
with emphasis on the impact of their changes on your plant operation. Their changes must
consider impact on your operation, and you must be prepared to both convey and discuss your
needs with the occupants and owners. Prepare in advance for heavy usages from special
clubhouse events by being aware of what will be happening there.
Entering the plant, the operator should smell and visually determine that there are no existing or
potential problems. The operator's daily checklist describes items to be included in this
inspection. You may wish to add others. The following describes in greater detail the items to be
covered in this inspection.
1. Control Panel Display — This is the information center of the treatment plant. The display
should be checked daily for alarm lights and plant status.
2. Flow Equalization Basin — The sewage level in the flow equalization basin should be
between the high and low level sensors. The inlet pipe should not be flooded. Check and
clean the bar screen. Observe the air diffusion for approximate uniformity of flow along the
width of the tank. Check the V -notch and weir in the head box for plugging and for proper
flow. Remove biological growth or solids on the orifices. Check for excessive foaming or
chemical odors in the equalization basin. This could be indicative of toxicity and potential
process problems.
3. Clarifiers — Remove debris from the collection weir. To remove surface scum, use hose, rake
or squeegee to remove or move to skimmers while skimmer is turned on. In the anoxic
reactors, skimmers are ineffective. Use instead the hose and spargers to cause sludge to settle
where it can be removed by air lift. Excessive scum usually indicates that the sludge is hung
up on the hoppers. To remedy, use squeegee and/or "burp" the offending sludge lift. If the

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section II
Page 2 of 10
problem persists, increase the duration or frequency of sludge lift cycle. The media should
serve to break up floating sludge, allowing it to resettle in the anaerobic reactors. Over time
the anaerobic reactors may build up an excessive bio -film growth which may plug the fluid
passages. Air spargers have been provided to dislodge this biomass periodically as required.
Sparge by simultaneously "burping" the air lift and opening the sparger air valve in bursts to
scour the film from the media surface.
Note that a surface layer of fine reddish -brown bubbles in anoxic reactors is indicative of a
healthy denitrification process and is of benefit to the process through oxygen exclusion. This
film is to be nurtured and cherished.
4. Aerobic Towers Open the access doors on each tower periodically to observe the media
and check the spray nozzles for clogging. Most particularly, if the pump pressure increases,
the nozzles should be checked. It is important to maintain clean nozzles to assure sufficient
process flow and distribution. The spray pattern should cover the entire surface with a flow
of greater than or equal to gpm/ft - and less than or equal to gpmlfe. The odor
should not be offensive. Psychoda fillies will inevitably be present in significant numbers and
will bloom in fall. This should not present a problem outside of housekeeping.
5. Sludge Transfer and Holding Tank — Sludge collected in all clarifiers is periodically airlifted
to the sludge holding tank. The frequency and duration of each lift operation is controlled by
adjustment of the respective air supply valves. The tank will naturally fill with a mixture of
sludge and water. A decanter is used to return the supernatant water to flow equalization and
to thereby concentrate the sludge, which is also aerobically digested in the sludge holding
tank. In the event the operator wishes to manually draw down the water level in the sludge
holding tank the following procedure should be followed: (1) shut off air to the tank (2)' allow
solids to settle (a definite interface should develop) (3) place the decanter pump to the depth
you wish to decant (4) turn on the decanter only long enough to allow the supernatant to
return to the equalization tank (5) return air sludge holding tank diffusers. All airlifts should
be periodically checked for proper operation. This may be done by inspection of the
discharge pipe flow during activation of each air lift. The sludge holding/thickening tank has
been fitted with a pump on an adjustable winch to enable complete dewatering or decanting
to any level. Care must be provided when using this unit so that the pump does not run dry or
pump thickened sludge. Either types of misuse may severely damage this pump.

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section H
Page 3 of 10
6. Mechanical Equipment — check the drive belts on the blowers for cracks, wear or slippage
and repair as necessary. It is a good idea to keep an extra belt of each size on hand at all
times. Make sure the relief valve is not blowing off excessively. Excess blow off probably
indicates closed valves or plugged diffusers. Check the main blowers, flow equalization
blower, bio -blower, and pumps for overheating and proper lubrication. Check the potassium
permanganate media in the bio -blower. It turns color from purple to brown to. gray as it is
used up. Every four to six weeks this media may have to be changed. To do this, take out the
trays and discard their contents. Refill the trays with fresh media and return them to their
appropriate slots. More frequent changing is a possible indication that anaerobiosis is
occurring in the plant or that there is an influent problem.
7. Low Air Pressure — The sludge tank blower is monitored by a low pressure alarm indicator
set to operate while the blower is on. Since flow equalization cannot maintain a given back
pressure, a sail -type flow switch has been installed in the main header which serves a similar
function, based on flow rather than pressure. The blowers are arranged such that one blower
supplies flow equalization, and the other serves sludge holding and airlifts. Normally -closed
valving interconnects the two systems so that fluctuations in the depth of water in flow
equalization does not affect performance of airlifts.
In the event blower fails, power will be shut off to the motor of this blower, and the alarm
will be activated . While repairs are performed, valving is provided to connect the blower air
system. A backup blower assembly is provided for replacement.
To troubleshoot, try to start failed blower on manual. If motor doesn't run, it is an electrical
problem; if motor runs but no air, it is a mechanical problem and the blower must be
checked. Be sure to check belts for slipping, as this is most often the cause of low pressure
when motor is running. Consult Blower d & M Manual supplied with this information.
Power must be turned off to the blower at the kill switch before beainnin to work on it.
8. Grinder and Dosing Pumps— These pumps are automatically set so if one fails, the other one
will come on. Both pumps may be operated on manual, BUT WATER LEVEL SH®ULD
BE WATCHED to prevent level of water in tank to EVER be pumped lower than pump
itself while on manual. Should this happen, pump will be improperly cooled, and damage to
the motor any occur. If pump is allowed to run dry, the seal may be damaged.

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Wastewater Treatment Plant O&M Manual, Section II
Page 4 of 10
Manual operation will bypass the normal float switch control system. However, the control
relays are wired directly from the uppermost and lowermost float switches in flow
equalization to the starter relays in the control panel. Thus under manual control, the
lowermost low water kill switch will cause either operating pumps to stop. Similarly, the
high level alarm will alternate both pumps without interaction with the control system as
long as the HOA switch is on H or A and as long as the low level kill switch is not activated.
Neither grinder pump will operate when in the "off' position, regardless of float position,
however the lock-out/tag out disconnects should be used when working on the pumps.
Manual operation will require more operator surveillance. If both grinder pumps have failed,
the plant will continue to operate by gravity flow. Such operation could result in peak
overloading of recirculation systems and clarifiers, resulting in possible noncompliance with
discharge specification limits, since flow equalization will be inoperative.
AGAIN — DO NOT LET SUBMERSIBLE PUMPS RUN WITHOUT WATER
CONTACT. To do so will cause the seals to fail and/or the motors to overheat.
The submersible are removed by disconnecting the union after the vertical discharge pipe and
disconnecting the electrical connection near the hatch opening. Pipe and pump are removed
(and replaced) together and reconnected at the unions. When reinstalling all pumps make
certain that the rotation is in the proper direction. Grinder pumps will pump water in either
rotation, but the cutter will not work properly with the wrong rotation, leading to jamming
and possible electrical overload and burnout. If a pump fails, test the cause by the following
procedure:
a. Check electrical — is pump getting required current? If not, check breakers and float
switch control. If theses function properly, check control relay for proper operation.
Otherwise, the problem is in the wiring.
b. If pump has power, attempt a momentary rotation reversal to see if impeller is
jammed. If this does not release the jam, the pump must be pulled.
c. Check for foreign material plugging or jamming the grinder.
d. Whenever grinder pumps are pulled, check condition of cutter, replace as needed.
e. If total failure is noted, replace with like piece of equipment as it can be put back into
the same system.
f. Consult 0 & M Manual from suppliers for further details of maintenance.

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Wastewater Treatment Plant O&M Manual, Section H
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9. Recirculation Pumps - Pressure sensing gauges and switches are placed downstream of the
recirculation pumps to monitor pressure variations. If operator notes indadequate pressure on
gauge where water goes to towers, then pump has failed or inlet suction has plugged. This
failure will also be indicated on the plant alarm system. Check to see if motor is running. If
not, check breaker or heater in main panel. If motor is running but not pumping, the checks
pump. If excessive pressure is observed, the spray nozzles have plugged. Spray nozzles
should be checked and cleaned regularly. The pressure switch will send an alarm signal if the
pressure is either too high or too low. Flow rate may be regulated the pinch valves in the
discharge line to control surface application rate. As the pressure drop across the nozzles is
very little, your alarm gauge may not be sufficiently sensitive to reductions in pump output.
Therefore checking of spray pattern adequacy is your best gauge of pump performance.
Check suppliers O & M Manual for maintenance procedures on pumps.
10. Bar Screen — Periodically clean bar screen with a rake. Be careful not to allow rakings to fall
into the equalization tank. If rakings consistently fall into the equalization tank, matting and
balling of the cellulose material will occur and lead to pump clogging or improper diffuser
operation. Collection of strings and rags can be effectively performed by suspending a loop
of barbed wire in the flow equalization basin to catch such items as they are circulated by
aeration. Wire must be periodically cleaned or replaced to be effective.
11. Airlifts - maintenance of the airlifts is critical to the proper operation of the plant. The most
common cause of sludge handling problems is due to improper airlift operation. The airlifts
should be checked for clogging periodically. The frequency will be determined by the
amount of solids loading. The primary clarifier should also be periodically squeegeed to
prevent ratholing and septic sludge. Should you notice mats of gray or black sludge floating
in a clarifier this will most likely be due to improper airlift operation or ratholing. Ratholing
is a term used to describe when an airlift does not evenly remove solids from the hopper and
thus allows a portion of the hopper to retain sludge. Retained sludge becomes septic and ,
with liberation of gas, will float to the surface or underside of the anaerobic media or plug the
airlift. The remedy is to squeegee the hoppers to dislodge jammed solids and/or "burp" the
hopper by closing the valve in the sludge discharge line which causes air to be forced out of
the airlift intake, thereby dislodging solids. If "burping" does not clear the lift, it can be
rodded out through the cap at the top of each lift which can be removed for this purpose. The
use of the spargers in the anaerobic reactors to dislodge excessive sludge buildup on the
submerged media has been described previously.

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Wastewater Treatment Plant O&M Manual, Section II
Page 6 of 10
12. Chemical Feeds — A solution feed tank and metering pump have been provided to control
alkalinity and pH. Lime and/or soda ash addition in a slurry is provided for alkalinity/pH
control. Optimum discharge pH (when added to flow equalization) is 7.3-7.6 Feed rates
should be adjusted to achieve this value.
13. Nitrogen Removal Methods — Unlike domestic sewage treatment systems, it is anticipated
that TKN influent composition may contain significant quantities of convertible ammonia,
which must be nitrified. This treatment plant has been designed to provide a variety of means
for such removal. Among the arsenal of means at your disposal, aside from the process
design described in the design report section of this manual are the following means which
may be employed using existing facilities.
Aerobic Capacily Au emg ntation
a. Ammonia Stripping — Water as supplied naturally from the wellhead has a pH in the
5-7 range. This makes it feasible to perform air stripping in flow equalization
facilities. Normally, alkalinity is added to flow equalization. If air stripping of
ammonia is desired, the pH must also be raised to 10, but it will require lowering to
the 7.5 — 8 range at the discharge from the main head box for direct distribution to
Aerobic Tower No. 1. This will maintain the high pH required for stripping in flow
equalization, but pH must then be artificially lowered for biological performance
through acidification, as the high pH is toxic to bacteria. Phosphoric acid is a good
candidate for such use, as phosphorus is not limited in the discharge. It should be
remembered when operating in this mode, that alkalinity (soda ash) may still be
required, as well as the neutralizing acid, which can also eat your alkalinity.
b. Aerobic Digestion in Flow Equalization — Equipment has been provided to enable
utilization of flow equalization as an aerobic digester for pretreatment of influent
organic materials. Sufficient air has been provided to accomplish this mission, and
detention times which exceed 1 day are available. To accomplish such treatment,
sludge from sludge holding is returned to flow equalization through the decanting
equipment provided. Biomass will increase naturally in this treatment unit, but
wasting will be continuous with the forward flow. Sludge wasting cycles in primary
clarification should be carefully monitored when operating in the mode to prevent
overloading of this treatment unit by the increased sludge load.

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Wastewater Treatment Plant O&M Manual, Section H
Page 7 of 10
All of the process considerations which are normal to conventional activated sludge
plants or contact stabilization plants would be required to be observed when operating
in this mode, including the maintenance of proper F/M ratios and MLSS
concentrations to achieve the degree of pretreatment desired. This mode of treatment
can be expected to considerably reduce BOD and ammonia into your treatment
process, reducing the aerobic load on the owner treatment units concurrently.
c. Redistribution of Air — When operating in the mode in which flow equalization is
being used for aerobic treatment, you will have several choices of operational mode:
This reduces the digestion load on the sludge facilities, and allows you to do two
things:
• Operate the plant in a contact stabilization mode using the sludge holding tank
as the aerated storage/digestion stage.
• Redistribute the blower air supply to selectively apply more air to flow
equalization, and less to sludge digestion. This air supply balance would be
determined by DO concentration in the various basins to maintain a
concentration suitable to optimum digestion performance (greater than 2
mg/1). In this mode, it is recommended to utilize fine bubble diffusers in the
place of the broadband diffusers supplied. Such diffusers provide significantly
improved oxygen transfer to the liquid at the penalty of somewhat greater
maintenance. Fine bubble diffusers also aid in the stripping efficiency for
ammonia removal.
d. Aerobic Tower Air Supvly — Your plant has been supplied with a 1,000 cfm Bio -
blower discharge blower. If it is found that excessive BOD strength increases tower
BOD above 400 mg/1 then augmentation of airflow in tower I may be called for to
prevent zero -order limitation of BOD removal. Airflow through tower I to counteract
this potential deficiency can be accommodated by enlarging the capacity of the
discharge bio -blower.
14. Nutrient Requirements — A nutrient balance which maintains a BOD:N:P ratio of 100:5:1
is always a requirement in biological systems to achieve a healthy and effective biomass.
Most domestic sewage sources produce a natural balance of nutrients. In commercial or
industrial sources, there can be an imbalance produced in which a deficiency is
encountered. You as operator should be aware of this potential problem area and be
repaired to deal with it. Phosphoric acid addition is the conventional means for

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Wastewater Treatment Plant O&MManual, Section II
Page 8 of 10
Fey
vwuel
r phosphorus addition, and this might be combined with an ammonia stripping operation
described in the section on nitrogen removal methods.
Additionally, as described elsewhere, alkalinity is a metabolic requirement for nitrifiers,
and sufficient quantities must be provided to maintain a minimal discharge of 60 mg/l. It
should be noted that phosphoric acid addition will require additional alkalinity and pH
adjustment, and may produce problems with its removal.
Anaerobic CaLacity Augmentation
a. Presentation of surface — The greatest cause of inadequate anaerobic performance is
short circuiting which limits detention time and surface exposure. Periodic removal of
excess biomass is required to prevent plugging or blockage of some of the parallel
paths through the anaerobic media. Confirmation of dwell time and surface contact
can be performed by dye test to be greater than or equal to at least 2 hours at full flow
(75 gpm). Routine checking for abnormal flow patterns as described elsewhere in this
manual is a good practice to forewarn you of any forming problem.
b. Use of the nitrogen gas bubble layer to prevent re -aeration — The denitrification
process will naturally release nitrogen gas bubbles which will form a thin foam layer
in the surface interstices of the media. This foam layer has a beneficial effect of
providing a pure nitrogen layer which separates the air and water interface. This
prevents oxygen from diffusing into the liquid to compete with nitrate as the oxygen
source for the denitrifiers. A good foam layer is an indication of good denitrification
performance and a benefit to the process. Uniformity of the foam layer is a gauge to
proper flow distribution.
c. Addition of BOD substrate — In cases of high nitrate loading and inadequate BOD,
BOD must be increased in order to achieve denitrification. The customary feed
material for this purpose is methanol. However, methanol in excess may be toxic to
nitrifiers, and is undesirable in the discharge. This material can be used for the
purpose of gravity feeding to anoxic reactors where appropriate to alleviate this BOD
deficiency. Stoichiometrically there is a least a 4:1 requirement of BOD per mg/1 of
nitrate to be removed, which would be increased by the DO concentration entering
the reactor. Excess BOD can be fed to Anaerobic lII because there is no limitation on
discharge BOD, and because excess BOD at this point will not affect any other plant
process. Addition of BOD at the first anaerobic should be unnecessary, and addition

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Page 9 of 10
of excess BOD at the second anaerobic could reduce the nitrification efficiency of the
third aerobic. Therefore, addition of excess BOD at this point is not recommended.
d. Adjustment of recirculation — Excessive nitrate loads on anaerobic reactor III can be
reduced through increased back-to-front recirculation. It is advantageous to recycle
greater flows to the front of the plant to thereby reduce nitrate concentration to
anaerobic III as much as practicable without exceeding zero -order denitrification
kinetics in either anaerobic I or II; and this practice should be applied especially
under low or under loading conditions. Insufficient BOD following Aerobic III
should be the norm under such conditions, making denitrification require BOD
addition in anaerobic III. This need can be minimized through increasing the ratio of
recycle: forward flow. The anoxic reactors have each been designed for 29 gpm flow
at 2 hours detention, which will permit a recycle ratio of up to 1.2:1, and 2.29
#/day/1000fl of nitrate removal capacity. As much nitrate as practicable should be
targeted for removal in the first two anaerobic units.
e. Denitrification in the aerobic reactors — Under conditions in which air has been
excluded, nitrification is practiced in aerobic towers of this design, and can be
accomplished here as well, though connections are not presently installed through
which air can be completely excluded from only tower III. Experience with such
reactors has shown , however, that in towers in which DO concentration in the
discharge does not exceed 0.5 mg/l, significant denitrification can be accomplished in
towers in which nitrification is also achieved. It is believed that this is accomplished
by layering the bio -film in which denitrifiers underlay the nitrifiers. The nitrifier layer
excludes oxygen from the denitrifiers and consume oxygen while producing nitrate
which is passed inward within the film where it is consumed by the denitrifiers which
also consume biomass as their carbon source, together with BOD which is passed
through the bio -film.
Although the minimal DO must be carefully controlled through throttling of the bio -
blower airflow, this operational mode may be applied under conditions in which
aerobic capacity is excessive and anaerobic capacity is insufficient. Such a case might
be where the flow equalization basin is being used in an extended aeration or contact
stabilization mode, and tower aerobic capacity becomes surplus. Under such
conditions, ammonia concentrations may reach discharge standards after the first
tower, for example, leaving towers II and III free for denitrification. Another such
condition might be where influent BOD concentration dropped significantly, with a

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Wastewater Treatment Plant O&M Manual, Section II
Page 10 of 10
corresponding increase in nitrogen. The operator should be aware that function of
these units can be converted under certain conditions to meet special requirements.
Aqueonics should be contacted to assist you in such a design change.

ROUTINE OPERATION CHECKLIST
A. Introduction
Your Aqueonics plant after start-up is designed to operate continuously and without constant
attention to process. The process is self-adjusting, so long as the pumps, blowers and equipment are
operating properly, and your housekeeping handles the solids produced. If radical changes in
influent conditions occur, you may wish to consult the start-up instructions to keep your plant
operating at maximal efficacy.
B. Daily Operation Checklist
The following is a daily checklist of items which you should do. It should take no more than 15 to
20 minutes a day, and will greatly reduce the need for emergency attention and repairs to the
mechanicalequipment.
The auto -dialer emergency alarm system will alert you between visits if an emergency condition
exists to allow you to effect repairs promptly and thereby minimize the possibility of non -conforming
discharge. A description of what the probable cause and remedy for each alarm co

The Cliffs at High Carolina
Wastewater Treatment Plant O&MManual, Section III
Page 2 of 4
DAILY OPERATOR'S INSPECTION ROUTINE CHECKLIST
1. On approach to plant, check for odors. Determine source and rectify.
2. On entering plant, did you note any unusual odors? Electrical overheat, septic, oil, rubber. If
so check for source.
3. Check control panel for alarm lights and for correct green lights. Make note of all caution
and alarms lights as a check list. After correction, make note of causes and response in the
daily log.
4. Check PLC data log for alarm reporting and make note of any alarm reporting in the daily
log.
5. Check your preventive maintenance schedule for specific equipment to be lubricated, etc.
today. Perform the required operations.
6. Do quick tour of equipment to check status.
Look:
a. At gauges to see if operation is in correct range
b. At flow meter to check continuity of operation
c. For leaks
d. For lube or rubber throw -off
e. For discoloration, defects, or damage
f. For loose, worn, or cracked blower belts
g. For liquid level in solution feed tanks
h. For appearance of each unit process discharge to observe proper function
i. Check and record flow equalization pump hour meter reading
Listen:
a. For bearing or gear noise
b. For air leaks or excessive blow -off
c. For unusual equipment operation, such as air starvation, excessive labor, cavitation
Feel:
a. Motors for excessive or too little temperature.
b. For adequate air draft and interior temperature
7. Periodically (once per week, or oftener if problems are encountered) check tower spray
distribution for uniform and sufficient_ distribution. Clean nozzles if needed. Are bacteria on
media of normal color?

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Wastewater Treatment Plant O&M Manual, Section III
Page 3 of 4
8. Periodically (once per month) open the bio -blower and check potassium permanganate filter
top tray to see if filter media is still active.
Change when required by emptying and refilling all trays. Bottom three trays take GAC.
Top tray takes KMn04 pellets.
9 Check bar screen. By inspection, is the water level in the flow equalization tank within
normal limits?
10. Record daily water usage, look for trends which could affect plant operation, adjust head box
as needed. Confirm with run-time total from hours meters.
11. Check flow equalization. Is water level within normal limits?
Check for unusual odor or appearance indicating unusual influent composition. Is there any
evidence of high level excess?
Is air diffusion uniform along the length of the tank (you may need a flashlight to observe
this). Liquid should look like raw wastewater, and should not have anoxic or chemical
odors. If it contains much sludge you probably need to waste.
Check pH and correct alkalinity if needed.
Are float switches floating freely and unencumbered?
12. Check head box. Is float switch floating freely? Clean out solids and hose off weirs. Scrub
down splash growth.
13. Check primary clarifier. Skim and waste sludge as needed. Do you have floating sludge?
Check source:
a. Is sludge hanging up in hoppers? If so, squeegee offending hopper
b. If not hanging up, increase air lift time cycle or waste sludge more frequently for
appropriate hopper
c. Is level OK, and is high level alarm float switch moving freely?
d. Is color/consistency of effluent normal? Hose weir, baffles, and sidewalls as appropriate.
14. Check anaerobic reactors. Look for abnormal flow patter (may indicate blockage of
underflow channels, or channeling through media). If surface sludge is observed, check for
source.
Note: if effluent sample is scheduled, take it prior to cleaning weirs or disturbing flow in
these reactors.
Periodically (once per month) check for sludge buildup on media surfaces. You will need to

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Wastewater Treatment Plant O&M Manual, Section III
Page 4 of 4
use the spargers approximately every six months to prevent blockage of pathways through
the media. Do not wait until media is -completely blocked to perform this maintenance.
15. Check sludge holding tank. Check sludge blanket level. Waste if you have a truckload —
don't wait till the whole tank is full.
Decant supernatant. Remember, if the sludge blanket gets too high, you will have difficulty
in keeping the solids in sludge holding, and little volume into which to waste sludge form
your clarifier.
Check proper operation of sludge lifts occasionally by observing a sludge wasting cycle. See
that all lifts are operating, and that sludge discharge is complete before each wasting cycle
has finished.
16. Check sand filter equipment for operation and cleanliness.
17. Check operation and cleanliness of UV disinfection equipment.
18. Check effluent dosing tank. Is liquid within normal limits? Are floats hanging freely?
19. Check alkalinity feed (if used), is it functional (if not functioning), and is material supply
adequate.
20. Make note of needed supplies and place on order any with delivery times which approach the
duration of the supply on hand. Order maintenance materials used for stock supply.
21. Pull necessary samples according to test schedule.
Check daily punch sheet to see if sample results have been received from lab, and if all
necessary reports and test required by permit have been taken, prepared, or reported, as
appropriate.
22. Take data measurements and complete operator's log. Be sure to note date of your
observation of abnormal conditions and any change in operation parameters or settings. Note
what you observed, what you did, and when it was done.

OPERATIQNAL DATA GATHERING
Aside from the data required by permit, which must be reported, you as operator will require certain
information which will enable you to determine the source of operation difficulties if they should
arise. Simply knowing that something is wrong won't generally give you the information you need
to know to fix the problem. The sample testing recommendations below will help you to pinpoint
the general causes of potential non -conforming operation before, hopefully, non -conforming
operation actually occurs. It will over time also give you an operational background which will
allow you to predict and ward off problems so that they will not occur.
In fixed film reactors, treatment capacity is fixed by the maximum surface area available. This plant
has been designed for certain conservatively chosen maximal values of flow, BOD, and ammonia in
the influent based on typical domestic sewage known compositions. Loadings which differ
significantly from the design values can be handled by your plant only when they do not exceed
design values when the proper adjustments are made. Since it is difficult to predict in advance what
particular conditions you may experience, so long as loadings do not exceed design values
Aqueonics can assist you in making the proper adjustments to achieve stable operation at any
reasonable flow rate or composition.
One key factor will be to adjust the flow rate through the plant to the average daily flow from your
collection system.
The bacteria work best in a constant environment, so they will adjust their types and populations for
the temperature, food type, and quantity which are available to them. Under overload, however, you
can expect certain things to happen: First, the activity of the aerobic heterotrophs which consume
BOD is greater than that of the autotrophic nitrosomonas and nitrobacter which convert ammonia to
nitrate (nitrifiers). The heterotrophs are therefore dominant, and when both populations are present
(as they always are) the heterotrophs will interfere with the efficiency of the nitrifiers, as they will
dominate the fixed available surface area. Thus when the plant is biologically overloaded, resulting
from either too much flow, or too great a BOD or ammonia concentration (or a combination), then
you will first see the effect in an increase in the ammonia discharge concentration, as the
heterotrophs will displace the nitrifiers on the available surface.
The ammonia discharge can also be adversely affected by a lack. of alkalinity in the water. This
condition is particularly appropriate to the aquifers in the area. The alkalinity is required and is
consumed in the nitrification process, so you should be aware that it is important to keep a close
check on this parameter. You should keep you,
levels to 60 or more mg/1 throughout the
process.
Optimum value of pH for both the nitrification and denitrification processes is at 7.5. You should
c°
attempt to keep it there. Keeping the pH at this level also conserves alkalinity.

The Cliffs at High Carolina
Wastewater Treatment Plant O&MManual, Section IV
Page 2 of 2
Recommended Data Acquisition:
Twice a month, during startup, operational changes, or problems. Less frequently when conditions
are steady and plant is operating normally.
Influent (Sample obtained from flow equalization)
• BOD
• Suspended Solids
• TKN
• Alkalinity
Effluent (Sample obtained from dosing well)
• pH
• BOD
• Suspended Solids
• Ammonia
• Nitrate (NO3-N)
• Alkalinity (as CaCO3)
• Hydraulic Flow (Daily average)
• Fecal Coliform/Fecal Streptococcus
Interstage Data (Samples taken at effluent weirs of Primary Clarifier and Anaerobic I and 11).
Interstage data should be taken frequently until stable conditions are established, and after
changes in operating parameters.
■ BOD
Ammonia (NH3-N)
Nitrate (NO3-N)
DO
An occasional measurement from the dosing well of fecal coliform and strep is useful in the test of
LTV efficacy, as is a handle on turbidity and UV transmissivity to assure proper LTV dosage.
Daily recordings of flow equalization level, operational changes, chemical usage, sludge wasting
volumes, total flow processed, and unusual observations should be maintained in your operator's
daily log.
Aqueonics retains an active interest in the performance of its plants and requests that you copy us
with this operational data for our records so that we can be of assistance to you should questions
arise. We look forward to working with you to maintain an exemplary operational record.

START-UP
Prior to starting up the plant, the licensed operator, who has familiarity and experience in the
operation of plants of similar design, must have familiarized himself with all aspects of this O & M
manual and received further specific familiarization with this facility from Aqueonics personnel.
After becoming familiar with the plant operation, each operator should prepare a daily punchlist
schedule of items to be performed with a check -off list for each month of operation. This will ensure
that all operational items are accomplished as scheduled according to the operator's time schedule
and availability, and the requirements of this manual and those of the equipment manufacturers.
Aqueonics will review and comment upon this schedule after it is prepared by the operator. This
procedure should be repeated each time new operating personnel are assigned to this facility.
Pump flow rates, tank levels, and weir levels have been previously set by Aqueonics personnel.
Prior to starting up the plant, the Flow Equalization basin (which can be partially filled), Primary
Clarifier, and Anaerobic Reactors should be filled with water. Once these have been accomplished,
these procedures should be followed:
1. Check to see if the potassium permanganate filter (top) tray is good (purple or brown
indicates good).
Turn on bio -blower. Open the compartment to make sure it is running. Make sure
compartment door is sealed after closing. Be sure all section seals are intact and in place to
prevent bypass of any treatment stage.
2. Check all equipment for proper lubrication.
Check all process valving for correct desired routing of both air and liquid.
3. Turn on the recirculation pump #1 after Anaerobic Reactor #1 has filled.
4. Adjust the flow rate by adjusting the regulating valve in the pump discharge line. Correct
flow is between .75 and 2.0 gpm/fe. Flow rate is determined according to theory explained
in IILA.2 to which you are referred for the finer points of plant operation.
Check for even distribution of flow on top media surface.
5. Watch the effluent weir of Anaerobic Reactor #2. When water flows over the weir, turn on
recirculation pump #2.
6. If Aerobic Tower III is used, wait until forward flow goes over final weir, then turn on

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Wastewater Treatment Plant O&MManual, Section V
Page Z of 3
recirculation pump #3. Adjust flow and spray distribution of this and Aerobic Tower II as
you did for Aerobic Tower I.
7. Turn on the Sludge Holding and Flow Equalization blowers and place on AUTO.
Check diffusers for air flow. Adjust valves for maximum air flow with even distribution. At
this setting, check Primary Clarifier airlifts for proper operation. If air pressure is
insufficient, reduce air flow evenly to Sludge Holding diffusers until airlifts operate properly.
8. Check the head box to ensure that the V -notch and overflow are functioning properly and are
set for the desired flow rate through the plant.
Check alarm float switch to see that it is operating.
Set the flow rate through the plant by adjusting the overflow weir.
9. Utilizing the skimmer, remove any scum on the surface of the Primary Clarifier with manual
controls.
10. Inspect each clarifier collection weir for an approximately even flow on all sides. Remove
any floating material from around the weir.
11. Inspect the Aerobic Towers for a satisfactory spray pattern over the entire media surface.
Measure the set total flow over media. Total flow should be between and gpm.
12. Check the display for alarms and rectify any problems.
13. Select process mode desired (if other than standard) by adjusting process mode valving.
14. Adjust all airlift gate valves for proper airlift operation (discharge flow should be steady,
even and no greater than gpm).
15. Fill and mix chemical feed tank and set chemical addition rate. (If needed.)
16. Start-up control unit and set timing sequence of airlift pumps for frequency and duration.
Initially, only the primary clarifier will be effective. This timing sequence will need
readjusted as the plant lines out and the sludge train approaches steady state.
Operator experience will be the best guide to the need for change. A start-up guide would
be:
Frequency: Once per 2 hours
Duration: Primary Clarifier - 10 seconds
Anaerobic I, II, and III - 0 seconds

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Wastewater Treatment Plant O&MManual, Section V
Page 3 of 3
17. Set effluent dosing pump float levels for proper anticipated duty cycle as determined from
current hydraulic loading (see Treatment Plant Design, dosing system appendix).
18. Fill UV channels. Run effluent dosing pumps on manual. Check rotation. NOTE: UV units
come on automatically when sand filter operate, so UV channels should be filled before units
are activated.
19. Start up and check UV units for proper operation.
20. Mix alkalinity source dry material and water in the mix tank. Sufficient water should be used
to maintain complete solution of the lime or soda ash. Solution strengths should follow
recommendations to be found in Appendix I.1 of Section V.
21. Turn on solution mixer to assure dissolution.
22. Test operation of both solution feed pumps. It is used only if biological nitrification is
desired, and only if insufficient alkalinity is present in the influent water. Alkalinity should
be added as needed to maintain a discharge pH of 7.5.
23. Sample and test for NH3-N and NO3-N. All should be within specification. BOD will not be
within specification until a sufficient biomass has accumulated. This should take
approximately 3 weeks. Nitrification requires up to 3 months to build sufficient biomass.
24. During start-up, it will be necessary to balance air flow through the Aerobic Towers,
alkalinity supply and BOD availability to perform nitrification and denitrification processes.
At flows lower than design flow it may be necessary to restrict Aerobic Tower spray
application and/or air flow to allow Anoxic Reactors to become anoxic.
It may also be necessary to add methanol or other organic substrate in extreme cases to
achieve the anoxic condition.
The acquisition of interstage data for BOD, DO, NH3 and NO3 is invaluable in determining
which steps are necessary and at which points in the process sequence they may be required.

SAFETY
Accident prevention is the result of thoughtfulness, and the application of a few basic principles and
knowledge of the hazards involved. It has been said that the "ABC" of accident prevention is:
'ALWAYS BE CAREFUL"
The overall dangers of accidents are much the same whether in manholes, pumping stations or
treatment plants. These hazards include physical injuries, infections, noxious gases and oxygen
deficiency.
Prevention of Physical Injuries
The prevention of physical injuries begins with good housekeeping. Tools, parts and other things
should not be left lying around. Hatches should be closed when not in use and protected when in
use. Use the knowledge that bending the knees and lifting with muscles of the legs can save strained
or injured backs. Horseplay and haste, as well as knowingly unsafe or unstable practices for the sake
of expediency are common causes of injury, and should always be avoided.
A safety belt and tether must be worn when entering any enclosed tanks (confined space) where
access is difficult and assistance may be needed to climb out. A second person should always be
"topside" and physically able to pull you out. This person should never enter the tank to remove you
without calling for help and donning appropriately protective equipment when entering the tank. All
normal operation and maintenance procedures may be accomplished without entry into confined
spaces.
Electrical shock hazards are always present where electrical equipment is being used. When
maintenance is being performed on such equipment the power to the unit must be disconnected.
Lock-out/tag out capability is provided on all disconnects, which are all within reach of the
controlled equipment. This is for the safety of the operator. Always use these devices when
working on any equipment.
Prevention of Infections
Workers who come in contact with sewage are exposed to all the hazards of water -borne diseases,
including typhoid fever, para -typhoid fever, amoebic dysentery, infectious jaundice and other
intestinal infections. Tetanus and skin infections must also be guarded against. Vaccines against
these diseases are recommended.
A first aid kit should be placed in the control room. No cut or scratch is too minor to receive
attention. A two percent tincture of iodine or Merthiolate should be immediately applied to all cuts.
Work clothes or coveralls should be worn and laundered frequently. You should be aware that you

The Cliffs at High Carolina
Wastewater Treatment Plant O&MManual, Section VI
Page 2 of 3
are in a bacterial environment, and you can and will carry these bacteria with you when you go
elsewhere.
There should be no smoking in any part of the plant. It is practically impossible to avoid
contamination by sewage of the ends of pipes, cigars or cigarettes. Smoking is also a potential
source of ignition for any flammable vapors present.
"Keeping the hands below one's collar", while working with sewage or sludge is an excellent rule. A
majority of infections reach the body by way of mouth, nose, eyes or ears. Hands should be washed
before smoking or eating. Soap preparations requiring no water rinse are available for field use. Of
course, the common drinking cup should be banned and paper cups used.
Prevention of Injury from Noxious Gases and Uxyaen Deficiency
A noxious gas is one that is directly or indirectly injurious or destructive to the health or life of
humans. They may cause burns, explosions, asphyxiation or poisoning. Non-poisonous gases may
asphyxiate simply by mechanically excluding oxygen.
Conditions for the presence of such gases can occur in sewage treatment plants.
Hydrogen Sulfide (rotten egg smell) is a poisonous gas associated with sewage. Generally it is
,., present in very small amounts, but in an enclosed tank containing sewage with no ventilation, it may
accumulate to deadly concentrations. Hydrogen sulfide is particularly dangerous since the human
sense of smell becomes desensitized to the odor with exposure.
Methane or sewer gas may form under similar conditions. Rather than being poisonous it is
flammable and potentially explosive. Like Hydrogen Sulfide, it may accumulate in non -ventilated
areas. This is one reason that proper operation and maintenance of your bio -air system is highly
important.
Gasoline or other flammable, corrosive, toxic, or explosive liquids may be dumped into the sewer
lines causing similar problems. Your plant maintains constant positive ventilation of the plant so
long as the bio -blower and vent blower are operated. It is therefore important that these units be kept
in operation at all times.
To protect himself from the danger of noxious gases, the operator must follow a few simple rules:
1. Never enter an enclosed non -ventilated area without a safety line and always have an
observer outside the area capable of pulling you out. This second person should never go
down in a rescue attempt without respiration equipment lest he be overcome as well.
2. Always have the blowers on when entering a tank.
3. Never smoke within the plant.
4. In case of doubt do not enter without making precautions below.
5. If it is necessary that you enter an enclosed or non -ventilated area then you must:

a) wear an air pack and mask
b) have a safety line
c) have someone on the outside who has the ability to remove you
d) have a system of communication or signals between you and the person outside
Handling of Chemicals
Aside from the physical safety aspect of proper lifting and handling the containers to avoid injury
from the chemicals themselves.
Each chemical provided must by law be accompanied by a Material Safety Data Sheet (MSDS). You
should always familiarize yourself with this information provided, including the provision and
donning of protective clothing or protective breathing or eye shielding apparatus, and the handling
steps recommended to minimize your exposure to injury.

EMERGENCY PLAN
General Discussion / Intro to Vulnerability Analysis
The NPDES permit number , page of in Part , requires a Vulnerability
Analysis to estimate the degree to which the treatment system would be adversely affected by each of
the following emergency situations:
• Natural Disaster (eg. Floods)
• Civil Disorder
• Strike
• Sabotage
• Faulty Maintenance
• Negligent Operation
• Accident
The analysis includes an estimate of the effects of the emergency on the power supply,
communication, equipment, supplies, personnel, security and emergency procedures.
Natural Disasters
To address the natural disaster issue, this analysis covers flood, tornadoes, hurricanes, and
earthquakes. The does not issue permits nor approve the construction of on-site sewage
treatment plants with discharge to groundwater that are'proposed for location in flood plain, nor is
this facility located near one; therefore a flood situation does not need to be addressed. In addition,
this area is not subject to tornadoes due to the hilly topography and therefore does not require that
the issue be addressed.
As for hurricanes (high winds), plants of similar design are located in May's Landing and Marmora,
NJ, approximately 2 miles form the Atlantic Ocean.
These plants were constructed in 1985 and 1989 and have sustained winds up to 90 miles per hour
during a storm in mid-December 1992 with no damage or interruption of the operation, therefore the
plant that will be constructed at The Cliffs at High Carolina in Asheville, NC should be able to
sustain even greater wind loads. Such winds are not known in this area.
The plant could suffer consequential damage from high winds such as damage from flying debris,
tree fall, or power outage; however these consequences are similar to the respective accident or
sabotage scenarios, and need not be described separately.
The remaining natural disaster is earthquake. This plant has been designed to withstand a seismic
Class H event, which is greater than the most probable seismic event classification in this area, so
seismic damage is not anticipated as a possible occurrence.

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section VII
Page 2 of 4
Faulty or Negligent Operations
To address the issue of faulty or negligent operation or maintenance, neither is acceptable behavior
on the part of the licensed operator, and is cause for immediate remediation and / or dismissal once
discovered.
As there is no fault with the facility, correction of deficiencies in operation or maintenance, once
discovered, is the proper procedure to return the plant to proper operation. There would be no cause
to haul or cease operation unless the improper operation resulted in imminent danger to public health
or safety, such as plant overflow, in which case immediate action should be taken to abate the non-
compliant condition. If such negligence should result in non-compliant discharge, the procedures
specified in the permit for such a situation should be followed as appropriate to the specific defect
resulting from the faulty operation. The most common negligent operation is failure to repair or
replace a failed backup unit of equipment promptly, so that a spare is not available when the second
unit also fails. This failure results in an emergency situation which must be dealt with as an
emergency according to this plan.
Accident or Deliberate Abuse
All objects are susceptible to destruction through determined attack. For this event, an assessment of
the resulting damage and its effect on operation would be required, after which the necessary repairs
would be made prior to resumption of operation and discharge. Temporary measures, on a case-by-
case basis would be taken to assure no non-compliance discharges during this period.
Compliance (and , if changes are to be made) would be involved in the approval of
measures taken and time schedule for completion of the work while such repairs were made.
Measures have been taken in the design and materials of construction to prevent debilitating damage
from casual acts of vandalism and accident. Tankage is of concrete and access is by latched
aluminum doorways which have been cast in, and access is through keyed entryways. The
equipment is located within a building and is accessed from inside. It is thus protected from most
forms of projection events or action. The exterior has been specifically designed to withstand impact
from golf balls, and so will be impervious to all but the most deliberate attack.
Damage to the Aerobic Tower housings and equipment protective covering can result from
projectiles. Perforations are unlikely to result in damage which would require emergency action,
however, impacts from large objects at speed, such as bullets, runaway vehicles or falling trees can
cause significant damage which cannot be repaired immediately. Consequently, it is recommended
that the landscaping plan include barriers which would stop or deflect vehicles from reaching the
plant, as a reasonably prudent prevention measure. At present, there are no trees in the area of the
plant which could inflict severe damage, but future considerations should be given to maintenance of
growth which could inflict damage.
Specific Defects
All treatment facilities and this one is no exception, are subject to failures of specific components.
Therefore redundancy has been built into the design to accommodate such specific failure modes. In

The Cliffs at High Carolina
Wastewater Treatment Plant O&MManual, Section VII
Page 3 of 4
many cases, switchover to redundant components is done automatically. In other cases, spare
equipment is maintained for immediate use or for preventive maintenance. Under emergency
scenarios such as considered below, multiple or unusual failures are typically generated which should
be separately considered.
These are considered on a case-by-case basis, as multiple failures can result from a single event, and
conversely the same defect can result from a number of different causes which would have the same
effect and he same course of action.
Table I has therefore been created which classifies the effects under each of the possible emergency
scenarios as regards each component to be affected, describing the effect, the nature of the
emergency created, and the action to be taken. As the descriptions are too length to fit appropriately
within the table, they are referenced by numbers and letters to more descriptive texts in which
alternatives are described.
Additionally, it is recognized that the disposal system is subject to failure as evidenced by overflow
of the surface impoundment, or high groundwater measurements found n the piezometers. Such
events are considered emergencies, as under such circumstances a non-compliant condition exists.
Until remediation of the condition, hauling of discharge wastewater to the as specified in the
permit, part , page of is to occur. Immediate notification of such a situation must
be made to , at and in writing via certified mail to Director , , ,
. In this notification, the nature of the emergency, cause of failure, and the remedial action
taken must be described.
Effect Text Table:
No.
Effect Texts
Emer enc T_ype
I
Loss of connection to area
A
2
Loss of connection to property
A
3
Loss of connection to plant
B
4
1 Equipment destro ed or removed
D
5
Equipment damaged
D
6
Equipment disconnected
D
7
Loss of source
E
8
Loss of reserves
E
Emergency Text Table:
No.
Emergency Texts
Emergency Type
I
Project evacuated per public safety regulations: no
inflow or outflow. No sewage emergency exists
IA
2
Possible overflow of plant and / or lack of treatment
2A
3
1 None
3A

The Cliffs at High Carolina
Wastewater Treatment Plant O&MManual, Section VII
Page 4 of 4
4
Possible non-compliance
2A
5
Potential non-compliance
4A
Action Texts:
IA. No action required.
2A Assess cause. If repairable before flow equalization basin fills, do so. If not, obtain
temporary replacement. If accomplished, no reportable event occurs. If not accomplished,
pumping and hauling will be required to avoid a reportable event.
3A More frequent checking should be done to confirm proper operation if project is occupied.
4A Determine availability of replacements. Continue operation with reserves pending
replacement as long as possible. When reserves are no longer available, discontinue
discharge and continue operation to maintain biomass until material and labor resources
have been restored.
Note: Whenever a non-compliant discharge occurs, it must be reported as specified in the permit.
These emergency procedures are all designed to prevent the occurrence of reportable events under
emergency conditions.
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IN
EMERGENCY PROCEDURE DECISION AND ACTION TREE
Objective: To prevent non-compliant discharge under emergency conditions.
This procedure is for the use of any person, including owner, tenant, operator or his assistants, or
public officials, including fire, police, public health, DEP, or municipal employees, who may be
called upon in an emergency situation to prevent or to abate a potential public health hazard which
might result from damage to or improper operation of the wastewater treatment facilities until proper
management and operation can be restored.
To use this manual, follow the step-by-step sequence. This will address the most serious problems
first, in order, and provide you with the means and facilities to solve the most serious of problems, at
least on a temporary basis.
1. Fire is observed. a. Call Fire Department immediately at 911,
or - Report fire at this
location ,
b. Attempt to extinguish.
c. Call operator '(see Ste #4)
2. Accident is observed or act of sabotage is a. If release of water is observed. Turn off
observed or discovered. power to plant immediately.
b. Obtain information on person causing
incident, and make written notes.
c. Call o erator see Ste 4)
3. Incident of strike or civil disorder is Notify owner:. .
observed.
Security:
4. Call plant operator. Explain emergency.
: (See Sten 4
5. Flow observed over -topping reservoir. Turn off discharge pumps at disconnect between
front and side doors outside plant.
6. Flow observed coming from plant a. Call licensed Hauler:
tankage. b. Go to Step #7
1 7. Check tanks. All tanks are flooded. I a. Find source of power outage and restore.

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section VII
Page 2 of 3
Power is off, and emergency generator is
b.
Check emergency generator. Does it
not running
have fuel? Fill and restart.
c.
If water level does not go down, go to
Ste #8.
8. Check disconnects for effluent dosing
a.
If off, turn on. One pump should come
pumps.
on and water level should drop in the
dosing tank (Hatch on corner nearest
front door.)
b.
If water level does not go down, go to
Step #9
9. Obtain access to plant controls. Check
a.
Turn pumps on automatic. One pump
effluent dosing pump indicator light on
should come on and water level should
panel. Green light not on indicates pumps
drop. If not go to Step #10
are not running-
unnin .10.
10.Lights do not come on and stay on
a.
Check circuit breakers and reset overload
protectors. Pump should come on. If
breaker trips, second pump should come
on. If that breaker trips, both pumps are
bad and must be repaired/replaced. A
temporary replacement must be installed,
or hauling must be initiated.
11. Lights come on, but level does not drop.
a.
Wiring disconnected, or pumps are
(switchover occurs)
running but not pumping. Check valves
for open status. If not, open them. If
open, check pumps for blockage. If
pumps are operating, blockage is in the
discharge line. Haul until repaired,
12. Put one pump in "Hand" position. Light
a.
Problem is in the float -switches or relays.
comes on, level drops.
Diagnosis and repair required. Plant can
be operated in hand mode.
13. Li t comes on, but level does not drop
a.
See Solution #I I above.
14. Turn other pump on hand. Light comes
a.
See Solution #11 above.
on, but level does not drop
15. Neither light comes on.
a.
See Solution #10 above.
16. Effluent dosing tank is empty, but other
a.
Blockage in piping internal to plant.
tanks are overflowing.
Unblock piping between tank and next -
stage non -overflowing tank. If this can't
be don readily, turn grinder pump off and
pump and haul flow equalization basin.
17. Damage to plant is observed, but no
a.
In Step #4, you have notified plant
water is discharged abnormally.
operator. Do not proceed beyond this pint
to make alterations in operation unless
you are qualified and trained in the

The Cliffs at High Carolina
Wastewater Treatment Plant O&MManual, Section VII
Page 3 of 3
N
operation of this plant. There is presently
no danger to the public. If, before the
operator arrives the status should change,
then repeat Steps 1-16 above.

ELECTRICAL CONTROL SPECIFICATION/OPERA.TION
1. EouALUATioN:
Two hp, phase, volt submersible grinder pumps, Model ,
rpm operate in an alternating simplex mode. Hour meters installed on the front door of
the control panel are available to record the elapsed run time on each grinder pump from the
immediately preceding 24 hour period. Use this data to set your head box weir for near 24
hour continuous operations.
Grinder pump activation (of either pump) also activates lime or soda ash feed pumps.
Four Float Switch Control
• Switch No. I kills both pumps regardless of Hand -Off -Auto (HOA) status (low water
alarm (Class II). Kill switch operates independently of HOA switch. Control system
returns to normal operation when switch no.3 floats, however low level light remains
on until manually reset.
• Switch No. 2 turns lead pump off (arms lead pump on way up).
• Switch No. 3 turns on lead pump. On way down after High Level alarm, deactivates
alternation function, but returns automatic float control
• Switch No. 4 sets a high water level alarm, turn on lag pump, turn off lead (indicate
alarm) (class II), alarm remains on until manually reset.
All alteration and alarm functions, starters, breakers, and HOA switches are incorporated in
control panel. Status lights are alarm lights will be on the control panel. Also, the "hand"
switch position operates the respective pump, regardless of status of any other pumps.
2. Primary Clarifier
High level float switch in primary clarifier to detect flood condition and activate high level
alarm in Plant Controller. Class I alarm.
3. Aerobic Tower Recirculation Pumps
Three hp, phase, volt recirculation pumps. Model ,
rpm. Pumps are to run continuously. Each pump will have a hand switch only mounted in
control panel. A red valve dual -limit flow switch will be placed up stream of each pump to
detect flow. The signal of no -flow status (alarm indication when out of range) and operation
will be monitored by the control panel, latching in an alarm light when out of limit band.
Class II alarm.
4. Air Blower System
Three hp, phase, volt blowers. One blower (equalization supply) runs
continuously. Starters and breakers are incorporated in control panel. Each blower has a
HOA switch and status light integral to the control panel.

The Cliffs at High Carolina
Wastewater Treatment Plant O&MManual, Section VIII
Page 2 of 4
Remaining two blowers alternate. The timing of alternation is controlled by the control panel.
Alternation interval may be changed.
The alternating pair has Furnas pressure control switch in series with "on" circuit. This
pressure switch works on time delay such that if after 60 seconds pressure fails to reach pre-
determined value, unit is shut down. A signal is sent to the control panel and PLC and the
alternating unit is started and alarm signal on non-operating unit is activated. On non -
alternating unit, alarm and shut down only are activated. Alarm sensor is by flow detector,
rather than pressure sensor. Both are Class II alarms.
5. Building Exhaust System
One on/off circuit with capacity for one room exhaust fan with characteristics of volt,
phase, hp, amps. Operation is by a thermally controlled switch and hand -
operated override. Motor driven shutters require amp, volt.
6. General Plant Alarms
General plant alarm activated by all alarm status indicators provides power to light bulb on
control panel. A second set of relay contacts for Class I alarms only activates Sensaphone
emergency dialer.
Alarm Indicators:
f a. Each alarm indication has a red light on panel specific to its function with label.
' b. Any alarm condition will trigger a red alarm light visible on the control panel.
c. Any Class I alarm condition will trigger an alarm dialer which will call out with a
general alarm condition.
7. Bio -Blower Odor Control System
An on/off circuit for the bio -blower with cfm, amp.
Characteristics of volt, phase. Operation is indicated by the control panel.
Alarm will indicate if bio -blower ceases to operate as indicated by loss of power to fan.
Class I alarm.
8. Air Lift Operations
Air lift sequencing of ( ) volt solenoid valves shall be achieved in the
control panel. Each lift is adjustable to run zero to five minutes in sequence. The sequence
is run at any repetition rate the operator deems necessary. Dry contacts are utilized to sense
"proper" or "improper" operation. "Improper" operation will mean that if, after an elapsed
period the cycle does not complete and reset the alarm will be triggered (Class Il alarm). All
timed solenoid banks have hand operation override switches. (Hand/Off switch not needed
since timer or hand valve can be used.). See solenoid sequencing page for details.
9. Auto Dialer
Sensaphone will call out (Class I alarm) when power is out.

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section VIII
Page 3 of 4
10. Lighting and auxiliary outlets:
Interior lighting: double w. fluorescent fixtures,
entry way switches
way. incandescent
w. fixtures
exit light.
Exterior lighting: - Watt Sodium Vapor fixture
Entry way switch
Outlets:
11. Ultrasonic Flow Meter
Flow meter and flow recorder.
,4-20 ma output.
amp, volt circuits.
12. Effluent Dosing Pumps
Effluent dosing pumps by others
volt, amp breaker, located in control room,
13. Sludge Decant Pumps
Sludge decant pump. Model with broadband float switch control, hp,
phase, volt sewage pump, HOA operation only from control panel. No alarm.
14. Chemical Feed System
Lime/soda ash feed system, with stirrer and low level switch. series metering
PUMP amp., volt. Activated only when either grinder pump is running. Class II
alarm when low level, shuts off pump and stirrer.
15. Ultraviolet Disinfection System
Two ultraviolet disinfection units to be operated only when its sand filter is running. The
failure indicator on the lead unit activates the other unit. Units are , Model ,
volt, amp.

The Cliffs at High Carolina
Wastewater Treatment Plant O&M Manual, Section VIII
Page 4 of 4
SOLENOID SEQUENCING
Lights are activated on the panel to indicate which sludge lift is operating. The operator must
have control over the frequency and duration of each lift cycle.
1. Timer - 24 lir. x 15 min. Turns on timer 1. Indicates alarm if reset has not occurred before
lift cycle starts. Class lI alarm. Range 0-5 minutes. Preset at 1 minute.
2. Timer I — Turns off air flow to sludge holding tank by turning off alternating pair of
blowers. Air flow is to stay off until end of decant cycle. Time range 0-120 minutes.
Turns timer Il on at end of cycle. Preset at 30 minutes.
3. Timer II — Actuated by Timer I, turns on decanter pump and turns it off after a suitable
elapsed decant time. Time range 0-60 minutes, starts timer III at end of elapsed time and
turns on lead blower of alternating pair.
Note that there is a float switch on the decant pump which will automatically turn it off
when it reaches a mechanically set level. Preset is 15 minutes.
4. Timer III — Starts timer IV after 60 seconds; which allows air pressure to built up in air
lift lines.
5. Timer IV — Turns on Anaerobic III sludge lifts by opening solenoid. Closes solenoid at
end and starts timer V. Ranger 0-5 minutes. Present at 20 seconds.
6. Timer V — Turns on Anaerobic II sludge lifts by opening solenoid. Closes solenoid at
end and starts timer VI. Range 0-5 minutes. Preset at 30 seconds.
7. Timer VI — Turns on Anaerobic I sludge lifts by. opening solenoid. Closes solenoid at
end of cycle and starts timer VII. Range 0-5 minutes. Preset at 45 seconds.
8. Timer VII — Turns on Primary Clarifier sludge lift by opening solenoid. Closes solenoid
at end and resets 24 hour timer for next cycle.