PHYSICAL - CHEMICAL
TREATMENT PLANT DESIGN
  Presented by Richard L. Woodward
          Vice President
     Camp Dresser & McKee Inc.
       Boston, Massachusetts
Prepared for Environmental Protection Agency
      Technology Transfer Seminar
          Atlanta, Georgia
             May 1973

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                 Physical  - Chemical  Treatment Plant  Design
                                     by
                            Richard  L.  Woodward
                        Camp Dresser &  McKee Inc.
INTRODUCTION
     Mr. Cohen has discussed the various unit processes used in physical  -
chemical treatment of wastewaters.   It seems most useful  that I use my
allotted time to tell of two projects in which we have been involved where
a physical - chemical process was selected.   One project at Fitchburg, Mass.,
is now under construction and the other at Niagara Falls,  N.Y.  should soon
be started, after some frustrating delays.  Some preliminary results from
a third project which is still in the study stage will also be  discussed.
 NIAGARA FALLS.  N.  Y.
      Geographic Situation
      This city  is  a  famous  tourist  center but it is also  the center of a
 large chemical  complex  with  such well  known names  as  Hooker, Union Carbide
 Dupont, Goodyear,  National  Lead, 01 in,  Carborundum and others.  The Niagara
 River, which  flows by the city,  is  an  international boundary water connecting
                                                                       3
 Lake  Erie and Lake Ontario  and  has  a  flow of about 200,000  cfs  (5,700 m  /sec).
 The city has  a  population of about  86,000.   We were retained by the city in
 January,  1970 to study  its  water pollution  control problems, to submit a
 preliminary design report by February,  1971  and to have the project under
 construction  by March 1, 1972.   Financing problems have delayed construction.
      Nature of  Wastes.  A sampling  and  gaging program of  all major industrial
 wastewater discharges in early  1970 showed  a total flow of  164  mgd

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                                     -2-
 (7.2 m /sec) a suspended solids load of 274,000  pounds  per  day (124,000 kg/day)
 and a COD load of 242,000 pounds per day (110,000  kg/day).   Only 63  mgd
       2
 (2.8 m /sec) went directly to  the municipal  sewers but  it contained  some
 70 percent of the suspended  solids,  about  55 percent of the COD  load.   This,
 of course, completely overshadows the domestic waste load.
      The waste reaching  the  existing treatment plant in  1970 frequently had
 a  pH of close to  11,  but acid  dumps  would  occasionally  drop this  to  below 3.
 Lime waste was evident and caused much of  the discoloration of the river which
 was noticeable below  the treatment plant.  Volatile vapors  from chlorinated
 hydrocarbons were occasionally so irritating to  the eyes and lungs of workers
 at  the treatment  plant that  they had  to  leave.   Occasionally chlorine residuals
 could be measured at  the  plant.   BOD  measurements on this wastewater were
 meaningless.   During  pilot plant  work it would sometimes be found that  the
 BOD increased  in  going through  physical  -  chemical  treatment.   A few coliform
 tests  on the raw  wastewater  showed concentrations of only 100 to 400 coliforms
 per 100  ml.   Clearly  this  wastewater  was not a suitable candidate for biological
 treatment.
      Effluent  Quality  Requirements.   All wastewater discharges to the Great
 Lakes  and  Niagara River in New York are required to remove phosphorus.  A
 limit  of 1 mg/1 of phosphorus  is the  general  requirement for wastewater dis-
 charged  to these waters.   The usual requirement for secondary treatment was
 not defined  in terms of BOD, but a limit of 112 mg/1 of COD  has been  prescribed
by the New York Department of Environmental Conservation along with a limit
of 35 mg/1 of suspended solids  and 0.23 mg/1  of phenol.
     Pilot Plant Operations.  A small pilot plant was constructed at  the
existing wastewater treatment plant and operated  for approximately three months
in mid-1970.  Figure 1 shows  schematically the facilities provided.   Because of

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                                     -3-
the high pH of the influent waste the chemical used for phosphate removal
was lime,operating at a pH of 11.2 - 11.6.  An average dose of 90 mg/1 of
lime was required to maintain this pH.  The average removal of COD in
clarification was only about 40 percent, but the suspended solids removal was
close to 80 percent.  Phosphorus removal averaged only about 65 percent in
the clarification stage.  The carbon columns increased the overall removal
of COD to about 75 percent, of suspended solids to over 90 percent, of
phosphorus to 70 percent.  Phenol  removal was about 95 percent.  The carbon
columns were operated at a 30 minute empty bed contact time.  Acid was used
to reduce the pH to around 7 prior to application to the carbon columns to
avoid precipitation of calcium carbonate on the carbon.  The clarifier sludge
in filter leaf tests dewatered readily to a solids content of more than 30
percent.  The cake produced was not putrescible.  The indicated carbon
exhaustion rate was about 250 pounds per million gallons.
     The pilot plant work was discontinued after about 3 months because it
was known that the waste characteristics would change markedly by the time
the plant was built because of reduced contributions of waste from industry.
     The only specific organic compound analyzed for was phenol and,  as
indicated above,  it was effectively removed.  The nature of organics  that
failed to be adsorbed are not known but substantial  amounts of organic
chlorine were found in the effluent and samples analyzed by mass spectrometry
showed the presence of mono- and dichlorobenzene in  both influent and effluent
samples.
     Negotiations with Industry.  From the start of  the project close contact
was maintained with the local industries through a committee on which all
important liquid  waste contributors were represented.   The entire pollution

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                                   -4-
abatement program was to be financed by user charges and each major industry
knew that it would be obliged to sign a long-term contract to pay its share
of the cost.  Rough preliminary costs figures were given to the industries
as soon as possible to enable them to determine what in-plant changes could
be made to reduce their treatment charges.   A three-part rate based on flow,
suspended solids and COD was used with the  18 larger industries, each of which
was contributing more than 100,000 gallons  per day of liquid waste, 250 pounds
per day of suspended solids or 250 pounds per day of COD.
     As the work progressed it was possible to refine the cost estimates as
better estimates of flow and waste load were received from the industries.  In
the end the industrial waste flow provided  for in the final design was 28 mgd
      3
(1.2 m /sec), the contribution of suspended solids was reduced to less than
one-third and of COD to less than half of what was going to the municipal
sewers in 1970.
     Plant Design.  With such uncertainties as to the changes in the amounts
and strength of the waste it was necessary  to provide for considerable flexibility
in designing the treatment plant.  Figure 2 shows a schematic diagram of the
plant as it will be built.  Figure 3 shows  an architect's  rendering of the
proposed plant.
     Final design on the initial construction program began in February, 1971
and was concluded in April, 1973.  The treatment process will  be similar to
that used in the pilot plant, and a schematic process diagram is shown as
Figure 2.  Some of the basic design criteria include 48 mgd average flow
with 86 mgd peak flow (estimated 2020 dry weather flow), 100,000 pounds per
day suspended solids and 145,000 pounds per day COD.  A composite population
equivalent based on these criteria is about 500,000.

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                                    -5-
     The wastewater from the east side of the city will  enter the main pump
wet well in the new treatment plant from the Southside Interceptor.   The
main pumping station will include four, 15,000 gpm mixed-flow pumps,  any
three of which will have the capacity to pump the design flow from the east
side, with one standby.  The discharge from the two sources (the main pumping
station and the new pumping station on the existing treatment plant site),
will flow through mechanically cleaned bar screens and into two rapid mix
basins with a combined detention time of about 1  min at 86 mgd.
     The materials which may be fed to the wastewater in the rapid mix basins
include lime, a metal salt (ferric chloride, alum, or most likely chlorinated
ferrous sulfate), a coagulant aid, return sludge from the primary sedimentation
basins, acid (if the treatment process includes depressing the pH rather than
elevating it), and the spent backwash water from the activated carbon beds.
            •
The change from the lime system to a metal salt system could be made  in a
matter of minutes, and the choice would be dependent on the pH of the incoming
waste, the cost and availability of chemicals, the ease of sludge dewatering,
and other factors.  There is a strong possibility that the lime discharges
to the sewers will be eliminated to reduce user charges and that either
aluminum or iron may be more economical chemicals.
     From the rapid mix basin the wastewater will be split hydraulically into
five flocculation basins, each followed by a sedimentation basin.  The
flocculation basins will be 60 ft square and each will have nine flocculators.
The flocculators will give decreasing "G" values in the direction of flow,
with 100 sec"  possible at the influent end and as little as 10 sec"   at
the effluent end of the flocculation basin.  The detention time in the basins
will be about 20 min at the peak flow.

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                                    -6-
     Sedimentation basins will be 60 ft by 250 ft long with an average
depth of 12 ft.  The overflow rate at the peak flow will  be 1,400 gpd/sf
and about 800 gpd/sf at the average flow.  The detention  time at peak flow
will be 1.4 hr.  Sludge will be drawn off from the sedimentation basins to
one of two 70 ft diameter gravity thickeners, although some of the sludge
may be returned to the rapid mix tank to aid in floe forming.
     The flow from the primary basins will go through an  acid mix tank to
adjust the pH to between 6 and 7 (if the high lime process is used), and from
there the liquid will be pumped to the activated carbon beds.  The pumping
facility will include four, 27,000 gpm mixed-flow pumps,  any three of which
will pump the peak flow plus the spent backwash water, with one standby.
     The granular activated carbon beds will be downflow  gravity beds.  There
will be 28 beds, each 17 ft by 42 ft with a 9 ft depth of activated carbon.
For a plant this size gravity concrete beds are considerably more economical
than steel pressure vessels.  The underdrain system will  consist of precast
concrete slabs with plastic nozzles placed 8-in on center.  The rate controllers
on the effluent piping of each of the beds will split the flow equally among
all of the beds on line.  The superficial velocity through the beds will be
3.3 gpm/sf at the peak flow.  The treated effluent will flow to a chlorine
contact chamber with a detention time of 15 min at 86 mgd.
     Each of the carbon beds will be backwashed at least  once each day with an
air wash followed by a water wash.   The maximum air wash  rate will be 3,000 scfm,
and the water wash will be up to 20,000 gpm from pumps taking suction from
the plant effluent line.  This 20,000 gpm corresponds to  a rise rate of
44 in/min in the bed.  This high rate would be needed only when removing
carbon for regeneration.  The spent backwash water could  flow either to the

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                                    -7-
rapld mix basin, where it would be mixed with the incoming flow and treated,
or it could be directed to its own rapid mix basin, where it would be mixed
with the incoming flow and treated, or it could be directed to its own
rapid mix basin and into an end flocculation basin.  It is likely that even
plain sedimentation may improve the spent backwash water quality to the point
where it could be discharged to the river, with chlorination, without having
to go through the activated carbon beds again.
     Carbon in beds which have reached their adsorptive capacities will be
taken out of the beds hydraulically for regeneration.  The regeneration facility
will include a six-hearth furnace, in which carbon will be applied to the
top hearth and slowly pushed from one hearth to the next lower one.  About
three days will be required to regenerate one bed.  The regeneration will
be done in the absence of oxygen, and steam will be applied as a source
oxygen for the adsorbed organic carbon to be driven off as CO..  Above the
top hearth, the gases from the regeneration will be burned at about 1800°F
to break down any chlorinated hydrocarbons that exist in the gas into CO
and HC1.  The gases will go through a wet scrubber which will dissolve the
HC1 and remove the particulate matter from the stack gas.  The scrubber
effluent will be recycled to the front end of the plant.
     Sludge Handling and Disposal.  About 80 tons of dry sludge solids per
day is the expected sludge production, if lime  is used.  Smaller amounts of
sludge are expected if iron or aluminum is used.  The sludge will be pumped
from the gravity thickeners and will be dewatered on four, 500 sf vacuum
filters, which will operate about 120 hours per week.  Ferric chloride, a ^
polymer and lime will be available for conditioning the sludge.
     The dewatered sludge will be hauled to landfill for burial.  Incineration
of the sludge was considered, during both the preliminary and the final design

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                                    -8-
phases, but it would be more costly than burial.  The plant influent
suspended solids contain a low percentage of volatile material, and this,
together with the inorganic chemical additions, would make incineration
little more than a drying process with most of the heat having to be applied
externally.  The reduction in volume and dry solids weight of the evaporated
sludge would not be significant over the vacuum filtered cake.  Similarly,
the large amounts of inert suspended solid in the sludge made lime recovery
appear unprofitable.  Changes in the waste characteristics as industries
reduce their waste loads may call for a review of this decision.
     Costs.  The estimated cost of the treatment plant is $37 M and various
necessary sewers, a pumping station and force main will add another $16 M.
Annual operating costs are estimated at $1.8 M.  The capital  cost  for the
treatment plant is amortized in 20 years at 6 percent interest the total
                                                        3
cost of treatment alone based on a flow of 48 mgd (2.1 m /sec) is $290.

FITCHBUR6. MASSACHUSETTS
     Geographic Situation.  Fitchburg, Massachusetts is an industrial  city
located in central Massachusetts and has a population of 43,000.   It is located
at the headwaters of the Nashua River.  Near the upstream end of  the city two
paper mills, the Weyerhaeuser Co. and the Fitchburg Paper Co. (a division of
Litton Industries) use all of the flow of the stream during low flow periods.
In fact, Fitchburg Paper Co. depends on Weyerhauser's waste flow for its raw
water supply.   Thus it was not feasible to intercept the waste from these
mills and treat it at a downstream plant which will serve most of the city.
     Figure 4 shows the Nashua River as it flows through Fitchburg, the
location of the mills and of the two proposed wastewater treatment plants.
The west plant will  serve primarily the two paper mills along with some domestic
waste from Fitchburg and an adjoining community.  The east plant  will  serve the
remainder of the area.

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     Nature of Wastes.  The wastewater from the two mills is primarily
white water containing paper fiber along with chemicals used in paper making
such as alum, starch, pigments and fillers.  The total  waste flow from the
two industries averages about 13.8 mgd (0.6 m /sec).  The waste has an
average BOD of about 50 mg/1 and suspended solids of 360 mg/1.
     Effluent Quality Requirements.  Because the effluent from the west
treatment plant will constitute the entire stream flow during low flow periods
a BOD of 5 - 7 mg/1 was needed.  To avoid aesthetically objectionable color
from the pigments used in making colored paper good removal  of color is
necessary.  Suspended solids should also be kept to low concentrations.
     Pilot Plant Operations.  When the pollution abatement problems of Fitchburg
were studied in 1968, biological treatment was proposed for both the east and
west Fitchburg plants and in 1970 pilot plant studies were made for both types
of waste.  The paper mill wastewater contains substantial amounts of alum
and by adding an alkali to increase the pH to about 6.7, a good floe is
formed which settles readily and removes some 50 percent of the BOD and more
than 90 percent of the suspended solids.  Although the activated sludge pilot
plant did a satisfactory job of removing BOD, color was not consistently
removed and there was some carry-over of the biological floe in the effluent.
It was necessary to add nitrogen and phosphorus to the waste as it was deficient
in both nutrients.  In addition, some problems were anticipated in operation
because both mills operate on a five-day week and shut down for a two-week
period each summer.  This would complicate the operation of a biological
treatment plant.
     A small pilot plant facility was established at the Weyerhaeuser mill
where waste was available from one of its primary clarifiers.  Wastes from the

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                                    -10-
Fitchburg Paper Co. mill were trucked to the site and mixed in suitable
proportion to Weyerhauser waste.  The combined wastes were settled in a
tank truck and then pumped to four carbon columns in series.   About 90 per-
cent of the settled BOD and COD were removed by the carbon columns operated at
a rate which would provide an empty bed contact time of 23 minutes.  Very
good color removal was obtained.  The exhaustion rate was such that the
carbon usage would be about 1,600 pounds of carbon per million gallons.  This
was much higher than we found at Niagara Falls and about double the rate
commonly reported in treating domestic wastewater.
     Negotiations with Industries.  The West Fitchburg plant  is to be paid for
primarily by the industries which will provide most of the flow.   A thorough
economic analysis of the relative costs of the physical-chemical  system is
compared with activated sludge.  This showed that the PC system would be about
6 percent more expensive, but nevertheless the industries as  well  as the city
and the state regulatory agency chose the more expensive system because of
its better effluent quality and operating stability in the face of major
changes in flows.
     Plant Design.  Figure 5 is a schematic of the West Fitchburg  plant.
Municipal wastewater will be settled and chlorinated heavily  before being
combined with the industrial wastewaters.  The primary sludge from the
municipal clarifiers will be processed at the East Fitchburg  treatment plant.
The combined wastes will be coagulated, flocculated and settled.   The chemicals
normally used will be lime and a polymer.  The industrial wastewater normally
has a pH in the range 4.2 - 4.7 and upon adjustment of pH to  6.7 the alum
in the waste forms a good floe.  At times of high turbidity when large amounts
of titanium are being used in paper making it will be necessary to add alum.

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                                    -11-
     Two circular municipal  clarlflers will  be provided Initially.   These
are designed for an overflow rate of 1,000 gallons per square foot  per day.
Two rapid mix and two two-stage flocculation basins will  provide 5-minute
and 30-minute detention periods, respectively, at maximum day flow  rates.
Two industrial clarlflers, each 130 ft in diameter will provide an  overflow
rate of 840 gallons per square foot per day at maximum days flow rate.
Sludge will be pumped off site to four sludge lagoons.
     Vertical turbine pumps will deliver the settled wastewater to  the
activated carbon columns.  Four variable speed pumps will be provided each
with a maximum capacity of 8,500 gpm at a design head of 145 ft. These have
been designed to provide for 10 ft of head loss through prefiltration facilities
if these should be needed.
     Twelve activated carbon columns, each 20 ft in diameter with a 15.5 ft
bed depth, are provided.  They will be operated in parallel.  The columns
and piping allow for two vessels to be out of operation,  one for backwashing
and the other for regeneration.  Ten active vessels were selected to permit
maximum utilization of the carbon.  The surface loading and empty bed contact
                                                          2
time for the 10 active vessels will be about 8 (gal/min/ft ) and 15 min,
respectively, at peak hourly flow, and the flow through the vessels will be
divided uniformly and controlled by individual rate controllers. The vessels
have been designed to operate at a maximum pressure of 50 psi.  The overall
vessel height from dished end to dished end is approximately 33 ft, which
will allow for a 40 percent expansion of the carbon bed on backwashing.
The filter bottom will consist of 1 ft of gravel over Leopold tiles.
     The columns will be backwashed with plant effluent utilizing two variable
speed, vertical turbine pumps, one of which will serve as a standby.  A
maximum wash water rate of 9,100 gal/min will insure 40 percent expansion

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                                    -12-
of the filter at 75°F and the water will  be discharged to a  backwash lagoon.
It is anticipated that each column will  be washed for 15 min daily,  with
one column backwashed every 2 hours on a time cycle, and will  also use a
surface wash.  A clear well with a volume equal  to approximately 1.0 times
a single backwash is provided, but the effective volume is greater since
there is a continuous flow into the clear well  at all  times  except at shutdown.
A backwash basin (two 65 ft diam. tanks) will be provided to uniformly return
the backwash water together with the carbon transfer motive  water to the head
end of the plant.  Under the most adverse conditions,  the maximum rate of
return to the head end of the plant will  be 2.2 million gallons per day or about
12 percent of the plant throughout.  Because the dissolved oxygen will be
depleted in passing through the carbon columns,  the effluent will be aerated
to maintain a level of 5 mg/liter of dissolved oxygen.
     Approximately once a week it will be necessary to replace the carbon in
one of the vessels.  Spent carbon will be transferred to a spent carbon storage
vessel through water eductors which are sized to empty or refill one vessel
in less than 6 hours.  The volume of the spent carbon and regenerated carbon
storage vessels will be equal to 2 times the carbon in any one filter vessel.
The carbon will be regenerated in a 10 ft - 9-in diameter six hearth furnace
utilizing steam.  It has been sized based on continuous operation with a
                                           2
loading rate of 100 pounds of carbon/day/ft  of hearth.  An  impingement
scrubber will be used to remove particulates from the gas stream.  In
transferring the carbon, two water streams are required:  fluidizing water
for maintaining the carbon-to-water ratio (1-2 Ib of carbon/gal of slurry)
and motive water to operate the eductors.

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      Fluidizing  water will  be  pumped  against essentially the static head
 and  motive  water at  the most efficient  combination of pressure and volume.
 Fluidizing  water and motive water  to  and from  the carbon vessels will be
 provided  by separate constant  speed pumps which will operate at 100 psi,
 with suction from the process  water header.
      Figure 6 shows  the plant  layout  and Figure 7 is an architect's
 rendering of the proposed plant.
      Estimated Costs.  Bids were taken for construction of this plant and
 a contract  was let in January, 1973 for $10,700,000.   It should go into
 operation in  early 1975.  The estimated first year operating cost is $515,000,
 based on  1971 prices.  Amortizing the plant construction cost of 6 percent
 over  20 years, this gives a treatment cost, including operation and mainte-
 nance, of $280 per million gallons.

 WESTERN CITY
      Geographic  Situation.  We are currently involved in a study of water
 pollution abatement facilities for a western city of about 200,000 population
 which is  located on a well regulated stream with a minimum flow of about
 2,000 cfs.
      Nature of Wastes.  The wastewater is rather representative of normal
 municipal wastes although there is a substantial  contribution of industrial
 wastes from food processing plants and local service industries.   There are
 no problems with toxic industrial wastes.
     Effluent Quality Requirements.  Some 30 miles downstream from the existing
 primary treatment plant a  150 ft high  dam has been built forming a reservoir
 some twenty miles long.   During the summer  this becomes  thermally  stratified
and the bottom waters become depleted  of dissolved oxygen.   There  have been
 increasing problems with algae  growths in the reservoir.

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                                    -14-
     The city has been ordered to provide facilities for phosphate
removal from its wastewater and to provide secondary treatment.
     Pilot Plant Operations.  Two principal schemes have been studied for
providing this treatment, namely chemical precipitation of phosphates in
the primary facilities followed either by carbon adsorption or by biological
treatment.  Both have been studied on a pilot plant scale using lime, alum
and ferric chloride as the precipitating chemicals.  Approximately 300 mg/1 of
lime, 175 mg/1 of alum and 90 mg/1 of ferric chloride appear to be necessary
to achieve about 90 percent removal of phosphates as is required.  Because
chemical costs are high with lime at about $40, alum at $70 and ferric chloride
at $160 per ton, lime, together with recalcination, seems to be the most
economical chemical.
     The activated carbon columns have not shown notably promising performance.
Early results indicate about 65 percent removal of both COD and BOD by the
carbon columns with effluent BOD's and COD's of about 40 and 63, respectively,
with an empty bed contact time of 30 minutes.  The indicated exhaustion rate
is about 1,100 pounds of carbon per million gallons and a COD loading of about
0.45 pounds of COD per pound of carbon.  Although these are only preliminary
results it would appear that the biological treatment will  be the more
economical in this situation.

SUMMARY
     At Niagara Falls a physical  - chemical treatment process was selected
largely because the wastes to be treated would have been toxic to biological
processes and many of the objectionable constituents would not have been
removed by biological processes.   At Fitchburg the process was chosen because
of the better quality effluent produced and the greater stability in operation
as compared with biological  treatment.  In each case the choice was a clear
one.  In a third city with no unusual industrial waste problems preliminary

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                                   -15-
results of pilot plant work indicate that a chemical  - biological  treatment
process will  probably be preferable to physical  - chemical  treatment.
     At the moment there has been no full-scale  experience  with independent
physical - chemical  treatment.  I think we all await such results  to enable
us to improve designs and cost estimates for such plants.  The delays  which
have held up construction and operation of the several  plants  of this  type
have been frustrating.  We hope that they are about at an end.

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RAW
SEWAGE   CHEMICAL
PUMP     ADDITION
COAGULATION
FLOCCULATION
TANKS
CLARIFIER
pH
ADJUST-  COAL/SAND
ME NT    FILTER
  LIME
  POLYMER
                        ACTIVATED
                        CARBON
                        COLUMNS
                             PH
                DISSOLVED     ADJUST-
                AIR FLOTATION  MENT
       ACTIVATED
       CARBON
       COLUMNS
                          ACID-
                                                 DISCHARGE
                                           DISCHARGE
          FIG. 1  PILOT  PLANT  FLOW  DIAGRAM
                   NIAGARA FALLS, NEW YORK

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          BAR
          RACK
RAPID  FLOCCULATION
MIXER  BASIN      CLARIFIERS
CARBON
CONTACT
BEDS
  INFLUENT
  SLUDGE TO.
  DISPOSAL
             VACUUM   SLUDGE
             FILTERS  THICKENERS
                                      CARBON
                                      REGENERATION
                               EFFLUENT
                               TO RIVER
                          CHLORINE
                          CONTACT
                          CHAMBERS
FIG. 2  SCHEMATIC  OF  WASTEWATER  TREATMENT  FACILITY
                    NIAGARA FALLS, NEW YORK

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FIG. 3 ARCHITECTS  RENDERING
    NIAGARA FALLS,  NEW YORK

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WESTMINSTER
                FIG. 4 FITCHBURG WASTEWATER  ABATEMENT FACILITIES

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  I. TOWN OF WESTMINSTER (FUTURE)

  2. MONTACHUSETT REGIONAL VOCA-
   TIONAL TECHNICAL HIGH SCHOOL

  3. CITY OF FITCHBURG
   PRIMARY SEDI-
   MENTATION
  COMMINU-
  TION
FLOW
MEASURE-
MENT
CHLORINA-
TION
  FLOW
  MEASURE-
  MENT
      r
  I. WEYERHAUSER CO.

  2. FITCHBURG PAPER CO.
        CHEMICAL
        ADDITION
                                       EAST FITCHBURG
                                       STP
                              PRIMARY
                              SLUDGE


                            SLUDGE
                            LAGOONS
                            (OFF SITE)
                            COAGULATION
                            FLOCCULATION
                                                          CARBON
                                                          REGENER-
                                                          ATION
                                  T   I

                                  I   I
                                  I
                                  I
                                  I	t
                                CARBON |
                                FILTER  I
                                       \
                    FILTER BACKWASH
LJ
ID

U_
U.
UJ
FIG. 5  SCHEMATIC   OF  WASTEWATER  TREATMENT  PLANT
                   WEST   FITCHBURG,   MASSACHUSETTS

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                                SLUDGE AND
                      CLARIFIERS  /  CHEMICAL  BUILDING
                                                             TREATMENT
                                                                PLANT
                                                                BUILDING
                      BOSTON   AND   MAINE    RR
                                                                 •-J  I-
SCALE IN FEET

  FIG. 6  WEST  FITCHBURG  WASTEWATER TREATMENT  FACILITY   SITE   PLAN

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           FIG. 7  ARCHITECTS  RENDERING
      WEST WASTEWATER  TREATMENT FACILITY
               FITCHBURG, MASSACHUSETTS
CAMP DRESSER & MCKEE

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