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                              359
-------
                          SECTION VIII

           COST, ENERGY, AND NON-WATER QUALITY ASPECTS


This   section   presents  an  analysis  of  cost  estimates  and
associated  energy  and  non-water  quality  impacts  of  various
alternative   technologies.    Selected   in-plant  controls  are
discussed herein, and the costs are included under the technology
costs.   The  determination  of  which  costs  and  benefits  are
acceptable  for  BPT  will  be made by the EPA prior to proposing
regulations.

The treatment alternatives for direct  and  indirect  dischargers
are  considered  together,  rather  than  separately, because the
majority of POTWs  (Publicly Owned Treatment Works) are unable  to
remove  the heavy metals found in this industry's wastewater.  In
many cases, an industrial source can  discharge  to  a  municipal
sewer  by  paying  a  service  charge  and providing some form of
pretreatment.  Pretreatment is required for  any  pollutant  that
"interferes  with,  passes through, or otherwise is incompatible"
with a POTW.  Many POTWs are secondary biological  systems  which
do not effectively treat heavy metals to low levels.  POTWs, like
other  discharge  sources,  have  limitations  on  the  levels of
pollutant they  discharge.   As  a  result,  municipalities  have
developed  sewer  ordinances  limiting the discharge level to the
POTW of pollutants that POTWs can not remove.  A survey of  these
ordinances  revealed that many municipalities limit the levels of
heavy metals being discharged to the POTW  (23) .  A summary of the
limits set in sewer ordinances are tabulated below.

                Minimum       Mode       Maximum      Number of
Pollutant     Limit  (mg/1)    (mg/1)    Limit  (mg/1) Municipalities

As               0.01          0.05         3            35
Cd               0.002         0.1;2       15            58
Cr               0.1           5           25            49
Cu               0.06          1;3         18            66
Pb               0.05          0.1          5            U9
Hg               0.0005        0.005        5            30
Ni               0.1           1           15            57
Se               0.01          0.02         5            2H
Ag               0.03          0.1          5            35
Zn               0.2           5           50            64
                                 361
-------
Therefore, nonferrous metals plants that discharge to POTWs must,
in many cases, remove heavy metals to levels comparable to direct
dischargers.   For  this  reason,  the treatment alternatives for
indirect and direct dischargers  are  developed  without  distin-
guishing between the two.

The  basis  used  to  develop costs for treatment technologies is
presented first, followed by the estimated costs and benefits for
the alternatives applicable  to  each  subcategory.   Energy  and
other non-water quality aspects are also presented.

Existing  plants  and  new  sources are discussed separately with
existing plants being covered first.

EXISTING SOURCES

In-Plant Control Measures

The in-plant control measures that exist in or are  available  to
plants in the nonferrous metals industry are discussed in Section
VII.   The  incorporation of in-plant controls into the processes
of an existing source can be a cost-effective means  of  reducing
pollutant   and  hydraulic  loadings  and  thereby  the  cost  of
treatment facilities.  Recycle of various process streams is  the
most  common in-plant control suggested for BAT.  The assumptions
used to develop the costs of recycling wastewater  are  presented
under  the  "Investment  Cost  Basis" portion of this section.  A
description of the recycled streams is  provided  in  the  "Plant
Costs" portion of this section.  The costs of the recommended in-
plant  controls  are  included  for  each treatment scheme in the
summation curves of annual costs.

Alternative Technologies and Basis of Cost Estimates

The results  of  detailed  cost  analyses  of  various  treatment
technologies for existing sources are described below.  Summation
curves  have  been  used  to present the annual costs.  Costs for
each subcategory are presented separately. In some  subcategories
the  individual wastewaters combine in ways that reguire a unique
set of treatment alternatives.  In other cases treatment  schemes
are essentially the same for more than one subcategory.  In these
cases,  the  same  annual cost curves for a given alternative are
presented under the discussion of more than one subcategory.

Investment Cost Basis and Technology Description

Investment costs include  equipment  and  installation  costs  of
treatment components and monitoring equipment plus allowances for
contingencies  and  engineering.   For  technologies currently in
use, i.e. chemical precipitation, vacuum filtration,  filtration.
                                 362
-------
pH  adjustment,  chlorine oxidation, activated alumina, activated
carbon, steam stripping, reverse osmosis, sedimentation,  holding
tanks, cooling towers, and evaporation, specific cost curves were
developed  from  current  bids,  the literature and other sources
(74, 99,  100,  127  through  159).   The  cost  information  was
equalized  by  updating all the costs to the 4th quarter of 1976.
The national average EPA-Standard  Treatment  Plant   (STP)  index
and/or  EPA-Large  City Advanced Treatment (LCAT)  index were used
to update the costs for preliminary engineering  estimates.   The
EPA-LCAT index was chosen because its component mix is indicative
of  the  treatment processes presented herein.  The EPA-STP index
was chosen because it was the index used by  a  majority  of  the
references from which costs were obtained.  These cost values are
averages  for  the  nation  and,  under  specific regional market
conditions, could  vary as much as 4056.   The  factors   (160)   in
Figure  VTII-1  can  be  used  to  obtain  the capital cost for a
particular location.

Total installed costs are broken into equipment and  construction
fractions as follows:   (160)

Process                       Equipment          Construction

Chemical Precipitation            20                  80
Vacuum Filtration                 35                  65
Multi-Media Filtration            20                  80
pH Adjustment                     35                  65
Chlorine Oxidation                35                  65
Activated Alumina                 50                  50
Activated Carbon                  50                  50
Steam Stripping                   35                  65
Reverse Osmosis                   50                  50
Holding Tank                      50                  50
Sedimentation                     10                  90
Cooling Tower                     35                  65
Evaporation Lagoon                10                  90

A  contingency allowance of 15% of the installed cost was used to
cover  unexpected  costs  due  to  local  plant  conditions   and
differences  between  actual  systems and those used for the cost
estimates.  No allowance  was  made  for  plant  shutdown  during
construction.  The need for a shutdown is dependent on the layout
of  each  plant.   Engineering  costs  were  estimated by using a
percentage  of  the  installed  cost  plus  contingencies.    The
percentage  used  was  to  the  nearest  0.55?  from  curve  A  in
Consulting Engineering  (ASCE MOP #45), which is a plot of percent
engineering costs versus construction costs.

Investment costs were developed for each level of  treatment  and
were  then  amortized  for  incorporation  into  the  annual cost
                                 363
-------
summation curves.  The summation curves present the cost of  each
alternative  as  a  plot  of annual cost ($/yr) versus plant flow
(mgd).  This approach allows the reader to determine the cost  of
any size plant.

The  alternatives  for  treatment  include  one  or  more  of the
following unit operations or processes in various combinations:

Chemical Precipitation.  Lime is used to precipitate  metal's  and
the  process  includes sedimentation and thickening of the sludge
plus sludge dewatering by vacuum  filtration.   Investment  costs
for  chemical  precipitation  were developed assuming lime as the
precipitant and including sedimentation, gravity  thickening  and
vacuum   filtration.    Lime   was   selected   because   of  its
comparatively low cost coupled with its proven  effectiveness  in
the  industry.   While it is recognized that caustic, iron salts,
and sulfides may be more appropriate in some applications,  costs
for  these  precipitants and their feed systems are comparable to
lime relative to the overall costs of  a  chemical  precipitation
system.

Specific cases were developed for chemical precipitation relating
investment  cost to lime dosage and sludge production.  The cases
are as follows:

            Case        Lime (mg/1)         Sludge  (Ib/mil gal)

              1          16,000                500,000
              2           7,300                250,000
              3           2,500                100,000
              a           1,100                 50,000
              5             580                 25,000
              6             285                 10,000
              7              50                  1,500

Units were sized for these cases based on  an  overflow  rate  of
40.75   m3/day-m2    (1000   gpd/ft2)  for  sedimentation  and  an
application rate of 122 kg/day-m2   (25  Ib/ft2/day)  for  gravity
thickening  (161) .

The  investment  costs  for  vacuum  filtration were developed in
terms of the amount of sludge to be dewatered.  The  filter  area
was  calculated using a dry solids loading rate of  19.53 kg/m2/hr
 (U Ib/ft2/hr) and an operating period of 10 hrs/day   (143) .   The
quantity  of  solids  requiring  dewatering  is  dependent on the
treatment alternative and the specific  lime   dosage  and  sludge
production   cases,  as  previously  described,  used  with  each
alternative.
                                  364
-------
Multi-Media Filtration.
        fine
        of
 	  A. granular media filter bed is  used  to
   particulates.   The  filter  bed consists of graded
 gravel,  coarse  anthracite  coal,  and  fine   sand.
the   filter  backwash  is  pumped  to  the  secondary
          However, when  filtration  is  used  without
               the  backwash  is  pumped directly to a
remove
layers
Normally
sedimentation tank
chemical  precipitation,
vacuum filter.
The hydraulic loading rate used  was  163  1/min-m2  (4  gpm/ft2)
(143).  Specific cases were developed for filtration as follows:
                   Case

                    1
                    2
                    3
                    4
                            TSS Removed (mg/1)

                                100
                                 50
                                 15
                                  5
The solids carried over to the filter from chemical precipitation
have  a  direct  influence  on  the  solids being recycled in the
backwash to the secondary clarifier  and  therefore  add  to  the
sludge volume applied to the vacuum filter.

Neutralization or p_H Adjustment.  H2SO4 (66°Be')  and/or NaOH (50%
liquid)  are  utilized  to  obtain  desired  pH values at various
points in any given alternative sequence.  The  investment  costs
include a mixing tank and chemical handling systems for both acid
and alkaline solutions, which also include storage tanks.

Chlorine  Oxidation.   Chlorine  gas  is used to oxidize or break
down  undesirable  pollutants  that  may  interfere  with   other
processes  or  remain  in  an  effluent.   Specifically, chlorine
oxidation is used for cyanide and ammonia destruction.

The investment costs include chlorine storage and  feed  systems,
and  a chlorine contact tank with a detention time of 30 minutes.
The costs also include a feed system for adjustment  to  alkaline
pH prior to chlorine addition.
Activated  Alumina.
           Contact columns containing alumina are used
          and  fluoride.   The  backwash   and   spent
to  remove  arsenic
regenerant  are  both recycled to the chemical precipitation unit
for removal of the concentrated pollutant.

The investment costs  are  based  on  a  system  using  activated
alumina  in  contacting  columns.   A surface loading rate of 122
1/min-m2 (3 gpm/ft2)  was  assumed  with  an  alumina  adsorption
capacity of 0.5% by weight for fluoride and arsenic  (80).
                                 365
-------
Activated  Carbon.  Granular activated carbon in downward flowing
contacting columns is used to adsorb colloids and large molecular
pollutants.  An exhaustion rate of .18 kg/m3  (1500  Ib/mil  gal)
was assumed for all subcategories except secondary silver.  A .66
kg/m3  (5500  Ib/mil  gal)  and  1.49  kg/m3  (12,400 Ib/mil gal)
exhaustion  rate  was  assumed   for   secondary   silver,   non-
photographic  and  photographic, respectively,  on-site multiple-
hearth furnace  regeneration  was  assumed  for  plants  treating
wastewater  flows  greater  than  1287, 435, and 193 m3/day (.34,
.115, and .051 mgd) for exhaustion rates of .18,  .66,  and  1.49
kg/m3  (1500,  5500,  and  12,400  Ib/mil gal) respectively.  For
plants smaller than those given for each exhaustion rate, it  was
assumed  that  the spent carbon would be discarded.  Many factors
influence the  investment  cost  for  activated  carbon  systems;
namely,   exhaustion   rate,  carbon  type   (manufacturer  &  raw
material), contact type  (upward, downward - packed, expanded)  and
regeneration method.

Steam Stripping.  A stripping tower and steam are used to  remove
ammonia  from  the  wastewater.   The  investment costs include a
stripping tower, a boiler, and a blower.  A surface loading  rate
of  81.5  1/min-mz   (2  gpm/ft2)  was  assumed along with a steam
requirement of 1 pound of steam per gallon of wastewater treated.

Reverse Osmosis.  To remove selected  ions  from  the  wastewater
streams,  prefiltration cartridges are used along with membranes.
The resulting brines are further concentrated into  a  disposable
sludge by multiple-effect evaporators.

The investment costs include prefiltration cartridges, membranes,
membrane housing, pumps, and mechanical evaporation of the brine.
Costs  were  based  on  a recovery of 85% of the flow through the
reverse osmosis unit and  a  98%  reduction  in  the  brine  flow
through the mechanical evaporator.

Holding  Tank  and  Cooling  Tower.   These  two  items  will  be
discussed together as they  are  incorporated  into  the  various
treatment  schemes  to  provide  cooling of contact cooling water
prior to recycle.

By reviewing the information  supplied  in  the  data  collection
portfolios  it  was  found  ,that   85%  of the plants that recycle
contact cooling water following treatment through cooling  towers
have  flows  greater  than  303 m3/day  (80,000 gpd).  It was also
found that 60% of the plants that  recycle contact   cooling  water
following sedimentation or no treatment have  flow rates less than
303  m3/day   (80,000 gpd).  For those plants that recycle contact
cooling water with no reported treatment, 86% had contact cooling
water flows less than 303 m3/day  (80,000 gpd).  It  was  therefore
assumed  that plants having contact cooling water flows less than
                                 366
-------
303 m3/day (80,000 gpd)  would provide recycle following  a  day's
retention  time  in a. holding tank and that plants having contact
cooling water flows greater than 303 mVday  (80,000  gpd)  would
provide recycle following treatment in a cooling tower.

The investment costs for a holding tank include tanks, pumps, and
1,000  ft  of  piping with the tanks sized to store a day's flow.
The investment costs for a cooling tower  assume  the  use  of  a
mechanical  (induced)  draft  tower and include the tower, pumps,
305 meters (1,000 ft) of piping, fans and packing.  The sizing of
the tower is based on a range of 13.9°C (25°F),  an  approach  of
5.6°C (10°F),  and a wet bulb temperature of 21.11°C (70°F) (162).

Sedimentation.   Primary  sedimentation  is  utilized  to  remove
suspended solids from the wastewater  stream  prior  to  recycle.
The investment costs include a primary sedimentation tank, solids
removal  mechanism,  and  305  meters  (1,000 ft) of piping.   The
costs were based on a hydraulic loading rate  of  32.6  m3/day-m2
(800 gpd/ft«)  (161) .

Evaporation.    A   lagoon  is  used  for  solar  evaporation  of
wastewater in regions of net evaporation.  The  investment  costs
include  excavation  and  dikes,  land  costs, asphalt or plastic
liner, pumps and pipes.  The sizing of the lagoons was  based  on
the  net  effective  annual  evaporation  rate.   This  value was
determined for each plant.

Monitoring.  The costs are based on  collecting  samples  of  the
influent  and  effluent  streams  of  the  treatment  plant.   The
sampling schedule is for 24-hour composite samples  to  be  taken
once  per week.  Continuous monitoring of the pH and flow is also
provided for the influent and effluent of all treatment plants.

The equipment items include two flow meters, two primary and  one
backup  refrigerated samplers, two pH meters, refrigerated sample
storage containers, and a refrigerator.  The costs are  based  on
equipment manufacturers' price lists  (157, 158, 159) .

The  above  treatment  operations  and  processes,  alone  or  in
combination, have been arranged in alternatives which may be  BAT
level  technologies.   Removal of metallic priority pollutants by
chemical precipitation  has  been  widely  demonstrated  in  this
industry.  Consequently, treated concentrations can be determined
with  a high degree of accuracy.  Removing metals to lower levels
by activated alumina and reverse osmosis has had limited  use  in
the  industry.  The effectiveness of activated carbon in removing
the organic priority pollutants has not been demonstrated in  the
nonferrous metals industry.  Reports are available, however,  that
discuss  the  degree of adsorbability of activated carbon for the
individual priority pollutant organics (102, 111, 163, 112,  17) .
                                  367
-------
Based  upon  these reports, conservative estimates have been made
for removals by carbon and its exhaustion rates  under  different
operating conditions.

Land Costs

Land  requirements   (129)   are  presented  in  Figure  VIII-2 for
individual  technologies.     The   technologies   are:   chemical
precipitation,   primary   sedimentation,  filtration,  activated
alumina,  activated  carbon,  steam   stripping,   oxidation   by
chlorine,  cooling tower,  pH adjustment, reverse osmosis, holding
tanks, and vacuum filtration.  The total land requirement can  be
determined   from   Figure   VIII-2  by  summing  the  individual
requirements of each technology for any given alternative.

Land costs are not provided, as costs are  highly  site  specific
and could vary by several magnitudes.  Land costs for evaporation
lagoons,  however, were taken to be $1,000/acre, as lagoons would
be  utilized  in  rural  areas  where  $1,000/acre  would  be   a
reasonable  cost  for  land.   Land  requirements for evaporation
lagoons are presented in Figure VIII-3  (98).

Annual Costs

Capital.  Capital costs were amortized at  an  interest  rate  of
7.75%  over  a  20-year period, i.e. cost of capital being 10% of
the investment per annum.  Consequently,  the  capital  investment
cost can be determined from the capital cost curve by multiplying
any  annual  capital  cost value by ten.  Since the current money
market is unstable, the annual capital costs may need  adjustment
for  higher interest rates.  The following table presents factors
to convert the amortized cost of capital  expenditures  shown  in
the annual cost summation curves to the amortized capital cost at
a  variety of other  interest rates.  These factors are based on a
payback period of 20 years.
                                 368
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       Interest         Capital Recovery         Multiplication
         Rate                Factor                   Factor

         7.75                .09996                   1.0
         8                   .10185                   1.02
         8.5                 .10567                   1.06
         9                   .10955                   1.10
         9.5                 .113/18                   1.13
        10                   .11746                   1.17
        10.5                 .12149                   1.21
        11                   .12558                   1.26
        11.5                 .12970                   1.3
        12                   .13388                   1.34
        12.5                 .13810                   1.38
        13                   .14235                   1.42
        13.5                 .14665                   1.47
        14                   .15099                   1.51

Decree iation.   Estimated  lives  of  the  components   of   each
alternative  were established and related to the investment costs
to determine the estimated design life of each alternative (131).
The estimated lives for each component are as follows:

              Technology                    Useful Life  (yrs.)

         Chemical Precipitation                  25
         Vacuum Filtration                       15
         Filtration                              15
         pH Adjustment                           15
         Chlorine Oxidation                      15
         Activated Alumina                       15
         Activated Carbon                        15
         Steam Stripper                          15
         Reverse Osmosis                         20
         Holding Tank                            20
         Sedimentation                           25
         Cooling Tower                           15
         Evaporation Lagoon                      25

The life of any alternative was determined by calculating a  cost
weighted  average  (dividing  the sum of the products of cost and
useful life for each process by the sum of the costs).  This  can
be expressed as:


Years = ($xYears) = ($C.PxYr C.P.) + ($VFxYr VF) + (SFxYrF) +...
            $           $C.P.      +   $VF      +   $F      + $...

The  installed  cost  plus  contingencies  were  depreciated on a
straight line basis for the calculated life of each alternative.
                                 369
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Operation and Maintenance Labor.  Estimates of  the  annual  man-
hours  required  to operate and maintain the various systems were
developed from the literature   (129,  164) .   A  productive  work
value of 6.5 hr/man/dayr or 1,500 hr/yr/man was assumed (164).  A
rate  of  $15/hr  was used as the total cost for wages, benefits,
and overhead expenses.   Supervisory,  administrative,  clerical,
and  laboratory  man-hours were developed and are included in the
OSM labor costs.  Figure VIII- 4 shows how  the  wage  rates  will
vary  with  location throughout the U.S.  The factors  (165) shown
can be multiplied by the assumed rate of  $15/hr  to  obtain  the
wage rate at that location.

Maintenance  Materials .   The annual costs of materials and parts
needed  to  maintain  each  process  were  developed   from   the
literature and equipment manufacturers.  (129, 131, 100, 99, 138,
139, mo,
Chemicals.    To   determine   the  chemical  cost  for  chemical
precipitation, lime was chosen as the  precipitant.   The  annual
use  for  a  given  installation  was  determined  by  the  cases
described under Chemical Precipitation which  correspond  to  the
wastewater characteristics .

Sulfuric  acid   (66°Be')  and  sodium hydroxide  (50$ liquid)  were
assumed to be used for pH adjustment.  A dosage of 0.5 pounds  of
acid  or  caustic  per  1,000  gallons  of  flow  was  used  as a
conservative assumption.

For chlorine oxidation  of  cyanide  a  dosage  of  800  mg/1  of
chlorine was assumed, while 3,04)0 mg/1 of chlorine was assumed as
the dosage for oxidation of ammonia.

Activated alumina chemical usage includes sulfuric acid  (66° Be')
and   sodium   hydroxide    (50%  liquid)  for  regeneration,  and
replacement of activated alumina.   For  regeneration,  four  bed
volumes  of  1fl  NaOH and one bed volume of .05N H2SO4 are needed
every two days.  An attrition rate of 10% per year for  activated
alumina was assumed.

The  activated  carbon  process  incurs  chemical  costs  for the
replacement of carbon.   For  small  plants  that  find  it  more
economical  to  discard  the  carbon after exhaustion, the entire
carbon inventory is replaced according to  the  exhaustion  rate.
For  those  plants  that  utilize  on-site  regeneration,  it was
assumed that 8% of the carbon is lost  during  each  regeneration
and must be replaced.

The  chemical  costs  for  reverse  osmosis  include the membrane
cleaning chemicals.  These costs were taken from literature  (139,
                                   370
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     149).  The costs of chemicals (166) were assumed  to  be  as
follows:

Chemical                Cost ($/ton)

Lime (CaO)                   30
SO2                         180
Activated Alumina           340
Activated Carbon           1000
NaOH (50% liquid)           160
H2SO4 (66° Be1)              47

Energy  and  Power.   Operating time for all equipment of all the
treatment alternatives, with the exception of vacuum  filtration,
was  assumed  to  be  24 hrs/day and 300 days/yr.  Vacuum filters
were sized to operate 10 hrs/day, 300 days/yr.

Annual electrical energy consumption values  for  each  component
were  developed  utilizing  technical  literature (167, 168, 169,
170, 146) and equipment manufacturers' specifications  (145) .   In
developing the costs, all electric motors were assumed to have an
efficiency  of  88%  (171) and the cost of electricity was assumed
to be 3.32/kwh.  This cost value is  an  average  value  for  the
entire  U.S.  taken  from  the industry data collection portfolio
responses.

Fuel oil and natural gas  costs  were  developed  from  the  data
collection   portfolio   responses   and   applicable   technical
literature  (134).  National average costs were determined  to  be
24£/therm for fuel oil and 182/therm for natural gas.

Vacuum  filtration  energy  consumption  varies with filter area.
The area, or size of the filter, is dependent on  the  amount  of
sludge  to  be  dewatered  which  is  a  function of the chemical
precipitation and filtration cases, and of the  flow  rate  being
evaluated.   Consequently,  energy  consumption  is  dependent on
these criteria also.

Energy consumption for activated carbon is dependent on the  flow
and  whether  the  exhausted  carbon is regenerated or discarded.
The remaining technologies1 consumption is based solely on flow.

Sludge Disposal.  Sludge disposal costs cover  hauling  dewatered
sludge,   exhausted  activated  carbon,  and  concentrated reverse
osmosis brine, when applicable, to an approved sanitary landfill.
The hauling costs were obtained from literature  (172,  173) ,  and
plotted  as  tons/yr of dry sludge hauled vs. $/dry ton.  A round
trip hauling distance of 10 miles was assumed.   (See Figure VIII-
5).
                                 371
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Sludge disposal costs are related  to  the  cases  developed  for
chemical   precipitation   and   filtration.   Recycle  of  spent
activated alumina regenerant to the chemical  precipitation  unit
increases the amount of sludge.

Costs  to  dispose of spent activated carbon are based on hauling
to a landfill.  It was assumed that the carbon would be dewatered
to 50% solids, i.e., containing its own weight in water.

Monitoring.   Monitoring   costs   include   outside   laboratory
analytical  charges  and time for reporting results to regulatory
agencies.  The costs associated with  collecting  and  delivering
samples are included under operation and maintenance labor.

Sampling  frequency  was  assumed to be once per week of both the
influent and effluent.  Criteria pollutants are analyzed once per
week and priority pollutants are analyzed once per month.

Laboratory cost estimates were based on  current   (Jan.  -  June,
1978) commercial laboratory price lists  (17U, 175, 176, 177, 178,
179,  180) .   Reporting  costs were based on $15/hr and allowed 2
hr/week for compiling data plus 8 hr/month for preparing reports.

Plant Costs

In the nonferrous metals industry, each subcategory  possesses  a
set  of  wastewater  streams  that  must  be  treated  to  remove
pollutants or for recycle.  Most plants differs from  each  other
in  the  combination of streams and/or the flow rate.  Wastewater
characteristics play an important role in  determining  treatment
alternatives and these characteristics are primarily dependent on
the  combination  of  streams existing at each plant.  Therefore,
the various subcategories in the nonferrous metals  industry  are
discussed  separately  in  order  to present the wastewaters, the
combinations of wastewaters, the rate of flow, and the  treatment
alternatives.

To  determine  a  specific  plant's  costs,  first  calculate the
process wastewater flow in gal/day.   The rate used  for  contact
cooling  water  should  be  5%  of the plant's use, or the amount
discharged,  whichever  is  less.   Rainfall   runoff   was   not
considered  as  a  process wastewater, nor was noncontact cooling
water.  The annual  costs  can  then  be  read  easily  from  the
appropriate curves.

For  example,  assume  a primary aluminum plant has the following
discharged flows:

                           Actual Flow      Flow for Costing
Anode bake plant             10,000         10,000
                                 372
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Potline scrubber             60,000         60,000
Casting (use=discharge)     140,000          7,000
Noncontact cooling          100,000	0_
                                            77,000

This plant would be included in  Combination  3.   Going  to  the
appropriate cost curves, the incremental annual costs would be as
follows:

Alternative 1      $150,000
Alternative 2       210,000
Alternative 3       320,000
Alternative H       250,000

and the total annualized costs would be as follows;

Alternative 1      $150,000
Alternative 2       360,000
Alternative 3       680,000
Alternative 4       610,000

The  treatment alternatives assume 95% recycle of contact cooling
water, after a  cooling  tower  or  a  holding  tank,  which  are
included  in  the  costs.  All other process wastewater presently
discharged is assumed to be treated  by  each  alternative.   For
example,  it  was assumed that the hypothetical plant above would
treat all its present effluent through  each  alternative,  i.e.,
77,000 gpd would be treated by reverse osmosis in Alternative 3.

Obviously,  where  recycle  is  employed  it is less expensive to
treat the recycled wastewater only to  the  extent  necessary  to
prevent  plugging,  fouling, or other problems.  The hypothetical
plant  above  could  recycle  50%  of  its  flow  after  chemical
precipitation, and 50% of the remainder after filtration, leaving
only  about  20,000  gpd  to be treated by reverse osmosis.  This
would result in annual savings of about $250,000.

Determination of the Benefits of Treatment

The wastewater concentrations for each waste stream given in  the
tables  below  were  determined  from  sampling data presented in
Section V.  The effluent quality from each treatment  alternative
was determined from information presented in Sections V and VII.

For each subcategory's waste streams, the water use and discharge
levels  (in  gallons  per  production  normalizing unit) for each
plant were calculated, as shown in Section VII.  BAT  flow  rates
were  selected  for  each.   In  all  cases,  wastewater flow and
production data  obtained  from  the  data  collection  portfolio
responses,  NPDES  Discharge  Monitoring  Reports, and the sample
                                 373
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collection program were considered in determining the appropriate
BAT flow rate.

PrimarY  Aluminum.   Four  groups  of  wastewaters  exist in this
subcategory.  These streams are:

    1.   Paste, bake plant, and cathode making wastewater
    2.   Air pollution control wastewater
    3.   Contact cooling water
    £*»   Cathode reprocessing wastewater with cryolite recovery

These four streams are  found  in  eight  different  combinations
throughout  the  subcategory.   The  first five combinations were
chosen for the cost analysis, because  they  cover  most  of  the
subcategory.  The combinations are tabulated below.  The costs of
treatment  for  plants  in  combination  6 are represented by the
costs  given  for  combination  5.   Combinations  7  and  8  are
represented by combination 3.

                                           CONTACT
                   PASTE                   COOLING    CRYOLITE
    COMBINATION    PLANT     SCRUBBERS     WATER      RECOVERY

        1           X                        X
        2                                    x
        3           x           x            x
        4                       XX
        5           x           x            xx
        6                       xxx
        7           x           x
        8                       x

Three  levels  of treatment were developed for combinations 1 and
2, and four levels of treatment were developed  for  combinations
3,   4,  and  5.    The  alternatives  are  described  below  and
schematically presented in Figure VIII-6.

Level 1. For combinations 1 and 2 — 95% of the  contact  cooling
water  is  recycled  through  a cooling tower, and a five percent
blowdown is combined with the other stream for combination 1  and
treated by chlorine oxidation, lime precipitation, and filtration
followed  by recycle.  For combinations 3, 4, and 5 — 95% of the
contact cooling water is recycled through a cooling tower, and  a
five  percent  blowdown  is  combined  with the other streams for
treatment by chlorine oxidation and lime precipitation,  followed
by recycle.

Level 2. For combinations 1 and 2 — reverse osmosis is added  to
level  1  and  the effluent is completely recycled.  For combina-
tions 3, U, and 5 — filtration and activated alumina  are  added
                               374
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•to  level  1,  followed by recycle.  For combination 3, costs may
tend to be conservative for those plants which  practice  recycle
of reduction scrubber wastewater following lime precipitation.

Level 3. For combinations 1 and 2 — activated carbon is added to
level 1, followed by recycle.  For combinations 3, 4,  and  5
reverse  osmosis  is  added  to  level  2 with the effluent being
completely recycled.

Level 4. For combinations 3, 4, and  5  —  activated  carbon  is
added to level 2, followed by recycle.

The  cost versus pollution reduction summary includes a summation
curve  for  each  level  of  treatment   of   each   combination,
accompanied  by  a  table showing the effluent quality (77 to 83,
110, 118 121, 122, 125, 147 and 181  to  190)  achieved  for  the
significant  pollutants  at  each  level  of treatment.  The cost
curves are presented in the figures listed below.  The  summaries
of  the associated pollution reduction are shown in Tables VIII-1
to 6.

         COMBINATION     FIGURES VIII-

              1              7-9
              2             10-12
              3             13-16
              4             17-20
              5             13-16

Secondary Aluminum.  Three wastewaters exist in this subcategory.
The streams are:

    1.   Dross milling wastewater
    2.   Demagging scrubber wastewater
    3.   Contact cooling water

These three streams are  found  in  five  different  combinations
throughout  the  subcategory.   The first three combinations have
been  chosen  for  the  cost  analysis.   The  combinations   are
tabulated  below.  Combination 4 is represented by combination 1,
and combination 5 is represented by combination 2.

                        DROSS                 CONTACT
         COMBINATION    MILLING   SCRUBBER    COOLING

             1            XX
             2                      xx
             3                                   x
             4            x
             5                      x
                               375
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Four levels of treatment were developed for combinations 1 and 2,
and three levels of treatment were developed for  combination  3.
The  treatment alternatives are described below and schematically
presented in Figure VIII-21.

Level 1. For  combination  1—settling  of  the   dross   milling
effluent   and  treating  the  supernatant  by  steam  stripping,
followed by combining the effluent with the  scrubber  wastewater
for treatment by lime precipitation followed by recycle.  For the
remaining  combinations, the combined streams are treated by lime
precipitation followed by recycle.

Level 2. Gravity filtration is added to the components  of  level
1, followed by recycle.

Level 3. Reverse osmosis and complete recycle of the effluent  is
added  to  the  components  of  level 2 for combinations 1 and 2.
Activated carbon is added to level 2 for combination  3  followed
by recycle.

Level H. Activated carbon is added to level 2 for combinations  1
and 2 followed by recycle.

The  cost  curves are presented in the figures listed below.  The
summaries of the associated  pollution  reduction  are  shown  in
Tables VIII-7 to 10.

              COMBINATION       FIGURES VIII-

                  1                22-25
                  2                26-29
                  3                30-32

CQlumbium-Tantalutn.  For costing purposes, the columbium-tantalum
industry  has  been  divided  into  two  groups.   The groups are
defined as:  ore to salt or metal; and salt to metal.

Ore to Salt/Metal

Three plants exist in this group and there are two  combinations.
Each combination consists of the following wastewaters:

1.  Digestion air pollution control wastewater
2.  Extraction raffinate and gangue washwater
3.  Precipitation supernatant
H.  Salt drying air pollution control wastewater
5.  Reduction air pollution control and leachate
                               376
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Combination  1  represents  those  plants  which  practice  steam
stripping  of   ammonia-laden   streams   and   at   least   lime
precipitation  of  the  overall  combined wastes.  Four levels of
treatment are presented.  The alternatives  are  described  below
and schematically presented in Figure VIII-33.

Level  1.  Oxidation  of  the  precipitation supernatant and salt
drying wastewater by  chlorination  and  filtration  followed  by
recycle, as appropriate.

Level  2.  Activated  alumina  is  added  to level 1, followed by
recycle, if necessary.

Level 3. Reverse osmosis and complete recycle of the effluent are
added to level 2.

Level 4. Activated carbon  is  added  to  level  2,  followed  by
recycle, if appropriate.

Combination  2  consists  of  a  plant  that  does  not treat its
ammonia-laden streams.  Five levels of treatment  are  presented.
The  alternatives are described below and schematically presented
in Figure VIII-33.

Level 1. Steam stripping and oxidation by chlorine  are  used  to
treat  the  precipation  supernatant  and  salt  drying effluent,
followed by recycle, if necessary.

Level 2. The   combined   wastewaters   are   treated   by   lime
precipitation and filtration, followed by recycle if necessary.

Level 3. Activated alumina is added to the  components  described
for level 2, followed by recycle if necessary.

Level t. Reverse osmosis and complete recycle of the effluent are
added to level 3.

Level 5. Activated carbon is added to  the  components  specified
for level 3, followed by recycle.

The  cost  curves are presented in the figures listed below.  The
summaries of the associated  pollution  reduction  are  shown  in
Table VIII-11.

              COMBINATION      FIGURES VIII-

                  1               34-37
                  2               38-42

Salt to Metal


                               377
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Two  plants  exist  in  this  group.  One plant performs tantalum
reduction with wastewaters from reduction air  pollution  control
and  leaching.   The  other  plant discharges wastewater from air
pollution control of columbium salt drying after  lime  treatment
and  sedimentation.   Treatment  costs  and removal summaries are
based on the former plant.  It is anticipated that the raw  waste
characteristics  of  the  salt  drying scrubber stream will be no
worse than those of the tantalum reduction streams, thus the cost
and  removal  estimates  for   the   columbium   plant   may   be
conservative.

The  plant  considered  in this combination discharges wastewater
from  the  reduction  process  without  lime  treatment  of   the
wastewater.   Tantalum  recovery  is  practiced,  but substantial
concentrations of fluoride are discharged.  As  a  result,  three
levels   of   treatment  are  presented.   The  alternatives  are
described below and schematically presented in Figure VIII-43.

Level 1. Treatment  is  provided  by   lime   precipitation   and
filtration, followed by recycle if necessary.

Level 2. Treatment of the combined streams from  level  1  is  by
activated alumina, followed by recycle, if necessary.

Level 3. Activated carbon is added to level 2, and  the  effluent
may be recycled.

The  cost  curves are presented in the figures listed below.  The
summaries of the associated  pollution  reduction  are  shown  in
Table VIII-12.

         COMBINATION      FIGURES VIII-

              1               44 - 46

Primary Copper.  The wastewaters are:

1.  Acid  plant  blowdown  and  related  air  pollution   control
wastewater
2.  Slag granulation wastewater
3.  Contact cooling water

Four combinations of these streams  exist  in  this  group.   The
combinations are shown in the following tabulation:
                               378
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                   ACID                CONTACT
    COMBINATION    PLANT     SLAG      COOLING   ELECTROLYTE

        1                                 x
        2            xx           xx
        3                     xx
        4            xx           x

Combinations 1 and 2 represent the group, with combinations 3 and
4 being included in combination 2.

Three  levels of treatment were developed for combination 1.   The
alternatives are described below and schematically  presented  in
Figure VIII-47:

Level 1. Recycle of the contact cooling water after cooling,   and
treatment  of  a  five  percent  blowdown  is  provided  by  .lime
precipitation followed by recycle.

Level 2. Filtration is added to level 1 prior to recycle.

Level 3. Activated carbon is added to level 2 prior to recycle.

Three levels of treatment are presented for combination  2.   The
alternatives  are  described below and presented schematically in
Figure VIII-51.

Level 1. Recycle of contact cooling water is provided combining a
five percent blowdown with the other streams prior  to  treatment
by lime precipitation and recycle.

Level 2. Filtration is added to level 1 prior to recycle.

Level 3. Activated carbon is added to level 2 prior to recycle.

The cost curves are presented in the figures listed  below.   The
summaries  of  the  associated  pollution  reduction are shown in
Tables 13 and 28.

         COMBINATION      FIGURES VIII-

            1                48-50
            2                51-53

A fourth level of treatment at primary copper plants can be added
to or used in place of any of the above alternatives provided the
plant  is  located  in  an  area  of  net   evaporation,   mamely
evaporation  lagoons.   The costs for lagoons in areas of 10, 20,
and 30 inches net effective evaporation per year are presented in
Figures VIII-58, 59, and 60 respectively.
                               379
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Secondary  Copper.   Four  wastewater  streams  exist   in   this
subcategory.  The streams are:

1.  Slaq milling and granulation
2.  Scrubber wastewater
3.  Electrolyte
4.  Contact cooling water

These  streams  exist  in  five  combinations in the subcategory.
These combinations are:

                    SLAG                              CONTACT
     COMBINATION    MILLING   SCRUBBER  ELECTROLYTE    COOLING

       1             x                                   x
       2                                                 x
       3                        x                        x
       4                        x
       5                        xxx

Three levels of treatment were developed  for  each  combination.
The  treatment alternatives are described below and schematically
presented  in Figure VIII-61.

Level 1. For Combination 1—the supernatant  from primary settling
of the t'.lag milling water is combined with   the  contact  cooling
water  for treatment by lime precipitation prior to recycle.  For
Combination 2--the contact  cooling  water   is  treated  by  lime
precipitation  prior  to recycle.  For Combination 3—the contact
coolin-g and scrubber water  are  treated  by lime  precipitation
prior  to  recycle.   For  Combination  4—the  scrubber water is
treated by lime precipitation prior to recycle.  For  Combination
5—the  contact   cooling  water is recyled through a holding tank
and a five percent blowdown is combined with the  other  streams
for treatment by  lime precipitation prior to recycle.

Level 2. Gravity  filtration  is  added  to  level  1  for   each
combination, followed by recycle.

Level 3,. For Combination 1 and 2—the effluent from  level  2  is
pumped  to a holding tank for recycle.  For  Combination 3, 4, and
5—activated carbon is added to level 2, followed by recycle.

The cost; curves are presented in the figures listed  below.   The
summaries  of  the  associated  pollution  reduction are shown in
Tables VIII-14 to 18.
                               380
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         COMBINATION      FIGURES VIII-  TABLE VIII-

             1               62-64         15
             2               65-67         16
             3               65, 66, 68      17
             4               65, 66, 68      18
             5               69-71         19

Primary Lead.  There are only  three  primary  lead  plants  that
discharge  any  wastewater.   All three plants have at least lime
precipitation in place.  Therefore, the stream to be  treated  is
the  effluent  from  the  existing  treatment.   Three  levels of
treatment are presented as add on to existing  treatment.   These
alternatives  are  described below and schematically presented in
Figure VIII-72.

Level 1. Filtration is added to the existing treatment,  followed
by recycle.
Level 2. Activated carbon added to level 1, followed by recycle.
Level 3. Reverse osmosis and complete recycle are added to  level
         2.

The cost curves are presented in Figures VIII-73 to 75, while the
summary  of  the  associated  pollution reduction is presented in
Tables VIII-19 and 28.

Secondary Lead. There are three sources of wastewater which  form
three  combinations in the group.  The combinations are presented
in the following tabulation:

                                                 CONTACT COOLING
                    BATTERY ACID    CONTACT         AND/OR
    COMBINATION     6 SAW WATER     COOLING        SCRUBBER

        1               x
        2               x                             x
        3               xx

Combinations 2 and 3 will be considered as one combination.

Four levels of treatment are presented  for  these  combinations.
The  alternatives are described below and schematically presented
in Figure VIII-76.

Level 1. The   combined   wastewaters   are   treated   by   lime
precipitation and filtration prior to recycle.
Level 2. Activated alumina is  added  to  level  1,  followed  by
recycle.
Level 3. Reverse osmosis and complete recycle are added to  level
2.
                               381
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Level 4. Activated carbon  is  added  to  level  2,  followed  by
recycle.

The  cost  curves are presented in the figures listed below.  The
summaries of the associated  pollution  reduction  are  shown  in
Tables VIII-20 and 21.

         COMBINATION      FIGURES VIII-

             1               77-80
             2               ei - en

Secondary  Silver.   This  industry  has  been  divided  into two
subcategories.  These subcategories are:

Photographic

In this group there are five wastewater streams.  The wastewaters
are:

1.  Precipitation supernatant
2.  Solution treating supernatant
3.  Furnace air pollution control wastewater
4.  Electrolysis wastewater
5.  Contact cooling water


Four levels of treatment are presented for all combinations.  The
alternatives are described below -and schematically  presented  in
Figure VIII-85.

Level 1. The  precipitation  supernatant  is  treated  by   steam
stripping, followed by recycle if applicable.

Level 2. The combined effluent is treated by  lime  precipitation
prior to recycle.

Level 3. Filtration is added to level 2, followed by recycle.

Level 4. Activated carbon  is  added  to  level  3,  followed  by
recycle.

The cost curves are presented in Figures VIII-86 to 89, while the
summary  of  the  associated  pollution reduction is presented in
Table VIII-22.

Non-Photographic

The streams present in this group are the same as those found  in
the  photographic group except that the first stream is leaching.
                               382
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precipitation and filtration supernatant, and the second  is  air
pollution control wastewater from precipitation and leaching.

Three  levels  of treatment are presented for these combinations.
The alternatives are described below and schematically  presented
in Figure VIII-90.

Level 1. The leaching, precipitation and  filtration  supernatant
    is treated by steam stripping, followed by recycle.

Level 2. The combined streams are treated by  lime  precipitation
    and filtration prior to recycle.

Level 3. Activated carbon  is  added  to  level  2,  followed  by
recycle.

The cost curves are presented in Figures VIII-91 to 93, while the
summary  of  the  associated  pollution reduction is presented in
Table VIII-23.

Primary Tungsten.  This industry is divided into two groups based
on plant configuration.  These are:

Ore to Salt/Metal

In this group there are three plants that  discharge  wastewater.
All  three  plants  have  the equivalent of lime precipitation in
place.  Substantial concentrations of ammonia may exist, however,
in the treated effluent.  This situation required the development
of two combinations.  Combination 1 includes those plants that do
not have excessive ammonia in their discharge.  Three  levels  of
treatment   have   been  developed  for  this  combination.   The
alternatives are described below and presented  schematically  in
Figure VIII-94.

Level 1. The combined effluent is treated by filtration, followed
by recycle if appropriate.

Level 2. Reverse osmosis with complete recycle is added to  level
1.

Level 3. Activated carbon  is  added  to  level  1,  followed  by
recycle if appropriate.

The cost curves are presented in Figures VIII-95 to 97, while the
summary  of  the  associated  pollution reduction is presented in
Table VIII-24.

Combination 2 includes those plants that have significant ammonia
concentrations  in  their  combined  effluent.   Four  levels  of
                               383
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treatment  are  presented.   The alternatives are described below
and schematically presented in Figure VIII-94.

Level 1. The combined effluent is  treated  by  steam  stripping,
followed by recycle if appropriate.

Level 2. Filtration is added to level 1, followed by recycle.

Level 3. Reverse osmosis and complete recycle are added to  level
2.

Level H. Activated carbon  is  added  to  level  2,  followed  by
recycle.

The  cost  curves  are presented in Figures VIII-98 to 101, while
the summaries of the associated pollution reduction are presented
in Tables VIII-26 and 27.

Salt to metal

Two levels of treatment  are  presented.   The  alternatives  are
described below and presented schematically in Figure VIII-102.

Level 1. The combined wastewaters are treated by steam  stripping
and filtration prior to recycle.

Level 2. Activated carbon  is  added  to  level  1,  followed  by
recycle.

The  cost  curves are presented in Figures VIII-103 to 104, while
the summary of the associated pollution reduction is presented in
Table VIII-25.

Primary Zinc.  All the plants in this subcategory have  at  least
the  equivalent of lime precipitation in place.  As a result, the
effluent stream from the existing treatment is the only discharge
stream.

Three levels of treatment were developed to add to  the  existing
treatment.   These  alternatives  are  described  below  and  are
schematically presented in Figure VIII-105.

Level 1. Filtration  and  activated  alumina  are  added  to  the
existing treatment, followed by recycle.

Level 2. Reverse osmosis and complete recycle are added to  level
1.

Level   3.   Activated  carbon  is  added  to level 1, followed by
recycle.
                              384
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The cost curves are presented in Figures VIII-106 to  108,  while
the summary of the associated pollution reduction is presented in
Table VIII-28.

Metallurgical  Acid  Plants.   It  was assumed that blowdown from
metallurgical acid plants would be treated  in  conjunction  with
the  other process wastewater at the plant.  Therefore, the costs
of treatment are included in the costs of treatment  for  Primary
Copper,  Lead  and  Zinc.   The associated pollution reduction is
presented in Table VIII-28.

NEW SOURCES

New sources, as opposed to existing sources/ are defined  in  the
Act  as "any source, the construction of which is commenced after
publication of proposed regulations  prescribing  a  standard  of
performance."   The new source cost information presented in this
section includes only end-of-pipe treatment and control and  does
not  include  in-plant  control  measures, as these costs will be
incorporated in the production plant construction costs.  A  cost
comparison  was  made  on  the  use of dry air pollution controls
versus wet air pollution controls  and  it  was  found  that  the
initial  investment  was  higher  for  dry systems but the annual
costs were higher for wet systems.

In-Plant Control Measures

New sources are expected to employ in-plant controls  extensively
to  reduce  the  quantity  of pollutants discharged, and possibly
eliminate some wastewaters found in existing  sources.   In-plant
control measures, as presented in Section VII, can greatly affect
the  type  and  size,  and  subsequently the cost, of end-of-pipe
treatment alternatives.

Treatment and Control Technologies

The technologies developed to meet new source standards  are  the
same  as  those developed for existing sources.  A description of
each technology and the assumptions used  to  develop  costs  are
presented  in the "Existing Sources" portion of this section.  As
with existing sources, new source  costs  will  be  presented  by
discussing each subcategory separately including a description of
the wastewaters, the various combinations of the streams, and the
recommended   treatment  alternatives.   The  ratio  of  mass  of
pollutants to mass of product was determined  by  evaluating  the
methods  that  existing  plants  have used to reduce or eliminate
wastewater flow.
                               385
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Primary Aluminum.  By use of in-plant controls and utilizing  dry
scrubbing  methods, new sources will have two wastewater streams.
These streams are:

    1.   Contact cooling water
    2.   Cathode reprocessing with cryolite recovery

The following combinations could exist:

         COMBINATION    CONTACT COOLING     CRYOLITE

              1                XX
              2                x

Four levels of treatment were developed  for  combination  1  and
three  levels  for combination 2.  The alternatives are described
below  and  schematically  presented  in  Figure  VII-109.    The
alternatives  for combination 2 are the same as for combination 2
for existing sources, and are described there.

Level 1. For Combination 1—recycle of the contact cooling  water
and  combining  a five percent blowdown with the other stream for
treatment by chlorine oxidation and lime precipitation,  followed
by recycle.

Level 2. For Combination 1—filtration and activated alumina  are
added to level 1, followed by recycle.

Level 3. For Combination 1—reverse osmosis and complete  recycle
are added to level 2.

Level 1. For Combination 1—activated carbon is added to level 2,
followed by recycle.

The cost curves are presented in the figures listed  below.   The
summaries  of  the  associated  pollution  reduction are shown in
Tables VIII

         COMBINATION      FIGURES VIII-  TABLE VIII-

             1               110 - 113        29
             2                10-12         5

Secondary Aluminum.  New sources in this  subcategory  will  have
two possible wastewaters.  These streams are:

    1.   Slag milling wastewater
    2.   Scrubber wastewater

The following combinations of these streams could exist:
                                386
-------
         COMBINATION    MILLING   SCRUBBERS

             1            xx
             2                       x
             3            x

The   following  levels  of  treatment  are  presented  for  each
combination with a  schematic  presentation  provided  in  Figure
VIII-117.

Level 1. For Combination 1—the slag milling water is  completely
recycled  after  primary settling.  The scrubber water is treated
by lime precipitation, followed by recycle.

         For Combination 2—the scrubber effluent is  treated  by
lime precipitation prior to recycle.

         For  Combination  3—the  slag  milling water is totally
recycled after primary settling.

Level 2.  For Combinations 1 and 2—filtration is added to  level
1, followed by recycle.

Level 3. For Combinatons 1 and 2—reverse  osmosis  and  complete
recycle are added to level 2.

Level 4. For Combinations 1 and 2—activated carbon is  added  to
level 2, followed by recycle.

The  cost  curves are presented in the figures listed below.  The
summaries of the associated  pollution  reduction  are  shown  in
Tables VIII

         COMBINATION       FIGURES VIII-  TABLE VIII-

             1               118 - 121        31
             2               122 - 125        32
             3                  126

Columbium-Tantalum.   The  columbium-tantalum  industry  has been
divided into groups based on plant configuration.   These  groups
are:   ore to salt/metal, and salt to metal.

Ore to salt/metal

New  sources  in this group will have streams similar to those in
existing sources.  Five levels of treatment have been  developed.
The  alternatives are described below and schematically presented
in Figure VIII-127.
                               387
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Level 1. Steam stripping and oxidation by chlorine  are  provided
for  treatment  of  the  precipitation  supernatant  and the salt
drying scrubber effluent, prior to recycle.

Level 2. The combined streams are treated by  lime  precipitation
and filtration, followed by recycle.

Level 3. Activated alumina is  added  to  level  2,  followed  by
recycle.

Level H. Reverse osmosis and complete recycle are added to  level
3.

Level 5. Activated carbon added to level 3, followed by recycle.

The cost curves are presented in Figures VIII- 128 to  132,  while
the summary of the associated pollution reduction is presented in
Table VIII-33.

Salt to Metal

New  plants will have wastewaters from the reduction scrubber and
leachate processes.  Five levels of treatment are presented.  The
alternatives are described below and presented  schematically  in
Figure VIII-133.

Level 1. The combined streams are treated by lime  precipitation,
followed by recycle.

Level 2. Filtration is added to level 1, followed by recycle.

Level 3. Activated alumina is added to level 2.

Level 4. Reverse osmosis and complete recycle are added to  level
3.

Level 5. Activated carbon  is  added  to  level  3,  followed  by
recycle.

The  cost  curves are presented in Figures VIII-134 to 138, while
the summary of the associated pollution reduction is presented in
Table VIII-34.

        Copper .  The primary copper industry has been  segregated
into  two  groups  based  on  plant  configuration.   They are as
follows:

Smelting and Refining
                               388
-------
New sources belonging  to  this  group  will  have  two  possible
wastewaters: air pollution control wastewater and contact cooling
water.   Four  levels  of  treatment  have  been  developed.  The
alternatives are described below and schematically  presented  in
Figure VIII-139.

Level 1. The  supernatant  from  primary  settling  of  the   air
pollution control wastewater is combined with the contact cooling
water for treatment by lime precipitation and filtration prior to
recycle.

Level 2. Activated alumina is  added  to  level  1,  followed  by
recycle.

Level 3. Reverse osmosis and complete recycle are added to  level
2.

Level 4. Activated carbon  is  added  to  level  2,  followed  by
recycle.

The  cost  curves are presented in Figures VIII-140 to 143, while
the summary of the associated pollution reduction is presented in
Table VIII-35.

Refining

New sources in this group will have only contact cooling water as
a wastewater.  Four  levels  of  treatment  are  presented.   The
alternatives  are  described below and schematically presented in
Figure VIII-144.

Level 1. Recycle of the contact cooling water and treatment of  a
five  percent blowdown by lime precipitation and filtration prior
to recycle.

Level 2. Activated alumina is  added  to  level  1,  followed  by
recycle.

Level 3. Reverse osmosis and complete recycle are added to  level
2.

Level 4. Activated carbon  is  added  to  level  2,  followed  by
recycle.

The  cost  curves are presented in Figures VIII-145 to 148, while
the summary of the associated pollution reduction is presented in
Table VIII-36.

An additional level of treatment can be added on to  or  used  in
place  of  the  alternatives given for both subcategories for any
                               389
-------
plant located in an area of net evaporation.   For  such  plants,
the  alternative is an evaporation lagoon.  The cost for a lagoon
located in an area of 20 inches  net  effective  evaporation  per
year is presented in Figure VIII-59.

Secondary  Copper.  New sources in this subcategory will have two
possible wastewater sources.  They are contact cooling water  and
slag milling wastewater.  Two possible combinations can exist and
are shown in the following tabulation.
         COMBINATION

             1
             2
CONTACT COOLING

     x
     X
MILLING
Alternatives  for  combinations  1  and  2  are  the  same as for
combinations 1 and 2, respectively, for  existing  sources.   The
alternatives are schematically presented in Figure VIII-87.

The cost curves are presented in Figures VIII-62 to 67, while the
summaries  of the associated pollution reduction are presented in
Tables VIII-14 and 15.

Primary Lead.  New sources in  this  subcategory  will  have  one
waste  stream:  blowdown from the acid plant.  Two conditions may
exist for this subcategory:  areas of net precipitation and areas
of net evaporation.

For all plants, three levels of  treatment  are  presented.   The
alternatives  are described below and are presented schematically
in Figure VIII-157.

Level 1. Lime precipitation and filtration, prior to recycle.

Level 2. Activated carbon  is  added  to  level  1,  followed  by
recycle.

Level 3. Reverse osmosis and complete recycle are added to  level
2.

Another  level  of alternative treatment for new sources built in
an area of net evaporation is evaporation lagoons.

The cost curves are presented in Figures VIII-158 to  160,  while
the summary of the associated pollution reduction is presented in
Table  VIII-39.   The costs for a lagoon located in an area of 20
inches net effective evaporation per year is presented in  Figure
VIII-59.
                               390
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Secondary  Lead. New sources in this group may have the following
wastewaters in the following combinations:

                           BATTERY ACID AND
         COMBINATION          SAW WATER          SCRUBBER WATER

              1                   X
              2                   x                   x
Alternatives for combinations  1  and  2  are  the  same  as  for
combinations  1  and  2, respectively, for existing sources.  The
alternatives are schematically presented in Figure VIII-76.

The cost curves are presented in the figures listed  below.   The
summaries  of  the  associated  pollution  reduction are shown in
Tables VIII

         COMBINATION       FIGURES VIII-    TABLE VIII-

              1               77-80            20
              2               81-84            21

Secondary Silver.   This  industry  has  been  divided  into  two
subcategories.  These subcategories are:

Photographic

New  sources  in this group will have three possible wastewaters;
precipitation/filtration  supernatant,  stripping  air  pollution
control,  and  furnace air pollution control.  These alternatives
are the same  as  for  existing  sources  and  are  schematically
presented in Figure VIII-85.

The cost curves are presented in Figures VIII-86 to 89, while the
summary  of  the  associated  pollution reduction is presented in
Table VIII-22.

Non-Photographic

New sources in this group will have the same wastewaters  as  the
photographic  group.   alternatives  are the same as for existing
sources and are schematically presented in Figure VIII-90.

The cost curves are presented in Figures VIII-91 to 93, while the
summary of the associated pollution  reduction  is  presented  in
Table VIII-23.

Primary  Tungsten.   This  industry  has been segregated into two
groups based on plant configuration.  The groups are:
                               391
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Ore to Salt/Metal

New sources in this group will have the same wastewaters  as  the
existing  sources.   Two  possible combinations could result, one
being those plants which do not have  significant  concentrations
of  ammonia  in their wastewater and the other being those plants
that do.

Three levels of treatment are presented for combination  1.   The
alternatives are:

Level 1. The combined streams are treated by  lime  precipitation
and filtration, followed by recycle.

Level 2. Reverse osmosis and complete recycle are added to  level
1.

Level 3. Activated carbon  is  added  to  level  1,  followed  by
recycle.

Four  levels  of  treatment are presented for combination 2.  The
alternatives are:

Level 1. The high ammonia streams are treated by steam stripping,
prior to recycle.

Level 2. Chemical precipitation and filtration are added to level
1, followed by recycle.

Level 3. Reverse osmosis and complete recycle are added to  level
2.

Level 4. Activated carbon  is  added  to  level  2,  followed  by
recycle.

The   alternatives   for   both  combinations  are  schematically
presented in Figure VIII-179.

The cost curves are presented in the figures listed  below.   The
summaries  of the associated pollution reduction are shown in the
tables.

         COMBINATION       FIGURES VIII- TABLE VIII-

               1               180 -  182       44
              2               183 -  186       45

Salt to Metal
                                392
-------
New sources in this group will have the same wastewaters  as  the
existing  sources.  Four levels of treatment have been developed.
The alternatives are described below and schematically  presented
in Figure VIII-187.

Level 1. steam  stripping  is  provided  for  treatment  of  high
ammonia streams, prior to recycle.

Level 2. Lime  precipitation  is  used  to  treat  the   combined
streams, followed by recycle.

Level 3. Filtration is added to level 2, followed by recycle.

Level 4. Activated carbon  is  added  to  level  3,  followed  by
recycle.

The  cost  curves are presented in Figures VIII-188 to 191, while
the summary of the associated pollution reduction is presented in
Table VIII-46.

Primary  Zinc.   New  sources  in  this  subcategory  will   have
wastewater  from  two  sources:  blowdown from the acid plant and
wastewater from air pollution control of the leaching  operation.
These  two  streams can be combined and treated by four levels of
treatment.    The   alternatives   are   described   below    and
schematically presented in Figure VIII-192.

Level 1. Lime precipitation is used for treatment of the combined
streams prior to recycle.

Level 2. Filtration is added to level 1, followed by recycle.

Level 3. Reverse osmosis and complete recycle are added to  level
2.

Level 4. Activated carbon  is  added  to  level  2,  followed  by
recycle.

The  cost  curves are presented in Figures VIII-193 to 196, while
the summary of the associated pollution reduction is presented in
Table VIII-47.

ENERGY ASPECTS

An  investigation  was  made  to  determine  the   added   energy
requirement   for  a  plant  caused  by  the  installation  of  a
wastewater treatment system.  The energy consumption reported  in
the data collection portfolios was tabulated and the median total
plant  energy  consumption  was  calculated  and  is  reported as
Btu*s/year for each industry group.  For each group,  the  median
                               393
-------
sized plant was determined, based on flow rate.  The most complex
set  of  treatment alternatives for each group, and corresponding
energy requirement for each level of  treatment  was  determined.
These  requirements are expressed as the maximum percent increase
in   energy  requirements  caused  by  the  installation   of   a
wastewater treatment system.  This investigation is summarized in
Table  VIII-48.  By reviewing this table, it can be seen that the
added energy requirement is less  than  1X  of  the  total  plant
energy  requirement  for  a  majority of the alternatives.  Those
alternatives that require an increase  greater  than  1%*  include
reverse osmosis in the treatment sequence.

NON-WATER QUALITY ASPECTS

Sludge

Sludge  disposal  is  a  problem  in  this industry.  As shown in
previous sections, the waste  streams  being  discharged  contain
large  quantities  of  heavy  metals;  the  most common method of
removing the metals  is  by  lime  precipitation.   Consequently,
large volumes of heavy metal-laden sludge are generated that must
be  disposed  of.  Table VIII-49 summarizes the methods currently
in use, along with their frequency of  occurrence,  for  treating
and disposing of sludges.

The technologies that directly generate sludge are:

1.  Chemical precipitation
2.  Multi-media filtration
3.  Primary sedimentation
4.  Reverse osmosis

Sludge is also indirectly generated by the recycling of the spent
activated  alumina regenerant, containing fluoride or arsenic, to
the chemical precipitation unit.

The sludge resulting from the four technologies listed above will
vary  in  characteristics  depending  on  the   subcategory   and
combination  of  streams  being treated.  However, in most cases,
the majority of the sludge  produced  is  a  result  of  chemical
precipitation.   This  sludge  will,  in  general,  contain large
quantities of calcium salts, due to the use of  lime,  and  large
quantities   of   precipitated  metals.   The  sludge  indirectly
generated from activated alumina will contain large quantities of
fluoride or arsenic.  The estimated characteristics of the sludge
generated by the sets of alternatives presented for BAT are given
in Table VIII-50.

A major concern in the disposal of sludges is  the  contamination
of  soils,  plants,  and animals by the heavy metals contained in
                               394
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sludge.  The leaching of heavy metals from sludge and  subsequent
movement through soils is enhanced by acidic conditions.  Sludges
treated  with  lime  prior to disposal possess high pH values and
exhibit little loss of metals (110).  Since the largest amount of
sludge that results from the alternatives presented previously is
generated by lime precipitation, it is not that the  metals  will
be  readily  leached  from  the sludge.  Disposal of sludges in a
lined sanitary landfill will further reduce  the  possibility  of
heavy metals contamination of soil, plants and animals.

Other  methods of treating and disposing of sludge are available.
Table VIII-49 shows that one method currently  being  used  at  a
number  of plants is reuse or recycle, usually to recover metals.
Table VIII-50 shows that the metal concentrations in some sludges
may be substantial.  Consequently, it may be cost  effective  for
some  plants to recover the metal fraction of their sludges prior
to disposal.

Hazardous Wastes

EPA recently proposed hazardous waste guidelines and  regulations
(December 18, 1978, 43 FR 58946-59027).  These proposals covered:

1)   criteria   for  identifying  and  listing  hazardous  waste,
identification methods, and a hazardous waste list;
2)  standards  applicable  to  generators  of  such   waste   for
recordkeeping,  labelling,  containerizing, and using a transport
manifest;
3)   performance  standards  for   hazardous   waste   management
facilities.

The  proposed  regulations  create a "cradle-to-grave" management
control system for hazardous waste.  Solid  waste  which  is  not
subject to the hazardous waste regulations will be subject to the
requirements  of  Subtitle  D  of  the  Resource Conservation and
Recovery Act of 1976, under which open dumping is prohibited  and
environmentally acceptable practices are required.

A   hazardous  waste  is  a  waste  which  is  toxic,  ignitable,
corrosive, or reactive, or which is listed in  40 CFR 250.14.   A
toxic  waste  is defined as one, which after undergoing an acetic
acid extraction, has more than the following  contaminant  levels
in  the  extract.   The  contaminants  and extract levels of most
concern to the nonferrous metals industry are:
                               394-A
-------
Contaminant        Extract Level (mg/1)

Arsenic                 0.50
Barium                 10.00
Cadmium                 0.10
Chromium                0.50
Lead                    0.50
Mercury                 0.02
Selenium                0. 10
Silver                  0.50

The specific hazardous wastes from the nonferrous metals industry
listed in 40 CFR 250.14 are the following, by SIC code:

3331     Primary copper smelting and refining electric
         furnace slag, converter dust, acid plant sludge, and
         reverberatory dust
3332     Primary lead blast furnace dust
3332     Primary lead lagoon dredging from smelter
3333     Zinc acid plant blowdown lime treatment:
         gypsum cake  (acid cooling tower and neutral
         cooling tower)
3333     Zinc production: oxide furnace
         residue and acid plant sludge
3333     Zinc anode sludge
3339     Primary antimony-electrolytic sludge
3339     Primary tungsten-digestion residues
3339     Primary lead sinter dust scrubbing sludge
3339     Primary antimony-pyrometallurgical
         blast furnace slag
3341     Secondary lead, scrubber sludge from
         SO2 emission control, soft lead production
3341     Secondary lead-white metal production
         furnace dust
3341     Secondary copper-pyrometallurgical blast
         furnace slag
3341     Secondary copper-electrolytic refining
         wastewater treatment sludge
3341     Secondary aluminum dross smelting-high
         salt slag plant residue

Spent potliners (or cathodes) from  primary  aluminum  reduction,
and  other  nonferrous metals industry wastes, were added to this
list in a proposal published  August  22,  1979  in  the  Federal
Register.

Air Pollution

Various  forms  of both wet and dry air pollution control methods
are utilized throughout the industry.  Replacement of wet systems
                              395
-------
by dry systems will reduce the pollutant loading discharged by  a
plant.  The alternatives for BAT presented in this section assume
that  those  plants  presently  using  wet  air pollution control
systems would not change to dry systems since it may be more cost
effective to treat and recycle the wastewater from the wet system
than to replace it with a dry system.  For those plants where  it
is  not  more  cost  effective,  the cost estimates presented are
conservative estimates.  It was assumed that  new  sources  would
install  dry  systems  instead  of  wet  systems when it has been
established that dry systems could sufficiently control  the  air
quality of a given process operation.

At  this  time there are no other known non-water quality aspects
in terms of soil infiltration, air pollution, noise or  radiation
that   may   result   from   the  application  of  the  treatment
alternatives presented.
                               396
-------
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                              ' ' ""I    '  '  '  • "•'[
                                REVERSE OSMOSIS
                                 VACUUM FILTRATION	
                                 STEAM   STRIPPING 8
                                 COOLING TOWER
                                 HOLDING TANK
        CHEMICAL PRECIPITATION
                                 OXIDATION BY CHLORINE
PRIMARY SEDIMENTATION
        ACTIVATED ALUMINA,
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   10
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                                          409
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                                             410
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                                  CHEMICALS-
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                                423
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                                        429
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LABOR
                                     DEPRECIATION

                                     CAPITAL
                                              , .,,1
                                           ml
                                                                       i i  11 i 11
                   0.01            O.I  _,-,„    J   1.0            10.0
                                     FLOW, mgd



        FIGURE VIII-58. PRIMARY COPPER EVAPORATION, 10 INCHES/YEAR
  I0r
  I0
CO

8
  10
    ENERGY

    MATERIALS

    LABOR
                                          DEPRECIATION

                                          CAPITAL
                           L A  I L
                                 ml
                                                        i	i	i iiiil
                   0.01
                                   -  FLOW, mgd
                                            10.0
       FIGURE  VIII-59.  PRIMARY COPPER EVAPORATION , 20 INCHES/YEAR
                                       431
-------
  10
  10
z
4
                            ENERGY 8

                            MATERIALS
                                      DEPRECIATION

                                      CAPITAL
                                              ..,.1
                   0.01
0-1 FLOW, mgd  ''°
10.0
        FIGURE VIII-60.  PRIMARY COPPER  EVAPORATION ,30 INCHES/YEAR
                                            432
-------
—
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                                   COMBINATION  5
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 FIGURE VIII-61  , SECONDARY  COPPER   TREATMENT  SCHEMES
                                         433
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  10
  .o6
w
o
o
  ,o4
                    SLUDGE REMOVAL
                    CHEMICALS
                    ENERGY	
                    MATERIALS
                                                           ABOR
                                                          DEPRECIATION
                                                          CAPITAL
                   0.01
             °J  FLOW,  -ngd  L0
10.0
            FIGURE  VIII-62. SECONDARY  COPPER   COMB. I,  ALT. I
  10
  .O6
w
o
o
_j
  ,o5
  .o4
SLUDGE REMOVAL
CHEMICALS
ENERGY
MATERIALS
                                                           ABOR
                                                          DEPRECIATION
                                                          CAPITAL
                   0.01
                                     FLOW, mfld
                             L°
10.0
            FIGURE  VIII-63.  SECONDARY  COPPER   COMB. I,  ALT. 2
                                         434
-------
  10
                     SLUDGE  REMOVAL
                     CHEMICALS
                     ENERGY 8 MATERIALS
  10
8
u
 i  5
  10
                                                            LABOR
                                                            DEPRECIATION
                                                            CAPITAL
                   0.01
0.1
                                      FLOW, mgd
1.0
10.0
               FIGURE VIII-64.  SECONDARY COPPER COMB. I, ALT 3
                                            435
-------
  10
                                   SLUDGE REMOVAL-
                                   CHEMICALS
                                   ENERGY•
  10
8
u
iio4
  10
                                                             LABOR
                                                             DEPRECIATION
                                                             CAPITAL
                                                                nl
                   0.01
OJ FLOW,  mgd  L0
10.0
             FIGURE  VIII-65. SECONDARY COPPER COMB. 2,3, OR 4, ALT. I
  10
  10
o
o
r
  10
                                 SLUDGE REMOVAL
                                 CHEMICALS, ENERGY
                                 MATERIALS
                                                             LABOR
                                                             DEPRECIATION
                                                             CAPITAL
                    0.01
 OJ FLOW, mgd   L0
 10.0
               FIGURE VIII-66. SECONDARY COPPER COMB. 2,3, OR 4, ALT. 2
                                         436
-------
  10
  .o6
i
u
Urf
  ,o4
                            SLUDGE REMOVAL , CHEMICALS,
                            ENERGY  8 MATERIALS-
                                                         LABOR
                                                         DEPRECIATION
                                                         CAPITAL
                  0.01
OJ
                                   FLOW, mgd
10.0
              RGURE VIII-67.  SECONDARY COPPER COMB.2.ALT.3
                                       437
-------
  ,o7
                                '"I    '  '  	I
                                SLUDGE REMOVAL	
                                CHEMICALS 6 ENERGY-
                                MATERIALS 	
  .o6
o
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^io5
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  .o4
                                                           LABOR
                                                           DEPRECIATION
                                                           CAPITAL
                             nl
                   0.01
°J FLOW,  mod  L0
10.0
              FIGURE VIII-68.  SECONDARY COPPER COMB.3 OR 4 , ALT 3
                                       438
-------
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  10
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                             1111 "I    r^  ' '""I
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    6
   10
    5
   10
 o>
 8
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             FIGURE VIII-69. SECONDARY  COPPER COMB. 5, ALT. I
                             SLUDGE REMOVAL S CHEMICALS-
                             ENERGY—
                             MATERIALS
                                                     LABOR
                                                     DEPRECIATION
                                                     CAPITAL
   .o3
III
                    I  I  I	I
                                      I I i I II
                   0.01
 OJ
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             FIGURE VI11-70.  SECONDARY COPPER COMB. 5 ,ALT.  2
                                        439
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  10
o
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z
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  K>4
                                 -l-TTj-r—•  r-r-r
                                 SLUDGE REMOVAL-
                                 CHEMICALS-
                                 ENERGY-
                                                             LABOR
                                                             DEPRECIATION
                                                             CAPITAL
                   0.01
°J FLOW,  mgd  L0
10.0
              FIGURE VIII-71.  SECONDARY COPPER  COMB. 5, ALT. 3
                                       440
-------

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REVERSE
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                        YALTERNATE 2
                                 YALTERNATE 3

                           COMBINATION  1
                         (COMBINED WASTEWATER)
FIGURE  VIII-72.PRIMARY  LEAD  TREATMENT  SCHEMES
                                  441
-------
  10
  10
M
o
0
                                   ENERGY 8 MATERIALS
                                                             LABOR
                                                             DEPRECIATION
                                                             CAPITAL
  10
                                 LuL
                   0.01
°J FLOW,  mgd  L°
10.0
              FIGURE VIII- 73. PRIMARY  LEAD   COMB. I, ALT. I
  10'
  10
at
8
  10
                                   SLUDGE REMOVAL
                                   CHEMICALS
                                   ENERGY
                                                             LABOR
                                                             DEPRECIATION
                                                             CAPITAL

                    o.oi
                                    '  FLOW,  mgd
                              10.0
               FIGURE VIII-74.  PRIMARY  LEAD  COMB. I.ALT 2
                                         442
-------
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  10
CO
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I
  ,o4
                                  SLUDGE REMOVAL-

                                  CHEMICALS

                                  ENERGY
                                                         LABOR

                                                         DEPRECIATION

                                                         CAPITAL
                   0.01
O.I
                                     FLOW,
1.0
10.0
              FIGURE  VIII-75. PRIMARY  LEAD   COMB, I.ALT. 3
                                         443
-------
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V
FILTRATION




ACTIVATED
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                    T ALTERNATE 2
                           lT ALTER NATE 3/4



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                  (BATTERY ACID AND SAW WATER)
                                                       RECYCLE
                              FILTRATION
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           ^ALTERNATE 1
                    VALTEBNATE 2
                           ^ALTERNATE 3/4




                     COMBINATION 2


        (BATTERY ACID AND SAW WATER .CONTACT COOLING AND/OR SCRUBBER)
FIGURE VIII-76. SECONDARY LEAD TREATMENT SCHEMES
                               444
-------
  10
  10"
S
u
  10
                                 SLUDGE REMOVAL-
                                 CHEMICALS
                                 ENERGY
                                                            LABOR
                                                            DEPRECIATION
                                                            CAPITAL
                                       j	J  j A I 111 I	|   j  1
                                                                     1   II II I 11
                   0.01
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10.0
 FIGURE VIM -77. SECONDARY  LEAD
                                                        COMB. I.ALT. I
  ,0s
3
  io4
.1  i 1 I II
                                 SLUDGE REMOVAL-
                                 CHEMICALS-
                                 ENERGY-
                                      ill    j
                                                            LABOR
                                                            DEPRECIATION
                                                            CAPITAL
                   0.01
                                    -  FLOW,  mgd
                                       L0
10.0
 FIGURE VIII-78. SECONDARY LEAD
                                                         COM!. I.ALT. Z
                                            445
-------
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  10
CO
o
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<
z
z
<
  I05
  10
                                 ™'  '   "^
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             1  I I I I I
                                             I I I I I I I    11  1 I I I I ll
                   0.01
0-1 FLOW,  mod  ''°
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 FIGURE VIII-79. SECONDARY LEAD
                                 COMB. I.ALT. 3
  10'
  I0a
CO
O
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3
O
  10
                                  SLUDGE REMOVAL-
                                  CHEMICALS
                                  ENERGY
                                                             LABOR
                                                             DEPRECIATION
                                                             CAPITAL
                                               i i iiil	i  ii i i itii	i
                    0.01
 OJ  FLOW, mgd   L0
10.0
 FIGURE VIII-80. SECONDARY  LEAD
                                  COMB. I, ALT. 4
                                         446
-------
  10
  to"  -

8
2
1
#
o
  10
                                                            LABOR
                                                            DEPRECIATION
                                                            CAPITAL
                   0.01
                                   '•' FLOW,  mgd
10.0
      FIGURE  VIII-82. SECONDARY LEAD
       COMB.2.ALT.2
                                           447
-------
  10
  10
CO
o
0
  10
                                                             LABOR
                                                             DEPRECIATION
                                                             CAPITAL
                                                                         i i  t i j ii
                   0.01
                                      FLOW, mgd
              10.0
      FIGURE VIII-8S SECONDARY LEAD
                    COMB.2.ALT.3
  10'
  10
CO
8
_l
3
  10
                                  SLUDGE REMOVAL •
                                  CHEMICALS
                                  ENERGY
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                            I  A J JJ 111    _I	II	I I I I
                                                             LABOR
                                                             DEPRECIATION
                                                             CAPITAL
                                                             i j i in
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'">
10.0
      FIGURE VIII-84. SECONDARY LEAD
                     COMB.2.ALT.4
                                       448
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^ YALTERNATE 2 j
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                              Y ALTER NATE 4

                        COMBINATION  1
                        (ALL WASTE STREAMS)
FIGURE VIII- 85. SECONDARY  SILVER TREATMENT SCHEMES
                      (PHOTOGRAPHIC)
                               449
-------
  10"
  .o5
8
u
  10"
                                                           LABOR
                                                           DEPRECIATION
                                                           CAPITAL
                   0.01
0>l FLOW, ingd   L0
10.0
      FIGURE VIM-86.  SECONDARY SILVER (PHOTOGRAPHIC) COMB.  I , ALT. I
  10

-
  10
             SLUDGE REMOVAL
             CHEMICALS 8
             ENERGY
             MATERIALS
                                                            LABOR
                                                            DEPRECIATION
                                                            CAPITAL
                   0.01
 OJ  FLOW,  mgd  L0
10.0
       FIGURE VIII-87.   SECONDARY SILVER ( PHOTOGRAPHIC ) COMB. I , ALT.2
                                        450
-------
  10'
  10°
I
  10
                         SLUDGE REMOVAL
                         CHEMICALS
                         ENERGY
                         MATERIALS
                                                   LABOR
                                                   DEPRECIATION
                                                   CAPITAL
                   0.01
°*' FLOW,  mgd  l<0
10.0
       FIGURE VIII -88.  SECONDARY SILVER (PHOTOGRAPHIC) COMB.  I , ALT. 3
  10
  10
s
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r
  10
                          SLUDGE REMOVAL 6
                          CHEMICALS
                          ENERGY
                          MATERIALS
                                                   LABOR
                                                   DEPRECIATION
                                                   CAPITAL
                   0.01
                                     FLOW,  mgd
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       FIGURE VIII-89 .  SECONDARY SILVER (PHOTOGRAPHIC) COMB. I , ALT.4
                                         451
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                  ~Y ALTERNATE 2
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                     COMBINATION  1
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FIGURE VIII- 90. SECONDARY  SILVER TREATMENT
                  (NON-PHOTOGRAPHIC)
                                              SCHEMES
                           452
-------
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  10
CO
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      FIGURE Vlll-91 . SECONDARY SILVER (NON-PHOTOGRAPHIC) COMB. I, ALT. I
  10
  10
CO
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  10
  10
                            SLUDGE REMOVAL

                            CHEMICALS 8 ENERGY-

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                                                           CAPITAL
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10.0
       FIGURE VIII-92. SECONDARY SILVER (NON-PHOTOGRAPHIC) COMB.I, ALT 2
                                         453
-------
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  10
m
o
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  10
               SLUDGE REMOVAL-
               CHEMICALS
               ENERGY
               MATERIALS
                                                           LABOR
                                                           DEPRECIATION
                                                           CAPITAL
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0.1
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1.0
10.0
      FIGURE VIII-93. SECONDARY SILVER( NON~ PHOTOGRAPHIC) COMB. I, ALT. 3
                                         454
-------



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                                                                 RECYCLE


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                         T ALTERNATE 2
                                 Y ALTERNATE 3/4

                           COMBINATION  Z
                         (COMBINED  WASTEWATER)
FIGURE VIII- 94. PRIMARY TUNGSTEN  TREATMENT SCHEMES
                    (ORE  TO  SALT/METAL)
                                   455
-------
   6
  10
  10
at
o
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                  SLUDGE REMOVAL, ENERGY
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                                            LLlL
                   0.01
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10.0
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     FIGURE VIII-95 . PRIMARY TUNGSTEN (ORE TO SALT/METAL ) COMB. I, ALT. I
  to7
  10
CO
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  io4
SLUDGE REMOVAL-

CHEMICALS

ENERGY
                                                            LABOR

                                                            DEPRECIATION

                                                            CAPITAL
                   0.01
                01 FLOW,  mgd  L0
10.0
     FIGURE VIII-96 .PRIMARY TUNGSTEN (ORE TO SALT/METAL) COJWIB. I  , ALT. 2
                                          456
-------
  10
  10
S
u
  10
                               SLUDGE REMOVAL-

                               CHEMICALS

                               ENERGY
                                                           LABOR

                                                           DEPRECIATION

                                                           CAPITAL
                                                     i  II
                   0.01
0-1 FLOW, mgd   L°
10.0
    FIGURE VIII-97. PRIMARY TUNGSTEN (ORE TO SALT/METAL) COMB. I, ALT. 3
                                         457
-------
  10"
  \0
co
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  ,o3
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                                                DEPRECIATION

                                                CAPITAL
I  I  I I  I I I
                       ni
       |  |	| i | j | I	J  1 I _| I I I li
                                                         1  |  I  I I I I I
                  0.01            O.I _,.,.,     .   1.0            10.0
                                    FLOW, mgd



    FIGURE VIII-98 .PRIMARY TUNGSTEN (ORE TO SALT/METAL) COMB. 2 , ALT.
  10
                SLUDGE REMOVAL

                ENERGY

                MATERIALS
  10
co
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  10
                                                LABOR

                                                DEPRECIATION

                                                CAPITAL
  10
                               LLJli
                                                     11 i
                   o.oi
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                                    FLOW,  mgd
                                      L0
10.0
    FIGURE VIII-99 .PRIMARY TUNGSTEN(ORE TO SALT/METAL) COMB.2, ALT.2
                                         458
-------
  10'
  10
CO
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  10
                    SLUDGE REMOVAL 8 CHEMICALS
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                    MATERIALS
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°-01
°J
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                                     FLOW, mgd

    FIGURE VIII-IOO. PRIMARY TUNGSTEN (ORE TO SALT/METAL) COMB. 2 , ALT. 3
  10'
  10
CO
  10
                    SLUDGE REMOVAL 8 CHEMICALS'
                    ENERGY —
                    MATERIALS
                                                   LABOR
                                                   DEPRECIATION
                                                   CAPITAL
                   0.01
                                   -  FLOW, mgd
                             10.0
    FIGURE VIII-IOI. PRIMARY TUNGSTEN(ORE TO SALT/METAL) COMB. 2, ALT. 4
                                          459
-------


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                   T ALTERNATE 1
                              Y ALTERNATE *

                        COMBINATION  1
                       (COMBINED WASTEWATER)
FIGURE VIII- I02. PRIMARY TUNGSTEN  TREATMENT  SCHEMES
                     (SALT TO METAL)
                                460
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  10
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          SLUDGE REMOVAL
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°J FLOW, mfld   L°
                                                              I0'°
    FIGURE VIII-103. PRIMARY TUNGSTEN(SALT TO METAL) COMB. I,  ALT. I
  10
M
8
  10"
                   SLUDGE REMOVAL
                   CHEMICALS
                   ENERGY
                   MATERIALS
                                                  LABOR
                                                  DEPRECIATION
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                                       l  i   1 i I I III    i  i  Illllll
                   0.01
OJ
                                     FLOW, mgd   -
                                            10.0
    FIGURE VIII-104. PRIMARY  TUNGSTEN ( SALT  TO METAL) COMB. I, ALT. 2
                                           461
-------
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                                  ACTIVATED
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                            Y ALTERNATE z7a~


                      COMBINATION  1
                     (COMBINED  WASTEWATER)
FIGURE VIH-I05.PRIMARY  ZINC  TREATMENT  SCHEMES
                                462
-------
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  10
 o
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 z
  to"
  10
                              • " ""I    '  '  • •' '"I
                                     SLUDGE REMOVAL a CHEMICALS
                                     ENERGY 8 MATERIALS
                                                              LABOR
                                                              DEPRECIATION
                                                              CAPITAL
                                                                       i   i  i i i i 11
°-01
                      °J
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                   FIGURE VI II -106 PRIMARY ZINC  COMB. I, ALT. I
                                                                 IO-°
   10'
^
   10
 o
   10"
                                    SLUDGE REMOVAL
                                    CHEMICALS
                                    ENERGY
I  l^rfllll	I  1  I I I I I li	I   1  I I I I III
                                                              LABOR
                                                              DEPRECIATION
                                                              CAPITAL
                    0.01
                      OJ FLOW,  mgd  L0
                                              10.0
                    FIGURE VI11-107 PRIMARY ZINC  COMB. I, ALT. 2
                                            463
-------
  10
                                  "1    '  '  ' Tt '"I
                                    SLUDGE REMOVAL-
                                    CHEMICALS
                                    ENERGY
                                    MATERIALS
  10°
CO
o
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  10
                            LABOR
                            DEPRECIATION
                            CAPITAL
                   0.01
°J
                                      FLOW, mgd
10.0
                   FIGURE VIII-108.PRIMARY ZINC COMB. I, ALT. 3
                                              464
-------
                     T ALTERNATE  3/4

               COMBINATION  1
            CONTACT COOLING.CRVOLITE)
              COMBINATION 2
              CCONTACT COOLING)
 FIGURE VIII-109.  PRIMARY  ALUMINUM
NEW  SOURCE TREATMENT  SCHEMES
                       465
-------
  10
  10
CO
o
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_1
I

I"
  10
                             1 ' ' '"1    ' ^  '  '' "'I

                                   SLUDGE REMOVAL-
                                   CHEMICALS-
                                   ENERGY-
                                                          LABOR
                                                          DEPRECIATION
                                                          CAPITAL
                                                               i.l
                   0.01
°J
                                     FLOW, mfld   -
10.0
  I07
co
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3
               FIGURE VIII-110. PRIMARY ALUMINUM COME I, ALT I
                               (NEW SOURCES)
                                   SLUDGE REMOVAL-
                                   CHEMICALS
                                   ENERGY-
                                                           LABOR
                                                           DEPRECIATION
                                                           CAPITAL
  10
                   0.01
                                    -  FLOW,  mgd   -
                             10.0
               FIGURE  Vlll-lll  PRIMARY ALUMINUM COMB. I, ALT.  2
                                (NEW SOURCES)
                                           466
-------
   10
                                    SLUDGE REMOVAL-
                                    CHEMICALS-
                                    ENERGY-
                                    MATERIALS-
^
  10
 w
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 3
                                                            LABOR
                                                            DEPRECIATION
                                                            •CAPITAL
   10
                                   ill
                                                                        i  i  i i 111
                    0.01
°J FLOW,  mad  L°
10.0
               FIGURE VIII-112. PRIMARY ALUMINUM  COMB. I, ALT. 3
                                (NEW SOURCES)
   10
   10
 CO
 o
 o
 z
                                 SLUDGE  REMOVAL-
                                 CHEMICALS
                                 ENERGY
                                 MATERIALS
                                                            LABOR
                                                            DEPRECIATION
                                                            CAPITAL
   10"
                              i  i t i iil
                                           i  i i  i 1111    i   i
                    0.01
ai FLOW,  mgd  '-0
10.0
               FIGURE  VIH-113. PRIMARY ALUMINUM  COMB. I , ALT. 4
                                 (NEW SOURCES)
                                      467
-------
  RECYCLE
~V ALTERNATE i
                   • ALTERNATE  2
                                                                    RECYCLE

CHEMICAL
PRECIPITATION

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f
' II
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                              Y ALTERNATE  3/4

                      COMBINATION  1
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                              YALTERNATE 3/4
                       COMBINATION  2
                        CFUUE  SCRUBBER)
                                                                     RECYCLE
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CHEMICAL .
PRECIPITATION ^

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V
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                              YALTERNATC i

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    FIGURE VIII-117. SECONDARY ALUMINUM
     NEW  SOURCE  TREATMENT SCHEMES
                               468
-------
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  ,o6
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             SLUDGE REMOVAL
             CHEMICALS
             ENERGY 8 MATERIALS
Mil
                                                           LABOR
                                                           DEPRECIATION
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                                 i nl	i  i   i i i 1111
                                                       i   iii
                                                                      i   i  i i i i 11
                   0.01
                ftl
                                      FLOW, mgd    -
10.0
            FIGURE VIII-118. SECONDARY  ALUMINUM  COMB. I , ALT. I
  10
 ',1
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  io4
                                                           LABOR
                                                           DEPRECIATION
                                                           CAPITAL
                                       I  1 I I I I I I     I  1 i I I I I I
                   0.01
                OJ  FLOW,  mgd   L0
10.0
            FIGURE VIII-II9 . SECONDARY ALUMINUM  COMB. I, ALT. 2
                                          469
-------
  10
  10
I

                         MATERIALS
                         ENERGY
                         CHEMICALS
                         SLUDGE REMOVAL
  10
. l.li
                         I  i	I  LLLLll	 1
                                  J
                                                           LABOR
                                                           DEPRECIATION
                                                           CAPITAL
                            ml
                   0.01            0.1 _._...     .   1.0            10.0
                                     FLOW, mgd

             FIGURE VIII-120. SECONDARY ALUMINUM  COMB. I , ALT. 3
  10
  10
w
3
r
  10
                             SLUDGE REMOVAL
                             CHEMICALS
                             ENERGY
                                 i i 11     i  i  I  I I I 111
                                                           LABOR
                                                           DEPRECIATION
                                                           CAPITAL
                                                            I III I I	 i  I i  I II It
                   0.01
OJ FLOW, mgd   L0
                                              10.0
             FIGURE VIII-121 . SECONDARY ALUMINUM COMB. I , ALT. 4
                                          470
-------
  10
  10
O
u

O
  .o4
                    SLUDGE REMOVAL-
                    CHEMICALS
                    ENERGY
                    MATERIALS
i  i i i 11 il
                                                          LABOR
                                                          DEPRECIATION
                                                          CAPITAL
                                           ill
                   0.01
                     °J FLOW,  mgd  ">
                                            10.0
  10
o
u
 MO"
              FIGURE VIII-122.  SECONDARY ALUMINUM  COMB. 2 , ALT. I
                    SLUDGE REMOVAL
                    CHEMICALS
                    ENERGY
                    MATERIALS
                                                          LABOR
                                                          DEPRECIATION
                                                          CAPITAL
                         i  i  i i 1 1
                                 i il
                                       i  i  i  i i 1 1
°-01
                                    ">
                                                              I0'°
                                   -  FLOW, mgd

               FIGURE  VIII-123.  SECONDARY ALUMINUM  COMB. 2, ALT. 2
                                         471
-------
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to
o
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1'°
                             ' ' ""I    '  '  '  •''•'I
                           SLUDGE REMOVAL-
                           CHEMICALS-
                           ENERGY-
                                                          LABOR
                                                          DEPRECIATION
                                                          CAPITAL
  ,o4
I  I I I I
      ..I
I I 11 i	I  I  I I I I I ll
                   0.01
                     0-1 FLOW,  mgd  l>0
                 10.0
              FIGURE VIII-124. SECONDARY ALUMINUM  COMB. 2 ,ALT. 3
  10'
  10
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  10
                          SLUDGE REMOVAL
                          MATERIALS
  lo5
o
o
1"
                                                          LABOR
                                                          DEPRECIATION
                                                          CAPITAL
  10
                  i.il
nl
             nil
                   0.01
0.1
                                     FLOW, mgd
1.0
10.0
            FIGURE  VIII-126. SECONDARY  ALUMINUM   COMB. 3, ALT. I
                                        473
-------




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         T ALTERNATE 1
                     ALTERNATE 2
                         Y ALTERNATE  3
                                 Y ALTERNATE <• / S
                            COMBINATION 1
                           (ALL WASTE STREAMS)
FIGURE VIII-127 COLUMBIUM/TANTALUM (ORE TO SALT/METAL)
              NEW SOURCE  TREATMENT  SCHEMES
                                474
-------
  10"
  I05
8
o
                                                 LABOR
                                                 DEPRECIATION
                                                 CAPITAL
  10*
                  I..I
            ...ll
                   0.01
0.1 _, _,.,     ,   1.0
   FLOW, mgd
10.0
  10
        FIGURE VIII-128.  COLUMBIUM / TA NTALUM (ORE  TO SALT/METAL)
                         COMB.  I , ALT. I
                           SLUDGE REMOVAL
                           CHEMICALS
                           ENERGY
  10
                                                           LABOR
                                                           DEPRECIATION
                                                           CAPITAL
                   0.01
                                     FLOW,  mgd
               L0
10.0
        FIGURE  VIII-129.  COLUMBIUM / TANTALUM ( ORE TO  SALT/METAL)
                         COMB. I, ALT. 2
                                          475
-------
  10
  10
2
u
  10
            SLUDGE REMOVAL
            CHEMICALS
            ENERGY
            MATERIALS
                                                       LABOR
                                                       DEPRECIATION
                                                       CAPITAL
                                                               ill
                                                                         I I i I I I
                   0.01
0.1 _. .....     .   1.0
   FLOW,  mgd
10.0
  FIGURE VIII-130. COLUMBIUM / TANTALUM ( ORE TO SALT/METAL) COMB. I.ALT. 3

   .7
  10
CO
o
u
             SLUDGE REMOVAL
             CHEMICALS
             ENERGY
             MATERIALS
                                               11 nl
                                                       LABOR
                                                       DEPRECIATION
                                                       CAPITAL
                   0.01
                                      FLOW,  mod
                L0
10.0
  FIGURE VIII-I3I . COLUMBIUM / TANTALUM (ORE TO SALT/METAL) COMB. I, ALT. 4
                                        476
-------
  10
  10°
S
u
             SLUDGE REMOVAL
             CHEMICALS
             ENERGY
             MATERIALS
                  LllI
                                                          LABOR
                                                          DEPRECIATION
                                                          CAPITAL
                            nil
                   0.01
OJ FLOW, mgd  L0
10.0
  FIGURE VIII-132.  COLUMBIUM / TANTALUM (ORE TO SALT/METAL) COMB. I, ALT. 5
                                          477
-------
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1 Y ALTERNATE Z
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REVERSE
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ACTIVATED
CARBON

4 1

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                              V ALTERNATE 4/5

                        COMBINATION  1
                  (REDUCTION SCRUBBER AND LEACH ATE)
FIGURE VIIH33.COLUMBIUM /TANTALUM  (SALT  TO METAL)
           NEW SOURCE  TREATMENT SCHEMES
                               478
-------
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  I06
CO
o
u
lit
  .o4
                                                           LABOR

                                                           DEPRECIATION

                                                           CAPITAL
               ill
                   0.01
               °J
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10.0
        FIGURE VIII-134. COLUMBIUM /TANTALUM (SALT TO METAL) COMB. I  ALT I
  10
o
u
z
z


5'°5
o
  10
                                  "r    •
                                   SLUDGE REMOVAL-

                                   CHEMICALS-

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                                                            LABOR

                                                            DEPRECIATION

                                                            CAPITAL
                                  III	L  I  I	l i lilt    l  I I  I LLIlt
                                                                      I  I  I  I I • t I
°-01
                                  °J
                                      FLOW, mgd



    FIGURE VIII-135. COLUMBIUM/TANTALUM (SALT TO METAL)  COMa ! , ALT. I
                                        479
-------
  10
  10
v>
o
u
I
  10
                                  "I

                                  SLUDGE REMOVAL-
                                  CHEMICALS-
                                  ENERGY-
                                                          LABOR
                                                           EPRECIATION
                                                          CAPITAL
          i   i  i i i i
                   0.01
                                     FLOW,  mgd
              10.0
     FIGURE VIIH36.COLUMBIUM/TANTALUM (SALT  TO METAL)   COMB.I , ALT. 3
  10'
 u
  10
                                 SLUDGE REMOVAL-
                                 CHEMICALS
                                 ENERGY-
                                                           LABOR
                                                           DEPRECIATION
                                                           CAPITAL
                         I  i 1_ III i 11
                   0.01
K0
10.0
                                  w
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  lor
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                                                         CAPITAL
                                                       i  i i  i 111
                                                                       i i i 111
                  0.01
                                0.1
                                    FLOW,  mgd
1.0
10.0
     FIGURE VIII-138. COLUMBIUM/TANTALUM (SALT TO METAL)  COMB. I, ALT. 5
                                       481
-------
                                                          RECYCLE
                      •"ALTERNATE 2
                              V ALTERNATE 3/4

                        COMBINATION 1
                      CSCRUBBCR, CONTACT COOLING)
FIGURE VIII-139. PRIMARY COPPER (SMELTING  AND REFINING)
           NEW  SOURCE TREATMENT  SCHEMES
                                 482
-------
  10
  10
CO
o
u
r
  10
                                  SLUDGE REMOVAL-
                                  CHEMICALS-
                                  ENERGY-
                                                           LABOR
                                                           DEPRECIATION
                                                           CAPITAL
                   0.01
0-1 FLOW, mgd   l>0
10.0
     FIGURE VIII-140. PRIMARY COPPER (SMELTING S REFINING) COMB.I. ALT. I
  10
o
u
J
«
^
o
  10
                                  SLUDGE REMOVAL-
                                  CHEMICALS-
                                  ENERGY-
                                  MATERIAL
                                                            ABOR
                                                           DEPRECIATION
                                                           CAPITAL
                   0.01
                                   -  FLOW, mod   -
                             10.0
     FIGURE VIII-141. PRIMARY COPPER (SMELTING a REFINrNG) COMB. I, ALT.2
                                        483
-------
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  10"
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o
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  10
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                                                              nil
                                                                     I   I  I I I I 11
                   0.01
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-------
                                               RECYCLE
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COOLING
TOWER

1




CHEMICAL
PRECIPITATION


t-
FILTRATION
 T ALTERNATE 1
         V ALTERNATE 2
                 V ALTERN ATE I/ 4

           COMBINATION  1
           (CONTACT COOLING)
FIGURE  VIII-144. PRIMARY COPPER (REFINING)
     NEW  SOURCE TREATMENT  SCHEMES
                 485
-------
                  SLUDGE REMOVAL , CHEMICALS
                  S ENERGY-
                  MATERIAL
  10
8
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I I 111	I  I  I
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               . ...i
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                                      FLOW,  mgd
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10.0
  •o7
           FIGURE VIII-145. PRIMARY COPPER (REFINING)  COMB. I , ALT. I
o
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  to4
                  SLUDGE REMOVAL a CHEMICALS
                           I  I I I II
                    0.01
                                    '  FLOW, mad   -
                 10.0
            FIGURE VIII -146. PRIMARY COPPER (REFINING)  COMB. I, ALT. 2
                                             486
-------
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o
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                             ' • ""I    	I
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                                   ENERGY
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  10
                                                           LABOR
                                                           DEPRECIATION
                                                           CAPITAL
                   0.01
OJ
                                     FLOW, mgd
10.0
           FIGURE Vllh 147.  PRIMARY COPPER (REFINING) COMB. I, ALT. 3
  10
  10
m
o
o
  10
                                  SLUDGE REMOVAL
                                  CHEMICALS
                                  ENERGY
                                  MATERIALS-
                                11 il	i  i  i i i 111
                                                          LABOR
                                                          DEPRECIATION
                                                          CAPITAL
                                                                    1   |  I I I I II
                   0.01
OJ FLOW,  «fld  L0
10.0
           FIGURE VI11-148. PRIMARY  COPPER (REFINING) COMB.I, ALT.4
                                          487
-------
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1
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CARBON

«^_
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REVERSE j
OSMOSIS 1
1
 "Y ALTERNATE
            Y ALTERNATE Z
                    Y ALTER NATE  3

              COMBINATION   1
             (ACID PLANT SLOWDOWN)
   FIGURE VIII-I57  PRIMARY  LEAD
NEW SOURCE  TREATMENT  SCHEMES
                    488
-------
  10
  .o5
8
u
I"4
                                SLUDGE REMOVAL-
                                CHEMICALS, ENERGY a
                                MATERIALS-
                                                           LABOR
                                                           DEPRECIATION
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                                           i  i i 1111	i   i  i i i 11 il
                                                                      i  i i i i 11
  I07
                   0.01
°J
10.0
                                     FLOW,  mgd

              FIGURE VIII-158.  PRIMARY  LEAD   COMB. I.ALT. I
  .O6
w
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  •O4
                                SLUDGE REMOVAL	
                                CHEMICALS  a ENERGY-
                                MATERIALS
                                                           LABOR
                                                           DEPRECIATION
                                                           CAPITAL
                   0.01
OJ
                                     FLOW,  mgd   -
10.0
              FIGURE  VIII-159. PRIMARY  LEAD  COMB. I, ALT. 2
                                         489
-------
  10
  10
g
o
g
  icr  -
  10
                                   SLUDGE REMOVAL
                                   CHEMICALS
                                   ENERGY
                                   MATERIALS
                                                            LABOR
                                                            DEPRECIATION
                                                            CAPITAL
                   0.01
                                     FLOW,  mgd
10.0
                FIGURE VIII-160. PRIMARY LEAD COMB. I, ALT.3

                                      490
-------



CHEMICAL
PRECIPITATION




V

K
"i
                      • ALTERNATE 1
                              T ALTERNATE

                         COMBINATION 1
                        (COMBINED WASTEWATER)
^ 	
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•
L J
\^ ~Y ALTERNATE 1
1 ~Y" ALTER NATE Z

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                                ALTERNATE S/4
                         COMBINATION 2
                       CCOMBINEO WASTEWATER)
FIGURE VIII- 179.PRIMARY TUNGSTEN  (ORE  TO  SALT/METAL)
            NEW  SOURCE  TREATMENT  SCHEMES
                             491
-------
  10
  10
CO
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  10*
  10
                                  I
                                  SLUDGE REMOVAL-
                                  CHEMICALS-
                                  ENERGY
                                  MATERIALS-
                                                           LABOR
                                                           DEPRECIATION
                                                           CAPITAL
                   0.01
°J
10.0
                                     FLOW,  mgd

  FIGURE VIII-180.  PRIMARY TUNGSTEN(ORE TO SALT/METAL) COMB. I , ALT.

   7
  10
  I0
o
u
z
 fur
o
  10
                                  SLUDGE REMOVAL-
                                  CHEMICALS
                                  ENERGY
                                                     LABOR
                                                     DEPRECIATION
                                                     CAPITAL
                   0.01
                                     FLOW, mgd
               L0
10.0
   FIGURE  VIII-I8I.  PRIMARY TUNGSTEN (ORE TO SALT/METAL^ COMB. I ,ALT. 2
                                      492
-------
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8
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                                                              ..I    .   .  .
                   0.01
 °J
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                          10.0
       FIGURE VIII-182. PRIMARY TUNGSTEN (ORE TO SALT/METAL)COMB. I  ,ALT.3
                                       493
-------
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  10   -
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2*
o
  10
                                                LABOR

                                                DEPRECIATION

                                                CAPITAL
                                        I  1 I * I I I I    I  I  Illflll
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0-1 FLOW, mgd   ''°
10.0
    FIGURE Vllf-183 PRIMARY TUNGSTEN (ORE  TO SALT/METAL) COMB. 2, ALT. I
  10
  10
 v>
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                   SLUDGE REMOVAL

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                                            LABOR

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                                            CAPITAL
                   0.01
 01  FLOW,  mgd  L0
10.0
     FIGURE VIII-184.PRIMARY TUNGSTEN (ORETO SALT/METAL) COMB. 2 , ALT. 2
                                        494
-------
  10
  10
s
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3
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  10
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                           CHEMICALS
                           ENERGY
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                                                      DEPRECIATION
                                                      CAPITAL
I  lit Li^ll	I   I  I I I I I li
                   0.01
                                     FLOW,  mfld   -
                     10.0
    FIGURE  VIII-185. PRIMARY TUNGSTEN (ORE TO SALT/METAL) COMB.  2 , ALT. 3
  10
  10
o
o
  10
  10"
                           SLUDGE REMOVAL
                           CHEMICALS
                           ENERGY
                           MATERIALS
                                                      LABOR
                                                      DEPRECIATION
                                                      CAPITAL
                                         j  |  I I I I I I
                                                        I  I __ | __ I | | | j    I _ |  I
                   0.01
                                   -  FLOW,  mgd
        L0
10.0
    FIGURE VIII-186.PRIMARY TUNGSTEN (ORE TO SALT/METAL) COMB. 2, ALT. 4
                                        495
-------
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CHEMICAL
PRECIPITATION
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FILTRATION
T ALTER NATE 1
                     t ALTERNATE 3
                            Y ALTER NATE 4

                      COMBINATION 1
                     (COMBINED WASTEWATER)
 FIGURE  VIII-187. PRIMARY TUNGSTEN  (SALT TO METAL)
         NEW  SOURCE TREATMENT  SCHEMES
                           496
-------
  I06
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  I05
  10
11.1
                                                                  LABOR
                                                                  DEPRECIATION
                                                                  CAPITAL
                                                              ml
°-01
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          FIGURE VIH-188. PRIMARY TUNGSTEN (SALT TO METAL) COMB. I.ALT. I
  10
          SLUDGE REMOVAL,
          CHEMICALS 8 ENERGY
          MATERIALS
  10
0>
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  10
                                                                 LABOR
                                                                 DEPRECIATION
                                                                 CAPITAL
                   0.01
 OJ
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                                            10.0
          FIGURE VIII-189. PRIMARY TUNGSTEN (SALT TO METAL) COMB. I , ALT. 2
                                            497
-------
  10
                       SLUDGE REMOVAL,
                       CHEMICALS B ENERGY
                       MATERIALS
  10
CO
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                                                               LABOR
                                                               DEPRECIATION
                                                               CAPITAL
°-01
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          FIGURE VIII -190. PRIMARY TUNGSTEN (SALT TO METAL) COMB. I, ALT. 3
  10
  10
v>
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^-
  10"
                       SLUDGE REMOVAL
                       CHEMICALS 8 ENERGY
                       MATERIALS
                             LABOR
                             DEPRECIATION
                             CAPITAL
                   0.01
                                    -  FLOW, mgd
                L0
                                             10.0
          FIGURE VIII-I9I . PRIMARY  TUNGSTEN (SALT TO METAL)  COMB.I.ALT.4
                                          498
-------
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REVERSE 1
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, Y ALTERNATE 1~ 1
"V ALTER NATE 2
ACTIVATEDL
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3.
                   Y ALTER NATE 3/4

             COMBINATION  1
       (ACID PLANT SLOWDOWN, LEACHIMC SCRUBBER)
    FIGURE VIIH92.PRIMARY  ZINC
NEW  SOURCE TREATMENT  SCHEMES
                     499
-------
  10
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                                   SLUDGE REMOVAL
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                   0.01
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                 FIGURE Vlli-193.  PRIMARY ZINC   COMB. I , ALT.  I
  10
   6
  10
8
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                                   SLUDGE REMOVAL-
                                   CHEMICALS-
                                   ENERGY 8 MATERIALS-
                                                             LABOR
                                                             DEPRECIATION
                                                             CAPITAL
                         i i_ i I 111	i
                   0.01
                                      FLOW, mgd
                L0
10.0
                 FIGURE VIII-194. PRIMARY ZINC  COMB. I  , ALT. 2.
                                            500
-------
  10
  10
o
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                                   SLUDGE REMOVAL-
                                   CHE MI CALS-
                                   ENERGY-
                                                            LABOR
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                    I   I I  I I I
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10.0
                 FIGURE VIII-195. PRIMARY  ZINC  COMB. I  , ALT.  3
  ,o7
   6
  10
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  4
  10
                                   SLUDGE REMOVAL-
                                   CHEMICALS-
                                   ENERGY-
                                                            LABOR
                                                            DEPRECIATION
                                                            CAPITAL
                   0.01
OJ FLOW, mgd   L0
                             10.0
                 FIGURE VIII-196. PRIMARY ZINC  COMB. I , ALT. 4
                                          501
-------
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         Chlorid*      OoOOS       o.&oQ    0,0'OS  O,&0% 0,008
riw Gf//n£nc^         O.o'y'        O'C**/^     OfOOfc>  &,/:~-~£? ^/T-/^
A-cenoph-fheneL.       O.OO^L       O,OO%_    O.OOf  O,OOf  /tf~*f"
                           '/
                        - or-
                                   502
-------
                   Q.-0I        $.01


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                              503
-------
S-f-r e.ctw\
At2?u_(=:    i/irr,.- 3
      —Toffr'n'.  /tt'r~  ^)Cr cu'v
                          LT&R/VflTICS'
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pH
l~ss
Th&fiolvs
/° -7
C / a/7A/«£-
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(0. 10, O.f 10,
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                               506
-------
                                                      e
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                                   . 03.
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H5
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C. t-irv* er»e
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0.00J.
0.0?
0.A
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0.01
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                                           507
-------
•rAetw-i -.'SeCorxddry Sl/vfnmt/ry   ' " -----       '    "
               VX  /           *
                         "Raw
                                              Effluent
                                                            U
rroc
rss
A///3
a
Cr-
Cu

2n
	 _ 	 { —
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2000.
o.7
2.
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I.
2.
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too.
ZOO.
0.7
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                                         508
-------
Subcategory
Combination
= SECONDARY ALUMINUM
= 1; Dross Milling, Scrubber
TREATMENT ALTERNATIVE
POLLUTANT

TSS
NH3
Sb
As
Be
Cd
Cr
Cu
Pb
Hg
Ni
Se
Tl
Zn
Raw
mg/1
6000
200
0.1
0.02
0.5
0.5
2
9
7
0.0007
1
0.01
1
7
1

70
7
0.001
0.005
0.2
0.01
1
0.1
0.2
0.0001
0.2
0.004
0.3
1
2
Effluent
10
7
0.001
0.004
0.1
0.01
1
0.1
0.05
0.0001
0.05
0.004
0.3
0.3
3
mg/1
0.5
0.3
0.001
0.001
0.01
0.001
0.05
0.01
0.01
0.0001
0.001
0.001
0.01
0.01
4

0.5
0.3
0.001
0.001
0.01
0.001
0.05
0.01
0.01
0.0001
0.001
0.001
0.01
0.01
Di-n-butyl
  phthaiate
                 ug/1
20
                              Effluent ug/1
V 1
                                         509
-------
Subcategory =  SECONDARY ALUMINUM



Combination = 2; Scrubber, Contact Cooling
                                        TREATMENT ALTERNATIVE
POLLUTANT
TSS
NH3
Sb
As
Cu
Pb
Hg
Se
Tl
Zn
Cyanide
Be
Cd
Cr
Ni

Raw
mg/1
2000
1
0.12
0.01
0.3
2
0.03
0.01
0.1
3
0.3
0.2
0.5
0.05
0.5
ug/1
1
60
0.5
0.001
0.002
0.05
0.2
0.0001
0.005
0.05
1
0.2
0.1
0.02
0.05
0.1

2
Effluent
9
0.5
0.001
0.002
0.05
0.05
0.0001
0.005
0.02
0.5
0.2
0.05
0.02
0.05
0.1
Effluent
3-
»g/l
0.5
0.5
0.001
0.001
0.002
0.005
0.0001
0.001
0.01
0.05
0.02
0.001
0.001
0.005
0.002
ug/1
4
0.05
0.02
0.001
0.001
0.001
0.001
0.0001
0.001
0.001
0.001
0.001
0.001
0.001
0.001
0.001

Dichlorobromo-
me thane
Di-n-butyl
phthalate
5

20
». 1

2
1

1
1

1
1

1
                                        510
-------
Subcateeorv = SECONDARY ALUMINUM

Combination = 3; Contact Cooiing
Di-n-butyl
  phthaiate
                                             TREATMENT ALTERNATIVE
POLLUTANT
TSS
Sb
As
Be
Cd
Cr
Cu
Pb
Hg
Ni
Tl
Zn
Raw
»g/l
4000
2
0.2
0.02
0.05
0.1
4
4
0.1
0.1
2
20
1 2
Effluent mg/1
90
0.1
0.05
0.001
0.001
0.005
0.2
0.2
0.001
0.02
0.5
0.5
9
0.1
0.05
0.001
0.001
0.001
0.1
0.02
0.0001
0.02
0.5
0.5
3
0.5
0.002
0.001
0.001
0.001
0.001
0.01
0.001
0.0001
0.001
0.02
0.05
                           ug/1
1000
100
                       Effluent ug/1
50
50
                                       511
-------
' /
                         — IF

               EJMT  <
        "Raw
f£
A/fe
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Co
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                 512
-------
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 300.
   0.8
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   0.1

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200.
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-------
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                           i 514
-------
                                      SOU' I
Subcategory =  SECONDARY COPPER

Combination = 1; Slag, Contact Cooling
                                             TREATMENT ALTERNATIVE
POLLUTANT
Raw
mg/1
1 2
Effluent mg/1
3
TSS
NH3
Phenolics
Sb
As
Be
Cd
Cr
Cu
Pb
Hg
Ni
Se
Ag
Zn
Fluoranthene
Bis(2-ethylhexyl)
  phthalate
Di-n-butyl
  phthalate
Pyrene
PCS-1254
PCB-1248
6000
0.1
0.1
0.2
0.2
0.1
0.3
0.2
60
50
0.005
1
0.2
0.2
700
ug/1
2
70
0.1
0.1
0.001
0.03
0.05
0.01
0.2
0.3
0.5
0.0001
0.2
0.1
0.1
4

1
20
0.1
0.05
0.001
0.02
0.05
0.01
0.2
0.3
0.3
0.0001
0.1
0.1
0.1
3
Effluent ug/1
1





\f\
b ^
K
QJ S
t \
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\I N-
A fe
V)





300

 10
  1
  0.5
  0.5
200

  1
  1
100
  0.5
  0.2
  1
  1
  0.1
  0.1
                                   515
-------
                                       scar
Subcategory =  SECONDARY COPPER



Combination = 2; Contact Cooling
                                             TREATMENT ALTERNATIVE
POLLUTANT
TSS
Phenolics
Sb
As
Be
Cd
Cr
Cu
Pb
Hg
Ni
Se
Ag
Zn


Fluoranthene
Bis (2-ethylhexyl)
phthalate
Di-n-butyl
phthalate
Pyrene
PCB-1254
PCS- 1248
Raw
mg/1
0.02
0.2
2
0.2
0.02
0.2
0.3
10
0.6
0.002
0.3
0.2
0.05
7

ug/1
5

20

5
5
0.5
0.5
1
0.02
0.1
0.02
0.05
0.01
0.01
0.3
0.1
0.2
0.0001
0.1
0.1
0.02
1


1

20

1
1
0.5
0.5
2 3
Effluent mg/1
0.02
0.1
0.02
0.02
0.01
0.005
0.3
0.1
0.05
0.0001 |J
0.05 ° tf
0.05 s) r
0.01 J §
0.3 0 :j
V) ^
Effluent ug/1 V)
1

10

1
1
0.1
0.1
                                   516
-------
                            i— e   jznr-
Subcateeorv =  SECONDARY COPPER

Combination = 3;  Contact Cooling,  Scrubber
                                             TREATMENT ALTERNATIVE
POLLUTANT

TSS
Phenolics
Sb
As
Be
Cd
Cr
Cu
Pb
Hg
Ni
Se
Ag
Zn

Fluoranthene
Bis(2-ethylhexyl)
phthalate
Di-n-butyl
phthalate
Diethyl phthalate
Pyrene
PCB-1254
PCB-1248
($) Total Capital:
($/yr) Total Annual:
($/yr) Add'l. Annual:
Raw
mg/1
4
0.01
0.1
0.01
0.005
0.01
0.2
20
0.5
0.0002
8
0.01
0.05
2
ug/1
5

20

5
1
5
0.5
0.5



1

4
0.005
0.001
0.002
0.001
0.001
0.2
0.1
0.1
0.0001
0.1
0.005
0.01
0.5

1

20

1
1
1
0.5
0.2
160,000
76,000
76,000
2
Effluent mg/1
0.001
0.005
0.001
0.002
0.001
0.001
0.2
0.1
0.05
0.0001
0.1
0.005
0.01
0.3
Effluent ug/1
1

10

1
1
1
0.1
0.1
360,000
180,000
104,000
3

0.001
0.001
0.001
0.001
0.001
0.001
0.01
0.05
0.001
0.0001
0.01
0.001
0.001
0.02

1

5

1
1
1
0.1
0.1
650,000
310,000
130,000
(over previous alternative)
(acres) Land Required:
0.61
0.65
0.69
                                      517
-------
                                      L/IIL: - '?-
Subcategory =  SECONDARY COPPER

Combination = 4; Scrubber
                                             TREATMENT ALTERNATIVE
POLLUTANT
Raw
mg/1
1 2
Effluent mg/1
3
TSS
Phenolics
Sb
As
Be
Cd
Cr
Cu
Pb
Hg
Ni
Se
Ag
Zn
Fluoranthene
Bis(2-ethylhexyl)
  phthalate
Di-n-butyl
  phthalate
Diethyl phthalate
PCB-1254
PCB-1248
4
0.005
0.10
0.01
0.001
0.01
0.2
20
0.5
0.0002
8
0.01
0.03
2
4
0.005
0.001
0.002
0.001
0.001
0.2
0.1
0.1
0.0001
0.1
0.005
0.01
0.5
0.001
0.005
0.001
0.002
0.001
0.001
0.2
0.1
0.05
0.0001
0.1
0.005
0.01
0.3
ug/1

  2

200

 10
  1
  5
  2
100

  2
  1
  2
  2
Effluent ug/1

     1

    50

     1
     1
     0.5
     0.5
                                           D.
                                           0.
                                0.001
                                0.001
                                 .001
                                 .001
                                0.001
                                0.001
                                0.01
                                0.002
                                0.001
                                0.0001
                                0.01
                                0.001
                                0.001
                                0.02
50

 1
 1
 0.1
 0.1
                                       518
-------
                                     JZUT-
Subcategory =  SECONDARY COPPER



Combination = 5;  Contact Cooling,  Scrubber, Electrolyte
                                            TREATMENT ALTERNATIVE
POLLUTANT
TSS
Phenol ics
Sb
As
Be
Cd
Cr
Cu
Pb
Hg
Ni
Se
Ag
Zn

Fluoranthene
Bis (2-ethylhexyl)
phthalate
Di-n-butyl
phthalate
Fluorene
Pyrene
PCS- 1254
PCB-1248
Raw
mg/1
8
0.01
0.3
0.1
0.005
0.1
0.2
6
1
0.0002
10
0.1
0.3
4
ug/1
20
100
50
50
100
1
0.5
1
8
0.005
0.005
0.02
0.002
0.005
0.2
0.2
0.2
o'.oooi
0.2
0.05
0.1
1

5
100
10
10
20
0.5
0.5
2
Effluent mg/1
8
0.005
0.005
0.02
0.002
0.002
0.2
0.1
0.1
0.0001
0.1
0.05
0.01
0.5
Effluent ug/1
2
50
5
5
10
K 0.1
K 0.1
3
0.2
0.001
0.001
0.001
0.001
0.001
0.01
0.005
0.01
0.0001
0.02
0.001
0.01
0.05

1
20
2
K 1
K I
K 0.1
K. 0.1
                                       519
-------
                              V>M M  — /1

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O.O^ O.OO2.
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-------
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-------
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      "SZZH- —
a NIT
Subcategory
Combination
= PRIMARY ALUMINUM (New Sources)
= 1; Contact Cooling, Cryolite
TREATMENT ALTERNATIVE
POLLUTANT

TSS
NH3
Phenolics
Cyanide
Sb
As
Cd
Cr
Cu
Pb
Hg
Ni
Se
Ag
Zn

Fluoran-
thene
Raw
mg/1
200
30
0.2
100
0.1
0.05
0.1
0.2
0.2
2
0.0001
1.0
0.01
0.05
0.5
ug/1

100
1

20
2
0.1
4
0.001
0.02
0.002
0.2
0.05
0.2
0.0001
0.2
0.005
0.01
0.3


20
2
Effluent mg/1
2
2
0.1
4
0.001
0.001
0.002
0.2
0.05
0.1
0.0001
0.1
0.005
0.01
0.01
Effluent ug/1

20
3

0.02
0.2
0.1
1
0.001
0.001
0.001
0.01
0.002
0.005
0.0001
0.005
0.001
0.001
0.005


1
4

0.02
0.3
0.005
0.2
0.001
0.001
0.001
0.01
0.002
0.005
0.0001
0.005
0.001
0.001
0.005


1
       530
-------
Subcategory =  SECONDARY ALUMINUM (New Sources)

Combination = 1; Milling, Scrubber
                                          TREATMENT ALTERNATIVE
POLLUTANT
             Raw
             mg/1
                           2              3
                             Effluent mg/1
TSS
NH3
Sb
As
Be
Cd
Cr
Cu
Pb
Hg
Se
Tl
Zn
2000
1
0.1
0.01
0.2
0.5
0.05
0.2
2
0.001
0.01
0.1
3
60
1
0.001
0.002
0.1
0.02
0.05
0.05
0.2
0.0001
0.005
0.05
0.5
10
0.5
0.0001
0.002
0.1
0.01
0.05
0.05
0.05
0.0001
0.005
0.02
0.5
0.5
0.5
0.001
0.001
0.005
0.001
0.005
0.002
0.001
0.0001
0.001
0.001
0.02
0.5
0.02
0.001
0.001
0.005
0.001
0.005
0.002
0.001
0.0001
0.001
0.001
0.02
Dichlorobromo-
 methane
Di-n-butyl
 phthalate
ug/1


3

5
                                              Effluent ug/1
                                    531
-------
                             TABLE VI I I -32
Subcategory =  SECONDARY ALUMINUM (New Sources)

Combination = 2; Fume Scrubber


                                TREATMENT ALTERNATIVE
POLLUTANT
Raw 1
mg/1
2 3
Effluent mg/1
4
TSS
NH3
Sb
As
Be
Cd
Cr
Cu
Pb
Hg
Se
Tl
Zn
2000
1
0.1
0.01
0.2
0.5
0.05
0.2
2
0.001
0.01
0.1
3
60
0.5
0.001
0.002
0.1
0.02
0.05
0.05
0.2
0.0001
0.005
0.05
0.5
10
0.5
0.001
0.002
0.1
0.01
0.05
0.05
0.05
0.0001
0.005
0.02
0.5
0.5
0.5
0.001
0.001
0.005
0.001
0.005
0.002
0.001
0.0001
0.001
0.001
0.02
0.5
0.02
0.001
0.001
0.005
0.001
0.005
0.002
0.001
0.0001
0.001
0.001
0.02
Dichlorobromo-
 methane
Di-n-butyl
 phthalate
ug/1


3

5
1

1
Effluent ug/1


1

1
1

1
                                    532
-------
                                  TABLE VIII-33

                                     EJS1T
Subcategory =  COLUMBIUM/TANTALUM (ORE TO SALT/METAL - New Sources)

Combination = 1 ; Combined Wastewater


                                        TREATMENT ALTERNATIVE
POLLUTANT    Raw
             rag/1
 2           3
Effluent mg/1
TSS 90
NH3 6000**
Fluoride 8000
Sb 2
As 0.1
Be 0.01
Cd 0.1
Cr 0.1
Cu 0.02
Pb 4
Hg 0.001
Ni 0.5
Ag 0.1
Zn 2
ug/1
1,2,4-Trichloro-
benzene 50
1,2-Dichloro-
ethane 50
Bis (2-ethylhexyl)
phthalate 200
Tetrachloro-
ethylene 20
PCB-1254 0.3
PCB-1248 0.2
90
20
8000
2
0.1
0.01
0.1
0.1
0.02
4
0.001
0.5
0.1
2


50

50

200

20
0.3
0.2
10
1
60
0.01
0.02
0.005
0.002
0.1
0.005
0.05
10
1
20
0.01
0.005
0.005
0.002
0.1
0.005
0.05
0.0001 0.0001
0.05
0.05
0.5


5

2

100

5
0.2
0.2
0.05
0.05
0.5
Effluent ug/1

2

2

100

5
0.2
0.2
0.5
1
20
0.01
0.005
0.001
0.001
0.005
0.001
0.005
0.0001
0.005
0.002
0.02


2

2

1

5
0.1
0.1
0.5
1
1
0.002
0.005
0.001
0.001
0.005
0.001
0.005
0.0001
0.005
0.002
0.02


1

1

50

1
0.1
0.1
** Calculated for a segregated stream.
                                     533
-------
                                  TABLE VIII-34

                                 EK1T  
-------
                                  TABLE VIII-35
Subcategory = PRIMARY COPPER (SMELTING, AND SMELTING AND REFINING
              New Sources)

Combination = 1; Scrubber, Contact Cooling
                                        TREATMENT ALTERNATIVE
POLLUTANT
TSS
Sb
As
Cd
Cu
Pb
Hg
Ni
Se
Ag
Tl
Zn
Raw
mg/1
3000
2
2000
7
300
100
0.05
6
0.01
0.5
0.1
90
1
10
0.01
9
0.2
1
1
0.0005
0.1
0.005
0.2
0.05
0.5
2
Effluent mg/1
10
0.01
0.5
0.2
1
1
0.0005
0.1
0.001
0.01
0.05
0.5
3*
0.5
0.001
0.01
0.01
0.05
0.05
0.0001
0.005
0.001
0.001
0.002
0.02
4
0.5
0.01
0.01
0.01
0.05
0.05
0.0001
0.005
0.001
0.001
0.002
0.02
* Quality of treated water available for recycle, no discharge
                                     535
-------
                                  TABLE VIII-36
Subcategory =  PRIMARY COPPER (REFINING - New Sources)

Combination = 1; Contact Cooling


                                        TREATMENT ALTERNATIVE
POLLUTANT
Raw
mg/1
123
Effluent mg/1
4
TSS
Sb
As
Cd
Cr
Cu
Pb
Hg
Ni
Se
Ag
Tl
Zn
400
1
0.2
0.1
0.2
30
0.5
0.01
0.4
0.3
0.5
2
0.6
20
0.01
0.02
0.001
0.2
0.1
0.05
0.0002
0.05
0.02
0.01
0.5
0.2
10
0.01
0.001
0.001
0.2
0.1
0.05
0.0002
0.05
0.02
0.01
0.5
0.2
0.5
0.001
0.001
0.001
0.01
0.01
0.001
0.0001
0.005
0.005
0.01
0.1
0.01
0.5
0.001
0.001
0.001
0.01
0.01
0.001
0.0001
0.005
0.005
0.01
0.1
0.01
                                         536
-------
                                 TABLE VIII-39
                                            da.uAL.iTy
Subcategory =  PRIMARY LEAD  (New Sources)
Combination = 1;  Acid Plant, Sinter Scrubber
                                          TREATMENT ALTERNATIVE
POLLUTANT
NH3
Sb
As
Be
Cd
Cu
Pb
Hg
Ni
Se
Ag
Zn
Raw
mg/1
2
0.01
0.2
0.001
0.3
2
40
0.0002
0.02
0.005
0.001
60
1 2
Effluent mg/1
1
0.001
0.02
0.001
0.01
0.1
0.5
0.0001
0.02
0..002
0.001
0.3
0.05
0.001
0.001
0.001
0.002
0.01
0.01
0.0001
0.005
0.002
0.001
0.01
3*
0.05
0.001
0.001
0.001
0.002
0.01
0.01
0.0001
0.001
0.001
0.001
0.005
* Quality of treated water  available for recycle, no discharge
                                       537
-------
                                  TABLE  VIII-44
Subcateeorv =
Combination =

POLLUTANT

TSS
Cyanide
As
Cd
Cr
Cu
Pb
Hg
Ni
Se
Ag
Tl
Zn
PRIMARY TUNGSTEN (ORE
1; Combined Wastewater

Raw
mg/1
200
0.01
4
0.05
0.05
0.1
10
0.002
0.1
0.02
0.05
0.5
2
TO SALT/METAL)

TREATMENT
1


ALTERNATIVE
2



3
Effluent mg/1
10
0.2
0.005
0.02
0.005
0.5
0.05
0.005
0.05
0.02
0.01
0.1
0.2
0.5
0.01
0.001
0.001
0.001
0.05
0.002
0.0002
0.002
0.002
0.001
0.005
0.01
0.5
0.01
0.001
0.001
0.001
0.05
0.002
0.0002
0.002
0.002
0.001
0.005
0.01
* Quality of treated water available for recycle, no discharge
                                  538
-------
                                  TABLE VIII-45
Subcategory =  PRIMARY TUNGSTEN (ORE TO SALT/METAL - New Sources)



Combination = 2; Combined Wastewater



                                        TREATMENT ALTERNATIVE
POLLUTANT
TSS
NH3
Cyanide
As
Cd
Cr
Cu
Pb
Hg
Ni
Se
Ag
Tl
Zn
Raw
mg/1
200
800
0.01
4
0.05
0.05
0.1
11
0.002
0.1
0.02
0.05
0.5
2
1
200
40
0.01
4
0.05
0.05
0.1
11
0.002
0.1
0.02
0.05
0.5
2
2
Effluent mg/1
10
20
0.2
0.005
0.02
0.005
0.5
0.05
0.005
0.05
0.02
0.01
0.1
0.2
3*
0.5
1
0.01
0.001
0.001
0.001
0.05
0.002
0.0002
0.002
0.002
0.001
0.005
0.01
4
0.5
2
0.01
0.001
0.001
0.001
0.05
0.002
0.002
0.002
0.002
0.001
0.005
0.01
* Quality of treated water available for recycle, no discharge.
                                    539
-------
                                  TABLE VIII -46
Subcategory =  PRIMARY TUNGSTEN (SALT TO METAL - New Sources)




Combination = 1; Combined Waste-water






                                        TREATMENT ALTERNATIVE
POLLUTANT
TSS
NH3
As
Cd
Cr
Cu
Pb
Ni
Se
Ag
Tl
Zn
Raw
mg/1
200
500
0.01
0.05
0.05
0.01
0.02
0.05
0.01
0.02
0.1
0.05
1
200
20
0.01
0.05
0.05
0.01
0.02
0.05
0.01
0.02
0.1
0.05
2
Effluent mg/1
20
20
0.002
0.02
0.002
0.002
0.01
0.05
0 , 005
0.01
0.05
0.05
3
10
20
0.005
0.002
0.02
0.005
0.02
0.005
0.01
0.02
0.1
0.1
4
0.5
1
0.001
0.001
0.001
0.001
0.001
0.001
0.001
0.002
0.005
0.005
                                         540
-------
                                  TABLE VIII-47
Subcategory =  PRIMARY ZINC (New Sources)




Combination = 1; Combined Wastewater




                                        TREATMENT ALTERNATIVE
POLLUTANT
TSS
Cyanide
Sb
As
Cd
Cr
Cu
Pb
Hg
Ni
Se
Ag
Tl
Zn

Methylene
chloride
Raw
mg/1
20
0.1
1
0.5
7
1
4
5
0.1
2
0.2
0.2
0.2
900
ug/1

200
1
10
0.05
0.005
0.05
0.2
1
0.2
0.2
0.001
0.1
0.1
0.05
0.05
5


2
2
Effluent mg/1
5
0.05
0.005
0.02
0.2
1
0.1
0.02
0.001
0.05
0.1
0.05
0.05
4
Effluent ug/1

2
3*
0.2
0.01
0.001
0.005
0.01
0.05
0.01
0.005
0.0001
0.005
0.005
0.005
0.002
0.2


2
4
0.2
0.001
0.001
0.005
0.01
0.05
0.01
0.005
0.0001
0.005
0.005
0.005
0.002
0.2


1
Bis(2-ethylhexyl)
phthalate
30
20
10
1
10
* Quality of treated water available for recycle, no discharge
                                        541
-------

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                                                                 545
-------






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546
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550
-------
                           SECTION IX

               BEST PRACTICABLE CONTROL TECHNOLOGY
                       CURRENTLY AVAILABLE
The best practicable control technology currently available  (BPT)
has been  established  for  a  number  of  subcategories  in  the
nonferrous  metals industry.  In accordance with the Act, BPT was
to be implemented by all industrial dischargers by July 1, 1978.

BPT effluent limitations are based on the  average  of  the  best
performance  by  exemplary  plants  found in the industry, taking
into account:

1.  The total cost of application of the technology  in  relation
to  the  effluent  reduction  benefits  to  be achieved from such
application.
2.  The age of the equipment and plant facilities involved.
3.  The production process employed.
H.  The engineering aspects of the application of  various  types
of control techniques.
5.  Process changes.
6.  Non-water  quality  environmental  impact  (including  energy
requirements).

While  BPT normally emphasizes end-of-pipe treatment, it may also
include the control technologies  within  the  process  that  are
considered normal practice within the industry.

PRESENT STATUS OF BPT LIMITATION GUIDELINES

Effluent   limitations   representing  the  degree  of  reduction
attainable by the application of BPT have  been  promulgated  for
several  of  the  subcategories  within  the  industry.  Effluent
limitations for bauxite, primary aluminum, and secondary aluminum
were published the  Federal  Register  on  April  4,  1974.   BPT
limitations  for  primary  copper, secondary copper, primary lead
and primary zinc were published on February 27, 1975.

BPT alternatives  for  the  columbium-tantalum,  secondary  lead,
secondary  silver,  and  tungsten subcategories, are evaluated in
this report.

BEST PRACTICABLE CONTROL TECHNOLOGY CURRENTLY AVAILABLE

Alternatives For Best Practicable Control Technologies

The  purpose  of  this   report   is   to   evaluate   wastewater
characteristics   and  control  and  treatment  methods  for  the
                               551
-------
industry,  and  to  present  alternative  treatment  and  control
schemes that yield various levels of effluent quality.  For those
subcategories  of  the  nonferrous  metals industry for which BPT
limitations have been published, the data  base  accumulated  for
this  report  was  reviewed  to evaluate those BPT limitations in
light of the Clean Water Act (PL  95-217).   In  all  cases,  the
existing BPT limitations were judged adequate.

For  those  subcategories  for  which  BPT limitations were never
established,  alternative  treatment  technologies  for  BPT  are
presented  herein.   In  each case, the effluent quality from the
application  of  the  given  alternative  is   presented.    This
information  could  serve  as  an  input  to the selection of BPT
limitations.

The alternatives for BPT effluent limitations are  based  on  the
average of the best plants in the subcategory.
                                552
-------
Primary  Coljinbiuin--T_antaluin  JC)re to  SaltJL-,   Alternatives 1 and 2
may be used for BPT«  Theso  alternatives  include  oteam  stripping
and  chlorine  oxidation  or  high  ammonia  streams,  and chemical
precipitation and filtration of the combined  streams.   Effluent
mass loadings are presented  oelow.
A///3
                                 •-> /**/
                                 v/- '
        Cu                       ^'              1°°'
        CJ                      *iOd,              30,
       Cr-                      Z ft            20$"
                                 x%              o.l
                                100.
 These  loadings   are   based  on  a  flow  rate  of  15  gal/lb  of
 precipitation capacity,  achieved by  2 out of 3 plants.
                                  553
-------
Primary Columbium-Tantalum (Salt to Metal).   Alternative 1 may be
used  for  BPT  for  treating the reduction  scrubber and leachate
wastewater.  This alternative  includes  lime  precipitation  and
filtration.  The effluent mass loadings are  presented  below.
                                   Ai-Tf£RMA-

                                        /
               7~5S                fooo.
                                     30,
               Cd                     o.Z
               Cr~                    20.
              Co                     & •
               ?L                     7.
              H3                     °
              A//"                    /o.
             ^^                    f^
                                      0.02.
                                      S.
                                      0.2.
                                      0.2.
                                      0.2.
 These loadings are based on a flow rate of 16  gal/lb  of  reduction
 capacity, achieved by  2 out of 4 plants.
                               554
-------
  Secondary  Lead.   Alternative  1  may  be   used   for  BPT.   This
  alternative includes lime precipitation  and  filtration  and  is
  utilized  to  treat the battery acid and saw water.   The effluent
  mass loadings are presented below.

  Battery Cracking
                                         H

                                      (&- ?)
                                        0.0 1
                 f^li                    O.

                 A?                    0.

                 &rt                    O.
                Oi-n- k>fj+vj            ef • 000 •
                                       O. 000
                                       a.

                                       O.
                Oi - r>—
These  loadings  are  based 6n a  flow  rate  of 100  gal/ton of lead
produced by the cracking operation,  achieved  by  17  out  of  32
                                555
-------
Reverb & Blast Furnace Scrubbers
                                          •'
 These loadings  are based on a flow rate  of  165  gal/ton of  furnace
 capacity,  achieved by 3  out of 1  plants, including the plant with"
 the highest water use.

 Kettle and Other Furnace Scrubbers

 Tentative   BPT   effluent  limitations   are  zero  discharge  of
 pollutants, achieved by 1 out of  9 plants.

 Casting

 Tentative  BPT  effluent  limitations  are  zero   discharge   of
 pollutants, achieved by 6 out of 8 plants.

                                 556
-------
 Secondary Silver (Photographic).  Alternatives 1, 2, and  3 may  be
 used for BPT.   These alternatives include steam stripping of  the
 high  ammonia   stream and combining the wastewaters for treatment
 by chemical precipitation  and  filtration.   The  effluent  mass
 loadings are presented below.

Film Stripping and Precipitation
        7-JFS
        jshewlfcS
                                - -]-.--
                        — -I  •*	
                                             JL£V  \IO  .	/£._!__.
                     — 4.-- \
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                                                              a
        W/
                                                            £>•*
                                                            e.f
                                                            c.
                                            4'ffl.
                                            i  .
          1 - G'C-hJare & -fh y/ff* e .
                                             .6 1
                           0.01
   These  loadings  are  based  on  a  flow rate of  50  gal/1000  troy
   ounces silver produced by the operation, achieved by 3  out  of   4
   plants.
                                 557
-------
Solution Silver Recovery
      P 0 u_t_ U -PA. rxj ~T
                                    :  L-j-^—'•'
                                   aJ?45Ll_ ..0.1    6.01
   4JLi_. *
   M.*
                                   4*'* 2
      XU.
                                           0. 143
                                   ^?, £7.2    «?, 
-------
Electrolytic Refining
                                                 ^^li/lIL'
                                                    3
                          ==t="'
                                          1^2.
                                    T" 1
                                    7.  \
                                               	0i_e3.  \
                                          i^.JL
&?2-
                                                  a ^_-
These   loadings  are  based  on  a   flow  rate of 20 gal/1000 troy
ounces  refined silver, achieved by  12  out of 15 plants.
                                 559
-------
Casting
                                          1-0
                                                  f\ i-.~rc5.0e4v AT i \J<&3
                                                    -i      3
                                                 $000
                                                          0.0J
   C *<
                                                  7      3
                                                  O.o3>    o.o/
  JL./,-
'e/ie.
                                           _/._.-!.
                                           O.f   ffi-l
                   JL*-'^.
                    3 £-3
                                                            ~ 3
These   loadings  are   based  on  a   flow rate of 12  gal/1000 troy
ounces  of silver cast,  achieved by  4  out of 7 plants  using water.
                                  560
-------
 Secondary Silver  (Non-Photographic).  Alternatives  1 and  2 may be
 used   for   BPT.    The alternatives  are  used  to  treat the  combined
 wastewaters and include chemical  precipitation  and   filtration.
 The effluent mass  loadings  are  presented below.

Leaching/Precipitation/Filtration
 These loadings  are  based on a flow  rate   of   240   gal/1000   troy
 ounces of  silver recovered, achieved by   5 out of  13  plants.
                                561
-------
Leaching/Precipitation/Filtration Scrubbers
                                                      ATI i/i=:
                                                       .2.
                                     e. -ff
                                                   I   I  I

 These   loadings   are  based  on  a flow rate of 515 gal/1000 trov
 ounces  silver recovered,  achieved by 5 out of 10 plants.
Furnace Scrubbers

Tentative   BPT   effluent  limitations  are  zero
pollutants,  achieved by 5  out of 6  plants.
discharge   of
                                 562
-------
 Electrolytic Refining
These loadings are based on a  flow  rate  of  20  gal/1000  troy
ounces refined silver, achieved by 12 out of 15 plants.
                                 563
-------
    ^ -" ;_ '.^ l-xi ~r/\ .-..' "r


                                      30   .  	;_..,!?:



                                        0.03          ,&

                                                       S)  I


                                      £0C              b .






                                        fi  i '           £>
                                        ** '  f +  ,   .   .  .™^-
                                        
-------
Primary Tungsten  (Ore to Salt).  Alternatives 1 and 2 may be used
for  BPT.   The  alternatives  are  used  to  treat  the combined
wastewaters and include  steam  stripping  and  filtration.   The
effluent mass loadings are presented below.


 Ore to Salt
 These_loadings  are  based  on  a  flow  rate   of  11.5  qal/lb  of
 aminonxum paratungstate  capacity,  achieved by 4  out of 5 plants.
                                565
-------
Primary  Tungsten JSalt to Metal).  Alternative 1 may be used for
BPT.  This alternative includes  steam stripping and filtration of
the  combined  wastewater.   The effluent  mass   loadings   are
presented below.

Salt to Metal
                                      £ F f
                                             To
          Cr
          Pb                                a.
These  loadings  are  based  on  a  flow  rate  of 1.12 gal/lb of
tungsten metal, achieved by 3 out of 5 plants,
                                 566
-------
                            SECTION X

           ALTERNATIVES FOR BEST AVAILABLE TECHNOLOGY
               FOR DIRECT AND INDIRECT DISCHARGERS
The  effluent  limitations that must be achieved by July 1, 1984,
are to  specify  the  degree  of  effluent  reduction  attainable
through   the   application  of  the  best  available  technology
economically achievable (BAT).

Consideration must also be given to:

1.  The age of equipment and facilities involved
2.  The process employed
3.  The engineering aspects of the application of  various  types
of control techniques
4.  Process changes
5.  Cost of achieving the required effluent reduction
6.  Non-water  quality  environmental  impact  (including  energy
requirements)

BAT  assesses the availability of in-process controls, as well as
control or additional treatment techniques employed at the end of
a production process.

INDIRECT DISCHARGERS

Industrial wastewaters discharged  to  publicly  owned  treatment
works  (POTWs)  are  regulated  by  301(b)  of  the Federal Water
Pollution Control Act as  amended  in  1977.   Such  sources  are
obligated  to  comply  with  pretreatment  standards  promulgated
pursuant to Section 307  of  the  Act.   The  objectives  of  the
Federal  Pretreatment  Standards  as  outlined  in  The  National
Pretreatment Stategy, 40 CFR 403, are:

1.  To prevent  inhibition/interference  with  the  operation  of
POTWs, including contamination of municipal sludge,
2.  To correct inadequate treatment by industry and  by  POTW  of
many pollutants prior to their release to the environment, and
3.  To improve opportunities to recycle and  reclaim  wastewaters
and the sludges resulting from wastewater treatment.

In  order  to  achieve  these objectives, EPA has established two
sets of pretreatment standards:   Prohibited-Discharge  Standards
and  Categorical  Pretreatment standards.  These are specified in
the General Pretreatment Standards, 40 CFR 403.

Prohibited-discharge standards prohibit the discharge by  a  user
of  a  publicly  owned  treatment  work of any non-domestic waste
                                567
-------
containing pollutants that would substantially interfere with the
operation of the POTW.  All industrial users, regardless of  size
or industrial subcategory, are subject to these regulations.  The
Prohibited-Discharge    Standards   specifically   prohibit   the
introduction of the following pollutants into POTWs:

1.  Pollutants that create a fire or explosion hazard in the POTW
2.  Pollutants  that  will  cause  corrosive  structural  damage,
unless  the  POTW  is  specifically  designed to accommodate such
discharges
3.  Solid or  viscous  pollutants  in  amounts  that  will  cause
obstruction   in   sewers   or   otherwise  interfere  with  POTW
operations.
4.  Discharges of pollutants, including oxygen  demand,  in  such
volume  or  concentration  that they interfere with the treatment
process
5.  Heat in amounts that  will  inhibit  biological  activity  in
POTWs;  in  no  case  can  temperature  at the influent to a POTW
exceed 40°C.

The categorical pretreatment standards apply to existing and  new
sources  in  a  specific industrial category.  In compliance with
the consent decree, the 65 classes of toxic pollutants are to  be
reviewed and standards set for any of the pollutants found not to
be susceptible to treatment by POTWs, or which interfere with the
operation  of the POTW.  The wastewaters of the nonferrous metals
industry contain significant concentrations of toxic  pollutants.
It  is  known that heavy metals can inhibit biological wastewater
treatment.  If the metals are not in high  enough  concentrations
to  inhibit  biological  treatment,  they  may concentrate in the
sludge or may pass through the POTW essentially  untreated   (28).
Many  of  the  organics  that  pose  potential  problems  in  the
nonferrous metals industry are not biodegradable  and  thus  will
pass   through   a  POTW.   Therefore,  it  is  recommended  that
wastewaters  from  the  nonferrous  metals  industry   that   are
discharged   to   POTWs   must  receive  the  same  treatment  as
wastewaters discharged directly to  rivers  and  lakes.   Indeed,
many  municipalities have already issued very strict pretreatment
regulations governing some priority pollutants  (28).   Thus,  the
treatment  technologies  for  indirect  and  direct  dischargers,
contained in this report are identical.

This report has  presented  the  wastewater  characteristics  and
several  wastewater  treatment  alternatives  for  the nonferrous
metals industry.  Each combination of wastewaters  is  associated
with  a  series  of treatment alternatives.  The alternatives are
arranged so that  unit  operations  are  added  to  the  previous
alternative  to  improve  effluent quality.  Thus, each series of
alternative  treatment  schemes  presents  a  range  of  effluent
                              568
-------
quality.   Furthermore,  the  cost  of  the  treatment  generally
increases as the effluent quality is improved.

This section presents a summary by subcategory of the alternative
treatment schemes and the effluent loadings associated with  each
scheme.

BEST AVAILABLE TREATMENT

BAT Treatment Alternatives

Each subcategory in the nonferrous metals industry is composed of
a  wide  variety  of  plants that produce specific metals by many
different processes.  Each process may have a unique  combination
of  wastewaters.  Sections VII and VIII of this report present in
detail the treatment methods for each combination of  wastewaters
and  the  cost  of  each treatment method (alternative).  Section
VIII also indicates the quality of the wastewater treated by each
method.

Following is a presentation of the effluent mass loading per unit
production produced by treatment alternatives that  are  suitable
for BAT for each subcategory.  In some subcategories. Alternative
1  is  equivalent  to  BPT;  these are omitted from the following
presentation and discussed in Section IX.  In all cases,  recycle
of  process  wastewater  is  included  as  part  of the treatment
scheme.  In some subcategories, the level of recycle may be  less
than in others.
                           569
-------
Primary  Aluminum.   The  various alternative levels of treatment
include:

1.   Chlorine oxidation and chemical precipitation,
2.  Filtration and activated alumina added to level 1,
3.  Reverse osmosis and complete recycle added to level 2,
4.  Activated carbon added to level 2.

Paste Plant
                                   *     2--"     3
        rss,
                             0.03    0.03    e'f    '"   0.0 3
       Cyantiz.              /ff-3

                              O.O/     O.O/            3* £-3
       C-r-
       As                  3.F-3   3. £-3           3.£-.
       n/r&ne,                o,O /
            5«f«e-              O.O/
            (wpyrene,          O,O2.    o.Of
  These loadings are based on a flow rate of 60 gal/ton  of  paste,
  achieved by 1 of the four plants.
                                   570
-------
Anode  Baking
         '**-r
         r\jrc.ne.
          TSS.            £               0-0C3
  X'
                            0.00?-
                                                             3 £-
These  loadings  are based  on a flow  rate of 20  gal/ton of baked
anodes,  achieved  by 1 out of 9 plants.
                      >:'n3j e.f-n'r>r-'.»^^.vViori , C ^ •?!"• • '..I   > » r' -,e- -r-ti~i,i^

                   J  ^5 IT Sir/-,,>.-r i .>*> i.  i 5,  g
                                     571
-------
 Cryolite


                                   TV* S A TASTED T
                                0.
   3                           /&          to                 it.

                                o.ot       0.ai               t


"Pb                            ty.oc,       -2               0.003
                               o. oot       a

                                               H              f £-6
           >  Chloride

   or-otn-i-h* n e
 These loadings are based on a flow rate  of  65  gal/ton of aluminum
 production, achieved by four  out  of  six  plants   using  w^ter
 Aluminum  production,  in  this case, means the  production at all
 the plants from which the spent cathodes came.
 Cathode Making
 this operation.                           ans wl<   use water for
                               572
-------
 Primary Potline Scrubbing
                             & —SX

        "P0UUT/WT
                               Effluent _
         rss  ,         200.        7.      $
                          0.00*1    o.ooJ
                         60.        3.
         /}<,              O.Ob    c
         Cr-              0.4      0-i             0.0^
                                    0.02.            0.00?
                                    //T-Y
                           0.0 f     O.OO'/
                           0.08     0.0*5
                           O.Of     O.O/            O.O/
                           o.oy     o, 03
                           o.o/     0.007
                          o.p?    oto7
These loadings are based on a flow rate of  225 gal/ton   aluminum,
achieved by 8 out of  12 plants.

*r                    j               L_
 ' *~c^*-~f *v\&r\ +•   i S>   c> e?.s c,r~r fc?^ «d   c'L'«i    c*. - j   i*\C*--± I O (^   3V % £7 T" ^",
                                573
-------
Secondary Potroom Scrubbing
           rss              30.

                              0.07.     0.02
                             O.OO4   O.OO3
                             oJ      0,07

           -«ro (aj pv^n^-      O.Z      O.3.
                             o.Z      o.f
                             o, 3      o.Z
'0.
0.0(0
0.02
o.f
7.
o.0t>
0.02.
OJ
7.
O.Ob
o.oZ
0.03
These  loadings   are  based  on  a  flow  rate  of 550  gal/ton  of
aluminum produced in  the potroom, achieved by three out of  seven
olan-t-c:.
plants.


    A^__
                       . f S.-I--S  & -f
                                 574
-------
Casting-DC
  TbUunVlNT
     T55
    PI>

  ActnapMhc-n*-
                              Effluent -
                                     /v,
                                     cf
                                    ?*//*/«
                        0.00*7

                        o.o/
                          0.002
                                                 o.7

                                                 o.oof
  These  loadings  are  based on a flow rate of  120  gal/ton of cast
  aluminum, achieved by 10 out of 28 plants.
                /  /S
                                         — -*-'
                              I -   <>
    C 0 KV\ b i K,  xl i ,
Casting-Sows &^ Pigs

Tentative  BAT  effluent  limitations  are  zero
pollutants, achieved by  11 out of 12 plants.
                                                      discharge    of
                                  575
-------
 Secondary Aluminunu  The various levels of treatment include:
                  steam stripping of slag milling water; and lime
              of the combined streams;
2.   Filtration added to level  1;
3.  -Reverse osmosis and complete recycle added to level 2- and
4.  Activated carbon added to level 2.


Chlorine Demagging
*—
FH
rss
A///3
a
Cr~
Co
Pb
in
/ 2. 3
Eff ItJtfnf _ /r?<7 //CO
J ' J
C«-(l k-c! Nc
&>. 3. T>e*f/rft.fc
0.2. o.l
0.0 f 0.00*1
0.03 0.03
0.03 0t02
& . 0&> o. 0 /
o. / o. /
^
(r-1
3,
0.2
0. 000*1
o*OQ Z
0.02.
6.003
o.o/
   These loadings are based on a flow rate of 75 gal/ton of degassed
   aluminum, achieved by 5 out of 10 plants.
   Dross Milling
   Tentative   BAT   effluent  limitations  are  zero  discharge  of
   pollutants, achieved by 3 out of 4 plants that use water for this
   process.
                                 576
-------
Casting
Tentative  BAT  effluent  limitations  are  zero   discharge   of
pollutants,  achieved  by  9  out of 14 plants that use water for
this process.
Aluminum Fluoride Demagging
Tentative  BAT  effluent  limitations  are  zero   discharge   of
pollutants.
                              577
-------
Primary Columbium-Iantalum (Ore to Salt).   The  alternative levels
of treatment include:

1.   Steam stripping and chlorine oxidation of  the  high  ammonia
streams;
2.    Chemical  precipitation  and  filtration   of  the  combined
streams;
3.   Activated alumina added to level 2;
4.   Reverse osmosis and complete recycle  added to  level 3; and
5.   Activated carbon  added to level 3.
                                  7
z&
/.£4
106,
7.4-y
^,/V
100.,
30,
206'
200,
100.
zo.
200.
           ^                  fr-7    *-?
           TS5>                 ?.Eb   /ooo,     tooo,  !>.•*,'.'-)•  fooo
          Cu                  /£lj     100.   /OO.            10
          C
         Zn                 3^    QOQ,    WO.          30.
                               100,     40,    HO,            0.
                                °t,      0,9    &8           °-
                                         ^       -            ^K
                               10,
                              /OO,     no.    20.            o
                              (00,     10,    /O.            °*f
  These   loadings   are  based  on  a  flow  rate  of  15  gal/lb of
  precipitation  capacity, achieved by 2 out of 3 plants.
                                  578
-------
Primary Col umbiuin-Iant alum   (Salt  to  Metal)
levels of treatment include:

1.   Chemical precipitation and filtration;
2   Activated alumina added to level 1 ; and
3.   Activated carbon added to level 2.
                                                  The   alternative
                                Effluent -
TSS
Atf/3
F/w-SJc
cd
Cr-
Cu
H
^3
A//'
Zn
J 2. - D'Cwe>roeJ-/ian&,
&£ (^f-^fff/ln^yl) p/)"fMi
K, Jf~ & C'fJ(&f~O &ifiy ' ^ ^ ^~
"^y^i iffi __ /j Ku
K&-a48
^•"7
fooo.
30,
/JE*4
o.Z
20 .
&•
7.
0.0*4
lo.
5*
•^ 8.
0.2*
aZ
O.Z
tooo*
30.
too.
o.'Z
ZO,
£>,
F
o.O?
/&,
fO.
0.0*2.
8.
o.g.
0*7-
0.2.
1000.
Jo.
/oo.
0.02.
2-
6.
A
tf.£>3
/•
^
|^V
-------
 include:
          Copper  (Smelting).   The alternative leve^ -  jf treatment
      Chemical precipitation with recycle;
 2.   Filtration and recycle added to level 1;  and
 3.   Activated carbon and recycle added to level 2.

 Tentative  BAT  effluent   limitations   are  zero   discharge   of
 pollutants.
Primary Copper  (Refining).  The alternative levels  of  treatment
include:

1.  Recycle of contact cooling water with a blowdown  treated  by
chemical precipitation;
2.   Filtration added to level 1; and
3.   Activated carbon added to level 2.
•Rfefining
        a
                         /        2.           -3
      T0UUT4NT
                                    -V/V-
pd
As'
Cr
Cu.
fti
A
Sz~
Ac\
<*-
-------
 Secondary Copper.  The alternative levels of treatment include  :

 1.  Primary  settling  of   the  slag  milling  water,  with   the
 supernatant combined with the contact cooling water for treatment
 by  chemical precipitation;
 2,  Filtration is added to  level 1; and
 3.   Storage in a holding tank


 Tentative   BAT   effluent  limitations  are  zero  discharge  of
 pollutants.
 Primary Lead.  The alternative levels of treatment include:

 1.   Filtration;
 2.   Activated carbon added to level 1; and
 3.   Reverse osmosis and complete recycle added to level 2.


Smelting
	^
—
7-55
£/
Cu
PL
^n
t Z
EffluerH-^/Tw/fo
vl J
e* /,
O.O^ o.oooi
0.0*} 0,0*1
0.0^ O.02.
2. O.O&
3
?
No
of 7
?tl/
-------
Secondary  Lead.   The  various   alternative  levels of treatment
include:

1.   Chemical precipitation  and  filtration;
2.   Activated alumina added to  level 1;
3.   Reverse osmosis and complete recycle added to level 2; and
H.   Activated carbon added  to level 2.

Battery Cracking
                                '         2

                                   Effluent
                               0.0J     o.oi

                              o>* I      0g
                                        '•*«              *.*y
          Oi - n- bu.+yj
          ^''
          A*                 <*•**     *••*-               *.***
                               •*       * • -?                0.03
                               03     0-03.
                                         ooo
                                       a- 000 6
                             0-0*      0.04              0.03

               '3*3)  ta.ffj   O. 0of   d.,

           '33.1
         &i - r> — oc-'fv/        o.
  These loadings are based on a flow rate of 100  gal/ton   of  lead
  produced  by  the  cracking  operation,  achieved by  17  out of 32
  plants.
                                 582
-------
Reverb &_ Blast Furnace Scrubbers

                                  -rJ?E*TH6NT * Ll*X.HATlire
                             fr~Cf      *-f     No          &-1

                             fr,1     fi.7     *4c^e   t,f
                             fi.H    #.
                                      ffi.tte
  P±
   M'
  A*
  Pi -/? -
These loadings are based on a flow  rate of 165 gal/ton of furnace
capacity, achieved by 3 out of 7 plants, including the plant with
the highest water use.


Kettle  and Other Furnace Scrubbers

Tentative  BAT  effluent  limitations  are   zero   discharge   of
pollutants, achieved by 7 out of 9  plants.
 Casting

 Tentative    BAT   effluent  limitations  are  zero  discharge  of
 pollutants,  achieved by 6 out of 8 plants.
                                 583
-------
Secondary Silver (Photographic).
subcategory  include:
The treatment levels  for  this
1.   Steam  stripping of the high ammonia streams;
2.  chemical  precipitation of the combined streams;
3.  Filtration  added to level 2; and
4.  Activated carbon added to level 3.
 F_i1m Stripping and  Precipitation
 T>ht

»

gjno/fc_S
/e/^

•
• - - 	 '







— -
. j
j




. J
- - - - -
. (p-C]
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j ' 3is>C
_: ' /<*><=
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;
ko
f
	 4« :
r
t





- ..
k~(\
<*0O
306
t*0
IO
J
/y
.»
..-**
                            I
                                    2.0
                 <5>/a
                                            j?_r*_
                                            A
                                           J^
               .  /.£>	/_£__
. G*'S
Ot'-r,- oc--*y/
                                                           0.01
  These  loadings are based on a  flow  rate  of   50   gal/1000  troy
  ounces  silver  produced by the operation, achieved by  3  out of 4
  plants.
                                 584
-------
 Solution Silver Recovery
                                                    "f^LJL
                                         {,-0?(f \  6.0O3  ./^-V_.
                                 (j?.^    #;008__,2.&-t/   3.£-*i
                                 0.007-   o.ooi   //?-y   .i^-y
W/
0, 000*4
0.
o.s
                                         o,
                                 Q. OOO3:


                                 0.eel
 These loadings are based on a flow rate  of the amount of  solution
 processed.

 Furnace Scrubbers

 Tentative  BAT  effluent  limitations   are  zero   discharge   of
 pollutants, achieved by 5 out of 6 plants.
                                  585
-------
Electrolytic Refining
        -• A. i
            ...I..
w/
   -x7- oe-^y/
                     -3
         -  r- i. (^ tijij-JjT  * 2,' K«
             C-ff   &~f?
          \'_ \30o    30
         -h


._	fL
       4 .1 .____*i	^.J
                            .
-------
 Casting
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jyti&r*&/ics
,£y<»S)feJ?
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l£^*>
^H .
LZ-3.
'*-3 :
           I  I

These loadings are based on a  flow  rate  of  12  gal/1000  troy
ounces of silver cast, achieved by '4 out of 7 plants using water.
                              587
-------
 Secondary  Silver  _tNon-Photographic) .  The alternative levels  of
 treatment include:
 1.  Steam stripping of the high  ammonia streams;
 2.  Chemical  precipitation  and  filtration  of
 streams; and
 3.   Activated carbon added to level 2.
                           the   combined
 Leaching/Precipitation/Filtration
              i  I	
                                  &,3


                               •ZCL&-
   fe
I_K
                      -M-
A//
                             10,000,
                     .  '  >?



                    i_/
                                                               i   i
f>
  These  loadings  are  based  on  a flow rate of  240  gal/1000 troy
  ounces of silver recovered, achieved by  5 out of  13 plants.
                                  588
-------
Leachinq/Precipitation/Filtration Scrubbers
                                                s^
                                              '
                                              _.
                                                             ;y_£*0_L
                                              L  L_*£_
 A*
.Pb


A//
t_	j
i
                  '	i—
                                                                    -^—.
                               / 0,000 :
                /
                                                   t	
                                                                 &,{,
                                                  6.6.
                                                             	_£_
                                   ffi.Aj.
  These loadings are based on a flow  rate  of  515  gal/1000  troy

  ounces silver recovered, achieved by 5 out of 10 plants.
  Furnace Scrubbers



  Tentative   BAT    effluent  limitations   are   zero   discharge   of

  pollutants,  achieved by  5  out  of  6  plants.
                                   589
-------
Electrolytic Refining
                                       V 7
            	I..
              I
              f~
              t
              I
            	,_.._.
                                                               e-1 __L
                                  ^S>_
                                          -•  .L£i
'?

 0-0.3-
 0. a?
 6.3L
                                                              10
                                                                    i——i
                                     -: a. .
 These loadings are based on  a   flow  rate   of  20   a^i/innn  *.
 ounces refined silver, achieved by  12 out  of 15 plan?sf °°°  "^
                                  590
-------
Casting
          __-_ [   I

                                 <*l£_y_
                        I
                       4-~
.-jgi5_!.._i	_-.l.-.i^
                              . -.<2
-------
Primary   Tungsten   (Ore  to  Salt).   The  various  alternative
treatment levels are:

1.   Steam stripping;
2.  Filtration added to level one;
3.  Reverse osmosis and complete recycle added to level 2; and
4.  Activated carbon added to level 2.
                          /       2       3

                              Effluent *-

£>H
7""C C
/V//5
/)
&r
Rb
/rO
M^l*^
L£-
4^ i^1^* /?^0 .
lOOQ* 1000.
?. 2.
20. . £>,
20. //,
^*
>/?<£. a 7 ^.3
/^X* *y 7 /X*"* — ^ 1
C^x "*" ' -- ^ {5? *^J
1000. ^00,
100. 1000,
o.4 2.
A <^.
4V ^.^
^» Y ^ . v
/•) ^ -O ") ^
t/» -2 ^* * J *S>
 These loadings are based  on  a  flow  rate  of  11.5  gal/lb  of
 ammonium paratungstate capacity,  achieved by 4 out of 5 plants.
                                  592
-------
Primary Tungsten  (Salt to Metall*  The levels  of  treatment  for
this subcategory  are:

I.   Steam stripping and filtration;  and
2.  Activated carbon added to level 1.
                                                            v &
-V 5-                         1 d
 A/^
 Cr
C,j
 PL                            (9.2.                  0.0?
/U                          d.f<£                 #>tf#6


These  loadings  are  based  on  a  flow  rate  of 1.12 gal/lb of
tungsten metal, achieved by 3 out of 5 plants.
                                 593
-------
Primary Zinc.  The  levels  of  treatment for this subcategory are:

1.  Filtration and  activated  alumina;
2.  Reverse osmosis and complete recycle added to level  1; and  3.
Activated carbon added to  level 1.
 Pyrometallurgical Z inc




         TbUuiT/INT
          T*"
          I +~".
          As
l-'f
o
0*00°[
o
o
O.O&
o
o
0
^9
o*ooC>
(, ~ 7
o
OtCXff
o
o
££-4
O
o
o
O,O 3
Qf OO£>
                                                         o
                                                         o
          /\J.-                   o           o             ^>
          5<2x                  O           O             £>

                                                          ^
         Zn                  ^"7       a6>J?        ^^>?
              Cnwric/c,
 These  loadings   are  based on a flow rate of 320 gal/ton of  zinc,
 achieved by 1 out of  2  plants.
                                 594
-------
Electrolytic Zinc
          M
                              /

fj t -1
55 o
> o
/
' 0.7
0*0^7
0
> O
o
A
o
o

6-7
O
o
o*OOrf
0.07
o
o
d
0. i
o
o
0.09.
I. -7
o
o
o.o?.
0,07
o
o
0
/~) f}£~J

o
o
OiO'sL-
 These loadings are based on  a   flow  rate  of   1200   gal/ton   of
 electrolytic zinc, achieved by  2 out of  4 plants.
                                  595
-------
Metallurgical Acid Plants.  The   levels  of  treatment  for  this
subcategory are the same  as those discussed under—Primary Zinc.
                           TJ?£«TM£NT
                                         2-        3
rss
As
Cr-
Cu
Pb
%
Se
A*
20,
0.07.
a f
o.^i
o,3
0,0(5 /
o,/
o /*?
0,07
*
20.
o.ooz
O+O*7~
0*0*1
o.O'S
O* OOO"^
o./
0*0^
0.00*7
20.
0.02
o.o
-------
                           SECTION XI

                  ALTERNATIVES FOR NEW SOURCES


                          INTRODUCTION

A  new  source  is  defined  in  the  Act  as  "any  source,  the
construction  of which is commenced after publication of proposed
regulations  prescribing  a  standard   of   performance."    .The
alternatives  developed for new sources discharging directly to a
stream, river,  etc.,  are  identical  to  the  alternatives  for
indirect  dischargers.  A discussion of the reasoning for this is
given in the beginning of Section X.

New source treatment alternatives are  developed  by  determining
what  higher levels of pollution control and treatment beyond BAT
are available through the use of  improved  production  processes
and/or  treatment  techniques.   Thus, in addition to considering
the best in-plant and end-of-pipe controls  and  treatments,  new
source  technology  is based upon an analysis of how the effluent
load may be reduced by changing the  production  process  itself.
Alternative  processes,  operating methods, or other alternatives
must be considered.  Consideration must  also  be  given  to  the
applicability  of  a  no discharge of pollutants standard for new
sources.

The  following  production  process  factors  are  considered  in
assessing new source treatment technology:

1.  The type of process employed and/or employable;
2.  Operating methods;
3.  Batch as opposed to continuous operations;
4.  Use of alternative raw materials and mixes of raw materials;
5.  Use of dry rather than wet processes.

NEW SOURCE PRETREATMENT AND PERFORMANCE STANDARDS

Alternative Technologies

The   purpose   of   this   report   is  to  evaluate  wastewater
characteristics, and control and treatment methods.  In addition,
alternative control and  treatment  schemes  that  yield  various
levels  of  effluent  quality are presented with tabulations that
describe the effluent quality for each subcategory.

Primary Aluminum.  The various alternative  levels  of  treatment
for new sources include:
                                597
-------
1.  Recycle of contact cooling with a blowdown combined with  the
cryolite  stream  for  treatment  by  chlorine oxidation and lime
prec ip itat i on;
2.  Filtration and activated alumina added to level 1;
3.  Reverse osmosis and complete recycle added to level 2; and
4.  Activated carbon added to level 2.

The control techniques applicable to primary aluminum plants  are
the  elimination  of potline scrubbing, paste plant scrubbing and
anode bake plant scrubbing wastewater by the use of baghouses  or
dry  scrubbing.  Additionally, by the use of the best hooding and
primary control techniques,  the  need  for  secondary  (potroom)
scrubbing  can  be eliminated.  Possible new source standards for
these operations are zero discharge of pollutants.  Possible  new
source  standards for contact cooling water and cryolite recovery
are the same as for BAT.

Secondary Aluminum.  The various levels of treatment include:

1.  Complete   recycle   of   slag   milling   water    following
sedimentation, and lime precipitation;
2.  Filtration added to level 1;
3.  Reverse osmosis and complete recycle added to level 2; and
4.  Activated carbon added to level 2.

Possible new source standards  for  chlorine  demagging  scrubber
process  wastewater  are  the same as for BAT for this operation.
Possible new source standards for the other operations  are  zero
discharge of pollutants.

Primary Columbium-Tantalum  (Ore to Salt) .  The alternative levels
of treatment include:

1.  Steam stripping and chlorine oxidation of  the  high  ammonia
streams;
2.  Chemical  precipitation  and  filtration  of   the   combined
streams;
3.  Activated alumina added to level  2;
4.  Reverse osmosis and complete recycle added to level 3; and
5.  Activated carbon added to level 3.

Possible new source standards are the same as for BAT.

Primary Columbium-Tantalum   (Salt  to  Metal).   The  alternative
levels  of treatment include:

1.  Chemical precipitation;
2.  Filtration added to level 1;
3.   Activated alumina added to level 2;
4.   Reverse osmosis and complete recycle added to level 3; and
                                 598
-------
5.   Activated carbon added to level 3.

Possible  new source standards corresponding to alternatives 2, 3
and 5 are the same as for BAT alternatives 1, 2 and 3.   Possible
new  source  standards  for  alternative  4 are zero discharge of
pollutants.

Primary CopjDer   (Smelting) .  The alternative levels of  treatment
include:

1.  Primary settling of the scrubber water with  the  supernatant
combined   with   the   cooling   water   followed   by  chemical
precipitation, filtration and recycle;
2.  Activated alumina added to level 1, followed by recycle;
3.  Reverse osmosis and complete recycle added to level 2; and
H.  Activated carbon added to level 2, followed by recycle.

Possible new source  standards  for  this  subcategory  are  zero
discharge of pollutants.

Primary  Conger   (Refining).  The alternative levels of treatment
include:

1.  Recycle of contact cooling water with a blowdown  treated  by
chemical precipitation, filtration and recycle;
2.  Activated alumina added to level 1, followed by recycle;
3.  Reverse osmosis and complete recycle added to level 2; and
>4.  Activated carbon added to level 2, followed by recycle.

Possible new source standards for alternatives 1 and  4  are  the
same  as  for  BAT  alternatives  2  and  3.  Possible new source
standards for alternative 3 are zero discharge of pollutants.

Secondary Copper.  The alternative levels of treatment include:

1.  Primary  settling  of  the  slag  milling  water,  with   the
supernatant combined with the contact cooling water for treatment
by chemical precipitation;
2.  Filtration is added to level 1; and
3.  Storage in a holding tank for complete recycle.

Possible new source standards are zero discharge  of  pollutants,
the same as for BAT.

Primary  Lead...   Possible new 'source standards are zero discharge
of pollutants.  All wastewater, apart from acid  plant  blowdown,
can be eliminated.
                                  599
-------
Secondary  Lead.   The  various  alternative  levels of treatment
include:

1.  Chemical precipitation and filtration;
2.  Activated alumina added to level 1;
3.  Reverse osmosis and complete recycle added to level 2; and
1.  Activated carbon added to level 2.

Possible new source standards are the same as for BAT.

Secondary Silver (Photographic) .  The treatment levels  for  this
subcategory include:

1.   Steam stripping of the high ammonia streams;
2.  Chemical precipitation of the combined streams;
3.  Filtration added to level 2; and
4.  Activated carbon added to level 3.

Possible  new  source  standards  for  electrolytic  refining and
casting  are  zero  discharge  of  pollutants.   For  the   other
operations,  possible  new  source  standards are the same as for
BAT.

          Silver (Non-Photographic).  The alternative  levels  of
treatment include:

1.  Steam stripping of the high ammonia streams;
2.  Chemical  precipitation  and  filtration  of   the   combined
streams; and
3.  Activated carbon added to level 2.

Possible new  source  standards  for  electrolytic  refining  and
casting   are  zero  discharge  of  pollutants.   For  the  other
operations, possible new source standards are  the  same  as  for
BAT.

Primacy   Tungsten    (Ore  to  Salt).   The  various  alternative
treatment levels are:

1.  Steam stripping;
2.  Chemical precipitation and filtration added to level 1;
3.  Reverse osmosis and complete recycle added to level 2, and
4.  Activated carbon added to level 2.

Possible new source standards are the same as for BAT.

Primary Tungsten  (Salt to Metal).  The levels  of  treatment  for
this subcategory are:

1.  Steam stripping;
                                 600
-------
2.  Chemical precipitation added to level 1;
3.  Filtration added to level 2; and
4.  Activated carbon added to level 3.

Possible new source standards are the same as for BAT.

Primary Zinc.  The levels of treatment for this subcategory are:

1.  Chemical precipitation;
2.  Filtration added to level 1;
3.  Reverse osmosis and complete recycle added to level 2; and
4.  Activated carbon added to level 2.

For  electrolytic   plants,   possible   new   source   standards
corresponding  to alternatives 2, 3 and 4 are the same as for BAT
alternatives 1,  2  and  3.   For  pyrolytic  and  electrothermic
plants, possible new source standards are zero discharge.

Metallurgical Acid Plants.  The alternative treatment and control
levels  for  this subcategory, and the corresponding possible new
source standards, are the same as for BAT.
                                601
-------
                           SECTION XII

                        ACKNOWLEDGEMENTS
The author is grateful  to  the  hundreds  of  people  that  have
assisted  in  the development of this report.  It is not possible
to acknowledge all of them  by  name,  but  some  who  have  been
especially helpful are recognized below.

Mr.  Ernst  Hall of the Effluent Guidelines Division who provided
project guidance and valuable insights throughout the study.

The personnel of Sverdrup & Parcel and  Associates,  particularly
Dr.  James Buzzell, Dr. Donald Washington and Mr. Garry Aronberg,
who directed and performed much of the work associated with  this
study.

Ms.  Ellen  Gonter and Ms. Linda Deans of the Analytical Services
Laboratory of NUS Corporation.

Mr. Jack Eagan of  Vulcan  Materials  Company  and  the  Aluminum
Recycling Association, and Mr. Seymour G. Epstein of the Aluminum
Association.

We  acknowledge  with  appreciation  the  hundreds  of nonferrous
metals  industry  personnel   who   completed   data   collection
portfolios and assisted during sampling visits.
                                 603
-------
                          SECTION XIII

                           REFERENCES
1.  Sampling & Analysis Procedures for  Screening  of  Industrial
Effluents for Priority Pollutants, USEPA Environmental Monitoring
and  Support  Laboratory,  Cincinnati,  OH   45268   (March, 1977,
revised April, 1977).

2.  "Mineral Facts and Problems," Bureau of Mines  Bulletin  667,
Washington, D.C., Department of the Interior (1975).

3.  Development Document for Effluent Limitations Guidelines  and
New   Source  Performance  Standards  for  the  Primary  Aluminum
Smelting Subcategory, EPA-440/l-74-019d, Environmental Protection
Agency  (March, 1974) .

4.  Development Document for Effluent Limitations Guidelines  and
New  Source  Performance  Standards  for  the  Secondary Aluminum
Subcategory, EPA-400/l-74-019e, Environmental  Protection  Agency
(March, 1974).

5.  Development Document for Interim Final  Effluent  Limitations
Guidelines  and Proposed New Source Performance Standards for the
Primary Copper Smelting Subcategory and Primary  Copper  Refining
Subcategory,  EPA-440/l-75/032b,  Environmental Protection Agency
(February, 1975) .

6.  Development Document for Interim Final  Effluent  Limitations
Guidelines  and Proposed New Source Performance Standards for the
Secondary Copper  Subcategory,  EPA-440/l-75/032c,  Environmental
Protection Agency (February, 1975).

7.  Development Document for Interim Final  Effluent  Limitations
Guidelines  and Proposed New Source Performance Standards for the
Lead Segment,  EPA-440/l-75/032a, Environmental Protection  Agency
(February, 1975) .

8.  Development Document for Interim Final  Effluent  Limitations
Guidelines  and Proposed New Source Performance Standards for the
Zinc Segment,  EPA-440/1-75/0.32, Environmental  Protection  Agency
(February, 1975) .

9.  Draft   Development   Document   for   Effluent   Limitations
Guidelines   and   New   Source  Performance  Standards  for  the
Miscellaneous  Nonferrous   Metals   Segment,   EPA-440/1-76/067,
Environmental Protection Agency (March, 1977).
                                605
-------
10. "Natural Resources Defense Council v.  Train,"  Environmental
Reporter - Cases 8 ERC 2120  (1976).

11. Development Document for Effluent Limitations Guidelines   and
New   Source  Performance  standards  for  the  Bauxite  Refining
Industry,  EPA-440/1-74/019C,  Environmental  Protection   Agency
(March, 1974).

12. Pound, C. E. and Crites, R. W., "Land Treatment of  Municipal
Wastewater  Effluents,  Design Factors - Part I," Paper presented
at USEPA Technology Transfer Seminars  (1975) .

13. Wilson, Phillip R., Brush Wellman, Inc., Elmore, OH, Personal
Communication  (August, 1978).

14. Description of the  Beryllium  Production  Processes  at   the
Brush  Wellman,  Inc.  Plant  in   Elmore, OH, Brush Wellman,  Inc.
(1977) .   (Photocopy) .

15, Phillips,  A.  J.,  "The  World1s  Most  Complex   Metallurgy
(Copper,  Lead  and  Zinc),"  Transactions  of  the Metallurgical
Society of AIME, 224, 657  (August, 1976) .

16. Schack, C. H. and Clemmons, B. H., "Review and Evaluation  of
Silver-Production  Techniques," Information Circular 8266, United
States Department of the Interior, Bureau of Mines  (March, 1965).

17. Technical Study Report:   BATEA-NSPS-PSES-PSNS-Textile  Mills
Point   Source   Category,   Report   submitted  to  EPA-Effluent
Guidelines Division by Sverdrup &  Parcel  and  Associates,   Inc.
(November, 1978) .

18. The Merck Index, 8th edition,  Merck  & Co., Inc.,   Rahway,  NJ
(1968) .

19. Rose, A. and Rose, E., The Condensed Chemical Dictionary, 6th
ed.,  Reinhold publishing Company,  New York  (1961).

20. McKee, J. E. and Wolf, H. W.  (eds.), Water Quality Criteria,
2d edition,  California   State  Water   Resources  Control  Board
(1963).

21. Quinby-Hunt, M. S., "Monitoring Metals   in  Water,"   American
Chemistry (December, 1978) ,  pp. 17-37.

22. Fassel,  V.  A.  and  Kniseley,  R.  N.,   "Inductively   Coupled
Plasma   - Optical  Emission Spectroscopy,"  Analytical Chemistry,
46, 13  (1974).
                                  606
-------
23. Study of Selected  Pollutant  Parameters  in  Publicly  Owned
Treatment   Works,   Draft   report   submitted  to  EPA-Effluent
Guidelines Division by Sverdrup &  Parcel  and  Associates,  Inc.
(February, 1977).

2U. Schwartz, H. G. and Buzzell,  J.  C.,  The  Impact  of  Toxic
Pollutants   on  Municipal  Wastewater  Systems,  EPA  Technology
Transfer, Joint Municipal/Industrial Seminar on  Pretreatment  of
Industrial Wastes, Dallas, TX  (July, 1978) .

25. Class notes and research compiled for graduate class.  Autumn
Qtr.,  1976-77  school  year at Montana State University by G. A.
Murgel.

26. Gough, P.  and  Shocklette,  H.  T.,  "Toxicity  of  Selected
Elements  to  Plants,  Animals  and Man—An Outline," Geochemical
Survey of the  Western  Energy  Regions,  Third  Annual  Progress
Report,  July, 1976, US Geological Survey Open File Report 76-729,
Department of the Interior, Denver  (1976).

27. Second Interim Report - Textile Industry BATEA.-NSPS-PSES-PSNS
Study, report submitted to EPA-Effluent  Guidelines  Division  by
Sverdrup & Parcel and Associates, Inc.  (June, 1978).

28. Proposed Criteria for Water Quality,  Vol.  1,  Environmental
Protection   Agency   (October,  1973)  citing  Vanselow,  A.  P.,
"Nickel, in Diagnostic Criteria for  Plants  and  Soils,"  H.  D.
Chapman,  ed.. University of California, Division of Agricultural
Science, Berkeley, pp. 302-309  (1966).

29. Morrison, R. T. and Boyd, R. N., Organic Chemistry, 3rd  ed.,
Allyn and Bacon, Inc., Boston  (1973).

30. McKee, J. E. and Wolf, H. W.  (eds), Water  Quality  Criteria,
2d  edition,  California  State  Water  Resources  Control Board,
(1963) citing Browning,  E.,  "Toxicity  of  Industrial  Metals,"
Butterworth, London, England  (1961).

31.	citing  Stokinger,  H.  E.  and   Woodward,   R.   L. ,
"Toxicologic  Methods for Establishing Drinking Water Standards,"
Journal AWWA, 50, 515  (1958).

32. 	 citing Waldichuk,  M.,  "Sedimentation  of  Radioactive
Wastes  in the Sea," Fisheries Research Board of Canada, Circular
No. 59  (January, 1961).

33. 	 citing "Quality Criteria for Water," U.S. Environmental
Protection Agency, Washington, D.C., Reference No. 440/9-76-023.
                                607
-------
34. Bronstein, M. A., Priviters, E. L., and Terlecky, P. M., Jr.,
"Analysis of Selected Wastewater Samples of  Chrysotile  Asbestos
and   Total   Fiber  Counts  -  Nonferrous  Metals  Point  Source
Category," Calspan Advanced Technology  Center,  Report  No.  ND-
5782-M-19  for  USEPA,  Effluent Guidelines Division  (November 1,
1978) .

35. Hallenbeck, W. H. and Hesse, C. S., "A Review of  the  Health
Effects of Ingested Asbestos," Review of Environmental Health, 2,
3, 157  (1977) .

36. McKee, J. E. and Wolf, H. W.  (eds), Water  Quality  Criteria,
2d  edition,  California  State  Water  Resources  Control Board,
(1963)  citing The Merck  Index,  7th  ed.,  Merck  &  Co.,  Inc.,
Rahway, NJ  (1960).

37. 	 citing Pomelee, C. S., "Toxicity of Beryllium,"  Sewage
& Industrial Wastes 25, 1424  (1953).

38. 	 citing Rothstein, "Toxicology  of  the  Minor  Metals,"
University of Rochester, AEC Project, UR-262  (June 5, 1953).

39. 	 citing Truhout, R. and Boudene, C., "Enquiries into the
Fats of  Cadmium  in  the  Body  During  Poisoning:   Of  Special
Interest to Industrial Medicine," Archiv. Hig. Roda 5, 19  (1954);
AMA Archives of Industrial Health 11, 179  (February,  1955).

40. 	 citing Fairhall, L. T., "Toxic Contaminants of Drinking
Water," Journal New England  Water  Works  Association,  55,  400
(1941) .

41. 	 citing Ohio River Valley Water  Sanitation  Commission,
"Report  on   the  Physiological  Effects  of  Copper  on Man," The
Fettering  Laboratory,  College  of   Medicine,   University   of
Cincinnati, Cincinnati, OH  (January 28, 1953).

42. 	  citing  "Copper  and  the  Human  Organism,"   Journal
American Water Works Association, 21, 262  (1929).

43. 	 citing Taylor, E. W., "The  Examination  of  Waters  and
Water  Supplies," P. Blakiston's Son and Co.  (1949).

44. 	 citing "Water Quality and   Treatment,"  2nd ed.,  AWWA
(1950) .

45. 	 citing Hale, F. E., "Relation of Copper and Brass  Pipe
to Health," Water Works Eng., 95, 240, 84, 139,  187  (1942).

46. 	 citing  "Drinking Water Standards," Title   42  -  Public
Health;  Chapter 1 - Public  Health Service, Department of  Health,
                                 608
-------
Education, and Welfare; Part 72 - Interstate  Quarantine  Federal
Register 2152  (March 6, 1962).

HI. 	 citing Derby, R.  L.,  Hopkins,  0.  C.,  Gullans,   0.,
Baylis,  J.  R.,  Bean,  E.  L.,  and  Malony, P., "Water Quality
Standards," Journal American water Works  Association,  52,   1159
(September, 1960).

48. McKee, J. E. and Wolf, H. W.,  (eds.) , Water Quality Criteria,
2d edition,  California  state  Water  Resources  Control  Board,
(1963)  citing  Klein,  L., "Aspects of River Pollution," Butter-
worth Scientific Publications, London and Academic  Press,  Inc.,
New York  (1957) .

49. 	 citing Fuchess,  H., Bruns, H., and Haupt,  H.,  "Danger
of   Lead   Poisoning  From  Water  Supplies,"  Theo.  Steinkopff
(Dresden)   (1938); Journal  American Water Works  Association,   30,
1125  (1938).

50. 	 citing "Ohio River Valley Water Sanitation  Commission,
Subcommittee  on  Toxicities,  Metal  Finishing Industries Action
Committee," Report No. 3  (1950).

51. 	 Pickering, Q. H. and Henderson, C., "The Acute Toxicity
of Some Heavy Metals to Different Species of Warm Water  Fishes,"
Intnat. J. Air-Water Pollution, 10:453-463  (1966).

52. 	 Murdock, H. R.   Industrial  Wastes,"  Ind.  Eng.  Chem.
45:99A-102A  (1953).

53. 	 Calabrese, A., et. al., "The Toxicity of  Heavy  Metals
of  Embryos  of  the  American  Oyster,  Crassostrea Virginicia,"
Marine Biology 38:162-166  (1973).

54.	  citing  Russell,  F.   C.,   "iMinerals   in   Pasture,
Deficiencies and Excesses  in Relation to Animal Health," Imperial
Bureau   of   Animal   Nutrition,   Aberdeen,   Scotland,   Tech.
Communication 15  (1944).

55. 	 citing Hurd-Kaner, A., "Selenium Absorption  by  Plants
and  their Resulting Toxicity to Animals," Smithsonian Inst.  Ann.
Rept., p. 289  (1934-35).

56. 	 citing Byers, H. G., "Selenium Occurrence  in  Certain
Soils  in the United States with a Discussion of Related Topics,"
U.S. Department of Agr. Tech. Bull. No. 582  (August, 1935).

57. 	 citing Fairhall, L. T., "Toxic Contaminants of Drinking
Water," Journal New England  Water  Works  Association,  55,   400
(1941) .
                                 609
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58. 	 citing Smith, M. I., Franke, K. W.,  and  Westfall,  B.
B.,   "Survey   to   Determine   the   Possibility   of  Selenium
Irvtoxification in the Rural  Population  Living  on  Seleniferous
Soil," Public Health P.epts. 51, 1496  (1936).

59. 	 citing Kehoe, R. A., Cholak, J., and  Largent,  E.  J.,
"The  Hygienic  Significance  of  the Contamination of Water with
Certain  Mineral  Constituents,"  Journal  American  Water  Works
Association, 36, 645  (1944).

60. 	 citing  Schwarz,  K.,  "Effects  of  Trace  Amounts  of
Selenium,"   Proc.  Conf.  Physiol.  Effects  of  Water  Quality,
U.S. P.H.S., p. 79  (September, 1960).

61. 	 Water Quality Criteria of 1972.  NAS Report.

62. 	 US Department  of  Agriculture,  Agricultural  Research
Science,  Consumer  and  Food  Economics Research Division, "Food
Consumption of Households in the United States,"  (Spring,  1965) ,
Preliminary  Report,  Agricultural  Research Service, Washington,
D.C.

63. Hill, W. R. and Pillsburg, D. M.,  "Argyria  Investigation
Toxicity   Properties   of  Silver,"  American  Silver  Producers
Research Project Report, Appendix II.

64. 	 citing Brown, A.W.A., "Insect  Control  by  Chemicals,"
John Wiley and Sons  (1951) .

65. 	 Lougis, P.,  "The  Physiological  Effects  of  Zinc   in
Seawater," Comptes Rendu, Paris, 253:740-741  (1961).

66.	Wisely, B. and  Blick,  R.  A.,  "Mortality  of  Marine
Invertebrate Larvae in Mercury, Copper and Zinc Solutions," Aust.
J.  of Mar. Fresh. Res., 18:63-72  (1967).

67. 	 Clarke, G. L.f "Poisoning and Recovery in Barnacles and
Mussels," Biol. Bull., 93:73-91  (1947).

68. Foreman, C. T., "Food Safety and the Consumer," EPA Jour.   4,
10, 16  (November/December, 1978).

69. Marnahan,  S. E., Environmental  Chemistry,  2d  ed.,  Willard
Grant Press, Boston  (1975) .

70. Methods   for  Chemical  Analysis   of   Water   and   Wastes,
Environmental  Monitoring  and  Support Laboratory, EPA-625/6-74-
003a USEPA, Cincinnati, OH  (1976).
                                 610
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71. Krockta, H. and Lucas, R. L., "Information Required  for  the
Selection  and  Performance Evaluation of Wet Scrubbers," Journal
Air Pollution Control Association, 22, 6, 459.

72. Pourbaix, M., Atlas of Electrochemical Equilibria in  Aqueous
Solutions,  Pergamon  Press, New York  (1966)  cited in Development
Document for Interim Final Effluent  Limitations  Guidelines  and
Proposed  New Source Performance Standards for the Primary Copper
Smelting Subcategory and  Primary  Copper  Refining  Subcategory,
EPA-440/1-75/032b,  Environmental  Protection  Agency   (February,
1975).

73. Draft   Development   Document   for   Effluent   Limitations
Guidelines   and   New   Source  Performance  Standards  for  the
Miscellaneous  Nonferrous   Metals   Segment,   EPA-440/1-76/067,
Environmental  Protection  Agency  (March, 1977) citing Miller, D.
G., "Fluoride Precipitation in Metal Finishing  Waste  Effluent,"
Water-1974:I.   Industrial Waste Treatment, American Institute of
Chemical Engineers Symposium Series, 70, 144  (1974).

74. Parker  &  Fong,  "Fluoride  Removal:   Technology  and  Cost
Estimates," Industrial Wastes  (November/December, 1975).

75. Rohrer,   L.,   "Lime,   Calcium   Chloride   Beat   Fluoride
Wastewater," Water and Wastes Engineering  (November, 1974), p. 66
cited  in  Draft  Development  Document  for Effluent Limitations
Guidelines  and  New  Source  Performance   Standards   for   the
Miscellaneous   Nonferrous   Metals   Segment,  EPA-440/1-76/067,
Environmental Protection Agency (March, 1977).

76. Zabben, W. and Jewett, H.  W.,  "The  Treatment  of  Fluoride
Wastes,"  Proceedings of 22nd Industrial Waste Conference, Purdue
University  (May 2-4, 1967), pp. 706-716.

77. Manual  of  Treatment  Techniques  for  Meeting  the  Interim
Primary    Drinking    Water    Regulations,     EPA-600/8-77-005,
Environmental Protection Agency (April, 1978).

78. Patterson, J. W., "Technology  and  Economics  of  Industrial
pollution  Abatement,"   IIEQ  Document  f76/22  Project f20.070A
(1976) .

79. Maruyama, T., Hannah, S. A., and Cohen, J. M., "Metal Removal
by Chemical Treatment Processes," Journal Water Pollution control
Federation, 47, 5, 962.

80. Gulp,  G.  L.  and  Gulp,  R.  L.,  New  Concepts  In   Water
Purification,   (Van  Nostrand,  Reinhold  and  Company,  New York
(1974) , pp. 222-224.
                               611
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81. Jenkins, S. N., Knight, D. G., and  Humphreys,  R.  E.,  "The
Solubility of Heavy Metal Hydroxides in Water, Sewage, and Sewage
Sludge,   I.    The   Solubility   of   Some  Metal  Hydroxides,"
International Journal of Air and Water Pollution, 8, 537  (1964).

82. Sittig, M., Pollutant Removal Handbook.   Noyes  Data  Corp.,
Park Ridge, NJ (1973).

83. Link, W. E.  and  Rabosky,  J.  G.,  "Fluoride  Removal  from
Wastewater   Employing   Calcium   Precipitation  and  Iron  Salt
Coagulation,"  Proceedings   of   the   31st   Industrial   Waste
Conference, Purdue University, pp. 485-500  (1976).

84. Beychak,  M.  R.,   Aqueous   Wastes   from   Petroleum   and
Petrochemical  Plants,  John Wiley and Sons  (1967) cited in Draft
Development Document for Effluent Limitations Guidelines and  New
Source  Performance  Standards  for  the Miscellaneous Nonferrous
Metals Segment, EPA-440/1-76/067, Environmental Protection Agency
(March, 1977).

85. "Stripping, Extraction, Adsorption, and Ion Exchange," Manual
on  Disposal  of  Refinery  Wastes  -  Liquid  Wastes,   American
Petroleum  Institute,  Washington,  D.C.   (1973)  cited  by Draft
Development Document for Effluent Limitations Guidelines and  New
Source  Performance  Standards  for  the Miscellaneous Nonferrous
Metals Segment, EPA-440/1-76/067, Environmental Protection Agency
(March, 1977).

86. Grantz, R. G., "Stripper Performance Tied to  NH3  Fixation,"
Oil and Gas Journal, 73, 24, 80  (1975) cited by Draft Development
Document  for  Effluent  Limitations  Guidelines  and  New Source
Performance Standards for  the  Miscellaneous  Nonferrous  Metals
Segment,   EPA-440/1-76/067,   Environmental   Protection  Agency
(March, 1977).

87. Wrek, W. J. and Snow, R. H., "Design of  Cross  Flow  Cooling
Towers  and  Ammonia  Stripping  Towers,"  Industrial Engineering
Process Design Development, 11, 3  (1972) cited by Draft  Develop-
ment  Document for Effluent.Limitations Guidelines and New Source
Performance Standards for the Miscellaneous Metals Segment,  EPA-
440/1-76/067, Environmental Protection Agency  (March, 1977).

88. Mioderszewski, D., "Ammonia Removal -  What's  Best," Water  and
Wastes  Engineering   (July,   1975)  cited  by  Draft  Development
Document  for  Effluent  Limitations  Guidelines  and  New Source
Performance Standards for the Miscellaneous Metals Segment,  EPA-
440/1-76/067, Environmental Protection Agency  (March, 1977) .

89. Schlauch, R.  M., and  Epstein,  A.  C.,  Treatment  of  Metal
Finishing Wastes  by Sulfide Precipitation,  EPA  600/2-77-049.
                               612
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90. Coleman, R. T., Colley, D. J., Klausmeier, R. F., Malish,  D.
A.,  Meserole,  N.  P.,  Micheletti, W. C., and Schwitzgebel, K. ,
Draft Copy Treatment Methods  for  Acidic  Wastewater  Containing
Potentially  Toxic Metal Compounds, Report by Radian Corporation,
Austin, TX, submitted to USEPA Industrial Environmental  Research
Laboratory, Cincinnati, OH  (1978).

91. Bettler,  C.  R.,   "Lime   Neutralization   of   Low-Acidity
Wastewater,"  Proceedings  of  32nd  Industrial Waste Conference,
Purdue University  (1977), p. 830.

92. Permutit Co., Inc., Proceedings of  seminar  on  metal  waste
treatment featuring the Sulfex process, Paramus, NJ, undated.

93. Larson, H. P., Shou, K. P., Ross, L. W., "Chemical  Treatment
of  Metal Bearing Mine Drainage," Journal Water Pollution Control
Federation, 45, 8, 1682  (197U) cited by Coleman, R. T.,  et  al.,
Draft  Copy  Treatment  Methods  for Acidic Wastewater Containing
Potentially Toxic Metal Compounds, Report by Radian  Corporation,
Austin,  TX, submitted to USEPA Industrial Environmental Research
Laboratory, Cincinnati, OH  (1978).

94. Murao, K. and Sei, N.f "Recovery of  Heavy  Metals  from  the
Wastewater of Sulfuric Acid Process in Ahio Smelter," Proceedings
of  Joint  MMIJ  AIME  Meeting  on World Mining and Metallurgical
Technology, Denver, September, 1976, Volume 2, pp. 808-16   (1976)
cited by Coleman, R. T., et al.. Draft Copy Treatment Methods for
Acidic  Wastewater  Containing Potentially Toxic 4etal Compounds,
Report by Radian Corporation,  Austin,  TX,  submitted  to  USEPA
Industrial  Environmental  Research  Laboratory,  Cincinnati,  OH
(1978) .

95. LaPerle, P. L., "Removal of Metals from Photographic Effluent
by Sodium Sulfide Precipitation," Journal Appl. Photogr. Eng.  2,
13U,  (1976) cited by Coleman, R. T., et al., Draft Copy Treatment
Methods  for Acidic Wastewater Containing Potentially Toxic Metal
Compounds, Report by Radian Corporation, Austin, TX, submitted to
USEPA Industrial Environmental Research  Laboratory,  Cincinnati,
OH  (1978).

96. Scott, M.  (Senior Marketing  Specialist,  Permutit  Company),
Private  communication  with R. Klausmeier  (November, 1977) cited
by Coleman, R. T., et. al..  Draft  Copy  Treatment  Methods  for
Acidic  Wastewater  Containing Potentially Toxic Metal Compounds,
Report by Radian Corporation,  Austin,  TX,  submitted  to  USEPA
Industrial  Environmental  Research  Laboratory,  Cincinnati,  OH
(1978) .

97. Development Document for Interim Final and Proposed  Effluent
Limitations  Guidelines  and New Source Performance Standards for
                                  613
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the  Ore  Mining   and   Dressing   Industry,   EPA-440/1-75-061,
Environmental  Protection  Agency  (1975) cited by Coleman, R. T.,
et al.,  Draft  Copy  Treatment  Methods  for  Acidic  Wastewater
Containing  Potentially  Toxic  Metal Compounds, Report by Radian
Corporation, Austin, TX, submitted to USEPA  Industrial  Environ-
mental Research Laboratory, Cincinnati, OH (1978).

98. Coleman, R. T. and Malish, D. A., Trip Report to Paul  Bergoe
and son, Eoliden Aktiebolag and Outokumpu as part of EPA Contract
68-02-2608,   Radian   Corporation   (November,  1977),  cited  by
Coleman, R. T., et al., Draft Copy Treatment Methods  for  Acidic
Wastewater  Containing  Potentially Toxic Metal Compounds, Report
by Radian Corporation, Austin, TX, submitted to USEPA  Industrial
Environmental Research Laboratory, Cincinnati, OH  (1978).

99. Maltson, M. E., "Membrane Desalting Gets Big Push,"  Water  &
Wastes Engineering  (April, 1975), p. 35.

100.  Cruver, J. E., "Reverse  Osmosis  For  Water  Reuse,"  Gulf
Environmental System  (June, 1973).

101.  	 "Water Renovation of Municipal Effluents  by  Reverse
Osmosis," Gulf Oil Corporation, San Diego  (February, 1972).

102.  Spatz, D. D., "Methods of Water Purification," Presented to
the American Association of Nephrology Nurses and Technicians  at
the  ASA10  AANNT  Joint  Conference, Seattle, Washington  (April,
1972).

103.  Donnelly, R. G., Goldsmith, R. L., McNulty, K.  J.,  Grant,
D. C., and Tan, M., Treatment of Electroplating Wastes by Reverse
Osmosis,   EPA-600/2-76-261,   Environmental   Protection  Agency
 (September, 1976).

104.  Rook,  J.  J.,  "flaloforms  in  Drinking  Water,"   Journal
American Water Works Association, 68:3:168 (1976).

105.  Rook, J. J.,  "Formation of Haloforms During Chlorination of
Natural Waters,"   Journal  Water  Treatment  Examination,  23:234
 (1974) .

106.  Trussell, R. R. and  Umphres,  M.  D.,  "The  Formation  of
Trihalomethanes,"   Journal  American  Water  Works  Association,
70:11:604  (1978).

107.  Nebel, C., Goltschling, R. D., Holmes, J.  L.,  and  Unangst,
P.  C.,  "Ozone  Oxidation of Phenolic  Effluents," Proceedings of
the 31st Industrial Waste Conference, Purdue  University   (1976),
pp. 940-951.
                                 614
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108.  Rosen, H. M., "Wastewater Ozonation: a Process  Whose  Time
Has Come," Civil Engineering, 47, 11, 65  (1976).

109.  Hardisty, D. M. and Rosen, H.  M.,  "Industrial  Wastewater
Ozonation,"  Proceedings  of the 32nd Industrial Waste Conference
Purdue University  (1976), pp. 9/40-951.

110.  Traces of Heavy  Metals  in  Water  Removal  Processes  and
Monitoring,  EPA-902/9-74-D01,  Environmental  Protection  Agency
(November, 1973).

111.  Symons, J. M., "Interim  Treatment  Guide  for  Controlling
Organic  Contaminants  in Drinking Water Using Granular Activated
Carbon," Water Supply Research Division, Municipal  Environmental
Research  Laboratory,  Office of Research and Development, USEPA,
Cincinnati, OH  (January, 1978).

112.  McCreary, J. J. and V.  L.  Snoeyink,  "Granular  Activated
Carbon   in   Water  Treatment,"  Journal  American  Water  Works
Association, 69, 8, 437  (1977).

113.  Grieves, C. G. and  Stevenson,  M.  K.,  "Activated  Carbon
Improves  Effluent,"  Industrial  Wastes  (July/August, 1977), pp.
30-35.

114.  Beebe, R. L. and Stevens, J. I., "Activated  Carbon  System
for   Wastewater   Renovation,"   Water  and  Wastes  Engineering
(January, 1967), pp. 43-45.

115.  Gulp, G. L. and Shuckrow, A. J., "What lies ahead for PAC,"
Water and Wastes Engineering  (February, 1977), pp. 67-72, 74.

116.  Savinelli, E. A. and Black, A. P., "Defluoridation of Water
with   Activated   Alumina,"   Journal   American   Water   Works
Association, 50, 1, 33  (1958).

117.  Paulson,  E.   G.,   "Reducing   Fluoride   in   Industrial
Wastewater,"  Chemical  Engineering,  Deskbook Issue  (October 17,
1977) .

118.  Bishop, P. L. and  Sansovey,  G.,  "Fluoride  Removal  from
Drinking   Water  by  Fluidized  Activated  Alumina  Adsorption,"
Journal American Water Works Association, 70, 10, 554  (1978).

119.  Harmon, J. A. and  Kalichman,  S.  G.,  "Defluoridation  of
Drinking  Water  in  Southern California," Journal American Water
Works Association, 57:2:245  (1965).

120.  Maier, F. J., "Partial  Defluoridation  of  Water,"  Public
Works, 91:90  (1960).
                                  615
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121.   Bellack, E.f "Arsenic Removal From Potable Water,"  Journal
American Water Works Association, 63, 7  (1971) .

122.   Gupta,  S.  K.  and  Chen,  K.  Y. ,  "Arsenic  Removal   by
Adsorption,"  Journal Water Pollution Control Association  (March,
1978), pp. 493-506.

123.   Johnson, D. E. L., "Reverse Osmosis  Recycling  System  for
Government  Arsenal," American Metal Market  (July 31, 1973) cited
in Draft Development Document for Effluent Limitations Guidelines
and  New  Source  Performance  Standards  for  the  Miscellaneous
Nonferrous   Metals   Segment,   EPA- 440/1-76/067,  Environmental
Protection Agency  (March, 1977) .

124.   Nachod, F. C. and Schubert, J.,  Ion   Exchange  Technology,
Academic Press, Inc. (1956).

125.   Volkert,  David,   and   Associates,    "Monograph   on   the
Effectiveness  and  Cost  of  Water  Treatment  Processes for the
Removal of Specific Contaminants," EPA 68-01-1833, Office of  Air
and Water (1974) cited by Contaminants Associated with Direct and
Indirect  Reuse of Municipal Wastewater, EPA- 6 00/1- 7 8- 01 9  (March,
126.  Clark, J. W. , Viessman, W. ,  Jr.,  and  Hammer,  M.,  Water
Supply and Pollution Control,  (3rd ed. ) IEP, New York  (1977) .

127.  AWARE  (Associated Water and Air Resources Engineers, Inc.) ,
"Analysis of National Industrial Water Pollution Control  Costs,"
(May 21, 1973) .

128.  AWARE, "Alternatives for Managing Wastewater in  the  Three
Fivers Watershed Area,"  (October, 1972).

129.  Bechtel,  "A  Guide  to  the  Selection  of  Cost-Ef fective
Wastewater Treatment Systems," EPA/430/9-75-002  (July, 1975) .

130.  Smith, P.., "Cost of Conventional and Advanced Treatment   of
Wastewater,"   Journal  Water Pollution Control Federation, 40,  9,
1546  (1968) .

131.  Icarus,  "Capital and Operating Costs of  Pollution  Control
Equipment Modules," Vol. I & II, EPA-R5-73-023a & b  (July, 1973).

132.  Monti, R. P.  and  Silberman,  P.  T.,  "Wastewater  System
Alternatives:  What  Are They... And What Cost011  Water And Waste
Engineering  (May, 1974), p. 40.

133.  Process  Design Manual for Removal of Suspended Solids, EPA-
625/175-003a  (January, 1975).
                                  616
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134.  Process Design Manual For Carbon Adsorption, EPA  625/1-71-
002a (October, 1973) .

135.  Grits,  G.  J.,  "Economic  Factors  in  Water  Treatment,"
Industrial Water Engineering  (November, 1971), p. 22.

136.  Barnard, J. L. and Eckenfelder, W. W., Jr., "Treatment Cost
Relationships for Industrial Waste  Treatment,"  Environmental   &
Water Resources Engineering, Vanderbilt University  (1971).

137.  Grits, G. J.  and  Glover,  G.  G.,  "Cooling  Slowdown  in
Cooling Towers," Water & Wastes Engineering  (April, 1975), p. 45.

138.  Kremen,  S.  S.,  "The  True  Cost  of  Reverse   Osmosis,"
Industrial Wastes (November/December, 1973), p. 24.

139.  Cruver, J. E.  and Sleigh, J. H.,  "Reverse  osmosis  -  The
Emerging  Answer  to  Seawater  Desalination,"  Industrial  Water
Engineering  (June/July, 1976), p. 9.

140.  Doud, D. H., "Field Experience with  Five  Reverse  osmosis
Plants," Water and Sewage Works  (June, 1976)  , p. 96.

141.  Lacey, R. E. and Loed, S.,  (eds.),  "Industrial  Processing
with  Membranes,"  in  The  Cost of Reverse Osmosis, John Wiley  &
Sons (1972) .

142.  Disposal of Brines Produced  in  Renovation  of  Industrial
Wastewater, FWQA Contract f!4-12-492  (May, 1970).

143.  Process Design Manual for Sludge  Treatment  and  Disposal,
EPA 625/1-74-006  (October, 1974).

144.  Black & Veatch, "Estimating Cost and Manpower  Requirements
for  Conventional  Wastewater Treatment Facilities," EPA Contract
#14-12-462  (October, 1971).

145.  Osmonics,  Inc.,  "Reverse  Osmosis   and   Ultrafiltration
Systems Bulletin No. G7606,"  (1978).

146.  Buckley, J. D., "Reverse Osmosis;  Moving  from  Theory  to
Practice,"  From  Fluid  Systems  Div.,  UOP,  Inc. (Reprint from
Consulting Engineer) , 45, 5, 55  (1975) .

147.  Process Design Manual for Nitrogen Control,  EPA-Technology
Transfer  (October, 1975) .

148.  Rizzo £  Shepherd,  "Treating  Industrial  Wastewater  with
Activated Carbon," Chemical Engineering (January 3, 1977).
                                617
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149.  Richardson,  "1978-79  Process   Equipment,   Vol.   4   of
Richardson Rapid System."

150.  Thiansky, D. P., "Historical Development of Water Pollution
Control  Cost  Functions,"  Journal   Water   Pollution   Control
Federation, 46, 5, 813  (1974).

151.  Zimmerman, O. T., "Wastewater Treatment," Cost  Engineering
(October, 1971), p. 11.

152.  Watson,  I.  C.,   (Control  Research  Inc.)   "Manual    for
Calculation  of  Conventional  Water  Treatment Costs," Office of
Saline Water (March, 1972).

153.  Gulp, R. L., Wesner,  G.  M.,  Gulp,  G.  L.,  Handbook  of
Advanced Wastewater Treatment, McGraw-Hill  (1978).

154.  Dynatech R/D Company, A Survey  of  Alternate  Methods   for
Cooling  Condenser  Discharge  Water  Large-Scale  Heat Rejection
Equipment, EPA Project No. 16130 DHS  (July, 1969).

155.  Development    Document    For...Steam    Electric    Power
Generating," EPA 440/1-73/029  (March, 1974).

156.  "Cooling  Towers  -  Special  Report,"   Industrial   Water
Engineering  (May, 1970).

157.  AFL Industries, Inc., "Product Bulletin #12-05.Bl   (Shelter
Houses) , Chicago, IL  (December 29, 1977) .

158.  Fisher Scientific Co., Catalog 77  (1977).

159.  Isco,  Inc.,  Purchase  Order  Form,  Wastewater   Samplers
(1977) .

160.  Dames &  Moore, Construction Costs  for Municipal  Wastewater
Treatment  Plants:  1973-1977, EPA-430/9-77-013,  MCD-37  (January,
1978).

161.  Metcalf  & Eddy, Inc., Wastewater Engineering:   Collection,
Treatment, Disposal, McGraw-Hill, New York  (1972) .

162.  Obert, E. F. and  Young, R. L., Elements  of Thermodynamics
and Heat Transfer, McGraw-Hill  (1962), p.  270.

163.  Paulson, E.  G.,   "How  to  Get  Rid  of   Toxic  Organics,"
Chemical  Engineering,  Deskbook Issue  (October 17, 1977) ,  pp.  21-
27.
                                 618
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164.  CH2-M-H111, "Estimating Staffing for  Municipal  Wastewater
Treatment Facilities," EPA #68-01-0328 (March, 1973).

165.  "EPA Indexes Reflect Easing Costs," Engineering News Record
(December 23, 1976), p 87.

166.  Chemical Marketing Reporter, Vol. 210,  10-26   (December   6
and December 20, 1976) .

167.  Smith, J. E., "Inventory of Energy Use in Wastewater Sludge
Treatment   and   Disposal,"   Industrial    Water    Engineering
(July/August, 1977).

168.  Jones, J. L., Bomterger, D. C.,  Jr.,  and  Lewis,  F.  M.,
"Energy  Usage  and  Recovery  in  Sludge Disposal, Parts 1 8 2,"
Water and Sewage Works (July and August, 1977), pp. 44-47 and 42-
46.

169.  Hagen, R. M. and Roberts, E. B., "Energy  Requirements  for
Wastewater  Treatment, Part 2," Water and Sewage Works  (December,
1976), p. 52.

170.  Banersi, S. K. and O'Conner, J. T., "Designing More  Energy
Efficient   Wastewater   Treatment   Plants,"  Civil  Engineering
(September, 1977), p. 76.

171.  "Electrical  Power  Consumption  For  Municipal  Wastewater
Treatment," EPA-R2-73-281  (1973).

172.  Hillmer, T. J., Jr., "Economics of Transporting  Wastewater
Sludge," Public Works  (September, 1977), p. 110.

173.  Ettlich, W. F., "Economics of Transport Methods of Sludge,"
Proceedings  of  the  Third   National   Conference   on   sludge
Management,  Disposal and Utilization  (December 14-16, 1976), pp.
7-14.

174.  NUS/Rice  Laboratory,  "Sampling  Prices,"  Pittsburgh,  PA
(1978) .

175.  WARF  Instruments,  Inc.,  "Pricing  Lists  and  Policies,"
Madison, WI  (June 15, 1973).

176.  Orlando  Laboratories,  Inc.,  "Service  Brochure  and  Fee
Schedule f!6," Orlando, FL  (January 1, 1978) .

177.  st.  Louis  Testing  Laboratory,  "Water   and   Wastewater
Analysis - Fee Schedule," St. Louis, MO  (August, 1976).
                                 619
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178.  Ecology Audits, Inc.,  "Laboratory  Services  -  Individual
Component Analysis," Dallas, TX  (August, 1976) .

179.  Laclede  Gas  Company,   (Lab  Div.),  "Laboratory   Pricing
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