EPA-R2-73-108
FEBRUARY 1973            Environmental  Protection Technology Series
            Treatment of  Laundromat Wastes

                                       Office of Research and Monitoring

                                       U.S. Environmental Protection Agency

                                       Washington, DC  20460

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            RESEARCH REPORTING SERIES
Research reports of the  Office  of  Research  and
Monitoring,  Environmental Protection Agency, have
been grouped into five series.  These  five  broad
categories  were established to facilitate further
development  and  application   of   environmental
technology.   Elimination  of traditional grouping
was  consciously  planned  to  foster   technology
transfer   and  a  maximum  interface  in  related
fields.  The five series are;

   1.  Environmental Health Effects Research
   2.  Environmental Protection Technology
   3.  Ecological Research
   H.  Environmental Monitoring
   5.  Socioeconomic Environmental Studies

This report has been assigned to the ENVIRONMENTAL
PROTECTION   TECHNOLOGY   series.    This   series
describes   research   performed  to  develop  and
demonstrate   instrumentation,    equipment    and
methodology  to  repair  or  prevent environmental
degradation from point and  non-point  sources  of
pollution.  This work provides the new or improved
technology  required for the control and treatment
of pollution sources to meet environmental quality
standards.

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                                                     EPA-R2-73-108
                                                     February  1973
            TREATMENT  OF LAUNDROMAT WASTES
                           By

                  Donald B. Aulenbach
                    Patrick C. Town
                    Martha Chilson
                   Project 12120  DOD

                    Project Officer

                    Richard Keppler
            Environmental Protection Agency
                 John  F.  Kennedy  Bldg.
              Boston,  Massachusetts 02203


                     Prepared for

           OFFICE OF RESEARCH AND MONITORING
        U.S.  ENVIRONMENTAL PROTECTION AGENCY
                WASHINGTON, D.C.  20460
For sale by the Superintendent of Documents, U.S. Government Printing Office, Washington, D.C. 20402
             Prloe 95 cents domestic postpaid or 70 cents QPO Bookstore

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                EPA Review Notice

This report has been reviewed by the Environmental
Protection Agency and approved for publication.
Approval does not signify that the contents necessarily
reflect the views and policies of the Environmental
Protection Agency, nor does mention of trade names or
commercial products constitute endorsement or recommenda-
tion for use.
                       ii

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                            ABSTRACT

Laboratory and field studies were conducted to evaluate the capabilities
of two commercially available laundromat waste treatment systems  to
treat laundromat wastes with the possibility of recycling the treated
effluent.  The Winfair Water Reclamation System (WWRS) involves  the
addition of alum to a pH of 4, sedimentation, sand filtration, carbon
absorption, and passage through ion exchange resins.  The American
Laundry Machinery Industries (ALMI) system employs chemical precipita-
tion prior to filtration through Diatomaceous Earth.

The WWRS achieved a 56% BOD reduction, 62% COD reduction, and 94% ABS
reduction, but suffered from a buildup of total solids in the effluent.
The system produced an effluent suitable for discharge into many streams,
For effluent recycling, a functioning demineral!zer would be required.

The ALMI system achieved a 63% BOD reduction, 69% COD reduction,  87%
ABS reduction, 94% PO^ reduction, and complete coliform removal.   The
increase in effluent alkalinity and hardness render very questionable
the suitability of the effluent for reuse without softening and pH
adjustment.  The use of the system would cost about 10C per wash.

This report was submitted in fulfillment of Project Number 12120  DOD
under the (partial) sponsorship of the Water Quality Office, Environ-
mental Protection Agency.
                              111

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                             CONTENTS
Section



  I        Conclusions




  II       Recommendations




  III      Introduction




           Part I




  IV       Basic Laundry Waste Treatment Systems




  V        The Winfair Water Reclamation System




  VI       Laboratory Studies of Detergent Removal




  VII      Treatment System Operation




  VIII     Discussion of the Winfair System




           Part II




  IX       The ALMI Filtration System




  X        Laboratory Analysis




  XI       Discussion of the ALMI System




  XII      Acknowledgements




  XIII     References




  XIV      Glossary
Page




  1




  3




  5









  7




 13




 17




 25




 35









 37




 43




 59




 61




 63




 65

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                             FIGURES


                                                                   PAGE


 1   LAUNDROMAT WASTE DISCHARGE                                      8

 2   RANGE OF LAUNDROMAT WASTE WATER QUALITY                         9

 3   TYPICAL COMPOSITION OF DETERGENTS                              10

 4   WINFAIR WATER RECLAMATION SYSTEM                               14

 5   EFFICIENCY OF ALUM TREATMENT OF LAUNDROMAT WASTES              19
       AT VARIOUS pH VALUES

 6   EFFICIENCY OF VARIOUS ALUM DOSAGES FOR TREATMENT OF            22
       LAUNDROMAT WASTES AT SEVERAL pH VALUES

 7   EFFICIENCY OF VARIOUS ALUM DOSAGES FOR TREATMENT OF            24
       LAUNDROMAT WASTES

 8   SCHEMATIC FLOW DIAGRAM —AMERICAN LAUNDRY MACHINERY            26
       INDUSTRY— DIATOMITE FILTRATION SYSTEM

 9   LAUNDROMAT TREATMENT PLANT                                     27

10   DETERGENT CONCENTRATIONS THRUOUT WINFAIR SYSTEM                28

11   SUMMARY OF TOTAL DISSOLVED SOLIDS IN WINFAIR SYSTEM            33

12   ALMI WASTE WATER TREATMENT SYSTEM                              38

13   SCHEMATIC FLOW DIAGRAM — ALMI -- DIATOMITE FILTRATION         39
       SYSTEM

14   DIATOMITE FILTER FILTRATION CHARACTERISTICS                    42

15   EFFLUENT TURBIDITY vs. pH IN THE ALMI SYSTEM                   47

16   EFFECT OF CaCl  DOSAGE ON TOTAL DISSOLVED SOLIDS IN            51
       EFFLUENT FROM ALMI SYSTEM

17   EFFECT OF pH ON PO^ REMOVAL IN THE ALMI SYSTEM                 53

18   EFFECT OF CaCl  DOSAGE ON P04 REMOVAL IN THE ALMI SYSTEM       54
                                VI

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                              TABLES
 1    Effect of pH on Alum Treatment of Laundromat Wastes             18

 2    Effect of Various Concentrations of Alum at Different pH's      21
        for Treatment of Laundromat Wastes

 3    Effect of a Wide Range of Alum Concentrations for Treatment     23
        of Laundromat Wastes

 4    Summary of ABS Removal in Winfair System                       29

 5    Summary of Overall BOD and COD Removal in the Winfair          31
        Reclamation System

 6    Summary of pH Values in Winfair System                         31

 7    Summary of Total Dissolved Solids in Winfair System             32

 8    American Laundry Machinery Industries Diatomaceous Earth       40
        Filtration System

 9    Summary of ABS Reduction with Various CaCl2 and Roccal         44
        Additions

10    Summary of Removal of Alkyl Benzene Sulfonate in the ALMI      45
        System

11    Summary of Reduction of Biochemical Oxygen Demand in the       45
        ALMI System

12    Summary of Reduction of Chemical Oxygen Demand in the ALMI      46
        System

13    Effluent Turbidity vs. Filter Aid                              48

14    Summary of Changes in the Organic Nitrogen in the ALMI System  50

15    Summary of the Increase in Total Dissolved Solids in the       50
        ALMI System

16    Summary of the Changes in Hardness in the ALMI System          52

17    Summary of PO^ Removal in the ALMI System                      55

18    Summary of the Alkalinity in the Raw and Treated Waste         57

19    Summary of the Acidity in the Raw and Treated Waste             57
                                vii

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                        TABLES (CONT'D.)

No.                                                                 Page_

20   Optimum Combination of Chemical and Mechanical Factors in       58
       Removal of Pollutants and Pathogens from Laundromat Waste
       Water in the ALMI Wastewater Treatment System
                              Vlll

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                            SECTION I

                           CONCLUSIONS

Part I

The Winfair Water Reclamation System was evaluated for its ability to
treat a laundromat waste for possible reuse.  Alum added to achieve a
pH of 4-5 resulted in an effluent containing an average of 11 mg/1 ABS.
This is twice the level recommended for the detergent removal ion ex-
change resin.  This will require replacing the resin twice as often as
specified.

The BOD reduction was in the order of 61%, and the COD reduction 71%.
This may be sufficient for discharge to many streams, and certainly
satisfactory for discharge to a subsurface disposal system.

The demineralizer system was absolutely non-functional.  This will re-
sult in a build-up of'total solids if the effluent is reused.  If the
effluent is to be discharged to waste, the demineralizer system is
not needed.

The system appears to operate satisfactorily without neutralization
before sedimentation.  The average ABS reduction was 94%, having an
average residual of 2.3 mg/1.

With satisfactory operation of a demineralizer system, this effluent
could be reused at least once in a laundromat.  Consideration of the
amount of make-up water to control the build-up of non-removed mater-
ials would have to be made.  The system produces an effluent which
should be suitable for discharge into many streams.

Part II

The American Laundry Machinery Industries (ALMI) Diatomaceous Earth Fil-
tration System can be an effective system for laundromat waste treatment.
Under optimum operating conditions the System can achieve better than
98% ABS reduction, 94% P04 Deduction, 70% BOD reduction, and 84% COD
reduction.  Coliforms can also be effectively removed.

A 98% or better removal of the ABS can be achieved with the addition of
24 mg/1 or greater of Roccal (a combination cationic detergent and germ-
icide).  No apparent relation was observed between calcium chloride
addition and ABS removal, or between chemical addition and BOD or COD
reduction.  In most cases the COD exceeded the BOD.

The total dissolved solids in the effluent was directly related to the
calcium chloride dose added.  Thus to minimuze the increase in total
dissolved solids, a minimum amount of calcium chloride should be used
to effect treatment.  The increase in total organic nitrogen due to
treatment was not significant.

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The turbidity of the effluent was directly related to the pH.   At pH
values above 8 with the addition of NaOH the transmittance was always
greater than 95%.  The transmittance dropped off sharply at pH values
below 7.

There was a general slight reduction in the hardness due to the treat-
ment; however, there are insufficient data to achieve a statistical
significance to this conclusion.  Several data suggest that an excess
of CaCl2 increases the hardness in the effluent.

Increased CaCl2 dosage can result in an increased removal of phosphate.
However, more significantly an increase in pH results in a marked in-
crease in phosphate reduction with lower CaCl2 dosages.  Pre-treatment
with alum followed by settling in the Winfair Water Reclamation System
(WWRS) prior to treatment in the ALMI system resulted in a high phos-
phate removal at a low CaCl2 dose.

The ALMI System meets most of the requirements for treatment of wastes
from coin-operated laundromats.  The introduction of this system into
existent laundromats would increase the cost of washes by about 10t.

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                           SECTION II

                         RECOMMENDATIONS

Individual recommendations must be made on the basis of specific  exist-
ing and potential uses of these treatment systems.

1.  Treatment of laundromat wastes for discharge into the ground  or to
a surface water.

Either system could be used for this degree of treatment.  The ALMI
system is recommended due to ease of operation and  greater reliability.
Additional studies could be made into the reason for the failure  of
the demineralizer system in the WWRS.

2.  Reuse of the treated effluent in the laundromat.

The WWRS was designed for reuse, whereas the ALMI system was not.  Due
to the malfunction of the demineralizer system of the Winfair Water
Reclamation System (WWRS), the effluent from this system cannot be rec-
ommended for continuous reuse.  Due to adverse conditions during  opera-
tion of the American Laundry Machinery Industries (ALMI) system,  no
determination of the buildup in total solids could be made.  In order
to determine potential reuse, it is recommended that additional studies
be made at a location where at least partial reuse of the effluent could
be practiced.

3.  Potential for phosphate removal.
In view of the use of alum in the WWRS and of calcium and potentially
ferric chloride or alum in the ALMI system, both these systems have a
potential for use in phosphate removal.  It is recommended that addi-
tional studies be made of the use of these treatment systems for  phos-
phate removal.  (Note:  This recommendation has already been carried
out as reported in a paper entitled "Phosphate Removal From Laundry
Waste Water" presented at the winter meeting of the New York Water
Pollution Control Association in New York, January 26, 1972.)

4.  Application to treatment of other types of liquid wastes.
Since both treatment systems have been shown to be  reasonably effective
in treating laundry wastes, they should also be effective in treating
normal domestic sewage, especially for phosphate removal.  The systems
used in these studies could be used for small housing developments or
shopping centers.  The principles could be expanded to serve larger
facilities.  It is, therefore, recommended that studies be made to
determine the applicability of these systems to treat domestic sewage,
particularly for phosphate removal.

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                           SECTION III

                          INTRODUCTION

There are many diverse types of wastes which produce problems today.
One of these is the wastes from coin-operated laundromats, particularly
those located in areas where sewer systems are not accessible.  Numer-
ous treatment systems have been devised for treating these wastes.  Two
such systems became available and formed the conception of this study.
It is the purpose of this study to evaluate these two systems for the
treatment of laundromat wastes.

The post-World War II era gave rise to three developments which compli-
cated the laundry waste problem.  First, was the mass production of
automatic home laundry equipment.  Second, the building boom in suburban
areas placed much of this equipment in unsewered areas.  Finally, the
appearance of coin-operated laundromats in these new suburban centers
meant that millions of gallons of detergent, germ, and soil-laden waste
water was being discharged into streams, estuaries, ponds and ground-
water supplies.

Since most of the early laundry detergents were not biodegradable, con-
ventional septic tank systems were ineffective in treating these wastes.
With the advent of biodegradable laundry detergents, some of the prob-
lems were ameliorated, but only if the coin-operated laundromats were
located in areas where there was a sufficient quantity of suitable land
for the construction of leaching fields.  This was seldom the case since
most of these installations were in densely populated new suburbs "where
land was at a premium.  Therefore, waste treatment facilities for coin-
operated laundromats in unsewered areas had to fulfill the following
requirements:
   1) provide an effluent acceptable to health regulations

   2) handle peak loads as well as normal demands
   3) require a minimum of service and operational maintenance skills
      and time
   4) be able to be easily dismantled, transported and reassembled
      at a new site
   5) occupy a minimum of space
   6) be economically feasible  in terms of cost per load  of wash, and

   7) whenever possible, recycle the water for further use.

The first part of this report evaluates the Winfair Wastewater Reclama-
tion System  (WWRS) which claims to fulfill all of  the above requirements

This second  part of the report  describes  the operation of the American
Laundry Machinery Industries  (ALMI) wastewater treatment  system,  which
claims to fulfill all but the recycle  requirement  of laundromat  waste
treatment system in unsewered areas, and  evaluates the actual function
of that system.

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                           SECTION IV

              BASIC LAUNDRY WASTE TREATMENT SYSTEMS

Wastes from both individual home laundries and multiple-unit coin-oper-
ated laundromats can present problems where they cannot be discharged
into sewerage systems provided with adequate treatment facilities.   The
spread of population into unsewered areas is followed by the establish-
ment of coin-operated laundromats in these unsewered areas.   An indica-
tion of the magnitude of the problem may be given by the estimate  that
there are over 120 laundromats in Suffolk County, Long Island,  New  York,
alone^^).  A summary of the amounts of wastes produced is shown in  Fig.
1  and representative quality parameters are shown in Fig. 2.  Nearly
all of these ultimately discharge their effluent into the ground.   The
switch to the use of synthetic detergents (syndets) has also contributed
considerably to the problem.  The conversion to linear alkyl benzene
sulfonates (LAS) (Fig. 3) has reduced this problem where aerobic biolog-
ical treatment is provided.  However, under anaerobic conditions,  such
as in septic tanks and saturated soil, there is little breakdown of the
LAS.  In saturated soils, these syndets may travel considerable distances
without being decomposed, thereby entering water supplies.  In  addition,
studies on Long Island'"^ have shown that the synthetic detergents  seem
to cause other pollutional material, specifically coliforms, to be  car-
ried greater distances than conventional soaps do.  This is in  partial
disagreement with work done by Robeck, et al.    who showed that in-
creased concentrations of ABS had no effect upon the travel distance of
coliforms in water-saturated, sandy soils under laboratory conditions.

The problems created by laundromat wastes have led to many studies  of
methods for treatment, and to the creation of numerous waste treatment
systems.  A large volume of work was done at Manhattan College  for  the
State of New York^5^.  Work was done to determine the amount of alum
needed to improve the quality of the waste (with no consideration  of
ABS removal), and further, the amount of powdered activated carbon
needed to remove the ABS.  An alum dose of 100 grains/gallon (1700  mg/l)
and an activated carbon concentration 7 times the ABS concentration are
recommended to remove substantially all anionic syndets.  Close scrutiny
of the data reveals that the optimum conditions for clarification  of the
waste without regard to ABS'removal are 1530 mg/l of alum at pH 5.7,
with the ranges being 850 - 2210 mg/l alum and pH 5.1   6.0. A dose of
1360 mg/l of alum and 340 mg/l powdered activated carbon at pH  6.0  pro-
duced an effluent containing 1.8 mg/l ABS.  No studies were made to de-
termine the removal of ABS by alum alone.

Flynn and Andres    recommended treatment with alum at pH 4.0 and  pow-
dered activated carbon to be effective in treating laundromat wastes.
Rosenthal, et al. ^) conducted a more thorough study of laundromat  waste
treatment using alum and activated carbon.  They found that 800 mg/l of
alum alone at pH 4.5 removed 77 percent of the ABS.  The acceptable pH
range was 4.3   4.6.  In the laboratory, 2000 mg/l powdered activated
carbon (Nuchar) increased the ABS removal to 97 percent.  In an actual

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00
                                                   FIGURE 1





                                          LAUNDROMAT WASTE DISCHARGE*
                   Avg.  Total Water Discharge/Laundromat                1.25 x 10  gal./yr.
                   Avg.  Pounds Detergent/Laundromat                        _

                         (and other compounds)                             "
                   Avg.  Wastewater Flow/Machine                          89-240 GPD
                   Maximum Avg.  Flow/Machine                            .   587  GPD
                   Minimum Design Basis for Treatment                    C[-A   ,  ,    , .
                              /•Tr, v.    -i  \                              550 gal./machine
                              (12 hour day)                                  &
                              *  120 Launderettes - Suffolk Co., New York (1963)

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         FIGURE 2
TYPICAL LAUNDERETTE WASTE
                         (4)
1
Substance

ABS
Suspended Solids
Dissolved Solids
COD
Alkalinity
Chlorides
Phosphates
pH
Nitrates
Free Ammonia
Sulfates
Range (mg/1)

Minimum Average
3.0 44.0
15.0 173.0
104.0 812.0
65.0 447.0
61.0 182.0
52.0 57.0
1.4 148.0
5.1
< 1.0
3.0
200.0


Maximum
126.0
784.0
2,064.0
1,405.0
398.0
185.0
430.0
10.0
-



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FIGURE 3
TYPICAL  COMPOSITION  OF DETERGENTS

  DETERGENTS                 CH,
                              i°
  ABS   NaS0  <>CH ..... CH- C-CH
                             CH
             3       2 .....  2-   -3
    LAS   CH3-CH2 ..... CH  -CH2 ..... COOH
                    0
                       o
                      S-ONa
       COMPOSITION  OF DETERGENTS  _%_
SURFACTIVES                      I0~30
AMIDE FOAM  STABILIZERS             3-6
POLYPHOSPHATES                  25 - 4O
SILICATES                         5-7
CARBOXY METHYL CELLULOSE        OR  ,n
     (SOIL  SUSPENSION)            Ut5~ LO
SODIUM SULFATE                  15 - 25
WATER                            6-15
                   10

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laundromat, alum plus 400 mg/1 powdered activated carbon resulted in
83 percent removal of the ABS.  The use of granular carbon in  a series
of three filters instead of powdered carbon increased the ABS  removal
to 99 percent in the laboratory and 93 percent in the plant.   Further
studies showed that alum coagulation at pH 11.4 with lime produced a
clearer effluent which settled more rapidly and used less alum to achieve
the same ABS reduction.  Passing the alum-lime effluent through a 10  foot
deep granular activated carbon pressure filter produced a 99.8 percent
reduction in ABS in the laundromat waste treatment plant.  Paulson *-5'
used granular activated carbon to remove syndets from filtered sewage
plant effluents.  He applied the effluent to 4 - 5 foot units  in series
at 10 gpm/ft2, and regenerated the first unit when the ABS in  the efflu-
ent reached 0.5 mg/1.  Weber'-1-0' determined that the ABS uptake by gran-
ular activated carbon increased with decreasing pH.

The basic types of laundry waste treatment systems have been  studied  by
Flynn and Andres^'.  Their conclusion is that those employing alum at
a pH of about 4.0 and powdered activated carbon produce the greatest  re-
duction of ABS at the most reasonable cost in operation time,  equipment
and chemicals.
                               11

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                            SECTION V

              THE WINFAIR WATER RECLAMATION SYSTEM

A proprietory treatment plant utilizing the basic treatment principles
of Flynn and Andres, that of employing alum at a pH of about 4.0 and
powdered activated carbon^  , is manufactured by the Winfair Corporation,
Green Lake, Wisconsin (now a subsidiary of the Oshkosh Filter Company,
Oshkosh, Wisconsin).  A complete Winfair Water Reclamation System was
installed at the Coin-Op Laundry at Burnt Hills, New York.  This is  a
small community north of Schenectady, where individual wells and waste
treatment systems are the only means available to obtain water and dis-
pose of liquid wastes, respectively.  The ground water table in the
immediate area surrounding the laundromat is near the surface, and is
used as a water supply by some neighbors.  Water about 70 feet below
the surface is highly sulfurous and has a total dissolved solids content
of around 700 mg/1.  Permission could not be granted to dispose of the
untreated laundromat waste in a septic tank system.  The problems of
water supply and disposal were both overcome by the installation of this
complete water reclamation system.

In this system (Fig. 4) the washer effluents are first screened and then
stored in a holding tank.  From here a 15 gpm pump conveys the waste
through the alum coagulation system.  Alum is added to pH 4.2   4.5 and
then the waste enters a 45 gallon upflow tank for floe formation (3 min.
contact time).  The effluent from this tank is treated with lye so that
the pH after settling is 7.0 (pH slightly higher than 7.0 at the test
point).  The waste now travels through 3/4 inch copper tubing to the
mid-depth of a large settling tank.  The sludge is disposed of periodi-
cally and the clear supernatant is pumped through 1 of 5 pressure sand
filters in parallel (3 gpm through each).  The sand filter effluent
passes up through a bed containing Duolite (Diamond Alkali Company,
Redwood City, California) anion exchange resin A 102 D for detergent re-
moval.  After removal of the detergent, the waste passes up through a
bed of granular activated carbon for taste, odor, and color removal.
From there, 1/3 of the flow passes through a cation and an anion exchange
resin for complete deionization.  After recombination, the waste is
chlorinated and the pH neutralized before it enters the clean water tank
prior to reuse.

It appears that such a system should provide a satisfactory water for
reuse in a laundromat.  It is claimed that the cost of the additional
treatment is offset by the saving of fresh water and reheating of the
water, since it is normally still warm after passing through this treat-
ment system.  However, some difficulty was encountered after the system
had been operating for several months.  The detergent removal resin be-
came saturated, and no longer functioned in its capacity to remove de-
tergents.  This resin cannot be regenerated by ordinary means and must
be returned to the manufacturer for regeneration.  Also, the two deion-
izer resins were entirely ineffective, causing the total solids in the
                               13

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     FRcfM
   HOLDING
     TANK
                 CHEMICAL
                   FEED
             COAGULATION
               TANK
                3min.
          pH
        CONTROL
     TO
   DISCHARGE
    SETTLING TANK
       1000 GAL.
CHLORINE
                           I
              L
                         CATION
                        EXCHANGE
                 SUPERNATA^J
            ANION
           EXCHANGE
                         A A'A A A
  I   T Tr T 1
SAND



1
F
ILTERS



\
ACTIVATED
 CARBON
  ANION
   ABS
EXCHANGE
 RESIN
FIGURE 4-WINFAIR   WATER   RECLAMATION   SYSTEM

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recirculating water to increase constantly.   These resins are normally
regenerated weekly by conventional acid and alkali techniques.  Efforts
to rejuvenate them proved fruitless, and the total solids continued to
increase.

The reason for the failure of the detergent removal resin was quite ap-
parent.  This resin was designed to function on the basis of an effluent
from the alum coagulation system containing 5 mg/1 of ABS or less.   By
test, the alum treatment effluent contained approximately 15 mg/1 ABS.
Thus, the resin became saturated in 1/3 the expected time.  Replacement
of this resin produced an effluent containing only 2 mg/1 ABS after com-
plete treatment.  Further, the anion exchange resin in the deionizer
would attempt to remove a portion of the residual detergent not removed
by the other portions of the system.  During the period when the deter-
gent removal resin was saturated, a high detergent concentration reached
the anion demineralizer where it was exchanged into the resin.  Since
the detergent cannot be removed from the resin by conventional means,
this resin became saturated with the detergent and no longer functioned
as an anion remover.  No similar analogy can be made for the reason the
cation exchange resin failed.

The major portion of the problem appeared to be the failure to achieve
the expected ABS removal in the alum coagulation system.  Whereas it
was expected that this system should produce an effluent containing
5 mg/1 of ABS or less, the actual effluent contained around 15 mg/1
ABS, or a removal, in the order of 50 percent.  Since the work done at
Manhattan College    did not include an evaluation of the removal of
ABS by alum alone, and the work done by Rosenthal et al. °' showed
77 percent removal of ABS by alum alone at pH 4.5, it was felt that
further  studies to determine the removal of detergent by alum coagula-
tion alone were needed to evaluate the problem.
                               15

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                           SECTION VI

             LABORATORY STUDIES OF DETERGENT REMOVAL

Three series of experiments were performed to study the removal of deter-
gents by the use of various concentrations of alum at various pH values.
All mixing and coagulation were done using a typical 6-place multiple
laboratory stirrer.  Inasmuch as possible, an attempt was made to have
the laboratory procedures reproduce the treatment provided by the Winfair
Water Reclamation System.  After adding alum, the samples were mixed at
50 rpm for 3 minutes.  Then the pH was adjusted to the appropriate value,
and coagulation was produced by stirring at 30 rpm for 10 minutes, after
which the samples were allowed to settle for 30 minutes.  Determinations
were made for ABS to determine the detergent removal, and for chemical
oxygen demand and turbidity to determine the quality improvement.  The
sludge volume after settling was also determined in order to provide
some additional information on the amount of sludge storage capacity
needed.  ABS was determined by the methylene blue extraction technique,
using 2 ml of sample.  This volume of sample did not tend to produce
emulsions during the extraction.  All other analyses were made according
to Standard Methods^9\

The waste samples were secured from the holding tank containing the
mixed laundromat wastes.  The only pre-treatment it received was screen-
ing to remove lint and other large particles.  The temperature of the
waste at the time of sampling was 40°C.

In the first test, sufficient alum was added to a portion of the waste
sample to lower the pH to 4.5.  This same amount of alum was then added
to four other samples; a control containing no alum was given the same
physical treatment.  After mixing for 3 minutes, the pH of the samples
containing alum was adjusted with acid or sodium carbonate as needed to
values of 3.5, 4.5, 5.5, 6.5, and 7.5.  No pH adjustment was made in the
control.  The results are summarized in Table 1, and the reductions in
ABS, COD, and turbidity are shown in Fig. 5.

The best reductions in ABS and COD occurred at pH 4.5, whereas the best
turbidity reduction occurred at pH 7.5.  Actually the turbidity reduc-
tion was good throughout the entire pH range.  The lowest sludge volume
occurred at pH 3.5, although the amount of sludge produced at pH 4.5
was still quite low.  The high total solids content of the waste reflects
the failure of the deionizer in the treatment system.  Also to be noted
is that the alum treatment resulted in an increase in the total solids
content of about 1,000 mg/1.  The results from the control containing no
added alum showed no ABS removal, and a slight increase in turbidity.
The reduction in the COD of the control is likely due to sedimentation
of larger particles.  There was some sediment on the bottom of this con-
tainer, but it was insufficient to measure on the percent scale.  It is
apparent that all the ABS reduction in the test samples was due to the
added alum, and not due to plain sedimentation.
                               17

-------
                                                    TABLE 1



                               EFFECT OF  pH  ON  ALUM TREATMENT OF LAUNDROMAT WASTES
00
      Sample



Alum Cone, mg/1



PH



H2 SO^ Cone, mg/1



Na0 CO  Cone, mg/1
  t-   O


pH Before Settling



Final pH



ABS, mg/1



COD, mg/1



Turbidity, mg/1



Sludge Volume, %



Temperature, °C



    - >
Total Solids, mg/1
Waste 1
1500
7.25 4.5
0.13
0
3.. 5
3.9
32.1 22
699 296
125 1
3.7
22
9,0'76 ' 13,364 '
2
1500
4.6
0
- o
4.5
4.5
13.6
285
5.5
8
-
10,176
3
1500
4.6
0
455
5.5
5.6
15.2
285
1
40
-
10,046
4
1500
4.6
0
740
6.5
6.6
17.6
293
0.8
24
-
10,116
5
1500
4.6
0
1150
7.5
7.5
17.9
300
0.5
28
-
10,376
6
0
7.25
-0
0
-
7.3
32.9
551
140
- 0
-
9,392';..

-------
 FIGURE 5
 EFFICIENCY  OF ALUM  TREATMENT
    OF  LAUNDROMAT WASTES AT
        VARIOUS  pH  VALUES
O
  100
  90
  80
  70
  60
I-
o
Q 50
LU
o:
  40

  30

  20

  10

                           ••cr-
                         TURBIDITY
                        COD
XUUL
   3.5.  4.0   45   5.0   5.5   6.0   6.5   7.0   75
                FINAL pH
              19

-------
In an attempt to determine if satisfactory results could be obtained at
any lower alum dosages, a second experiment was run adding 1,000,  1,250
and 1,500 mg/1 alum.  Further, in order to evaluate the recommended oper-
ation of the Winfair treatment system in which the alum treated mixture
is neutraJized to pH 7.0 before sedimentation, duplicate samples were
run:  1 with no pH adjustment, and the other adjusted to pH 7.0 with
sodium carbonate after 3 minutes mixing at 50 rpm and before 10 minute
coagulation at 30 rpm.  The results are summarized in Table 2, and the
reduction in ABS, COD, and turbidity for the unneutralized and the neu-
tralized samples are compared in Fig. 6.  The pH was similar with all 3
alum dosages.  The ABS removal without pH adjustment was consistently
near 60 percent over the range of alum additions, whereas in the samples
adjusted to pH 7.0, the greatest ABS reduction was about 50 percent with
1,000 mg/1 alum, and this reduction dropped to 40 percent with 1,500 mg/1
alum.  Neither the alum concentration nor the pH in the ranges covered
had any significant effect upon the COD removal.  The turbidity removal
was poor with 1,250 and 1,500 mg/1 of alum without pH control, but at
pH 7.0 the turbidity removal was nearly constant at 90 percent.  At all
alum dosages used, the sludge volume without pH adjustment was about 1/3
that at pH 7.0.

Since the previous experiments indicated better ABS removal with no pH
neutralization, but covered only a narrow range of alum dosages, the
next logical step seemed to be to study the effects of a wide range of
alum dosages with no pH neutralization.  Alum was added to samples of
the waste in 250 mg/1 increments from 500 to 1,750 mg/1.  No attempt was
made to maintain the pH near 4.5.  Mixing and coagulation were maintained
as in the previous experiments.  The results are summarized in Table 3,
and the efficiencies of removal of the ABS, COD, and turbidity are shown
in Fig. 7.  The addition of 500 mg/1 alum lowered the pH to only 5.5
whereas the addition of 750 mg/1 and greater lowered the pH to nearly
4.5 and even slightly below this level with 1,750 mg/1 alum.  The maxi-
mum ABS removal of 67 percent occurred with the addition of 1,000 mg/1
alum, and only slightly less removal occurred in the range of 750 to.
1,250 mg/1 alum.  Poor ABS removal occurred with only 500 mg/1 of alum,
and again with 1,500 mg/1, but increased removal again occurred with
1,750 mg/1 alum.  The COD removal was fairly consistent above 750 mg/1
alum, but was somewhat less with only 500 mg/1.  The best turbidity
removals occurred between 750 and 1,250 mg/1 alum.  There was no sig-
nificant difference in the sludge volumes produced with the various alum
additions.  The total solids generally show the effect of the added alum,
but there appeared to be a slight reduction in total solids with the
addition of 500 and 750 mg/1 alum.  Generally, it appears that optimum
conditions for ABS, COD and turbidity removal are 750 to 1,250 mg/1 alum
in the pH range of 4.5 to 4.8.

An important observation of these lab studies is that the lowest ABS con-
centration achieved for any procedure was in the order of 10 mg/1.  This
is twice the value claimed by the manufacturer, and upon which "the ABS
removal resin  is based.  This means simply that the resin will be satu-
rated  in half the predicted time, or to put it another way, the cost for
the ABS removal by the resin will be twice that predicted by the manufac-
turer.

                               20

-------
                                    TABLE 2



                  EFFECT OF VARIOUS CONCENTRATIONS OF  ALUM AT

               DIFFERENT pH'.S FOR TREATMENT OF LAUNDROMAT WASTES
      Sample^



Alum Cone, mg/1



Na0 CO  Cone, mg/1
  £.   d


pH Before Settling



Final pH



ABS, mg/1



COD, mg/1



Turbidity, mg/1



Sludge Volume, %



Temperature, °C           20
Raw
Waste
-
-
7.1
-
38.7
625
128
_
1
1000
0
4.7
4.6
16.8
382
15
9.5
2
1000
560
7.0
6.9
19.6
400
3.9
22.2
3
1250
0
4.6
4.6
15.6
382
52
8.7
4
1250
780
7.0
7.1
21.6
385
4.6
28.5
5
1500
0
4.6
4.5
15.9
385
76
8.2
6
1 1
1500
925
7.0
7.0
23.5
389
5.4
26

-------
FIGURE 6
EFFICIENCY OF VARIOUS  ALUM  DOSAGES
  FOR  TREATMENT OF LAUNDROMAT
   WASTES AT  SEVERAL pH  VALVES












2
p
o
—V
—}
Q

\
\
\
\ <^
^^x^-ABS
^ ^^N^
° 	 r° 	 a ^~*i 	 ^
^COD °" ^COD
-
-
-
iii iii
        1,000  l£50 1,500       1,000 1,250  1,500

          ALUM  CONCENTRATION  mg/l
               22

-------
                                                     TABLE  3

                                 EFFECT OF A WIDE RANGE OF ALUM CONCENTRATIONS
                                      FOR TREATMENT  OF LAUNDROMAT  WASTES
CO
Sample
one. mg/1
pH _
'g/1
ig/1
ity, mg/1
Volume, %
Raw
Waste
-
7.2
33.2
585
135
_
1
500
5.5
23.5
358
65
9
2
750
4.8
12.3
314
7
13.2
3
1000
4.7
10.8
307
8
12
4
1250
4.5
14.9
307
15
10
5
1500
4.5
18.3
314
60
10
6
1750
4.4
14 .4
314
90
7.5
Final pH

ABS, rag/

COD, mg/

Turbidit;

Sludge V

Temperature, °C
                                          21
                Total Solids, mg/1
                       9,334
9,118     9,132     9,316     9,478
9,670     9,862

-------
 FIGURE 7

 EFFICIENCY OF VARIOUS ALUM DOSAGES
FOR TREATMENT OF LAUNDROMAT  WASTES
    100


    90


    80


    70



  o 60
  o

  Q
  LU
  CC
50



40



30



20



10
     0
         5.5
                      TURBIDITY
         4.8  4.7  4.5   4.5
                    PH
                          ABS
4.4
     0   500  750  IpOO 1,250 1,500  1,750

        ALUM  CONCENTRATION mg/l

-------
                           SECTION VII

                   TREATMENT SYSTEM OPERATION

The above studies were performed under the auspices of the New York
State Health Department, and showed the need for a more thorough study
of the system.  Meanwhile, the laundromat operator had to discontinue
use of the Winfair system due to complaints by customers of odors and
foaming in the recycled water.  In an effort to alleviate the problem,
he purchased and put into use a treatment system designed by American
Laundry Machinery Industries.  This system is based upon the precipi-
tation of the anionic syndets by means of a cationic syndet, the pre-
cipitation of phosphates and other materials with CaCl_, and separating
the solids by means of a pressure diatomaceous earth filter (Fig. 8).
Whereas this provided satisfactory treatment of the waste, it did not
solve the problem of water supply nor the hydraulic discharge of the
treated effluent.  Thus, the operator was forced to discontinue his
laundromat operation at Burnt Hills.

However, the operator retained the 2 treatment systems and offered their
use for research purposes.  When a Federal Water Pollution Control Admin-
istration Grant became available, he graciously offfered their use at
another laundromat.  They were set up in a shed which was somewhat re-
modelled and electrified.  The flow diagram is shown in Fig. 9.  A 4,000
gal. holding tank was installed and four 1,000 gal. tanks were provided
for settling, sludge holding, and treated water.  Chlorination was ap-
plied in the treated water storage tank.  The system was designed so
that the waste would flow into the holding tank, and when it was full,
the waste would overflow into the existing distribution boxes and tile
drainage field.  Physical problems were encountered with these last two
appurtenances, in that trucks delivering to the adjacent food market
would drive over them, crushing them and blocking them.  This resulted
in the overflow of raw wastes from our holding tank.

The Winfair system was set up and put into operation first while re-
placements were awaited for the filtering elements for the ALMI system
which were found to be rusted beyond use upon receipt of the units.
The Winfair system was operated for a period of 9 months.  Analyses
were performed for ABS, COD, BOD, pH, and total dissolved solids.

The ABS concentration throughout the system is shown in Fig. 10.  The
actual values are summarized in Table 4.  The greatest removal of ABS
was accomplished by the alum addition followed by sedimentation.  This
was in the order of 76% of the initial ABS, and resulted in an average
ABS, after settling, of slightly over 11 mg/1.  This is in the same
order as the laboratory experiments.  The sand filter removed a little
more ABS, but the detergent removal resin lowered the ABS to an average
of less than 3 mg/1.  This resin actually removed in the order of 70%
of the remaining ABS.  The activated carbon and the demineralizer system
removed little additional ABS.  The average overall ABS removal was 94%.
                               25

-------
    TO CHLORI NATION,
    AND DISCHARGE
 TRANSFER
  PUMP
                   PRECOAT
                   FLOAT
                   CONTROIL
                         i-CHEMICALS
                     PUMP t
                      CHEMICAL
                        TANK
                  FILTER
                  PUMP
              FLOAT
             CONTROL
y
r

Ln






1
               HOLDING   TANK
                                    No. I
                                   FILTER
   4-tX-
   SLUD
   PUMP
                                RAW WATER
                               "FROM WASHER
                 No.2
                FILTER
TO SLUDGE
HOLDING TANK
                                              VALVE  SETTINGS
     PRECOAT  ON STREAM  DESLUDGE
OPEN  1,2,3,6,7,8    1,2,3,6,7     4,5,6,7
CLOSED 4,5      4,5,8      1,2,3,8
FIGURE  8
SCHEMATIC  FLOW   DIAGRAM-AMERICAN  LAUNDRY
MACHINERY  INDUSTRY-DIATOMITE FILTRATION  SYSTEM

-------
J3S' TO LAUNDROMAT
  25'
                      HOLDING
     TANK
                          4,000 GALS.
                                       0 o
                  ALMI
SYSTEM
                                       WINFAIR
                                    40'
                               CLEAN WATEF
                                8 CHLOR-
                                INATION
                                1,000 GALS.
 ALL 1,000 GAL. TANKS
 APPROXIMATELY 6'x4x7'DEEP
                                     60' TO
                                     DISCHARGE
              FIGURE  9
LAUNDROMAT   TREATMENT   PLANT
                          SYSTEM

                                                                  
-------
100
 10
CO
m
 0.1
        1440
        109.0
         FIGURE 10

DETERGENT  CONCENTRATIONS

THRUOUT  WINFAIR   SYSTEM
    EACH DOT OR CIRCLE
   - REPRESENTS 1 ANALYSIS

   ^ LINE CONNECTS AVG. VALUES
                         o

                         QjU.
                   O
                   m
                   oc
                                     a:
                                     LJ
                                     N
        <
        oc.
 1-UJ
 UJ
 en
QUJ




1
                               ou.
                        (TUJ
                        UJ
UJ
Q
                   28

-------
                                                         TABLE 4




                                         SUMMARY OF ABS REMOVAL IN WINFAIR SYSTEM
ID
      Unit





Raw Waste




Settling Tank




Sand Filter




Detergent Removal




Activated Carbon




Detnineralizer
Number
of
Samples
75
67
67
68
68
74

Max.
144.0
31.5
27.0
4.7
3.8
4.4
ABS, mg/1
Min.
21.5
2.5
4.6
1.4
0.54
0.08

Avg.
47.15
11.25
9.69
2.86
2.61
2.31
Avg.
% of
Original
76
3
14
0.5
0.6
Reduction
> % of
Remaining
76
13
70
8
11
                  Overall
                                                                        94.1

-------
The BOD and COD results are summarized in Table 5.   These parameters
were determined to show the effectiveness of this  system as a treatment
system.  If the effluent is to be recycled,  these  parameters must be
followed in order to be alerted to an undesirable  build-up.  If the
effluent is to be discharged, their concentrations  must be known in
order to determine if the effluent will be acceptable in the receiving
body of water.  The average BOD of the effluent was 52 mg/1 and the
average BOD reduction was in the order of 56%.   The average COD of the
effluent was 114 mg/1 and the average COD reduction was 62%.

The pH (Table 6) of the raw waste was generally near neutral to slightly
alkaline.  On only two occasions was the pH below  6.8.  These are con-
sidered due to the production of septic conditions  in the holding tank.
The pH adjustment in the flocculating tank was  maintained between 3.9
and 5.1 with one value at 6.0.  The pH increased more than one unit on
an average as it passed through the settling tank.   By the time it
reached the end of the treatment system it reached an average value
great er than 6.0.

The total dissolved solids pose a problem if the effluent is to be reused
in a laundromat.  The dissolved solids through  each unit of the system
are summarized in Table 7.  The variation was greatest in the raw waste
which had a minimum value of 625 mg/1 and a maximum of 1,4-50 mg/1.  The
primary concern is that the overall system resulted in an increase of
total dissolved solids, rather than the desired reduction.  This is shown
in Fig. 11.  The greatest increase was due to the  alum addition, and was
in the order of 20 mg/1.  The demineralizer, which was designed to reduce
the dissolved solids, resulted in an average increase of 6 mg/1, or essen-
tially no effective reduction.

The effluent from the system was chlorinated in the final holding tank
before being discharged to a swampy area of a slow-running stream.  This
stream was little more than a drainage ditch which helped to drain the
high water table of the surrounding area.  All  the houses in the area
are provided with septic tank and tile field systems.  The overflow from
the holding tank (as described previously) also reached this swampy area.
During warm weather an offensive odor arose from the stagnant stream,
causing complaints by the neighbors.  An injunction was brought against
the laundromat operator to prevent the overflow of wastes from the hold-
ing tank.  It was decided to install a float valve on the holding tank
so the system would operate automatically when  the holding tank was full.
Even with the promise to have the float valve operative within a week's
time, the judge closed the laundromat.  This also  resulted in the land
owner's filling in the swamp and digging a channel to carry off the
water, thereby eliminating the problem created by  the stagnant water.
Whereas the injunction closed the laundromat, there was no claim against
the operation of the treatment system.  Arrangements were made to trans-
fer 2,000 gal./day of laundromat waste from another laundromat about 3
miles away.  This allowed operation of the treatment system without mov-
ing the equipment.  However, no further studies were performed using the
Winfair system.
                               30

-------
                             TABLE 5

             SUMMARY OF OVERALL BOD AND COD REMOVAL
             IN THE WINFAIR WATER RECLAMATION  SYSTEM
            No. of      Influent mg/1       Effluent  mg/1     Average %
Parameter   Samples   Max.  M_in._.  Ayg._   Max.   Min.   Avg^   Reduction

   BOD        101     185    50   119.2   118   20.5   52.2      56.4


   COD         70     438   136   293.4   244   38   113.8      62.1
                             TABLE 6

             SUMMARY OF pH VALUES IN WINFAIR SYSTEM
      Unit

Raw Waste

Flocculation Tank
  c -
Settling Tank

Sand Filter

Detergent Removal

Activated Carbon

Demineralizer
No. of
Samples
134
136
117
117
117
117
134
Ma?c.
7.6
6.0
6.7
6.7
7.0
6.9
6.8
Min.
5.0
3.9
4.2
4.5
5.0
5.2
5.1
Avg.
7.13
4.45
5.58
5.76
5.95
5.99
6.07
                               31

-------
                                   TABLE 7




             SUMMARY OF TOTAL DISSOLVED SOLIDS IN WINFAIR SYSTEM
        Unit





Raw Waste




Settling Tank Eff.




Sand Filter Eff.




Detergent Removal Eff.




Activated Carbon Eff.




Demineralizer Eff.
Number
of Samples
81
79
79
79
79
81 -
Total Dissolved Solids, mg/1
Max.
1,450
1,425
1,400
1,375
1,410
1,325
Min.
625
750
700
690
700
750
Avg.
931
952
953
956
968
974

-------
                FIGURE  II


 SUMMARY OF TOTAL  DISSOLVED  SOLIDS
       IN  WINFAIR  SYSTEM - mg/1
 980 r
 970
 960
E950
CO
o

_l
o

00 940
o
 930
^920
  910
 900
 890
             O
           o
           UJ
         LU
 cr
QUJ
                   CO
                        C9
                        UJUJ
                        oo:
                                    a:
                                    ut
                 a:
                 LU
           o<
           
-------
                          SECTION VIII

               DISCUSSION OF THE WINFAIR SYSTEM

The Winfair Water Reclamation System was operated for a period of nine
months adjusting the pH of the raw waste with alum in the range of 4.0
to 5.0, but with no neutralization prior to sedimentation.  The average
ABS content after settling was 11 mg/1, which correlates well with the
results of the lab studies.  The value is double that which the manufac-
turer claims can be expected from this portion of the system.  However,
it is less than the 15 mg/1 obtained by the original operator.  It does
confirm that the anion ABS exchange resin will be depleted in half the
time predicted by the manufacturer.  So long as consideration is made
for this, it will not create a serious problem except for an increase
in cost for the operation.  The overall ABS reduction was 94%, result-
ing in a residual ABS of 2.3 mg/1.  This is greater than the recommended
drinking water standards but should be satisfactory for reuse in a
laundromat.

The BOD and COD removals are intermediate between primary and secondary
treatment.  The residual may or may not be acceptable for discharge
depending upon the receiving stream.  This would also depend on the
volume of the waste from each individual laundromat under consideration.
Generally speaking, the average BOD of 52 and the average COD of 114 in
the effluent are considered rather high for recycling of the effluent.
Chlorination may reduce these slightly and also prevent septic condi-
tions in the recycle holding tank.

pH was to have been an important key in this study.  Since the initial
pH adjustment was difficult to establish, it was expected that a wide
range of pH values would be obtained allowing for an evaluation of the
degree of treatment over a wide pH range.  Instead, the lab assistants
went to extreme pains to maintain the pH between 4.0 and 5.0 in order
to obtain what the laboratory studies had shown to be the pH for the
greatest purification.  An attempt was made to correlate the pH vs
treatment, but the results showed no conclusive trend.  It is inter-
esting to note that when the system was first set up and operated to
get the bugs out, on one occasion the pH in the flocculation tank was
6.0, and the ABS in the effluent was recorded as 0.0.  Since this was
a break-in period both from the standpoint of operating the system and
perfecting lab techniques, no great value can be placed on this single
result.

One of the greatest disappointments was the operation of the demineral-
izer system for removal of the total dissolved solids.  The increase in
the total dissolved solids due to the addition of the alum of about
20 mg/1 was less than that of up to 1,000 mg/1 experienced in the lab
studies.  This indicates better control and separation in the system
than in the lab.  The increases in passing through the remaining units
of the system are insignificant.  However, when it comes to the deminer-
alization, this is supposed to reduce the total solids, not result in an
                               35

-------
insignificant increase.  When the system was started up,  fresh resins
were placed in the units.   Some difficulty was found in balancing the
valves so that approximately one-third of the flow passed through the
demineralizers.   After this was established samples were secured for
the dissolved solids test which showed no reduction.  It is possible
that in establishing the flow, the resins became exhausted.  Therefore,
they were regenerated as per specifications, but with no change in
results.   Numerous efforts were made to regenerate the resin and they
were completely  replaced later in the study.  The flow was regulated
to all extremes  including passing all the liquid through the resins.
All of these efforts proved fruitless.  It can only be concluded that
the demineralizer system provided by the company was not capable of
performing the job for which it was designed.  This is the same con-
clusion reached with the initial evaluation of the failure of the sys-
tem in its first location.

Although the possibility of reuse of the treated effluent was considered,
it was not attempted in any of these studies.  The water supply for the
laundromat was adequate, and it was felt that the existing good quality
water would be preferred to reused water.  The only advantage that could
have been gained by reuse would have been a saving in waste water that
would have had to be discharged.  The quality of the effluent is con-
sidered to be adequate for reuse in a laundromat, but certainly not for
drinking.  No consideration could be made of the number of reuse cycles
that could have  been made before the build-up of non-removed materials
would reach an undesirable level.

It is also considered that this treatment would result in an effluent
which could be discharged into a subsurface disposal system with a min-
imum of problems.
                               36

-------
                           SECTION IX

                   THE ALMI FILTRATION SYSTEM

As early as 1944, the U.S. Army Corps of Engineers developed a diatomite
filtration unit for use in supplying safe and potable water for field
troops^-1'.  These units had to (a) be portable and (b) operate at a
high rate of output.  Since the nation was then involved in a global
war, the economic factor was not of great import in evaluating the over-
all success of the system.  In addition to the conventional health and
aesthetic requirements, the system had to remove the cysts of Endamoeba
histolytica and the cercaria of schistosomes.  This was particularly
crucial in both the South Pacific and the Mediterranean Theatres of war.
At flow rates of 6 to 12 gpm psf, many cysts passed through conventional
sand type filtration units.  On the other hand, the diatomite filters
affected virtually complete removal of cysts under the most severe tests.

These findings were again utilized as the post World War II boom of home
laundries and public laundromats spread into unsewered areas, increasing
the need for effective treatment units.  The American Laundry Machinery
Industries (ALMI) Diatomaceous Earth Filtration System was developed for
such laundry waste treatment.

Structually, the ALMI wastewater treatment system (WWTS) used is a con-
tinual water filtration system consisting of a mixing tank, 2 chemical
feed tanks, 2 pressure filter units operated in parallel, and the appro-
priate pumps, valves, and connecting piping.  Additional appurtenances
include a :4,000 gal." raw wastewater holding tank to provide flow equal-
ization, a 1,000 gal. treated water tank which served as a chlorine
contact tank, and a 1,000 gal. sludge holding tank which retained the
filtered materials plus the spent diatomaceous earth (DE) until hauled
away by a scavenger.  Each filter unit contains 45 vertical mesh screen
tubular elements (total of 90 elements) which serve as a septum for the
diatomaceous earth (DE) precoat.  Figure 12 shows an 8,000 GPD system.
A schematic flow diagram is shown in Figure 13.  The principal charac-
teristics of this unit are listed in Table 8.

System operation consists of applying a precoat on the filter elements
by recirculating a water suspension of DE from the mixing tank through
the filters with return to the mixing tank.  The precoat operation usu-
ally requires 3-6 min. using a 45 Ib. change of diatomaceous earth.
Following precoating, the waste purification cycle is intitiated by
pumping wastewater from the holding tank to the mixing tank, through
the filters and to the treated water tank.  A purification cycle nor-
mally lasts 15 minutes during which 400 gallons of wastewater are proc-
essed at a flow rate of 25 GPM.  Following each 15 minute filtration
cycle, a timer switch shuts off the filter pumps and activates a mechan-
ical shaker mechanism which "bumps" off the precoat from the filter ele-
ments.  The precoat and filtration cycles are then repeated following
completion of the bump phase.  The periodic bump to remove and re-precoat
the filter elements restores pressure drop loss which occurs as solids
                               37

-------
co
oo
                                                                                        V
                                               Wc: 12. AMERICAN LAUNDRY mCHIHERY  IND3UTRIES WASTE WATER TRfiATMEST SYSTEM

-------
co
10
                  TO CHLORI NATION,
                  AND DISCHARGE
               TRANSFER
                 PUMP
          •*»-
                                        rCHEMICALS
                                        f
                                     CHEMICAL
                                      TANK
FILTER
PUMP
                             FLOAT
                            CONTROL
r




1
                              HOLDING   TANK
                                                  No. I
                                                 FILTER
                      I-H-
                     SLUD
                                              RAW WATER
                                              "FROM WASHER
-«-•
                                   N..2
                                  FILTER
  TO SLUDGE
  HOLDING TANK
                                                            VALVE   SETTINGS
                       PRECOAT  ON STREAM  DESLUDGE
                   OPEN 1,2,3,6,7,8   1,2,3,6,7    4,5,6,7
                   CLOSED  4,5     4,5,8     1,2,3,8
               FIGURE 13
               SCHEMATIC  FLOW  DIAGRAM-AMERICAN  LAUNDRY
               MACHINERY  INDUSTRY-DIATOMITE  FILTRATION  SYSTEM

-------
                            TABLE 8
              AMERICAN LAUNDRY MACHINERY INDUSTRIES
              DIATOMACEOUS EARTH FILTRATION SYSTEM
Overall Size

   Base

   Height


No. Filter Elements

   Size

   Mesh


Filter Element Area

   Total
5'-3"  X  5'-5"

7'-2"


90

25.5" long  X  1" dia.

60


0.564 ft2/element

50.76 ft2
Normal Flow

   In

   Out


Flow Loading


Diatomite Charge


Normal Total Daily Flow


Chemical Feed Solution Rate
25-26 gpm

14-15 gpm
   0.5 gpm/ft  filter area
45 pounds (0.89 Ib./ft )


6300-8500 gals.


60-70 ml./min.

-------
accumulate on the filter elements.   Figure 14 illustrates  the  rate of
pressure drop increase (and flow decrease) as a function of number of
filtration cycles /2)  Usually, it is possible to achieve  10-15 filtra-
tion cycles with one DE charge, which allows processing of 4000-6000
gals, of wastewater.

The recommended chemical operation of the ALMI system consists of the
addition of CaCl2 and Roccal (commercial name for a quaternary ammonium
compound which is in effect both a cationic detergent to remove residual
anionic detergents and a germicide to kill bacteria) to the raw waste
in the mixing tank.  In addition, NaOH, alum and ferric chloride were
added in tests to study the removal of phosphates.  Finally, sodium
hypochlorite (Clorox) was added to the effluent to reduce bacteria.

The entire chemical reactions of the ALMI Wastewater Treatment System
take place in the mixing tank.  They are designed to neutralize and/or
precipitate phosphates, spent detergents, nitrates, organic matter and
suspended particulates in the wastes.  To the degree that the the chem-
ical process is effective, these substances are then trapped upon the
filter medium, theoretically leaving a clear, odorless and non-pathogenic
effluent low in organic matter.

This entire phase of this study was conducted under less than ideal con-
ditions.  Just prior to commencing Part II of this project, an injunc-
tion was obtained against the laundromat operator, forcing him to shut
down his operation.  This was due to an overflow of wastes from the
holding tank at the treatment plant.  The system was designed so that
when the holding tank was full, the waste would spill over into a septic
tank and leaching system.  However, delivery trucks had crushed the pipes
leading to the septic tanks and tile fields, so that the waste overflowed
at the holding tank.  Fortunately, the injunction which closed the laun-
dromat said nothing about the treatment plant, so arrangements were made
with the operator of a laundromat about 3 miles away to truck 2,000 gal.
per day from his septic tank to our holding tank.  This waste was septic
and not fresh as the local waste was.  This probably made the waste more
difficult to treat.  It was assumed that if this system could treat this
septic waste satisfactorily, it could do an even better job of normal
fresh laundromat wastes.

-------
o> 3

ul
I  2

u_
                         25 ._
                            (0
                            o.


                         20
                                        a:
                                        a.

                                        o;
                                        UJ
  60



iu 50

o
  40
0)
  30
g 20
   10
         I
I
I    l
I
    0   2   4   6   8   10   12   14  ,16

                  CYCLES


    FIGURE 14-ALMI SYSTEM PRESSURE DROP-

              FLOW CHANGES

-------
                            SECTION X

                       LABORATORY ANALYSIS

Discussion of the information available from the data is expanded for
each of the parameters measured, and then the most nearly optimum oper-
ating conditions are evaluated.

ABS Removal

With one exception, 97% or better ABS removal was achieved with Roccal
dosages of 26 mg/1 and greater as summarized in Table 9.  With one ex-
ception, the ratio of CaCl2 to Roccal ranged between 4.78   5.1 on these
occasions.  Poorer ABS removals occurred when the Roccal addition dropped
below 26 mg/1 and the CaC^:  Roccal ratio was greater than 10.  The sum-
mary of the removal of ABS is shown in Table 10.  The concentration of
ABS in the raw waste was fairly constant with a variation only from 16
to 26 mg/1 and an avg. of 20 mg/1.  The highest value in the effluent was
5.2 mg/1 and on numerous occasions the ABS was removed completely.  The
avg. ABS in the effluent was 2.5 mg/1, representing an avg. reduction of"
87%.

BOD Reduction
The values of the BOD reduction are summarized in Table 11.  The highest
BOD recorded in the influent was 371 mg/1, but the next highest value
was 168 mg/1.  The avg. BOD of the waste was 126 mg/1.  The avg. BOD of
the effluent was 47 mg/1.  The avg. reduction was 63%; the max. was 82%
and the minimum 7%.  The 82% reduction was achieved using a 4-6 Ib. charge
of Pitcher Celatom and resulted in an actual reduction of BOD from 109
mg/1 to 20 mg/1.

COD Reduction

Table 12 shows the summary of the COD reduction.  The COD of the influent
ranged from 200 to 455 mg/1 with an avg. value of 340 mg/1.  The values
in the effluent ranged from 42 to 196 mg/1 with an avg. of 104 mg/1.  The
greatest reduction of 84% occurred on two occasions and the poorest re-
duction was 31%.  The avg. reduction in .COD was 69%.  The best COD reduc-
tion was achieved using Diatomite in a 44 Ib. charge resulting in actual
reductions of 258 6 285 mg/1 to 42 g 45 mg/1, respectively.

Turbidity Reduction^

The turbidity of the effluent varied appreciably with the pH as shown in
Fig. 15.  (Percent transmittance is plotted instead of actual turbidity;
a high transmittance indicates a low turbidity.)  It may be seen that
the best turbidity removal occurs when the pH is adjusted to values
greater than 8.  Table 13 shows the variation of the effluent turbidity
with various dosages of each of the diatomaceous earths used.  The best
                               43

-------
                    TABLE  9
     SUMMARY OF ABS  REDUCTION WITH VARIOUS
          CaCl2 AND  ROCCAL  ADDITIONS
Date
8/27/69
8/6/69
8/27/69
8/7,8,11/69
9/17/69
8/21/69
8/19/69
8/12/69
8/26/69
8/26/69
9/17/69
8/19,21/69
8/13/69
9/20/69
9/22/69
8/29/69
9/20/69
11/18/69
8/28/69
8/29/69
9/3/69
9/11/69
8/14,15/69
9/3,4/69
Ratio CaCl2
Roccal Dosage (mg/l) To Roccal
110.0
105.0
88.5
84.0
64.0
63.2
63.0
56.0
55.6
48.5
45.0
32.0
29.2
26.2
24.0
23.8 (NaOH Added)
20.2
20.0 (Alum + FeCla Added)
19.8 (NaOH Added)
18.3 (NaOH Added)
15.4 (NaOH Added)
15.2
12.0
9.2 (NaOH Added on 9/3
4.8
4.8
4.6
4.8
4.9
11.5
4.8
4.8
4.8
5.1
4.9
4.8
4.8
9.9
6.75
24.0
9.7
No Data
23.8
23.8
22.7
10.1
4.7
23.7
Average
Reduction %
100
No Data
97.77
100
97.76
99.04
91.59
100.00
99.31
98.10
97.78
98.25
99.37
97.93
38.33*
97.96
88.45 .
No Data,
81.02
80.48
72.43
75.98
77.58
46.34
            Only - Results Not
            Typical)
1500 mg/l Alum Added,  Settled in  WWRS  Before ALMI  Treatment
                     .44

-------
                                           TABLE 10

                              SUMMARY OF REMOVAL OF ALKYL BENZENE
                               ; SULFONATE IN THE A.L.M.I.  SYSTEM
             INFLUENT
    High
Low
AVE
Date  - mg/1   Date   mg/1   mg/1

8/26   25.7    8/8   15.7    20
                              EFFLUENT
High
                                                      Low
Av«
                   9/3   15.3  8/2,7,8,
                                11,27
                                                       REDUCTION
High
Low
                  Date   mg/1   Date   mg/1   mg/1    Date
                                     2.5   8/2,7,   100
                                           8,11,27
                                                         Date
                                              9/3
                                                                                            18
                                   87
                                          TABLE  11

                              SUMMARY OF REDUCTION OF BIOCHEMICAL
                              OXYGEN DEMAND  IN  THE A.L.M.I. SYSTEM
            INFLUENT
                              EFFLUENT
    High
Low
            High
                                    Low
      „       _____   	    -	  	  Avg.-
Date   mg/1   Date   mg/1   mg/1    Date    mg/1  Date   mg/1   mg/1

8/14    371   8/21    80     126    8/16     102    9/4     15     47
                                                                                  REDUCTION
                                    High
                                                                                        Low
                                                                       Date

                                                                       8/21
                                                              82
                                                         Date

                                                         8/16
                                                    7.3
                                                                               AVE
                                                                                63

-------
                                                  TABLE  12
                                   SUMMARY OF REDUCTION OF CHEMICAL  OXYGEN
                                         DEMAND  IN THE A.L.M.I. SYSTEM
                    INFLUENT                            EFFLUENT                           REDUCTION
            High          Low       Avg.         High          Low       Avg.     '  Higfr^^       Low ~~~~   AT

        Date   mg/1   Date   mg/1   mg/1    Date   mg/1   Date   mg/1   mg/1    Date    %    Date    %


        8/19    455    8/8    200    340    8/6,19   196   8/26    42     104   8/26,29  84   8/19    31    69
•F
O>

-------
    FIGURE 15-  EFFLUENT  TURBIDITY  VS  pH  IN   THE

                A.L.M.I.  SYSTEM
  too
   90
   80
o
z

-------
                            TABLE 13

                EFFLUENT TURBIDITY VS.  FILTER AID
Filter Aid
Diatomite
Diatomite
Diatomite
Pitcher Celatom
Pitcher Celatom
Pitcher Celatom
Dosage
Lbs.
24
42
44
46
43
50
Average
pH
7.1
7.4
7.4
N.D.
N.D.
9.1
Avg. % Transmittance
87
85
81
61
No Data
96
 (NaOH Added)
Diatomite
 (NaOH Added)

Diatomite
 (NaOH Added)

Diatomite
 (NaOH Added)

Diatomite
 (NaOH Added)
43
37
43
43
N.D.
N.D.
N.D.
N.D.
  91
No Data
No Data*
  59.5
Johns-Manvilie
Hyflo-Supereel

Celite 545
44
44.5
N.D.     No Quantitative Data (Poor)
7.6
  79.5
    *  Six (6) Minute Precoat Hereafter
                               48

-------
reduction of turbidity was achieved using Pitcher Celatom at a 50 Ib.
charge resulting in an effluent which manifested 96% transmittance.

Organic Nitrogen

The small number of results for Kjeldahl nitrogen available are summar-
ized in Table 14.  Although the data are not statistically significant,
on one occasion there was an increase in the organic nitrogen of 146%
from the influent to the effluent; on the other two occasions there was
a reduction.

Total Dissolved Solids Increase
In all cases, due to the chemicals added for the treatment, there was an
increase in the total dissolved solids as shown in Table 15.  The aver-
age increase was 61%.  The greatest increase was 144% from 450 mg/1 to
1,100 mg/1.  The least increase, 3%, from 390 and 400 mg/1 to 400 and
410 mg/1, respectively, occurred using Diatomite in a 44 Ib. charge com-
bined with 56 mg/1 of CaCl2 and 12 mg/1 of active Roccal.  That the
increase in total dissolved solids is directly related to the CaCl2
added is shown visually in Fig. 16.

Hardness
The scant hardness data do not lend themselves to statistical evaluation.
It would be useful to correlate hardness in the effluent with CaCl2 dos-
age, but this is not possible.  A summary of the existing data is shown
in Table 16.  The hardness in the influent varied only between 172 and
248 with an average of 209 mg/1.  On two occasions on the same day there
was an extreme increase in hardness in the effluent to 620 and 668 mg/1.
Including these two values the average hardness in the effluent was 284
mg/1 showing an average increase of 36%.  Excluding these two abnormal
values there was an average reduction of 20% to 166 mg/1.

Phosphate Removal

It is well known that phosphate removal is directly related to the pH of
the solution.  This is shown clearly in Fig. 17.  Below pH 7.5 the phos-
phate removal was in the order of 25%, whereas above pH 8.5 it was above
90%.  To show any effect of CaC^ dose on phosphate removal, Fig. 18 was
constructed.  It may be seen that increased CaCl2 dosage does result in
a greater removal of phosphate, but this removal approaches only 50%
with CaCl2 dosages up to 700 mg/1.  On the other hand, CaCl2 dosages in
the range of 400 to 600 mg/1 removed over 90% of the phosphate when NaOH
was added.  When alum was added and the waste settled in the Winfiar sys-
tem prior to treatment in the A.L.M.I, system, an 85% reduction of phos-
phate was achieved using only 150 mg/1 CaCl2-  For these reasons, the
summary of the phosphate removal results (Table 17) is divided into sec-
tions showing the removals with CaCl2 alone, with addition of NaOH, and
with alum and settling.  The maximum phosphate removal, from 169 mg/1 to
                               49

-------
                                                   TABLE 14

                                       SUMMARY OF CHANGES IN THE ORGANIC
                                        NITROGEN IN THE A.L.M.I. SYSTEM
                    INFLUENT
            High
           Low
                                         EFFLUENT
                            Ave.
High
Low
        Date

        8/6
mg/1

10.1
              Date   mg/1   nig/1    Date   mg/1

              8/7     5.6    7.8    8/7    13.8
          Date

          8/8
   mg/1

    7.5
Avg.
mg/1
11.25
                                                                                      CHANGE
   High
          Low
Date

 8/8
-24
Date_

8/7
+146
              AVE
01
o
                                                   TABLE 15

                                  SUMMARY OF THE INCREASE IN TOTAL DISSOLVED
                                         SOLIDS IN THE A.L.M.I. SYSTEM
                    INFLUENT
                                         EFFLUENT
            High
           Low
      	   Avg.        High          Low       Avg.
Date   mg/1   Date   mg/1^   mg/1    Date   mg/jl   Date   mg/1   mg/1

8/19    690   8/15    390    442    8/21  1,100   8/15    400    713
                                                                                    INCREASE
                                    High
                                   Low
                                                                                             Date
                                  Avg.
                                                                 Date    %    	  	  	

                                                                 8/21   144   8/15   2.5    61

-------
     FIGURE 16- EFFECT  OF  CaCI2   DOSAGE  ON  TOTAL  DISSOLVED  SOLIDS
                 IN  EFFLUENT  FROM  A.L.M.I.  SYSTEM
o
Ul
   1201-
co
o
IJ  100
o
CO
o
in
CO
80
   60
Ul
CO
<
LU
(T
o
   40
   20
                             O
                                O
                 O
             100       200       300       400       500

                                Ca CI2  DOSAGE ,  mg/l
                                                      600
700
800

-------
                                                   TABLE 16


                                           SUMMARY OF THE CHANGES IN
                                        HARDNESS IN THE A.L.M.I. SYSTEM
01
ro
INFLUENT
High
Date
8/19
mg/1
248
Low
Date
9/3
mg/1
172
Avg.
mg/1
209
                                                        EFFLUENT
                                                              Low
    High          Low	   Avg.
Date   mg/1   Date   mg/1   mg/1

8/21    668   8/19    96     284

8/19*   218*                 166*
                                                   CHANGE
High
Low
                                                                                Date    %

                                                                                8/19   -56
         Date_

         8/21
   +660
Avg.
+ 36

-20*
                            *  Excluding two (2) extremely high values on 8/21

-------
  lOOr-
   90k
   80
   70
   60
<  50
o
2  40
   30
     FIGURE 17-EFFECT  OF pH  ON  P04  REMOVAL
    10
                IN THE  A.L.M. I.  SYSTEM
                             8
                            PH
                                             10
                          53

-------
 too
  90
                      FIGURE 18 - EFFECT  OF  Ca CI2  DOSAGE  ON
                        £     A   P04  REMOVAL  IN  THE A.L.M.I.
                                  SYSTEM
  80
  70
   CaCI2 ONLY

   CaCI2 + NaOH
   ALUM ADDED, SETTLED IN
   WINFAIR SYSTEM, THEN CoClg ADDED
  60
5
  so
o.
#
  40
  30
  20
  10
        100  200   300  400      600
                CaCI2  DOSAGE, mg/l
BOO

-------
                                                    TABLE 17
                                  SUMMARY OF  PO^. REMOVAL IN THE A.L.M.I. SYSTEM
                 INFLUENT
           High
Low
        Date mg/^ Date mg/1 mg/1

        9/11  199 8/12   84   146
                             EFFLUENT
                                       REDUCTION
High
Low    Av(
                          Date mg/1 Date m_g_/_l_ mg/1

               CaCl2 Only 9/11   199 8/21   55    113
High
Low   Avg.
                                     Date   %   Date  _%	%_

                         CaCl2 Only  8/21   50  9/11   0   22.6
                                              9/20   0
en
en
               CaCl,
                                     NaOH
                                                8/28   28 8/29   3  11.7
                         CaCl.
                                                       NaOH
                                                                  8/29  98 8/28 86   94
                                    Alum;
                                  Settled  In
                                    Winfair;
                                  Then  CaCl2
                           9/22   36  9/22    9     24
                          Alum;
                       Settled  In
                         Winfair;
                       Then CaCl,,
                          9/22  95 9/22 80   87

-------
3 mg/1, representing a 98% reduction, was obtained using Pitcher Celatom
in a 50 Ib. charge with the addition of NaOH to a pH of 9.55, and 435
mg/1 of CaCl  with 18.3 mg/1 of Roccal (23.77 to 1 ratio).

Alkalinity

The results of the alkalinity are summarized in Table 18.   The average
alkalinity in the raw waste was 368 mg/1 with a range of 340 to 420 mg/1.
With no addition of NaOH, there was an average slight reduction in alka-
linity to 329 mg/1.   With the addition of NaOH, the alkalinity increased
to an average of 475 mg/1.

Acidity

The results of the acidity are summarized in Table 19.   The average acid-
ity in the raw waste was 91 with a range of 73 to 124 mg/1.  With no NaOH
added, the average acidity showed a slight increase to 112  mg/1 during
treatment.  Upon addition of NaOH the acidity was lowered to an average
value of 31 mg/1, with occasional instances of completely removing the
acidity (pH > 8.3).

Optimum Operating Conditions

There was no one set of operating conditions which produced the maximum
reduction of all parameters of pollution.  However, the best overall
results, as shown in Table 20, were produced under the following con-
ditions:  (1) 50 Ibs. of Pitcher Celatom as filter aid; (2) a three
minute pre-coat time; (3) 567 mg/1 of CaCl2; (H) 23.8 mg/1 of active
Roccal during a 7,530 gallon run; and (5) with the addition of NaOH.
This combination of treatment resulted in:  (1) 98% reduction of ABS
from 21.6 mg/1 to .20 mg/1, satisfactory for USPHS Drinking Water Stand-
ards; (2) a 73% reduction of BOD from 133 to 34 mg/1; (3)  an 85% reduc-
tion of COD from 285 mg/1 to 45 mg/1; (4) a 94% reduction of POi^ from
169 mg/1 to 6 mg/1;  (5) a 97% transmittance for turbidity of the efflu-
ent; (6) no significant change in acidity; (7) raising the pH from an
influent value of 7.2 to 8.5; (8) increasing the total dissolved solids
(TDS) 44% from 488 mg/1 to 715 mg/1; (9) little change in the alkalinity;
(10) an 8% increase in the hardness from 208 mg/1 to 266 mg/1; and (11)
< 10 coliform/100 ml when chlorinating the effluent.
                               56

-------
                                           TABLE 18
                    SUMMARY OF THE ALKALINITY IN THE RAW AND TREATED WASTE

              INFLUENT                          EFFLUENT                         EFFLUENT

                                             NO NaOH ADDED                      NaOH ADDED
    High
Low
AVE
High
Low
Date   mg/1   Date   mg/1   mg/1   Date   mg/1   Date   mg/1

9/3     420   8/21    340    368   8/19    350   8/21    288
Avg.
mg/1
                                              329
High
Low
                                          Date

                                           9/3
                                      mg/1

                                       500
                               Date

                                9/3
                 mg/1

                  452
          m.g/1

           475
                                           TABLE 19

                      SUMMARY OF THE ACIDITY IN THE RAW AND TREATED WASTE

            INFLUENT                           EFFLUENT

                                             NO NaOH ADDED
                                                                 EFFLUENT

                                                                NaOH ADDED
    High
Low
Avg.
High
Low
Avg.
Date   mg/1   Date   mg/1   mg/1   Date   mg/1   Date

9/3     124   8/19    73     91    8/19    158   8/19
High
Low
Avg.
                                      mg/1   mg/1   Date   tng/1   Date   mg/1   mg/1

                                       87     112   9/3     68    9/3      0     31

-------
                                                   TABLE 20

                            OPTIMUM COMBINATION OF CHEMICAL AND MECHANICAL FACTORS
                            IN REMOVAL OF POLLUTANTS AND PATHOGENS FROM LAUNDROMAT
                            WASTE WATER IN THE A.L.M.I. WASTEWATER TREATMENT SYSTEM,
                            FILTER AID-PITCHER CELATOM USING A 3 MINUTE PRE-COAT
                            TIME-RESULTS BASED UPON 7530 GALLONS OF TREATED WASTE.
en
oo
Filter Aid
Dosage
50 Ibs.
COD
Inf. Eff.
mg/1 mg/1
285 45
Acidity
Inf. Eff.
CaCl2
Dosage
567
(mg/1)
Red'n.
85
Red'n.
%
Active Roccal
Dosage 1
23.8
(mg/1)
TDS
Inf. Eff. Incr.
mg/1 mg/1 %
488 715 44
Alkalinity
Inf. Eff. Incr.
/i <-| g.
                                                    NaOH

                                                    Yes

Inf.
mg/1
21.6
Turb.
% Trans.
Eff.
ABS
Eff. Red'n. Inf.
.20 98 133
P04
Inf. Eff. Red'n.
mg/1 mg/1 %
97 169 6 94
Hardness Coliform/100
Inf. Eff.
mg/1 mg/1
Incr. Inf.
%
BOD
Eff. Red'n.
mg/1 %
34 73
pH
Inf. Eff.
7.2 8.5
ml
Eff.
         91
89
368
372
208
266
> 2,000
< 10

-------
                           SECTION XI

                  DISCUSSION OF THE ALMI SYSTEM

The first criterion for a satisfactory effluent is that it meet health
department standards.  In New York, this demands (1) an effluent which
manifests a coliform count of zero after chlorination based upon a 1 ml
sample and (2) a reduction of 75% in biological oxygen demand.  The ALMI
System meets the requirement with respect to the elimination of coliform
organisms and at optimum conditions achieves a 73% reduction of BOD.
The AriS and total solids in the effluent meet the U.S.P.H.S. drinking
water standards.

The second requirement of a wastewater treatment system is the ability
to handle peak loads as well as normal demands.  The ALMI System proved
able to treat a maximum of 25-26 gpm and also produce a satisfactory
effluent at a regular flow of 14-15 gpm resulting in a total daily flow
of 6300-8500 gallons per day.  At two runs per day this unit can treat
a total of 7530 gallons per day.  At a maximum average flow of 587 gpd
per washing machine as shbwn in Fig. 1, the maximum average daily efflu-
ent from 12-13 machines could be treated in these two runs.  It required
252 minutes or 4.2 hours to treat the average daily effluent from approx-
imately seven machines.  Based upon a 12 hour day, the ALMI system could
treat the average daily flow from approximately 20 machines.  The holding
tank of 4000 gallon capacity provided storage during peak flows.

The third requirement is that it requires a minimum of service, opera-
tional and maintenance skills and operator time.  After the optimum com-
bination of chemical and mechanical aids was determined, it required
very little time to add the DE charge and refill the chemical solution
reservoirs.  However, with two runs a day, the operator would have to
return to add the second DE charge.  All the other operations were such
that the system could be activated automatically by a float valve in
the holding tank.  It would be possible to install an automatic DE
charging setup so that the system could operate unattended during the
weekend which is usually the peak usage period of the laundromat.  Also
the sludge holding tank must be pumped out periodically, approximately
on a weekly basis.  This is best handled by a conventional septic tank
service.                        ,
                                /
The fourth criterion is easily met be the ALMI system  which was dis-
mantled and removed to the R.P.I, laboratories with a minimum use of
labor and transport facilities.  It should be noted, however, that re-
moval of the 4,000 holding tank, 1,000 gal. clean water tank and 1,000
gal. sludge tank was not included, as these are fairly permanently
installed in the ground.

As for the space requirement, the fifth criterion, the ALMI system, ex-
clusive of holding and storage tanks, required no more than 80 square
feet, including storage of filter aids and chemicals, with a normal
ceiling height.
                               59

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An estimate was made for the cost of operation of the system.   This was
broken down as follows:

                                                    cost/8,500 gal. day

   Chemicals              $1.00/1,000 gal.                  $  8.50

   Electric power    1.5 KW/hr., 9 hr./day @ 3C/KW             .50
   Labor, maintenance     1 hr./day @ $2.25/hr.               2.25
   Sludge scavenging           $20/wk.                         3.00

   Misc.                                                       .75
   Total

Based upon 30 gallons per wash, there are approximately "-*VA"   280 washes
per day.  At $15.00 per day, this results in ^fso"   6*/wasn-   This value
is slightly high, and would require the addition of at least 5£ to the
cost of each wash.  This value does not include amortization of the cost
of the treatment equipment.  This would probably increase the total cost
for treatment to IOC per wash.  This is a significant increase in the
cost.  Thus, this system does not meet the requirements for an economical
system.

The goal of recycling water for further use should be an ultimate aim of
any waste water treatment system.  In terms of reduction of spent deter-
gents, phosphates, coliform organisms, turbidity, organic nitrogen, BOD
and COD, the effluent could be reused for uses other than drinking.
However, the increases in TDS, and pH, while within the upper limits of
U.S.P.H.S. drinking water standards, might not be suitable for certain
agricultural and industrial uses.  Furthermore, the increase in alkalinity
and hardness, due to the addition of NaOH, and the high ratio of CaCl2
to Roccal (22.3:1) in order to increase PO^ removal, render very question-
able the suitability of the effluent for reuse without softening and pH
adjustment.

The American Laundry Machinery Industries Diatomaceous Earth Filtration
System can thus be an effective system for the treatment of laundromat
wastes.  Whereas there was no single optimum operating condition under
which all waste parameters were removed to the greatest extent, there can
be reached an optimum chemical addition and operation which will effect-
ively treat the waste and render it safe for certain reuse or discharge
into a receiving water.
                               60

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                           SECTION XII

                        ACKNOWLEDGEMENTS

The laboratory studies in this project were supported by the New York
State Department of Health, Division of Laboratories and Research.

The authors would like to thank Mr. James A. Messina for allowing the
use of his laundromat treatment equipment for this project, Mr. Ralph
Carpenter for providing the building to house and the power to operate
the equipment, and Mr. Edwin Lagasse for cooperating in providing the
laundromat waste .  Diatomaceous Earth for this study was provided by
the Johns-Manvilie Corp., Celite Division.

The operational studies were supported by a grant from the Federal
Water Pollution Control Administration (now Federal Water Quality
Administration), Department of the Interior.  Special thanks is also
extended to Mr. Richard Keppler, Project Officer, for his guidance.
                                61

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                           SECTION  XIII

                            REFERENCES

 1.   Black,  Hayse  H.,  and Spaulding, Charles H.,  "Diatomite Water Filtration
     Developed for Field Troops," Jour.  AWWA 36_,  1208 (Nov. 1944).

 2.   Eckenfelder,  Wesley, Proceedings  of 19th Industrial Waste Conference,
     Purdue  University,  (1964)  p. 467.

 3.   Flynn,  J.M.,  "Long  Island  Ground  Water Pollution Study Project,"
     Proceedings at 1st  Annual  Water Quality Research Sumposium, New York
     State Department  of He lath, Albany, N.Y. (Feb.  1964).

 4.   Flynn,  J.M.,  and  Andres, B., "Launderette  Waste Treatment Processes,"
     Jour. Water Poll.  Control  Fed.,  35, 783 (1963).

 5.   Paulson,  E.G., "Organics in Water Supply," Water and  Sewage Works,
     110, 216, (1963).

 6.   "Removal  of Synthetic Detergents  from Laundry  and Laundromat Wastes,"
     Research  Report No. 5, New York State Water  Pollution Control Board,
     Albany  (March I960).

 7.   Robeck, G.G., Bryant, A.R., and Woodward,  R.L.,  "Influence of ABS on
     Coliform Movement Through  Water-Saturated  Sandy Soils," Jour. AWWA
     54_, 75   (1962).

 8.   Rosenthal, B.L.,  O'Brien,  J.E., Joly, G.T.,  and Cooperman, A.,  "Treat-
     ment of Laundromat  Wastes  by Coagulation with  Alum  and Adsorption
     Through Activated Carbon," Mass.  Dept.  of  Public Health, Lawrence
     Experiment Station, (March 1963).

 9.   "Standard Methods for the  Examination of Water and  Wastewater,"
     12th ed., A.P.H.A., New York,  (1965).

10.   Weber,  W.J. Jr.,  and Morris, J.C.,  "Kinetics of Adsorption on Carbon
     from Solution," Jour. San. Eng.  Div., A.S.C.E.  89,  SA2, 31 (1963).
                                63

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                           SECTION XIV

                            GLOSSARY

ABS - Alkyl benzene sulfonate; a constituent of  detergents;  in this
paper used to connote both the older branched-chain non-biodegradable
forms and the newer LAS.

Anion   An electronegative 3on.

Cation - An electropositive ion.

Cerearia - The larval form of a parasitic worm.

Coliforms - A group of  bacteria, native  to  the human  intestinal  tract,
used as a water pollution index.   The  concentration of coliform  bacteria
is indicative of the extent of fecal contamination to the  water.

Cysts - A capsule surrounding a microorganism  in its  resting state;  it
is shed after the organism resumes activity.

Diatomaceous earth  - A  fine earth  derived from the cell  walls of diatoms
and used as an absorbent.

LAS - Linear alkyl  benzene sulfcnate;  now a conrtituent  of the new bio-
degradable detergents.

Roccal - The commercial name for a quaternary  ammonium  compound  which
is both a cationic  detergent to remove residual anionic  detergents and
a germicide to kill bacteria.

Schistosome - A genus of worm, parasitic in the  blood of man.

Syndets - Synthetic detergents.
                                65
                                              4U.S. GOVERNMENT PRINTING OFFICE: 1973 5U-15J/200 1-3

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SELECTED WATER
RESOURCES ABSTRACTS
INPUT TRANSACTION FORM
                                                  w
  Treatment of Laundromat Wastes
                                                                            Sept. 1971
  Donald B.  Aulenbach, Patrick C. Town, Martha Chilson
  Rensselaer Polytechnic Institute
  Troy, New York    12181
                                                                   12120 DOD
:-?,TT. -  -w  Environmental Protection Agency
                                                                  Pc'\o^ uo'-cr-.   Final
                                                                 3/1/64 - 11/30/69
           Environmental Protection Agency report
           number, EPA-R2-73-108, February 1973.
  Laboratory and field studies were conducted to evaluate the laundromat waste treat-
  ment capabilities and the effluent recycling possibilities of two systems.  The
  Winfair Water Reclamation System (WWRS) involves the addition of alum at a pH of 4,
  sand filtration, and passage through an ion exchange resin.  The American Laundry
  Machinery Industries (ALMI) Diatomaceous Earth Filtration System employs chemical
  precipitation prior to filtration.

  The WWRS resulted in a 61% BOD reduction, 71% COD reduction, 94% ABS reduction,
  and a buildup of total solids in the effluent.  The system produced an effluent
  suitable for discharge into many streams.  For effluent recycling, a functioning
  demineralizer would be required.

  The ALMI System achieved a 70% BOD reduction, 84% COD reduction, 98% ABS reduction,
  94% PO^ reduction, and complete coliform removal.  The increase in effluent alka-
  linity and hardness render very questionable the suitability of effluent reuse
  without softening and pH adjustment.  The introduction of the system into existent
  laundromats would increase the cost of washes by about IOC.
    Ids x'
JO. 
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