SURVEY OF METAL FINISHING INDUSTRIES
PRINTED CIRCUIT BOARDS
MAY 1973
U. S. ENVIRONMENTAL PROTECTION AGENCY
Surveillance and Analysis Division
REGION I
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TABLE OP CONTENTS
Part I Statistical Summary
Part II Poxboro Company
East Bridgewater, Massachusetts
Part III Raytheon Corporation
Missile Division
Lowell, Massachusetts
Part IV Western Electric
North Andover, Massachusetts
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PART I
STATISTICAL SUMMARY
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TABLE OF CONTENTS
Title Page
List of Figures I—iL
Introduction
Data Analysis 1—4
Conclusions 1—7
Appendix I—A (Probability Plots)
Appendix I—B (EPA’s Proposed Effluent Limits)
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LIST OF FIGURES
Figure No. Description
I—i Frequency of Occurrence versus Total
Metals minus Dissolved Metals
(manganese, zinc, copper, iron)
1—2 Frequency of Occurrence versus Total
Metals minus Dissolved Metals
(manganese, zinc, copper)
1—3 Total Copper minus Dissolved Copper
versus Frequency of Occurrence
1—4 Frequency of Occurrence versus
Absolute Variation of the Difference
between Operating Day Composite Sample
Concentrations and 4-Hour Composite
Sample Concentrations Expressed As A
Percentage of the Operating Day Concentration
(Dissolved Copper)
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SURVEY OF METAL FINISHiNG INDUSTRIES
PRINTED CIRCUIT BOARDS
May 1973
STATISTICAL SUMMARY
Introduction
The U. S. Environmental Protection Agency, Region I, Surveillance
and Analysis Division (S & A), was requested to sample and analyze the
waste from metal finishing industries having “well run” waste treatment
facilities.
The purpose of this survey was to gather information on which to
base effluent limits. The sampling program emphasized industries manu-
facturing printed circuit boards. Diverse treatment systems and wastes
having a variety of heavy metals were desirable features to incorporate
in the study. Because Lancy integrated treatment systems had been
examined during a previous study of small metal finishing plants (less
than 20,000 gallons per day), Lancy systems were not incorporated in
this study.
The Commonwealth of Massachusetts, Division of Water Pollution
Control, supplied the names of five metal finishing companies which
they considered to have “well run” industrial waste treatment plants.
Of the five companies named, two manufactured jewelry, and one of these
has a Lancy system. The remaining three companies (Foxboro Company,
East Bridgewater; Raytheon Corporation, Lowell; and Western Electric
Company, North Andover) manufacture printed circuit boards; therefore,
these three companies were selected for the study.
I—i
-------
All three companies incorporate similar treatment systems: co—
precipitation of metal hydroxides preceded by chromium teduction and
cyanide destruction systems where applicable. Foxboro Company does
not use chromium or cyanide in its process. Raytheon Corporation follows
precipitation with sand filtration.
During the study the Foxboro and Western Electric treatment plants
were not operating properly. The Foxboro plant was having problems
with coagulation and settling. Alum was used as a coagulant which formed
a fine floc that remained in suspension, and was discharged with the
final effluent.
Western Electric’s treatment system was hydraulically overloaded.
The average daily flow was 20% higher than design capacity and peak
flows were 50% higher than design. Also, nineteen hours after the
start of the sampling period, the treatment plant suffered an “upset”.
The ferric chloride (the coagulant) proportioning pump failed. For the
remainder of the survey, ferric chloride was gravity fed through a hose,
first to the acid/alkali waste stream, and later to the rapid mix cham-
ber. The feed rate was manually adjusted. Because of these conditions,
the data from Western Electric is of dubious value; however, it will be
included in this analysis to show trends in data.
Raytheon’s treatment plant, on the other hand, was operating at
only 30% of design capacity. Therefore, the data from this plant may
show better treatment efficiencies than might be experienced at or near
design capacity.
1—2
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Data Analysis
The data was analyzed to:
1. Determine how the plants were operating at the time of the
survey with respect to historical data.
2. Compare the data with EPA’s proposed effluent limits for metal
finishing industries.
3. Determine the relationship between dissolved and total metal
concentrations.
4. Determine the relationship between waste concentrations in the
operating day and 4—hour composite samples.
Probability plots were used to make the preceding determinations.
The first analysis determined how the treatment plants were operating
compared with historical data. Foxboro Company and Western Electric
submit monthly operating reports to the Massachusetts Division of Water
Pollution Control, and these reports provided histroical data. Raytheon
Corporation could not be analyzed in this manner because routine operating
reports were not available.
Examination of the flow records and Figure 11—3 showed that Foxboro
Company was operating at flows which provided representative hydraulic
conditions (39% and 80% probability that flows would be equal to or less
than the flows recorded).
The Western Electric flow plot (Figire IV—8) shows that flows would
be less than those during the survey 99.9% of the time. The plot also
shows that the flows should be less than the design capacity 99% of the
time. Interestingly, historical data showed a tendency for the flow to
increase with time (Appendix IV—D). The lowest monthly average daily
flows were reported in April 1972, and the highest in April 1973. The
1—3
-------
April 1973 average daily flow was 1,220 cubic meters (0.33 MCD), a
value which probably will be exceeded less than 15% of the time, unless
production rates have increased.
Historical data were also plotted for total copper at Foxboro
Company (Figure 11—4 and Western Electric (Figure IV—2). Based upon
operating—day composite samples, the total copper concentration in the
final effluent at Foxboro Company can be expected to be less than the
survey values (1.96 and 1.92 mg/i) 97 percent of the time (See Figure
11—3), and at Western Electric the expected concentrations will be equal
to or less than the survey values (1.76 and 2.54 mg/l) 80 and 86 percent
of the time (see Figure IV—2).
Western Electric Company performed monthly analyses on a number of
parameters, and it was possible to determine the reliability of the
data collected during the survey with several other parameters: dis-
solved fluoride, cyanide and total phosphorus. The operating day com-
posite concentrations in the effluent from Western Electric Company
could be expected to equal or be less than the survey data as follows:
dissolved fluoride (11.8 and 14.8 mg/i) 59 and 75 percent of the time
(Figure IV—5), total phosphorus (9.18 and 0.42 mg/i) 18 and 44 percent
of the time (Figure IV—4), and cyanide (1.75 mg/i) 56 percent of the
time (Figure IV—6).
Because wastes from the manufacture of printed circuit boards
primarily result from metal finishing, the survey data were reviewed
with respect to EPA’s proposed limits for the metal finishing industry
dated January 1973 (see Appendix I—B).
1—4
-------
Based upon operating day influent composite samples, total and
dissolved copper were potential problems at the three companies. At
Foxboro Company, dissolved lead also presented a potential problem.
At Raytheon, total and hexavalent chromium and at Western Electric, total
and dissolved iron, as well as the chromiums, were potential problems.
Following treatment, total and dissolved copper concentrations at
Western Electric exceeded Schedule B limits, as did total and dissolved
iron. At Foxboro Company, total copper concentrations also exceeded
Schedule B limits. Dissolved copper and dissolved lead concentrations
exceeded Schedule A limits. At Raytheon Corporation, total chromium
concentrations exceeded the Schedule B limit.
Many of the other parameters stipulated in the proposal were not
present at the three companies, or the influent concentrations were
less than the allowable effluent concentrations in Schedule A.
The relationship between dissolved and total metals was also ex—
amined Of course, with Western Electric being hydraulically over-
loaded and Foxboro Company having poor floc formation, such an examina-
tion is somewhat academic but may prove useful. Realizing that the
settling which would occur at design capacity or with proper floc for-
mation was not occurring, and realizing that proper removal would in-
crease the slope of the probability, a 70% probability that values will
be equal to or less than a measured concentration should provide a
satisfactory indicator of attainable concentrations. Figure I—i shows
the relationship between the total and dissolved forms of iron, copper,
zinc and manganese. Seventy percent of the time the difference between
1—5
-------
the total and dissolved concentrations was less than 1.1 mg/i. If iron,
found only at Western Electric Company and causing significant problems
there, is not plotted (Figure 1—2), the 70% probability value is 0.67 mg/l
and approximately 80% of the time the value would be less than 1.0
mgIl. With zinc and manganese plotted the curve is biased to show low
differences between total and dissolved metal concentrations. Removing
these two from the plot leaves copper, a metal which was a potential
problem at the three companies. The probability curve for only copper
(Figure 1—3) shows that 70% of the time the difference between total
copper and dissolved copper would be equal to or less than 1.25 mg/i.
Another analysis performed was evaluating the relationship between
4—hour composite samples and the operating day composite samples. Since
copper was the only metal which was present at all companies and had
the potential for creating problems, dissolved copper was used to make
the comparison. The absolute difference (plus or minus) between the
concentrations in the 4—hour composite samples and in the operating day
composite samples were taken as a percentage of the operating day con-
centrations and plotted against the percent occurrence (see Figure 1—4).
Foxboro Company’s waste had the least absolute variation. The
variation ranged from 4.2% to 33.3% of the operating day concentrations.
Surprisingly, the variations at Raytheon Corporation (job—shop operation)
were also low, ranging from 16.7% to 33.3%.
Western Electric’s waste exhibited large variations, from 13% to 113%
as shown in Figure 1—4. Figure 1—4 does not include data related to the
May 31 operating day composite sample at Western Electric. The 4—hour
1—6
-------
composite sample collected from 0400—0800 on June 1 contained 8,400 mg/i
of dissolved copper. This concentration predominated the operating day
concentration (see Table IV—6), and in so doing prevented meaningful
interpretation of the 4—hour composite samples versus the operating day
composite sample.
Whether or not the fact that Western Electric Company operates
24 hours a day (three shifts) influences the variation is debatable.
Foxboro Company and Raytheon Corporation generally operate approxi-
mately eight hours per day (one shift). Chances are Western Electric’s
wastes will vary more from shift to shift. On both sampling days at
Western Electric waste strength increased significantly after midnight,
however the reason this occurs is unclear. Was it normal for the oper-
ating cycle or was it associated with the malfunctioning chemical feed
system?
Based upon the data gathered, Figure 1—4 shows that 66% of the time
the absolute variation between the 4—hour composite samples and the
operating day composite sample will be within 50% of the operating day
composite sample value. It also shows that 85 percent of the time the
variation will be less than twice the operating day composite sample
value.
Conclusions
Based upon the probability plots, and considering the way the plants
were malfunctioning during the study, Schedule A of the proposed effluent
limits for metal finishing industries January 1973, appear to be viable
limits for manufacturers of printed circuit boards.
I—?
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APPENDIX I-A
Probability Plots
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-------
APPENDIX I —B
EPA’s PROPOSED EFFLUENT LIMITS FOR
METAL FINISHING INDUSTRIES
JANUARY 1973
-------
4’
UNITED STATES ENVIRONMENTAL PROTECTION AGENCY
‘l O WASHINGTON. D.C. 20460
81 JAN 1973
.MEMORANDU
TO: All Regional Permit Program Directors
FROM: Director, Office of Permit Programs
SUBJECT: Revised Metal Finishing Guidance
The Guidance of September 1972 has been revised to include
only those parameters which are of significance and more
directly reflect ind szrial practice. The limit for fluoride
has been ncreasedto a level resülfin9from unit process
stream precipitation. Relative to pollutiun abatement, this
is not an increase in allowance. The other limits are derived
essentially on this basis as well.
The Guidance should be applied only to establishments using
20,000 G?D or r ore of p -3ceSS water.
The parameter limits are expressed in units of pounds per
1000 gallons of process water. This reflects emphasis given
to-pounds limitations in other industrial categories.
Specifically such parameters as ammonia, phosphorous,
refractory cyanide, and arsenic have been excluded. For
chromium, the separate parameter for the dissolved trivalent
form is excluded.
From the 1967 Census of Vanufacturer, Rureau of Census it
is estimated that this Guidance aoplies to 44°c of the total
number of establishments accounting for 88% of the total value
of shipments by establishr ents in the SIC 3471 cateaory. It
is estimated that this Guidance applies to 39% of the total
number of estab1ish ents and 9i of the total value of shipments
by establishments in the SIC 3479 category.
C. Printz, Jr.
-------
I
DTSCI c ( L1Ifl S F0 TW I’:T . rr’s’ , I’3JST Y (a). (b )
(c)
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2.0 0.0 67
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5 — 9 1
(a) Pietal concentrations are based on analysis of filtered clear solutions.
(a) Tue Riaatmum pcrnassible concentration for a particular meta’. In the to a1s ispan ed solids shall be mgil . (0.00834 lbt/l,000 gal.)
ioted for Chromlirn.
(c) Limited slgniftcance In this ind istry, should be consIdered on case by case basis.
! A?’E T Q
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-------
PART II
FOXBORO COMPANY
EAST BRIDGEWATER, MASSACHUSETTS
-------
TABLE OF CONTENTS
Title Pa No .
List of Tables I l—i l
List of Figures fl- ui
Introduction 1 1-1
Waste Treatment 11—2
Sampling Program 1 1—4
Analytical Results and Conclusions 11 —6
Snnvnpry of Conclusions 1 1—16
Appendix Il—A (Monthly Operating
Reports)
Appendix It-B (EPA Proposed Effluent-Limits for
Metal Finishing Industries)
Appendix I l—C Probability Plots
-------
LIST OF TABLES
Table No. Title Page No .
1 1—1 Process Waste Flow at the Final Effluent 11—5
11—2 Sta tion Locations 11—7
11—3 Standard Abbreviations and Units of Measure 11—8
11—4 pH and Temperature 11—9
11—5 Analytical Data (General Analyses) 11—10
11—6 Analytical Data (Heavy Metals) 11—12
“—ii
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LIST OF FIGURES
Figure No. Title
I L—i Flow Diagram, Foxboro Company, Industrial
Waste Treatment
11—2 Ammonium Persulfate Closed-Loop Recovery
System
11—3 Flow, Frequency of Occurrence
11—4 Total Copper, Frequency of Occurrence
11—5 Total Phosphorus, Frequency of Occurrence
“—iii
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FOXBORO COMPANY
EAST BRIDGEWATER, MASSACHUSETTS
Introduction
Foxboro Company, East Bridgewater, Massachusetts manufactures
printed circuit boards, electrical metering devices, relays, switches,
and valve controls. The plant operates from 0700 to 1530 hours Monday
through Friday and employs approximately 700 persons, 60 of whom work
in the circuit board department. Eight persons are employed in the
plating room.
Foxboro Company discharges process wastes at a rate of 170 liters
per minute (45 gallons per minute). The waste flow is attributable
to the manufacture of circuit boards. Most of the flow is from the
plating room with 75 liters (20 gallons) of developer (lZ sodium
carbonate) discharged twice daily from a photo dry film room.
Three years ago the company was manufacturing approximately 30
boards per week. Currently production figures are averaging 750 boards
per week and the company is contemplating expanding production to 2,000
boards per week. The circuit boards are 30.5 centimeters by 45.7
centimeters by 0.3 centimeters thick (12” x 18” x 1/8”) sheets of a
glass epoxy onto which the company plates copper. The plated boards
are drilled to accept electrical components and then replated to plate
the holes. Following the second plating, they are sent to a dry film
photo room or to a silk screening operation to prepare the boards for
circuitry.
-------
In the dry film room, ultra—violet light sensitive materials are
laminated to the board. A circuit template is placed on the board and
the board is fed through a printer. Ultra—violet light exposes
and polymerizes areas of the board where no circuitry is desired.
The board is then developed in a 1% solution of sodium carbonate which
removes the photo laminate material where circuitry is desired. The
board then goes back to the plating room where it is cleansed and
fluoboric plating operations deposit one mu of copper on the
circuitry. Following this, solder is plated over the circuitry. The
solder prevents removal of the copper circuitry when ammonium per—
suif ate etches extraneous copper plating from the boards. Following
the etching rinses the boards are sent to other areas of the plant to
receive electrical components. Figure lI—i is a flow diagram of the
processes.
Waste Treatment
Foxboro Company has removed problem wastes from it production
line. At one time, chromium was used in the production of circuit
boards. The company had designed and constructed a chrome reduction
system, but because they had difficulty controlling chromium levels in
the waste stream, they removed chromium from the plating line.
Because of the difficulty of removing ammonia nutrients from the
waste stream, Foxboro Company replaced ammonium persulf ate with
sodium persulfate as a cleaning agent prior to plating operations.
However, ammonium persulfate is still used in the copper etching opera—
tion at the end of the plating line. This etching operation is a
closed loop system.
I 1—2
-------
NaOH
Cleaner
1_RinseI-
( Sodium
Persuif ate
( NaS 2 0
( lO°k
f Cleaner
100/, HC1
/ Cleaner
•rI
I E: ii1 -
Stannous
Chloride
( L Sensitizer
F luoborate
Copper
Plate
Ac id
cleaner
pH 4.0
N Drying
Sodium Carbo
E I Developer
0I
0I
I
E I i Ultra-violet
-1II
.,-l J I
Exposure
ii
>%
$-iI
I
Circuit
o
i-ia Template
0I
. I
‘
\
ii
natej I
I
I
I I
j i
I
I
I
I
I
I
Photo-sens tive
Laminate
Silk Screening /
for Circuitry
FLOW DIAGRAM
Foxboro Company
F luoborate
Copper
Plate
Sodium
Persuif ate
NEUTRALI ZATION
TANK
Chemical Feed
&
Mixing
Palladium
Chloride
Activator
c o
SETTLING
TANK
Rinse i
FIGURE lI—i
-------
Foxboro Company disposes of its process wastes in three ways——
chemical—physical waste treatment, scavengers and sanitary landfill.
The photo room wastes and rinse wastes from the plating room are
subjected to a physical—chemical treatment system. The wastes are
gravity fed to a neutralization tank where they are buffered to approxi-
mately pH 8.0 and alum is added as a coagulant. The wastes are
then pumped to a settling tank having a detention time of approximately
two hours. Following the settling tank, a pH sensor records the pH
of the final effluent and controls chemical addition in the neutral-
ization tank.
The anzmonium persuif ate etching is a closed loop system utilizing
ion exchange. Aninonium persulfate is fed from a holding tank into the
etching tank. The strength of the etchant is electronically recorded
to determine when new etchant is required, the used solution is trans—
ferred to a holding tank and bled to a recovery system. The recovery
system is a refrigeration unit which lowers the temperature of the used
etchant below 4°C. At temperatures less than 4°C, the copper compounds
crystallize, are caught in bag filters, and sold to a scavenger. The
remaining solution is returned to the persulfate feed tank.
When the circuit boards leave the etchant, they pass through a
series of rinses. The rinse waters are treated in ion exchange
columns and recycled to the rinse tanks • The anion exchange column
is periodically regenerated with sulfuric acid and the backwash is
returned to the ammonium peráulfate feed tank. The cation column is
regenerated with sodium hydroxide and the backwash material is
barrelled and sold to scavengers. Figure 11—2 is a diagram of the
ammonium persulfate closed loop system.
11—3
-------
Board
a)
U
Equation for recovery unit:
Cu + (NH4)S20 8 -1. CuSO4(NH4)2S0 2 + 6H20
<4°C
AMMONIUI4 PERSULFATE CLOSED-LOOP
RECOVERY SYSTEM
-------
Concentrated wastes from the plating operation have posed a
problem to Foxboro Company. In the past, they have disposed of con-
centrated wastes at the East Bridgewater sanitary landfill. The
company had dug a special leaching pit at the landfill for the
disposal of the concentrated wastes, but because of new state regu-
lations regarding hazardous materials, the sanitary landfill will
no longer be able to accept these wastes. Therefore, Foxboro Company
is planning to place these wastes in a holding tank and slowly bleed
them into the current industrial waste treatment system.
Sampling Program
On May 17 and 18, 1973, personnel from the Environmental Protection
Agency Region I collected samples at Foxboro Company, East Bridgewater,
Massachusetts.
The circuit board production was 200 boards per day and waste flows
ranged from 60 to 240 liters per minute (1pm) [ 15 to 64 gallons per
minute (gpm)J and averaged 160 1pm (43 gpm). Based upon historical
data (See Appendix Il—A) these are typical daily flows. Table 11—1
presents the flow data collected, and Figure 11—3 shows the probability
of occurrence of the daily flows based upon historical data.
Foxboro Company was having problems with coagulation. The alum was
forming fine floc that was remaining in suspension. Some was being
carried through the baffles and out of the settling tank. Company
personnel said that they had tried a polyelectrolyte, but it had not
proved to be an effective coagulant for metal hydroxides. The personnel
said that they were planning to try some other polyelectrolyte in the
near future.
11—4
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TABLE LI—i
Process Waste Flow Recorded at Final Effluent (FCO3)
FOXBORO COMPANY, EAST BRIDGEWATER, MASSACHUSETTS
May 17 and May 18, 1973
Date Time FLOW
Hours Liters per minute (1pm) Gallons per minute (gpm)
05/17/73 0815 150 40
0915 140 38
1015 180 47
1115 190 50
1215 190 50
1315 160 43
1415 140 38
1515 60 15
Average = 150 1pm 40 gpm
Daily Discharge = 109.2 cubic meters — — — 28,860 gallons *
05/18/73 0730 140 38
0830 190 50
0930 240 64
1030 170 44
1130 140 38
1230 170 44
1330 210 55
1430 130 35
Average = 170 1pm 46 gpm
Daily Discharg 86.6 cubic meters — — — 22,880 gallons *
*Reported byFoxboro Company from flow totalizer
11—5
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On each of the two days an eight hour composite sample, two four
hour composite samples and several grab samples were collected at the
influent to the neutralization tank and the effluent from the clarifier.
The composite samples were collected proportional to the plant’s recorded
flow at the time of sampling. In addition, two sets of grab samples
were collected of the waste from the dry film room prior to its being
batch dumped. The samples were analyzed for total and dissolved metals
(copper, lead, nickel, tin), total non—filterable residue, dissolved
fluoride, and total phosphorus. In addition, some grab samples were
analyzed for oil and grease. The sampling stations are identified in
Table [ 1—2 and the analytical results are shown in Tables 11—3, 11—4
and 11—5.
Analytical Results and Conclusions
The sampling crew recorded pH and temperature at the influent to
the neutralization tank and the effluent from the settling tank. The
temperature of the effluent (FCO3) ranged from 21.0 — 24.5°C. The
influent p11 was acidic ranging from 2.5 to 6.3 standard units. The
average value was 4.0 standard units. The pH range of the effluent
was 8.6 — 9.4 and averaged 9.0 standard units, thus the effluent pH
always exceeded the 8.5 maximum specified in the Massachusetts Water
Quality Standards for receiving waters.
Fifty—six percent of the effluent samples exceeded the 9.0 standard
units proposed as a maximum pH in the EPA’s Effluent Limits for the
Metal Finishing Industry, January 1973. Plant records (Appendix It—A)
showed that the pH after clarification ranged from 8.1 — 8.5 during the
11—6
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TABLE 11—2
STATION LOCATIONS
FOXBORO COMPANY
BRIDGEWATER, MASSACHUSETTS
STATION DESCRIPTION
FCO1 Surface of neutralization tank
at influent.
FCO2 Developer tray in the dry-film room.
FCO3 Effluent from settling tank.
11—7
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TABLE 11-3
SAMPLE ANALYSES
STANDARD ABBREVIATIONS AND UNITS OF MEASURE
ANALYSIS REPORTED DESCRIPTION MEASURED IN
Temperature Sample temperature at Degrees Centigrade (°C)
time of collection
pH Standard Units (SU)
Total Non—Filterable Total suspended solids Milligrams per liter
Residue (mg/i)
Dissolved Fluoride mg/i as fluoride
Total Phosphorus mg/i as phosphorus
Oil and Grease mg/i as oil and grease
(hexane extractable)
Cyanide mg/i as cyanide
Hexavalent Chromium Micrograms per liter
(Cr+ 6 ) (ugh) as hexavalent
chromium
Total Metals Total: Copper ugh
Nickel
Zinc
Tin
Lead
Cadmium
Chromium
Silver
Manganese
Iron
Dissolved Metals Dissolved: Copper ugh
Nickel
Zinc
Tin
Lead
Cadmium
Silver
Manganese
Iron
Letters Preceding a Reported Value Denote the Following:
J — value not accurate (estimated)
K — actual value is known to be less than value given
R — sample lost
-------
TABLE 11—4
pH AND TEMPERATURE
FOXBORO COMPANY — EAST BRIDGE WATER , MASSACHUSEflS
DATE TIME FCO1 FCO3
pH TEMP. pH TEMP.
5—17 0815 5.9 25.0 8.7 21.0
0915 5.2 27.5 8.8 23.5
1015 4.3 26.0 8.7 23.0
1115 3.4 24.5 8.6 24.0
1215 3.2 24.5 8.7 23.5
1315 3.2 24.5 8.7 24.0
1415 4.2 27.0 9.1 24.5
1515 6.3 16.0 9.2 240
H
5—18 0730 4.8 26.0 8.6 220
0830 3.4 25.5 9.2 23.5
0930 2.5 25.5 9.4 23.5
1030 3.6 26.0 9.2 23.0
1130 4.1 24.5 9.3 23.5
1230 3.2 25.0 9.2 23.5
1330 3.9 23.0 9.3 23.0
1430 3.1 22.0 9.3 22,0
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TABLE 11-5
ANALYTICAL DATA
Foxboro Company
East Bridgewater, Massachusetts
May 17 and 18, 1973
Total Dissolved Total
Station Non—filterable Fluoride Phosphorus Oil & Grease
No. Date Time Residue (mg/i) (mg/i) (mg/i)
(mg/i)
FCO1 5/17 Comp—8 10 10.8 0.61
0745—1545
5/18 Coinp—8 15 9.2 —
0700—1500
5/17 Comp—4 17 10.2 0.45
0745—1.145’
5/17 Comp—4 7 11.8 0.65
1145—1545
5/18 Comp—4 20 9.2 11.0
0700—1100
5/18 Comp—4 11 8.6 6.01
1100—1500
5/17 1115 — 27.0
5/17 1315 — 15.1
5/17 1515 —. 18.0
FCO2 5/17 1015 18 .4 0.38 —
5/17 1310 13 .5 0.28 —
5/18 1045 18 .3 0.38 —
5/18 1410 11 .4 0.43 —
-------
TADLE 11—5 ‘(Continued)
Total Dissolved Total
Station Non—filterable Fluoride Phosphorus Oil & Grease
No. Date Time Residue (mg/i) (mg/i) (mg/i)
(mg/i)
FCO3 5/17 Comp—8 14 7.6 0.25
0745—1545
5/18 Comp—8 65 5.4 0.66
070 0—1500
5/17 Comp—4 32 9.4 0.20
0745—1145
5/17 Comp—4 18 6.0 0.44
1145—1545
5/18 Comp—4 53 6.2 0.52
0700—1100
5/18 Comp—4 41 6.8 0.74
H 1100—1500
‘1’ 5/17 0915 13 70 0.15 —
5/17 1115 5 7.6 0.23 26.5
5/17 1315 12 8.2 0.21 12.5
5/17 1515 4 7.2 0.27 32.7
5/18 0730 35 7.2 0.43 —
5/18 0930 16, 5.6 0.57
5/18 1130 19 6.6 0.77
5/18 1330 15 6.8 0.47
-------
TABLE 11—6
ANALYTICAL DATA
Foxboro Company
East Bridgewater, Massachusetts
May 17 and 18, 1973
STATION COPPER (ugh) LEAD (ugh) NICKEL (ugh) TIN (ugh)
NUMBER DATE TIME TOTAL DISSOLVED TOTAL DISSOLVED TOTAL DISSOLVED TOTAL DISSOLVED
FCO1 5/17 Comp—8 13100 12000 750 1(50 40 30 3500 1(2000
0745—1545
5/18 Comp—8 54000 49700 550 400 40 30 4500 K2000
0700—1500
5/17 Comp—4 22700 — 650 1(50 20 1(10 3500 1(2000
0745—1145
5/17 Comp—4 10000 7900 900 650 1(10 1(10 3500 1(2000
1145—1545
5/18 Comp—4 97000 92500 600 500 80 20 4000 1(2000
0700—1100
5/18 Coinp—4 4700 4900 400 350 40 1(10 4000 1(2000
1100—1500
YC02 5/17 1015 3610 J280 J50 1(350 J75 J50 1(32000 1(32000
5/17 1310 J410 J480 J100 1(350 J90 J60 J3000 1(32000
5/18 1045 J500 3200 J50 1(350 J100 J95 1(32000 1(32000
5/18 1410 3520 J370 J100 1(350 3100 390 J2000 1(32000
FCO3 5/17 Comp—8 1960 240 1(50 1 (30 K10 K10 1(2000 1(2000
0745—1545
5/18 Comp—8 1920 280 100 1(50 20 K1O 1(2000 K2000
0700—1500
5/17 Comp—4 1980 160 1(50 K50 20 K10 1(2000 1(2000
0745—1145
-------
TABLE II—6 (Continued)
ANALYTICAL DATA
Foxboro Company
Eas€ Bridgewater, Massachusetts
May 17 and 18, 1973
STATION COPPER (ugh) LEAD (ugh) NICKEL (ugh) TIN (ugh)
NUMBER DATE TIME TOTAL DISSOLVED TOTAL DISSOLVED TOTAL DISSOLVED TOTAL DISSOLVED
FCO3 5/17 Comp—4 2000 230 50 1(50 20 K1O 1(2000 1(2000
1145—1545
5/18 Comp—4 2300 200 100 1(50 20 1(10 1(2000 1(2000
0700—1100
5/18 Comp—4 1840 350 50 1(50 20 1(10 1(2000 1(2000
1100—1500
5/17 0915 2400 — 1(50 K50 10 10
5/17 1115 2790 180 50 1(10 K1O 1(2000 1(2000
5/17 1315 2300 240 1(50 1(50 K10 K10 1(2000 1(2000
5/17 1515 935 — 280 50 1(50 K10 1(10 K2000 1(2000
5/18 0730 740 — 250 1(50 20 K10 1(2000 K2000
5/18 0930 1700 160 150 1(50 50 1(10 1(2000 1(2000
5/18 1130 1890 380 50 1(50 1(10 1(10 1(2000 1(2000
5/18 1330 1660 320 50 1(50 20 1(10 1(2000 1(2000
-------
study period. At the time of sampling the field crew noted that the
recorded pH was considerably less than what they were measuring.
Total non—filterable residue (TNFR) concentrations in the influent
ccmposite samples ranged from 7 — 20 mg/i and based on the 4—hour
composite samples averaged 14 mg/i. The effluent composite samples
had higher concentrations. They ranged from 14 — 65 mg/i and the
four hour composite samples averaged 36 mg/i. These results verify that
floc is escaping and that other coagulants or coagulant aids should
be tested.
The TNFR levels in the effluent exceeded the 10 mg/i which EPA
proposed in January 1973 as the Schedule A TNFR limit upon effluents
from metal finishing industries. However only one sample, the 8—hour
composite collected on 5/18, exceeded the 50 mg/i concentration
stipulated in Schedule B.
Dissolved fluoride, while present, never exceeded the 18 mg/i
limit proposed by EPA. The maximum value reported in the influent
(FOCi) was 11.8 mg/i. Based upon the samples collected, sedimentation
removes approximately twenty percent of the dissolved fluoride.
Total phosphorus concentrations in the effluent ranged from 0.15 —
0.77 mg/i. The significance of these concentrations is difficult to
ascertain without a study of the receiving waters. The Massachusetts
Water Quality Standards have established 0.05 mg/i phosphorus as the
total phosphate concentration allowable in Meadow Brook, thus con-
centrations in the effluent were 3 — 15 times greater than the standard
for receiving waters.
11—14
-------
Oil and grease (hexane extractables) are apparently passing
through the system undiminished. The three grab samples collected
from the neutralization tank (FCO1) contained 15.1 — 27.0 mg/i oil and
grease and three grabs from the effluent contained 12.5 — 32.7 mg/i.
The effluent end of the settling tank has a baffle system to retain oil
films so that they may be skimmed from the tank manually. During
the study period, oil sheens were visible in the settling tank, but
an oil build—up was not evident behind the baffle.
Influent total and dissolved nickel concentrations were less
than 0.1 mg/i and 0.05 mg/i, respectively, and dissolved tin values
were less than the detectable limit (2.0 mg/i). The analyses of
heavy metal samples collected from the dry film room (FCO2) were
reported as approximate values because the samples had high pH values
prior to analyses. The samples had been preserved in the field but
the waste apparently is highly buffered as the pH did not drop below
3.0 standard units as is recommended by EPA Methods for Chemical
Analysis of Water and Wastes .
Nearly all the copper in the influent is dissolved. Averaging
the two influent eight—hour composite samples produces total and dis-
solved copper concentrations of 33.6 mg/i and 30.8 mg/i, respectively.
Total lead values of the influent did not exceed 900 ugh and dissolved
lead concentrations ranged from less than 50 ugh to 650 ugll. Dis-
solved lead concentrations in the effluent were less than 50 ugh.
With the exception of copper, dissolved metals in the effluent
(FC03) were at or less than the detectable limits and total metal
1 1—15
-------
concentrations were less than EPA’s proposed limits (see Appendix Il—B).
Dissolved copper concentrations in the effluent ranged from 160 ugh to
380 ugh, and total copper contrations from 740 ugh to 2790 ugh.
St rnmRry of Conclusions
Foxboro Company’s treatment plant was not functioning well. A
fine floe was visible in the effluent leaving the settling tank and
the pH always exceeded the 8.5 maximum Massachusetts Water Quality
Standards established for receiving waters. Fifty—six percent of the
effluent samples exceeded 9.0 standard units (EPA’s proposed maximum).
The pH controller is apparently malfunctioning. Re—calibration of the
probe and adjustment to the control mechanism will improve the p11 of
the effluent.
Influent copper and dissolved lead concentrations were the only
metals exceeding EPA’s proposed effluent limits, but copper is the only
metal posing a problem at Foxboro Company. Dissolved copper concen-
trations in the effluent were less than the 500 ugh specified under
Schedule B of the proposed limits, but usually exceeded the 200 ug/l
specified under Schedule A. Total copper concentrations in the com-
posite samples did not comply with the proposed effluent limits. Based
upon historical data, 97% of the time the total copper concentrations
will be equal to or less than the average of the concentrations reported
during the study (see Figure 11—4).
The company is experiencing problems with alum coagulation and
precipitation. As a result, total non—filterable residue concentrations
in the effluent are excessive as are total copper concentrations.
11—16
-------
Selection and use of a new coagulant or coagulant aid could reduce
both residue and copper concentrations to levels necessary to meet
effluent limits.
Total phosphorus concentrations in the effluent are 3 — 15 times
higher than the concentration allowable in the receiving waters.
Whether or not the effluent causes a violation of water quality
standards was beyond the scope of the study. Based upon the survey
data, phosphorus concentrations at Foxboro Company can be expected
to be less than 0.5 mg/i 70Z of the time (see Figure 11—5).
Oil and grease (hexane extractables) are escaping the settling
tank and discharging to Meadow Brook. Federal regulations 1 ’ 2 stipu-
late that oil discharges shall not create a film or sheen on receiving
waters, nor cause sludge or emulsions to develop beneath the surface
or upon adjoining shorelines. The problem with oils in manufacturing
processes is that they are usually cutting oils. They are somewhat
soluble and will generally be present in wastes as emulsions. Oils
in these forms are not amenable to simple gravity separation. If
Foxboro Company is to reduce the concentration of oil and grease in
its effluent, an oil—water separator should be installed or the oil
contained at its source.
1. Section 31l(b)(4), Statute 86, 92 USC S 2770.
2. 40 CFR, Section 110.3.
11—17
-------
APPENDIX tI-A
Foxboro Company’s Monthly Operating
Reports
Submitted to
Massachusetts Division of Water Pollution
Control
September 1972 to May 1973
-------
.4SSACXUSETTS WATER RESOURCES COMMISSIOX
DtvIsIo d o
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Ed .?L rd e &/er
CLARIFIER
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DIVISION OF
WATER POLLUTION CONTROL
MONTH A ri1
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Fred Teci.
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.02
7
281
I________
.
21 ()() _cc
.015
MED A . 8.14 8.0 -• 21870 .73 .02 7
-------
.5 WATER RESOURCES COV 1ISS!ON
DIVISION OF
WATER POLLUTION CONTROL ____
pc ?
CLARIFIER
MONTH
March 19 OPERATOR
—‘T
-!: S..;.,
Ch rnr ’-
Tank #1
CHROMIUM T]
2,500 ga1.Ta
tI (“-‘
—
j .
.
7. -
—
7.0
27180
. ..- . .. —
1 i.
——— . .
.02
8
—
i
.
7.0
6.8
2385Q
l.J
.02
8
3
4
!.
7.0
6.8
26080
1.5
.015
8
7 .0
6 . .9
261.10
1.7
.02
7
2_
7.0
Fc ..S
22Z .i 0
1.8
..02
-
- --
-
-
7.1
• 7 .(
lu
6.8
26910
1.2
.02
6--”-
---- -—
--•-
-
-
-
-
6 .R
238R0
iii
.02
7
11
-
2 .
.015
8
i .
7 ...0
6 -
•
!
7.°
6P
.2L 0
i.’6
.02
9
.
6.8
6.s
2.2
.015
9
!
! .
7.0
7.0
6 ,5
6 .s
1.8
1.7
.02
.02
6
8
!L
•
.
18
i .
7.0
6.5
26170
1.2
02
7
.?
I!.
7_..5
7 ..R
7 .2
7.3
23820
26L o0
1..5
.02
.02
7
8
7.8
7.9
7.
7.2
266 0
2 580
1.0
1.1
.02
.015
6
5
24
-__
26
7.8
7.2
28580
1.
.02
7
8.2
7.5
23750
1.7
.015
8
&6
7.6
2 7W
1.
.02
7
8J.i
7.2
21200
2.2
.02
7
7.8 7.2 2 5 0 1.2 . 02
‘OTAL 558660
_(
EDIAt. 6.o 2l rX 1.c .O1
9
.
-
-
7
-------
-. . iR RESOURCES COM M SS 3N
DrVI5IO f OP
..(ER POLLUTIC
1 .’ank I/i 2,500 cal.Ta
‘TT l.n p
(‘i, I Cr ’ T ”
n i. .,
--
!j Ct !)T
‘ Forborô £ o vipa1ly
7L &rcJ e wa/cr
CLARIFIER
MCNTH February
797’ OPERATOR Fred Teceno
I
S
CHROMIUM T
I
7.8
7,h
8
7
7 5
7.2
237 0
1.1
.oi’i
6
7.0
7.0
20110
1.0
.02
7
.
7.0
6.8
2 u8o
1.1
.02
A
I
7 . 1 i
7.1
1.1
O2
8
7.2
6.8
25960
1.
.02
6
fi.
7.2
7.0
23950
1.9
7
10
•
‘-
.
H
-
72
6.8
325)Q_
2.1 -
02
7
.
! 7.
14 7.2
! 7.2
! 7.2
17
18
•7a0
7.0
3 300
22260
2 i4
.02
.02
7—
6
7.0
21090
1.2
02
7
...__‘
7.0
2
-
.019
-
6
,. .
!
20
!
? .
£
7.2
7 .2
1I4 OO
02
7
.
7.2
6.9
1390
1.8
.
8
7.3
7.0
28100
2.6
.02
7
I________
•
7.2
7.0
5160.
2. .l
.02
A
.
7a2
7.0
162o
2..1
.02
A
24
25
?
!?
7.5
7.2
4550
ia
.02
0
—___
7.2
i .6
.02
A
O
7..2
70
1.2
02
.
7
30
5-i-
.1
—_____
-!
,
i
I
,
“ I
k 1 o
—-
.
7.2
7.0 2 31 8 Q_ .L02 -
7
-
-------
C4U 1TS WAT S .ZSCURC S COMMISSION
OtVISION OP
WAT’ R POLLUT!OX COWT1 OL
MONTH Jar ’aa*’r I 73 O?ERATO
Fox bpro Co np y -
East 5r,S9ewa7’ er .
CLARIFIER
-
•
CH CMIUM TE
T k #1 2 ,5C0 gal .Tar
-
- r
•
4
-,
— .L
r
—
——‘-‘ r — —
- -- .——• - - --—---
-
——‘--‘- —‘—
‘•v -’ - -
— — — I..— — 4
11
7.
7.2
1
26b .20
i.
02
9
.
.
I________
7 l
7.2
2W .8o
1.0
02
7 ..0
6.8
i c5o
..9 I
.rn
A
• . ____
7-0
&8
I
6.8
25570
1.0 1
I
.02
6
I
-
7.0
19270 1
1.0
.015
7
7.2
7.0
29950 j
1.1
.02 :
8
1
—____
!. 2. 7.
7.2
278 0
•g
.02
8
—.
71 .
7.0
!
7..2
6J .j
.
2B° 0 I
22850
-
i..O 02 8
11 I 015 -
5
.
14
.
. 7.0
6.8
2 590
.8
.02
7
7.0
6.8
271 20
1.1
..02
•8
17 7.8
1! 7 .
i 7.0
.7..2 2 C’)
7 ..2 -
2 1t3&)
1.2 .015
1.1 ..02 1
1.0 1 .02 8 I
•
—___
.
-
.
2 1
i
7.2
! 7.2
7 . .O
7 ..0
7.2 —
1--i
3’ 0 J. . .
2 C 0 I 1.0
.015
.O
.015
7
7
7
2 7 h
? 7.2
7.2 . 7 40
7.0 1. 29570
1.2
...8
.02
.015
6
7 -
27
23
.
.9. 7.0
7I
7.0 2 1I204 1.0
7.2 I 1.1
.02
.02
8
6
-
7.2
7.1
2 270
1.0
.02
7
OTAL
7.2
rI
73870
- - -
7.0
25600
1.1
.017 7
-------
rut. u I uI.,.I I
2
26 I __________ ________ ______
2? _________ _____________
2. 1 Q. . .._ 21 1:L _
-- -— — .ISF -rr-
Fo x b ô rc Co n - i o’ 1 )/
c i f3rid 2 e c -/er
——
•
.
CLARIFIER
CHflO}4.EUN
Tank 111 2,500 gal.
—-
it ffi ‘Ltr.J L
ii 7.2 6.8 18700 — 1 .1 .02 6
2
3
-
7.14
7.14
J 7.5
L ...z
I L
‘9
IC
1! 7 -0
J
7Jt_
t
7,2
7.2
70
7.2
7 .2 . . ....
.8
6..8
1 2.__
7 ..fl
7 0
18300
28750
2JJi 20
3 18O
]39 40
2 00
7UP__
._2’ã30_
1.0
1.0
— 1.1
1.2
1 .2
.9
1.0
1.1
.9
1.0
.02
.02
‘ .015
02
.02
.02
.02
.015
02
J 2
8
8
7
7
7
8
—
7
7
8
.
•
1
—
M__
.
7 .14
!P!__7 2_
!J_7 .2.,_
? .L_7 2
231
i____
7 _.
7.0
7.0
7.0
afl5.0JL
2S 0_
2 .000_ ..
Q_,
2000
L.3
.8
1.0
1.0
1.Q_.
.02
.02
.015_
___
7
6
6
7_
.
7n
tR
16’20
‘ .. 02 8
—__-— ——
7.0
—
.w —— -
—. I ‘—J
7
——
“f
1.0 .02 6
.—.—.—__—-‘—
——
271 0 -7
.015
—7
7..2
7.0 ii 7260_
.8
..02
-—.—
—_
._ _-. .-__J_-__ —
._——_ .a.a
.a_e_ _
630
..,.-._. n.. p—*a .. .4 - — — - — -aanaa — — — n f l — —— —
___ -
-------
-A’rrR PbLLurIou CO9TROL
21
22
1
.7 0
7-
—I--.
23
24
25
2!!
.6 .8
7 .0
F ,‘. r
2 thn
I
.1
1
(
02
- c)2
iL1 6.8 ____ ____ ____ ________ ___
31 _____ ______ ___ ________
--- --—---- —
:.i:’ J . .2 .._ ;P..._._.Q1 . Q2
.-
I P x&rô 2oii’p’ ”7
51 L S r ’ Ud
CLARIFIER .
— ———.
CliROMI
. - C3L22 Tfl_
J__7 I .___ 7.2 32110_ 1.1 .02 6
Tank 111 2,500 ga
I L
.
! 7 5
7 14
36780
.7
.02
6
7 1
7.2
6338o_
i..O
.02
6
4
5
.
- 7.5
7 ) 4 -
27110
- .8
.015
7
!. 7 . 1 L
!) 7.14
1 ! 7)4
!Q . 7.2
7 .2_
7.2
7.2
7.0
2276Q.
LL
1.3
1.1
1.1
.02
.02
.02
.015
5
y
6
Ill
i1
7.0
7.0
..
7.o
7M
19220 -
_L3_
1.1
Q15
.02 -
I
i! .
1
. —
1!!
7 .2_
. -‘
7.0
1
J
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— . .i
1.2
0
.
.02
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. JJ.)
8
J
.
7.2
7.0’
2L 1 3
0
.02
9
Ii
1i
.
20
in
R
‘ n
1
n
in
-
——--a.,-
6.8
16 L
1..0
.( 2
A_.
—
7.0
6 3
3 3
1.1
8
._7 p___
6.8
79co -
.8
.oi
• -_______
6 £
315 0
C)
- Q:).5
(;
.
—___
- —
-
- - —
9
-7--
-------
ATE POLLUTIC’!’I CCM RW.
• (
L
-;.
9r#’d e ’ ’
CLA RIFIER
.
CHROMIUM
Tank I/i 2,500
_) :iL:_,.
1
n ..
Ch
b
J 1)W
—
T L
J i
2
7.2
15770
1.3
.02
9
.
.
4 7L
33230
. ..j.2
.015
8
7.2
33270
1.2
.02
8
- 7
i_7. 1
hi
13 1
7.2
7.2
2c32Q_
2R20
_.l.2
.02
9
8
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7.2
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1.5
. .02
9
1 1 7.
? .
2 . .
7.2 —
30690
1.5
.02
8
2
7.2
26150
1.1
.02
6
?___
.6
.02
6
7.
6
.7.11
9380
.02
7_
114
rT .
rp —
—— I •
Iii L5___
k 7.6 ‘
I
L5
2
22
—__
r.
—,
Q
— . u
. —
7,I .
31(eo
.02
8 —
.
7.11
177110
L .2 0
.015 8
.oi 6 —
.8
._,02
8
.
.
1
7.2
1 1O
.7
. ..ois
8
711
7.2
2L630
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.02
8
i
Li
_7
7.
7, _
.02
7
_
72_
291 Q_
.9
.02 -
9
2
7.0
is 6o_
.015 -
6
I
-
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7.1.1
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L 2
72
,__. ._.. .ae.aSS
l7 Q_
2 770
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. .J. .j___
1.1
- — —‘—
.02
.02
S.3-. t_
r . ——- .
I
rflIfl .WSC
U
—
536360
— — — p
a
-&e —— —
L . ____________________ _________________ _____________________ ___________________ ___________
•1 C
26 ___ _________ _________ ________ __________ _________ _____
2? ___________ ___________ ____________ __________ ____________ ___________ _______
30 ____ ______ _____ ___________ _____ ___________ __________ ______
3• ________ _____ ____ ____ _____ ______ ______
liii
- a
• ‘ 7. 4 7.2 2 G3O .9 . 019 6
— — — . .•_ . — . . .a,_.s._a. t . esa r — - S . . a Dr a . fla.Wra arb - —. as WS..
-------
I
_..,_. fl, _.
TATER PCLLUTIO I COHIROL
I_- - - -———-, — . -.————..—.-— —.—.——— -——- - —
F OX6O’° Copip5”Y •?. 7Z
ps,L Hr,d . ’ewd1er
•
CLARIFIER
cxao tr’
Tank 1 2,500 gal
y-..
I 7 I 4
2j________
fl. ,..
7.2
JL’L .
2 70 •145
LP
.015
T2 IrJ
5
J J D
.
. J J1
3
4
i 1.2
J_ 7 . 3
2 7.3
7.2
9
In
I I
— !t .2
— 7.2
7.?
7.2
! j____
7.0
‘T..l
5 IOO
22 6O
l
i..o
. .p
..o
8
.
7.2
26270
1.0
.015
7
7.1
282 40
1.1
.015
7
,
2 8O
1.0
.02
7
7.0 1
.7
.015
8
7.0 I 2 CS0
.8
.015
8
.
7.2 I 25230
1.0
.015
9
7.2
9320
1.1
.02
9
4., I
I,
7.5
.
.
7.1.1
1.3
.02
!
—
7
. 2 010
.02
7
.
? . 7.2
7 5 -
7.5
72
7.2
I br,oi __
20.’70
‘.2
1.1
•O1
.02
R
8
7.2
27 1 C0
1.3
.019
- 8
2
24
25
.a35 o
1 .1
26
21
26
,31
T11T.M
i(A
mc
02
0
8
___
3.2
7.13
7 14
7.2
7.2
4 27520
I2 8CL
1.3
.015
8 -
B
3 9780
7.2
.019 8
-------
APPENDIX I l —B
EPA ’s PROPOSED EFFLUENT LIMITS FOR
METAL FINISHING INDUSTRIES
JANUARY 1973
-------
-
UNITED STATES ENVIRONMENTAL PROTECTION AGENCY
WASHINGTON. D.C. 20460
j JA 4 1973
MEMORANDUM
TO: All Regional Permit Program Directors
FROM: Directo,r, Office of Permit Programs
SUBJECT: Revised Metal Finishing Guidance
The Guidance of September 1972 has been revised to include
only those parameters which are of significance and more
directly reflect ind is;rial practice. The limit for fluoride
has been increased to a level resUltin9from wilt process
stream precipitation. Relative to po1lutiL n abatement, this
is not an increase in allowance. The other limits are derived
essentially on this basis as well.
The Suidance should be applied only to establishments using
20,000 G?D or more of p cess water.
The parameter limits are expressed in units of pounds er
1000 gallons of process water. This reflects emphasis given
to-pounds limitations in otner industrial categories.
Specifically SUCh parai eters as ammonia, phosphorous,
refractory cyanide, and arsenic have been excluded. For
chromium, the separate parameter for the dissolved trivalent
form is excluded.
From the 1967 Census of anufacturer, Bureau of Census it
Is estimated that this Guidance aoplies to 44° of the total
number of establishments accounting for 88% of the total value
of shipments by estabflshm nts in the SIC 3471 category. it
Is estimated that this Guidance applies to 39% of the total
number of establishments and 9i of the total value of shipments
by establishments in the SIC 3479 category.
Printz, Jr.
-------
j ..L I
L1Ii! S F0 Iii! P’ .T _ T 1S’ ?G T?:DJSTRY (a). (5 )
_______________________ SC’!D t! A ________ S I C0 ’ TS
U U.i.(iTfTF 1 . .tjJ ç .. ;.urrjCb 1T j gal.
PA’ Ar’.E1!R ru /l v-ill
Cc)
I —
— I
—
153
10
0.fl0
50
0.417
CV1 1IrIt Dast. , Cl 2
0.03
0.00fl5
0,1
0. 00 0034
rL’JonID
.
-
n cn
ALI2 4IIiU’i
0.2
0.0 167
C.5
0.0 04 17
eARIUrI 1.0
0.0 3
- 2.0
0.0 67
hUM
- 0.1
0.00033 0.2
0.33 - 17 0.1
0.00167
4b
C’ 0MIW CR
0.05
0.000824
.
CR 1 .
0.25
0.C 9 ! 0.5
0.0C4 17
5o vtion & S spenoed Solids.
tOPPEk
0.2
0.0fl’67 0.5
I 0.00417
.
(
0.5 j 0. ’.i7 1 1.0
C.0 3’. I
o.os I 0 ‘c ’7 . 0.1
0.Or-C334 I
1.0
2.0
0.0157
1 1.0 1
C 33 - 2.0 0.C 167 .
SaVER
0.05
0.0’ l7- 0.05
0.C C4i7
7!9C I
- 0.5 l. -
0.C’ 3 a
14 (Ave. D I1y 01 cP..)
6—9 1
—
(a) Metal concentrations are based on analysis of fil tered clear solutions.
(a) The manimum pcmiss b1e concentration for a particular mat& in the to .a1sjs,ar. ev solids shall be ingil. (0.00834 lbt/1,000 gal.)
noted for Ch,omtuii. -
(c) Limited sI nIftcance In this IndJstr3’. should be consIdered on case by case basis.
-------
APPENDIX Il—C
PROBABILITY PLOTS
-------
99.9 99.8
99 98
::.
ThT1Th__
1-
4_f 4.
1 •
-t
1 •
I
— -
- -4
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T
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1 .L
I
4,
4.
- 4— -
• *
If .
95 90 80 70 60 50 40 30
tr
4.
20 10 5
I t tt I 1
FOXBORO COMPANY
Flow
Frequency of Occurrence
(Historical Data)
11 Ii [
-
• :1
1 T i 1 ;r.4f L• •iit 1
: :i
-ii
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‘H
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• .- •
14 ! $
4 t
+4.
• I
I —
ft
0.5 0 2 0.1 0.05
-‘4 4— —
f’F T
:
r
•
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L 1
,
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— T *r* _
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- -——-
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3
r
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•
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IL
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ift
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: 1111
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1. 1 •-
—
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2
10 0 30 40 50 60
99.8 99.9
0 01
99.99
Pa rtDvit. a f Ph Nin Pnn.1 f, , r Tøa Ph ,i Ii Cf-ei. A
99.99
oOq
(22.7)
--4 4,
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+
ri
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1-f
1 ’ i
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p4I
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p1 ’ .
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0
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40,00Q - - ‘
(15.1)
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TI
it
p.
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20,00Q
( 76)
• -
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I *
i •j -
U
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0.01 0.05 0.1 0.2 0.5 1
- ii-- -
10 80 0 95 98 99
-------
o 99.9998 99.5 99 98 95 90 80 70 50 40 30 20
—
— = .
L.
::
i:
;
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tt t
J 41TT
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: :
HT_t TfT
r±
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r
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H E I EEl
1 1J
0.05 0.1 0.2 0.5 1
lii
FOXBORO CO)U ANY
Total Copper
Frequency of Occurrence
(Historical Data)
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TOTAL PHOSPHORUS (m /l)
1.00 10.0
-------
PART III
RAYThEON CORPORATION
MISSILE DIVISION
LOWELL, MASSACHUSETTS
-------
TABLE OF CONTENTS
TITLE PACE NO.
Table of Contents l i t—i
List of Tables u I—u
List of Figures l It—ill
Introduction i n —1
Industrial Waste Treatment 111—1
Sampling Information 111—4
Analytical Results and Conclusions 111—8
Summary of Conclusions 111—12
Sample Analysis, Abbreviations and 111—14
Units of Measure
Analytical Data 111—15
References 11 1—24
Apj endix Il l—A (Proposed EPA Effluent Guidelines
for Metal Finishing Industries,
January, 1973)
It 1—i
-------
LIST OF TABLES
TABLE NO. TITLE PAGE NO.
TABLE 111—1 Metal Surface Treatments and Processes 111—2
Used in the Lowell Facility
TABLE 111—2 Approximate Production Levels for 111—6
May 15 and 16, 1973
TABLE 111—3 Station Location 111—7
TABLE 111—4 Process Waste Flow Recorded at Final 111—13
Effluent (RLO3)
TABLE 111—5 pH and Temperature 111—15
TABLE 111—6 Analytical Data (TNFR, cyanide, 111—16
dissolved fluoride, total phosphorus)
TABLE 111—7 Analytical Data (total and hexavalent 111—19
chromium, total and dissolved copper,
nickel and silver)
TABLE 111—8 Analytical Data (total and dissolved 111—22
lead, tin and cadmium)
“—ii
-------
LIST OF FIGURES
FIGURE NO TITLE
FIGURE Ill—i Industrial Waste Treatment
Flow Diagram
“—iii
-------
RAYTHEON CORPORATION
MISSILE DIVISION
LOWELL, MASSACHUSETTS
MAY 15 AND 16, 1973
The Missile Division of Raytheon Corporation, located in
Lowell, Massachusetts, manufactures various parts and accessories
for air to air missiles. Many of these items are sent to the finish-
ing department for various cleaning, coating, plating and etching
processes. Due to current cut backs in contracts the metal finishing
department is operating at approximately 30% capacity. This department
primarily works one eight hour shift, however a second shift may be
employed to conduct etching operations as needed. Except for sanitary
waste the metal finishing department produces all liquid waste.
The various processes available at the Lowell facility and their
related wastes are summarized in Table 111—1. Because Raytheon operates as
a job—shop, the types of processes used on a particular day are variable.
Because of this and the units plated, it is very difficult to obtain an
accurate prediction or record of the levels of production.
Industrial Waste Treatment
Raytheon’s industrial waste treatment plant was designed by
William H. Kahl, Toledo, Ohio, and placed into operation in 1972. The
wastes are segregated into three classifications: cyanides, chromiums
and acid/alkalis, and are piped directly to the appropriate treatment
system. A flow diagram of the entire treatment system is shown in
Figure Ill—i.
The entire system has an estimated design capacity of 470 liters
-------
TABLE 111—1 -
- -. r’T ’ ‘Y’ - .. r :nr’ ’ ‘c. ’c 7 t’ -’ f ’ 1’
— — __._\__ — — — — -- - L I — S_,___S____.I .. — _,# l
1 — rrt P
-
C c.c: .. ‘.fz. ;. .
—I’- - -- —.
5
ic:
Chrom
ECOIS \C Z L
N:c:...
u id C i:c c Plat:ng
:
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5
P ::.g
:
i’ ckc_
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?1 n
Tin
[
- P? - : :. ;ii - -
Cy c
C. e:
Cac a m Pia ..:-..g
Cva:
C £
:_
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Cya: 5 ....
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,
__________
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O: 3i ¼..
.
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,
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:_
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Reference No. 1
III— 2
-------
TO R/P X’
/25 7V /fD
CRL LOMS PFR
,$l.WU7_t
eZI7#?IP/tR
FLOW DIAGRAM
PREPARED BY FRED SPINAZZOLA 2
FIGURE 111—1
-------
per minute (1pm) (125 gallons per minute (GPM)J, with the cyanide
destruction system capable of treating 98 1pm (26 CPM), chromium 45
1pm (12 GPM) and acid/alkali 330 1pm (87 CPM). Currently the treatment
plant is receiving approximately 30% of these flows.
All cyanide wastes are collected in one of three 68 cubic meters
(18,000 gallons) batch treatment tanks. Three tanks are located out-
side and adjacent to the treatment plant. Sodium hydroxide raises
the pH, and chlorination with chlorine gas destroys the cyanide.
Oxidation—reduction potential (ORP) probes and pH probes monitor the
treatment tanks and control chemical addition. During cyanide
destruction the pH is maintained above 8.5 at all times. Following
complete cyanide destruction, a bucket of sodium sulfite is added to the
treatment tank to remove any residual chlorine which will oxidize the
trivalent chromium to the hexavalent form. The cyanide wastes are then
combined with other process wastes in the neutralization tank for further
treatment.
Chromium wastes are piped to a surge tank which equalizes the flow
to the chromium reduction system. Concentrated chromium solutions are
collected in holding tanks and bled into the surge tank. In the
treatment system the pH is lowered to less than 2.5 with sulfuric acid,
and sulfur dioxide gas is used to reduce the hexavalent chromium (Cr+ 6 ) to
trivalent chromium (Cr+ 3 ) . The treated chromium waste is then piped to the
acid/alkali surge tank, where it mixes with the dilute acid/alkali wastes.
The acid/alkali wastes include all the remaining plating room
wastes from rinse water overflows, and dumps of cleaning and plating
111—3
-------
baths. Concentrated dumps are collected in a holding tank and bled
into the general collection sump. The dilute acid/alkali wastes and
reduced chromium wastes enter a surge tank which overflows into the
general collection sump. This waste is pumped to a neutralization
tank where the pH is adjusted to approximately 8.0 with either lime
or sulfuric acid. Aluminum sulfate and the poly—electrolyte Rohin and
Haas A—l0 is added to promote precipitation.
Following neutralization, the wastes flow to a clarifier where
solids and metal hydroxides are allowed to settle Out. A portion of the
resultant sludge is returned to the neutralization tank as a coagulant
aid. A rotary vacuum filter de—waters the remaining sludge. The de—
watered sludge is sent to a landfill and the filtrate returned to the
clarifier. Following clarification, the waste Is pumped to one of two
sand filters and the final effluent discharges through a 90° V—notch
weir to the Merrimack River.
All oil and grease containing solvents or cleaners are isolated,
collected and purchased by a licensed scavenger.
Sampling Information
On May 15 and 16, 1973, U. S. Environmental Protection Agency,
Region I personnel, collected samples at the Raytheon, Lowell industrial
waste treatment plant.
During this sampling program, only a portion of the metal surface
treatments and processes shown in Table 1 were utilized. Processes in
operation include: chromate conversion coating; copper, silver, cadmium
and gold plating; chemical cleaning prior to painting, welding, etc.;
111—4
-------
stripping of plated material from rejected units; and printed circuit
board operations which include copper and tin — lead plating. No
etching was performed during this period, however 208 liters (55 gallons)
of concentrated Macdermice etchant (chromium—sulfuric acid solution) was
bled into the chromium reduction system. At 1300 hours on May 16, 1973,
95 liters (25 gallons) of concentrated acid copper plating solution was
neutralized, treated with ferric chloride and bled into the general
collection sump.
Fred Spinazzola, Senior Industrial Engineer, estimated the production
levels as shown in Table 111—2.
On each of two days, an 8—hour composite sample, two 4—hour composite
samples and several grab samples were collected prior to and following
cyanide destruction, chromium reduction, clarification and sand filtration.
Due to the unpredictable variations in flow rates, it was not possible
to composite these samples proportional to flow. Every hour the same
volume of sample was added to the composite sample. All samples except
hexavalent chromium were collected and analyzed in accordance with U. S.
E.P.A. Methods for Chemical Analysis of Water and Wastes, 1971 . Hexavalent
chromium was collected and analyzed in accordance with’ Standard Methods
for the Examination of Water and Wastewater, Thirteenth Edition . The
samples were analyzed for total and dissolved metals (copper, silver,
nickel, cadmium, lead, tin), total non—filterable residue, total and
hexavalent chromium, dissolved fluoride, total phosphorus and total
cyanide. The sampling stations are identified in Table 111—3 and
analytical results are shown in Tables 111—5 through 111—8.
111—5
-------
TABLE 111—2
APPROXIMATE PRODUCTION LEVELS FOR
MAY 15 AND 16, 1973
RAYTHEON — LOWELL, MASSACHUSETTS
PROCESS APPROXIMATE SURFACE AREAS TREATED
DURING STUDY PERIOD
Chromate Conversion Coat 18.6 square meters (S.M.)
(200 square feet (S.F.))
Copper, Silver and Gold 1,935 square centimeters (S.CM.)
Plate (300 square inches (S.I.))
Cadmium Plate Less than .9 S.M.
(10 S.F.)
General Cleaning Less than 9.3 S.M.
(100 S.F.)
Stripping of Reject Units 483.9 S.CM.
(75 S.I.)
Printed Circuit Boards 50 Boards @ 12.9 S.CM./board
(copper and tin — lead 645 S.CM.
plate) (2 S.I./board = 100 S.I.)
Etching — no etching per— 208 liters
formed, however a con— (55 gallons)
centrate dump of
etchant was bled into
system (Macdermice
etchant — 1:1 Chrome —
sulfuric acid)
III— 6
-------
TABLE 111-3
STATION LOCATION
Raytheon Corporation
Lowell, Massachusetts
MAY 15 AND 16, 1973
STATION NO. DESCRIPTION
RLO1 General collection sump
RLO2 Clarifier effluent sump inside the
treatment plant
RLO3 Effluent from sand filters (final
effluent) at the 900 V-notch weir
RLO4 Influent to the chromium reduction
system at the surge tank (prior to
pH adjustment)
RLO5 Effluent from the chromium reduction
system as it enters the acid/alkali
surge tank
RLO6 Cyanide destruction outside the treatment
plant. (Tank on far left looking at the
three treatment tanks from the back of the
building.)
RLO7 Effluent from the cyanide destruction tank
as it enters the neutralization tank
111—7
-------
Analytical Results and Conclusions
As previously stated, the industrial wastewaters from the Raytheon —
Lowell plant have been segregated into three waste streams (cyanides,
chromiums and acid/alkalis) for treatment. The cyanide destruction
system and the chromium reduction system will be discussed separately.
Since cyanide wastes and chromium wastes enter the acid/alkali waste
stream for further, more generalized treatment, the remaining chemical
parameters of the entire waste stream will be discussed as a unit.
Cyanide Destruction
- Cyanide destruction tank No. 3 was sampled before and after treat-
ment. During the 28 hour treatment period the cyanide level was reduced
from 99.0 mg/i to 0.01 mg/l. Although this tank was not discharged to
the main waste stream during the sampling period, another previously
treated tank was being discharged. Analysis of this waste stream
(Station RLO7) showed that it contained 0.04 mg/i of cyanide. On May 16
three grab samples collected at the combined final effluent (RLO3) con-
tained a maximum cyanide concentration of 0.02 mg/l.
The cyanide concentrations of the final effluent are less than the
0.03mg/i limitation which has been proposed in the EPA Discharge Limits
for the Metal Finishing Industry, January, 1973, which are shown in
Appendix A.
Chromium Reduction
The chromium reduction system accomplished nearly complete hexa—
valent chromium reduction. Based upon eight hour coinpositing samples
the system reduced hexavalent chromium concentrations to less than
I I 1—8
-------
100 ugh, a greater than 99% reduction.
No measurable change in hexavalent chromium was noted following
mixing with the remaining waste stream in the general collection sump.
Hexavalent chromium levels dropped off to less than the detectable
limit following clarification. The final effluent contained less
than the 40 ugh] detectable limit, except for one four hour composite
sample which had a concentration of 42 ugh. All hexavalent chromium
concentrations following clarification were less than the 50 ugh con-
centration stipulated in Schedule A of the proposed guidelines.
Total chromium concentrations diminished 55 — 87 percent in the
chromium reduction system. Immediately one assumes that sedimentation
occurs in the reaction tank, however, Raytheon personnel said that no
sludge build—up occurs and they have never had to remove sludge from
the reaction tank. Since the tank is fiberglass, plating onto the
tank has also been eliminated as a cause of the chromium loss. Also, no
diluent is introduced into the system which could reduce chromium
centrations so significantly. Thus the cause of the lowered chromium
concent rations are unresolved.
Flow
As previously stated, the treatment system currently operates at
approximately 30% capacity. Hourly flow readings at the final effluent
and subsequent eight hour (a typical day’s operation) averages and
ranges are shown in Table 111—4. This wide range of flow rates is not
unusual in a metal finishing shop which operates as job—shop. The
production line is not consistent, therefore the type and quantity of
ItI—9
-------
waste produced is not consistent. Intermittent discharges of treated
chromium waste and cyanide wastes as well as concentrated wastes which
are bled into the system add to the flow rate variations.
pH and Temperature
Hourly p11 and temperature readings for all except the cyanide
stations (RLO6 and RLO7) are shown in Table 1 11—5. Except for one sample,
the pH at the general collection sump (RLO1) remained relatively
constant throughout the two day sampling period, ranging from 2.5 to 2.8.
The one exception was the 1400 hours pH reading on May 16 when 5.0
standard units was recorded. The pH of the wastes entering the chromium
reduction system ranged from 1.8 to 3.0 and that of the treated chromium
wastes (Station RLO5) ranged from 2.3 to 2.6. The treated cyanide waste
discharging to the neutralization tank (RLO7) had a pH of 9.5. The pH
of the final effluent (Station RLO3) ranged from 6.3 — 7.5.
The temperature of the final effluent ranged from 14.0°C to 16.5°C
with a two day average of 15.0°C. No significant increase or decrease
was noted during treatment.
Ceneral Waste Flow
Prior to pH neutralization, the chromium and acid/alkali wastes
combine in a general collection sump. Cyanide wastes combine In the
neutralization tank. Analysis of the wastewater collected from the s nnp
(RLO1) showed low concentrations of total non—filterable residue (TNFR).
Except for the grab sample taken at 1400 hours on May 16, the TNPR con
centrations in the sump were less than 10 mg/i. As noted above, this
same sample had a high pH. However, the effluent from the clarifier
111-10
-------
(RLO2) showed a slight increase in TNFR. This is probably attributable
to a carry—over of floc from coagulation in the clarifier. Examination
of the wastes after sand filtration (RLO3) indicates no decrease in TNFR.
Thus the concentrations of TNFR leaving the plant during the study period
were greater than the concentrations entering. Only one final effluent
sample, a 4—hour composite, exceeded the EPA proposed discharge limit of
10 mg/i and that sample was 11 mg/i TNFR.
Heavy Metals
Of the metals analyzed, lead, chromium and copper were the only
metals entering the clarifier at concentrations greater than the
effluent limits which EPA has proposed. The results also showed, as
expected from the review of the TNFR data, that most of the influent
metals are in the dissolved state. Following neutralization and
chemical precipitation CR1.02) all the dissolved heavy metal concentrations
are less than those stipulated in the proposed limits. The eight hour
composite samples showed that total chromium was reduced 93 — 97 percent,
total copper 90 — 95 percent and dissolved copper 99+ percent. All the
total chromium samples and one grab sample for total copper exceeded
the proposed limits.
Based upon the composite samples, sand filtration removes up to
65% of the remaining total copper, however, dissolved copper concentrations
generally increased during sand filtration. Following filtration the
copper concentrations were less than the limits proposed by EPA. The daily
total chromium reductions in the sand filters varied from 24— 70 percent.
However, on neither day were chromium removals substantial enough to meet
- 111—il
-------
Schedule A of the proposed effluent limits and on May 15 the chromium
concentration exceeded the proposed Schedule B limit.
Dissolved fluoride concentrations in the waste stream never ex-
ceeded 2.1 mg/i and after treatment never exceeded 1.0 mg/i.
Currently there is no proposed limitation for total phosphorus,
however, total phosphorus concentrations in the final effluent were
generally twice as high as the allowable concentration (0.05 mg/i) in
the Massachusetts Water Quality Standards for receiving water.
Suimn ry of Conclusions
The effluent from Raytheon Corporation will generally meet
Schedule A of the proposed EPA effluent limits with the exception of
the total chromium concentrations. The effluent from chemical pre-
cipitation meets the requirements on dissolved metals limits, and
removal of total metals, except chromium, is generally adequate.
The cyanide destruction and chromium reduction systems operated
efficiently. The unexplained loss of more than 50 percent total
chromium in the reduction system warrants further investigation.
Sand filtration is needed primarily for chromium removal, however 1
the total chromium values still exceeded the proposed limits.
111—12
-------
TABLE 111-4
Process Waste Flow Recorded at Final Effluent (RLO3)
Raytheon Corporation, Lowell, Massachusetts
May 15 and 16, 1973
Time FLOW
Date ( hours) Liters per minute (1pm) Gallons per minute (gpm )
05/15/73 0815 180 48
0915 300 80
1015 170 46
1115 310 83
1215 180 48
1315 60 15
1415 100 26
1515 120 32
Average 180 47
Total Daily Flow = 85 cubic meters 23,000 gallons
05/16/73 0800 100 26
0900 360 94
1000 180 48
1100 140 38
1200 200 53
1300 150 40
1400 210 55
1500 140 38
Average = 180 49
Total Daily Flow = 89 cubic meters 24,000 gallons
111—13
-------
SAMPLE ANALYSES
STANDARD ABBREVIATIONS AND UNITS OF’ MEASURE
ANALYSIS REPORTED DESCRIPTION MEASURED IN
Temperature Sample temperature at Degrees Centigrade (°C)
time of collection
pH Standard Units (SU)
Total Non—Filterable Total suspended solids Milligrams per liter
Residue (mg/i)
Dissolved Fluoride mg/i as fluoride
Total Phosphorus mg/i as phosphorus
Oil and Grease mg/i as oil and grease
(hexane extractable)
Cyanide mg/i as cyanide
Hexavalent Chromium Micrograms per liter
(Cr+ 6 ) (ugh) as hexavalent
chromium
Total Metals Total: Copper ugh
Nickel
Zinc
Tin
Lead
Cadmium
Chromium
Silver
Manganese
Iron
Dissolved Metals Dissolved: Copper ug/i
Nickel
Zinc
Tin
Lead
Cadmium
Silver
Manganese
Iron
Letters Preceding a Reported Value Denote the Following:
J — value not accurate (estimated)
K — actual value is known to be less than value given
R — sample lost
-------
TABLE 111—5
pH AND TEMPERATURE
Raytheon Corporation
Lowell, Massachusetts
May 15 and 16, 1973
RLO1 RLO2 RLO3
RL O4
RLO5
Date
Time
pH
Temp
(°C)
pH
Temp
(°C)
pH
Temp
(°C)
pH
Temp
(°C)
pH
Temp
(°C)
5/15
0815
2.7
13.5
7.1
14.0
6.9
16.5
2.8
14.0
2.5
13.5
0915
2.8
13.0
7.0
14.0
7.3
14.5
2.8
14.5
2.6
13.5
1015
2.7
13.0
7.5
14.0
7.4
15.0
2.8
14.0
2.6
13.0
1115
2.7
12.5
7.4
14.0
7.0
14.0
2.8
13.0
2.6
12.5
1215
2.7
12.5
7.5
14.0
7.5
14.0
2.2
13.5
2.5
13.0
1315
2.7
13.0
7.7
14.0
7.0
16.0
2.4
13.0
2.5
13.0
1415
2.7
13.0
7.6
14.0
6.4
14.5
2.8
16.0
2.5
14.0
1515
2.5
14.0
6.8
14.0
6.9
14.5
3.0
15.0
2.6
13.5
5/16
0800
2.7
14.5
6.3
14.0
6.8
15.5
2.3
12.5
2.5
12.5
0900
2.8
13.0
6.5
14.5
6.3
15.5
2.3
13.5
2.5
12.0
1000
2.8
14.0
7.2
14.5
6.8
15.0
2.2
13.0
2.5
12.5
1100
2.8
14.5
7.3
15.0
7.1
14.5
2.2
13.0
2.4
12.5
1200
2.7
14.0
7.5
14.5
74
15.0
1.8
13.5
2.4
12.0
1300
2.6
14.0
7.6
15.0
7.5
14.5
1.9
16.5
2.3
12.5
1400
5.0
14.5
7.7
14.5
7.1
15.0
2.4
22.5
2.3
13.0
1500
2.8
14.0
7.8
16.0
7.3
15.0
—
—
—
-------
TABLE 1 •6
ANALYTICAL DATA
Raytheon Corporation
Lowell, Massachusetts
May 15 and 16, 1973
TOTAL DISSOLVED TOTAL
STATION NON—FILTERABLE CYANIDE FLUORIDE PHOSPHORUS
NO. DATE TIME RESIDUE (mg/i) (mg/I) (mg/i)
(mg/i)
RLOI. 5/15 Conip—8 1 2.1 0.49
0745—1545
5/16 Comp—8 6 0.5 0.28
0730—1530
5/15 0915 2
5/15 1115 0
5/15 1315 2
5/15 1515 0
5/16 0800 8
5/16 1000 4
5/16 1200 2
5/16 1400 23
RLO2 5/15 Comp—8 10 1.1
0745—1545
5/16 Comp—8 16 0.7 0.12
0730—1530
5/15 Comp—4 1.0
0745—1145
5/15 Comp—4 8 1.1
1145—1545
5/16 Comp—4 13 0.7 0.11
0730—1130
5/16 Comp—4 16 0.6 0.17
1130—1530
-------
TABLE I l l-b CONTINUED)
TOTAL DISSOLVED TOTAL
STATION NON-FILTERABLE CYANIDE FLUORIDE PHOSPHORUS
NO. DATE TIME RESIDUE (mg/i) (mg/i) (mg/i)
(mg/i)
RLO2 5/15 0915 1
5/15 1115 3
5/15 1315 20
5/15 1515 2
5/16 0800 6
5/16 1000 6
5/16 1200 31
5/16 1400 4
RLO3 5115 Comp—8 6 1.0 0.13
0745—1545
5/16 Comp—8 4 0.8 0.08
0730—1530
5/15 Coznp—4 ii 0.9 0.17
0745—1145
5/15 Comp—4 5 1.0 0.10
1145—1545
5/16 Comp—4 7 0.9 0.08
07 30—1130
5/16 Comp—4 8 0.8 0.11
1130—15 30
5/15 0915 6
5/15 1115 6
5/15 1315 10
5/15 1515
5/16 0800 10 —
5/16 0900 — 0.02
-------
TABLE 111—6 (CONTINUED)
TOTAL DISSOLVED TOTAL
STATION NON-FILTERABLE CYANIDE FLUORIDE PHOSPHORUS
NO. DATE TIME RESIDUE (mg/i) (mg/i) (mg/i)
(mg/i)
RLO3 5/16 1000 5
5/16 1200 9 0.00
5/16 1400 7 0.02
RLO6 5/1.5 0950 99.0*
5/16 1400 0.O1**
RL O7 5/16 1105 0.04
* Cyanide tank before treatment
** Cyanide tank after treatment
-------
TABLE 111—7
ANALYTICAL DATA
RAYTHEON CORPORATION
Lowell, Massachusetts
May 15 and 16, 1973
STATION CHROMIUM (ugh) COPPER (ugh) NICKEL (ugh) SILVER (ugh)
NUMBER DATE TIME TOTAL HEXAVALENT TOTAL DISSOLVED TOTAL DISSOLVED TOTAL DISSOLVED
RLO1 5/15 Comp—8 44,000 70 17,000 17,000 95 85 30 1(10
0745—1545
5116 Comp—8 20,000 76 9,640 9,400 130 120 200
0730—1530 -
5/15 0915 38,000 16,100 30 — 20 —
5/15 1115 44,200 19,000 19,000 20 10 20 K1O
5/15 1315 64,400 30,000 30,000 260 240 20 1(10
5/15 1515 19,000 6,980 6,980 - 100 100 1(10
5/16 0800 23,000 9,840 9,600 630 630 40 1(10
5/16 1000 4,900 2,000 2,000 40 40 1(10 1(10
5/16 1200 14,000 5,160 4,880 1(10 10 K10 1(10
5/16 1400 27,300 — 18,000 18,000 50 30 75 K10
RLO2 5/15 Comp—8 1,260 K40 850 130 30 1(10 20 K1O
0745—1545
5/16 Coinp—8 1,410 K40 985 40 K10 1(10 50 20
0730—1530
5/15 Comp—4 920 K40 700 180 20 20 20 1(10
0745—1145
5/15 Comp—4 1,210 805 80 20 1(10 K10 1(10
1145—1545
5/16 Comp—4 1,110 42 820 55 10 1(10 20
0730—1130
5/16 Cotnp—4 1,740 1(40 1,190 20 20 1(10 55 20
1130— 15 30
5/15 0915 3,800 62 2,910 — 40 — 40 —
5/15 1115 595 K40 480 120 10 10 20 1(10
-------
TABLE 111-7 (‘ NTINUED)
ANALYTICAL DATA
Raytheon Corporation
Lowell, Massachusetts
May 15 and 16, 1973
STATION CHROMIUM (ugh) COPPER (ugh) NICKEL (ugh) SILVER (ugh)
NUMBER DATE TINE TOTAL HEXAVALENT TOTAL DISSOLVED TOTAL DISSOLVED TOTAL DISSOLVED
RLO2 5/15 1315 2,600 1,740 100 10 10 20 K1O
5/15 1515 420 340 65 20 10 K10 —
5/16 0800 390 — 300 35 10 10 K1O K1O
5/16 1000 210 K40 150 30 10 20 Kl0 KlO
5/16 1200 — — 2,100 20 20 10 65 20
5/16 1400 230 42 20 K1O 10 50 20
ELO3 5/15 Comp—8 995 K40 690 120 20 10 20 K10
0745—1545
5/16 Comp—8 430 K4O 380 55 K1O K10 20 20
0730—1530
5/15 Comp—4 1,100 K40 800 160 10 10 20 K10
0745—1145
5/15 Comp—4 770 K40 560 100 10 10 20 K1O
1145—1545
5/16 Comp—4 320 42 310 65 20 K10 20 10
0730—1130
5/16 Comp—4 480 K40 400 45 10 20 20 20
1130—1530
5/15 0915 1,570 K40 1,130 — 10 — 20 —
5/15 1115 605 K40 490 130 10 10 K10 Kl0
5/15 1315 1,120 — 765 95 10 K10 10 K10
5/15 1515 400 360 100 10 K10 10
5/16 0800 450 — 420 95 20 K1O 10 20
5/16 1000 180 K40 220 60 20 K1O 10 20
5/16 1200 490 — 420 35 10 10 20 20
5/16 1400 340 K40 310 40 20 K10 20 20
-------
TABLE III— “ONTINUED)
ANALYTICAL DATA
Raytheon Corporation
Lowell, Massachusetts
May 15 and 16, 1973
STATION CHROMIUM (ugh) COPPER (ugh) NICKEL (ugh) SILVER (ugh)
NUMBER DATE TIME TOTAL HEXAVALENT TOTAL DISSOLVED TOTAL DISSOLVED TOTAL DISSOLVED
BLO4 5/15 Conip—8 200,000 200,000
0745—1545
5/16 Comp—8 296,000 —
0730—15 30
RLO5 5/15 Comp—8 90,800 70
0745—1545
5/16 Cotnp—8 37,800 58
0730—1530
-------
TABLE 111-8
ANALYTICAL DATA
Raytheon Corporation
Lowell, Massachusetts
May 15 and 16, 1973
STATION LEAD (ugh) TIN (ugh) CADMIUM (ugh)
NUMBER DATE TIME TOTAL DISSOLVED TOTAL DISSOLVED TOTAL DISSOLVED
RLO1 5/15 Comp—8 50 50 1(2,000 1(2,000 20 30
0745—1545
5/16 Comp—8 50 K50 1(2,000 1(2,000 40 40
0730—1530
5/15 0915 50 — 1(2,000 — 10 —
5/15 1115 1(50 K50 1(2,000 1(2000 20 20
5/15 1315 350 250 1(2,000 1(2,000 70 65
5/15 1515 K50 1(50 1(2,000 K2,000 10 10
5/16 0800 500 400 1(2,000 1(2,000 80 80
5/16 1000 50 1(50 1(2,000 1(2,000 10 10
5/16 1200 K50 1(50 1(2,000 1(2,000 1 (5 K5
5/16 1400 1(50 1(50 1(2,000 K2,000 150 150
RLO2 5/15 Comp—8 1(50 K50 K2,000 1(2,000 10 5
0745—1545
5/16 Comp—8 1(50 K50 K2,000 K2,000 5 K5
0730—1530
5/15 Comp—4 1(50 1(50 K2,000 1(2,000 10 5
0745—1145
5/15 Comp—4 1(50 K50 K2,000 1(2,000 5 1(5
1145—1545
5/16 Comp—4 1(50 1(50 K2,000 1(2,000 1(5 1(5
0730—1130
5/16 Couip—4 1(50 K50 1(2,000 K2,000 5 5
1130—1530
5/15 0915 1(50 — K2,000 — 30 —
5/15 1115 K50 1(50 K2000 1(2,000 5 1(5
-------
TABLE 111—8’ 1NTINUED)
ANALYTICAL DATA
Raytheon Corporation
Lowell, Massachusetts
May 15 and 16, 1973
STATION LEAD (ugh) TIN (ugh) CADMIUM (ugh)
NUMBER DATE TIME TOTAL DISSOLVED TOTAL DISSOLVED TOTAL DISSOLVED
RLO2 5/15 1315 1(50 K50 K2,000 K2,000 10 1(5
5/15 1515 1(50 1(50 K2,000 K2,000 5 5
5/16 0800 K50 1(50 K2,000 1(2,000 5 K5
5/16 1000 1(50 1(50 K2,000 K2,000 K5 1(5
5/16 1200 1(50 K50 1(2,000 K2,000 20 1(5
5/16 1400 1(50 1(50 K2,000 K2,000 5 1(5
RLO3 5/15 Comp—8 1(50 K50 K2,000 1(2,000 20 10
0745—1545
5/16 Comp—8 1(50 K50 K2,000 1(2,000 20 10
0730—1530
5/15 Comp—4 1(50 1(50 1(2,000 1(2,000 20 10
0745—1145
5/15 Comp—4 1(50 1(50 1(2,000 1(2,000 10 5
1145—1545
5/16 Comp—4 1(50 1(50 K2,000 1(2,000 10 10
0730—1130
5/16 Comp-4 1(50 1(50 K2,000 1(2,000 20 10
1130—1530
5/15 0915 1(50 — 1(2,000 — 10 —
5/15 1115 1(50 1(50 K2,000 K2,000 5 KS
5/15 1315 1(50 1(50 1(2,000 1(2,000 5 K5
5/15 1515 K50 1(50 K2,000 K2,000 10 10
5/16 0800 1(50 1(50 1(2,000 K2,000 20 10
5/16 1000 1(50 K50 1(2,000 1(2,000 10 10
5/16 1200 K50 1(50 K2,000 1(2,000 20 10
5/16 1400 1(50 1(50 1(2,000 1(2,000 20 10
-------
REFERENCES
1) Obtained from the Massachusetts Division of Water Pollution
Control file on Raytheon Corporation, Lowell, Massachusetts.
2) Report on The Metal Finishing Waste Treatment Facility, Prepared
by Fred Spinazzola, Senior Industrial Engineer, Raytheon,
Lowell, Massachusetts
111—24
-------
APPENDIX Ill-A
U. S. ENVIRONNENTAL PROTECTION AGENCY PROPOSED
DISCHARGE LIMITATIONS FOR KETAL FINISHING
INDUSTRIES, JANUARY 1973
-------
tT r
, —
UNITED STATES ENVIRONMENTAL PROTECTION AGENCY
WASHINGTON. D.C. 20460
$1 JA 1973
.NEM0RANDU
TO: AU Regional Permit Program Directors
FROM: Director, Office of Permit Programs
SUBJECT: Revised Metal Finishing Guidance
The Guidance of September 1972 has been revised to include
only those parameters which are of significance and more
directly reflect ind iszrial practice. The limit for fluoride
has been thcreasedto a level resUltinoTrom unit process
stream precipitation. Relative to pollution abatement, this
is not an increase in allowance. The otherlimits are derived
essentially on this basis as well.
The Guidance should be applied only to sta5lishcients using
20,000 G? or more of p OCeSS water.
The parameter i m1tS are ex ressed in units of pounds er
1000 gallons of process water. This reflects emphasis given
to-pounds limitations in other industrial categories.
Specifically such parameters as arnonia, phosphorous,
refractory cyanide, and arsenic have been excluded. For
chromium, the separate parameter for the dissolved trivalent
forrn.is excluded.
From the 1967 Census of Ma ufacturer, Bureau of Census it
Is estimated that this Guidance aoplies to 44 of the total
number of establishments accounting for 88% of the total value
of shipments by establishr ents in the SIC 3471 cateaory. It
Is estimated that this Guidance applies to 39% of the total
number of establishments and 9i of the total value of shipments
by establishments in the SIC 3479 category.
I
Albert C. Printz, Jr.
-------
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-------
PART IV
WESTERN ELECTRIC
NORTH ANDOVER, MASSACHUSETTS
-------
TABLE OF CONTENTS
TITLE PAGE NO.
Table of Contents IV—i
List of Tables IV—ii
List of Figures iv—ni
Introduction IV—l
Industrial Waste Treatment IV-2
Sampling Information IV—5
Analytical Results and Conclusions IV—8
Historical Data IV—14
SLunmary of Conclusions IV—15
References IV— 17
Appendix IV—A — Analytical Data
Appendix IV—B — Proposed EPA Effluent Guidelines
For Metal Finishing Industries,
January, 1973
Appendix IV—C — Probability Plots
Appendix IV—D — Western Electric’s Monthly Reports
Submitted to the Massachusetts
Division of Water Pollution Control,
April, 1972 to April, 1973
‘v-i
-------
LIST OF TABLES
Table No. Title PAGE NO .
TABLE IV—l Station Location IV—6
TABLE IV—2 Process Waste Flow Recorded IV—A—2
At Final Effluent (WEO2)
TABLE IV—3 pH and Temperature IV—A-5
TABLE IV-4 Analytical Data (TNFR, IV—A—7
cyanide, dissolved fluoride,
total phosphorus and oil, and
grease)
TABLE IV—5 Analytical Data (total and IV—A-ll
dissolved zinc, manganese,
iron and lead)
TABLE IV—6 Analytical Data (total and IV—A- 15
hexavalent chromium, total
and dissolved copper and
nickel)
TABLE IV—7 S mmiary of Historical Data IV—C—l
and EPA Survey Results
‘v —li
-------
LIST OF FIGURES
FIGURE NO. TITLE
FIGURE IV—l Flow Diagram, Western Electric Industrial
Waste Treatment
FIGURE IV—2 Total Copper, Frequency of Occurrence
FIGURE IV—3 Total Iron, Frequency of Occurrence
FIGURE IV—4 Total Phosphorus, Frequency of Occurrence
FIGURE IV—5 Dissolved Fluoride, Frequency of Occurrence
FIGURE IV—6 Cyanide, Frequency of Occurrence
FIGURE IV—7 Total Metals Minus Dissolved Metals, Frequency
of Occurrence
FIGURE IV—8 Flow, Frequency of Occurrence
Iv—i ii
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WESTERI4 ELECTRIC
NORTH ANDOVER, MASSACHUSETTS
May 30 and 31, 1973
The Western Electric plant, located in North Andover, Massachusetts,
produces printed circuit boards, thin film devices, and various metal
plated parts and accessories for communications systems. Ferrite powder
for molding into transformer parts is also produced. The North Andover
plant employs 10,000 persons and operates three shifts. The printed cir—
cult board and plating shops operate two shifts per day from 6:30 A.M. to
3:00 P.M., and 4:00 P.M. to 12:30 A.M. Thin film devices are also
produced during these shifts as well as on a third shift from 10:00 P.M.
to 6:30 A.M.
The priiited circuit board operation consists of a series of chemical
cleaning baths, plating tanks of copper and gold, rinse water baths and
component etchings. The small metal plating shop is a job-shop operation.
When an urgent need for parts exists, or when small quantities are
desired the parts are produced In this plating room.
Thin film devices are miniaturized units similar to circuit boards.
A substrate, composed of 99.5% alumina is metallized with tin, lead or
gold, followed by a series of photo—resist applications, development and
removal. Copper and nickel are then plated, followed by another series of
photo—resist applications, development and removal. The product is then
subjected to a final series of etchings and gold, titanium and palladium
plating operations.
All of the plant’s liquid waste is generally segregated into sanitary
waste or industrial waste. Sanitary wastes and ammonium persulfate industrial
wastes are treated in a wastewater treatment facility which consists of
IV-l
-------
extended aeration and sand filtration, Industrial waste treatment
consists of specialized physical—chemical treatment.
Industrial Waste Treatment
Western Electric’s industrial waste treatment facility has a
design capacity of 18.9 liters per second (ips) (300 gallons per
minute (gpm)), however currently the plant is overloaded by as much
as 50%.
On a daily basis, the industrial waste contains approximately
60% printed circuit board and metal finishing rinse waters and 30%
thin film device rinse waters. A reasonably constant discharge of
ferrite waste, and intermittent discharges of varying quantities of
cooling tower blow-down and concentrated dumps make up the remainder
of the industrial waste. Concentrated dumps are collected and bled
into the treatment system.
The liquid wastes from the previously described processes contain
acids, alkalis, cyanides and metals in both the dissolved and suspended
form. For treatment, these wastes are separated into four classifi-
cations: acid/alkali, cyanide, chromium and ferrite wastes. Figure IV—l
is a flow diagram of the treatment system.
Dilute and concentrated acid/alkali wastes are collected in two
separate surge tanks located outside the treatment building. As the
dilute wastes are pumped to the general collection flume, concentrated
acids and/or alkalis are bled in. Neutralization is accomplished with
sodium hydroxide. Hydrofluoric acid is collected in a separate surge
tank, neutralized with lime and pumped to the sludge storage tank.
IV-2
-------
I I
I I IJAYI I
I STC I
1
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Scull
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1 t&YuduT I
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AC IATIS.
Talk
-------
All cyanide wastes are piped directly to one of three 75 cubic meter
(20,000 gallon) batch treatment tanks. Concentrated cyanide wastes are
stored and bled into the system. The cyanide destruction system (con-
version to carbon dioxide, nitrogen and water) utilizes destruction by
chlorination (sodium hypochiorite) at an elevated pH. Oxidation
reduction potential probes and pH probes monitor the treatment tanks
and control chemical addition. Every two or three days a treated tank
of cyanide waste having a high chlorine residual is pumped to the general
collection flume.
Chromium wastes are collected in a surge tank outside the treat-
ment plant. The chromium wastes consist of 98% cooling tower blow—
down and 2% process waste. In the treatment system, the pH is lowered
to less than 2.5 with sulfuric acid and sodium bisulfite is used to
reduce the hexavalent chromium (Cr+6) to trivalent chromium (Cr+ 3 ). The
chromium reduction system is capable of continuous operation, however it
operates intermittently depending upon the liquid level in the surge tank.
Following chromium reduction the waste is discharged to the general
collection flume where it mixes with the neutralized acid/alkali waste
and the treated cyanide waste.
The general collection flume empties into a rapid mix chamber where
ferric chloride and ferrite waste combines with all other wastes. Ferric
chloride is a waste product, which is also a useful coagulant.
Ferrite waste is a dark brown liquid which contains manganese carbonate.
zinc oxide, iron oxide, gum arabic and zinc stearate.
Following rapid mix, the waste flows through aeration and deaeration
IV-4
-------
for final oxidation of iron. As the waste enters the center of
the clarifier an anionic polyelectrolyte is added to promote
flocculation. Currently Western Electric is experimenting with ferric
sulfate and various polymers as coagulant aids.
Following clarification, the waste discharges over a 600 V—notch
weir. Just prior to discharge the filtrate from the sludge vacuum
filter enters the waste stream. The de—watered sludge is trucked to
a landfill.
Sampling Information
On Nay 30 and 31, 1973, U. S. Environmental Protection Agency
Region I personnel, collected samples at the Western Electric, North
Andover, industrial waste treatment plant. On each of two days, a
24—hour composite sample, six 4—hour composite samples, and several
grab samples were collected at various stations. Samples were collected
from the cyanide destruction tank following treatment, prior to and
following chromium reduction, at the ferrite waste discharge, at the
influent acid/alkali waste stream and at the final effluent following
clarification. Table IV—l identifies and describes the sampling stations.
Composite samples collected from the acid/alkali waste stream
(WEO1) and the final effluent (WEO2) were collected proportional to
flow. Due to the fairly constant flow rate of the ferrite waste,
composites at this station (WEO6) were composited with a constant
amount of sample being added hourly.
All samples except hexavalent chromium were collected and analyzed
in accordance with U.S. E.P.A. Methods for Chemical Analysis of Water
IV-5
-------
TABLE IV-l
STA IION LOCATION
Western Electric
North Andover, Massachusetts
STATION NO. DESCRIPTION
WEO1 Acid/alkali waste following neutralization,
Just prior to entering the general collec-
tion flume
WEO2 Final effluent at the 600 V—notch weir
WEO3 Cyanide destruction tank No. 1
WEO4 Influent to chromium reduction system at
the surge tank
WEOS Effluent from the chromium reduction system,
Just prior to entering the general collection
flume
WEO6 Ferrite waste as it enters the rapid mix
chamber
IV-6
-------
and Waste, 1971 . Hexavalent chromium was collected and analyzed in
accordance with Standard Methods for the Examination of Water and
Wastewater, Thirteenth Edition . The samples were analyzed for total and
dissolved metals (copper, nickel, iron, zinc, manganese, lead),
total non—filterable residue, total and hexavalent chromium, dissolved
fluoride, total phosphorus and total cyanide. In addition, several grab
samples were analyzed for oil and grease. The analytical results are
shown in Tables IV-3 through IV—6 which appear in Appendix IV—A.
During the 48 hour sampling period the treatment plant had an
“upset”. At approximately 0200 hours on May 31, the ferric chloride
proportioning pump failed and shortly thereafter the pH of the final
effluent increased sharply. For the remainder of the first day (5 hours),
ferric chloride was gravity fed through a hose to the acid/alkali waste
stream (WEO1). Prior to starting the second day’s sampling, the ferric
chloride gravity feed line was moved to discharge into the rapid mix
chamber. Ferric chloride is a very corrosive liquid and Western Electric
ha; iau i -uuv e mainEaining equipment. To eliminate this
problem, Western Electric plans to replace ferric chloride with ferric
sulfate.
By visual inspection, the ferrite waste appeared to be overloading
the treatment system with dark brown solids during the first sampling day.
It was dark brown and contained large amounts of fine solids. Also on
this day a reddish brown color was imparted to the wastes in the clarifier
and was visible in the final effluent. During the second day, the ferrite
waste was light brown and the final effluent appeared clear.
IV—7
-------
Analytical Results and Conclusions
The industrial wastes from the Western Electric processing plant
have been segregated into four waste streams (cyanide, chromium, acids!
alkali and ferrite wastes) for treatment. Since cyanides and chromiunis
receive pre—treatment, they will be discussed separately. The acid!
alkali waste, ferrite waste and the pre—treated cyanide and chromium
wastes are combined and treated for the removal of generalized waste
constituents——heavy metals, residues, etc. Therefore the remaining
chemical parameters will be discussed with respect to the entire waste
stream.
Cyanide
During the two day sampling period cyanide destruction was inadequate
Two grab samples of treated cyanide wastes from tank No. 1 (WE03) con-
tained 3.25 and 1.87 mg/l of cyanide. During the period that this
treatment tank was being drained, two grab samples of the final effluent
contained <0.01 and 1.75 mg/l of cyanide. Thuc three f tho ft r cyaaL te
samples analyzed contained higher cyanide levels than the 0.1 mg/l
limitation proposed in Schedule B of EPA ’s effluent limits for metal
finishing industries. The proposed U. S. Environmental Protection Agency
effluent limits for metal finishing industries are shown in Appendix TV—B.
In conjunction with the high cyanide concentrations were the low pH
values of 6.9 and 7.5 for the two samples collected from tank No. 1
(WEO3). The low pH probably prevented further destruction of cyanide
since the optimum pH range for single stage cyanide destruction is 8.5
to 9.5. Maintaining a higher pH during cyanide treatment will improve
1 1 7-8
-------
the destruction of cyanide probably to levels which would comply with
Schedule A (0.03 mg/i) of the proposed limits. If raising the pH does
not in itself reduce cyanide concentrations to an acceptable level, the
treatment system has the capacity to provide a longer detention time,
which should insure satisfactory destruction. Also, prior to discharge
to the general collection flume any chlorine residual should be removed.
Chromium Reduction
The chromium reduction system discharged for two short periods
during the sampling program. Once during each period grab samples
were collected of the reduction system’s influent and effluent. Based
upon these samples, hexavalent chromium reduced 96% and 98%. Sixty—
two and 39 ugh of hexavalent chromium were discharged to the general
collection flume (WEO5). The 24—hour composite samples of the final
effluent (WEO2) contained 39 and 30 ugh of hexavalent chromium and
110 and 120 ug/l of total chromium which are less than the proposed
Schedule A limitations of 50 ugh and 250 ug/l respectively. Th e
concentrations are, however, significant considering the length of
time chromium wastes were discharging through the system.
The high hexavalent values may be due to reoxidat ion of trivalent
chromium by the chlorine present in the cyanide waste stream. The chlorine
residual of the treated cyanide waste was not obtained during the survey,
however according to a discussion with one of the treatment plant operators
the chlorine residual of the treated cyanide waste is generally high.
General Waste Flow
Flow
As previously stated, the treatment system currently operates 50%
IV—9
-------
higher than the hydraulic design capacity at peak flow periods and 15%
to 20% above hydraulic design capacity on the daily average. The
discharge at the final effluent (WEO2) ranged from 11 ips (170 gpm) to
28 ips (440 gprn) with 24—hour averages of 24 ips (370 gpm) and 22 ips
(340 gpm). Hourly flow rates are shown in Table IV—2. This wide variation
in flow rates is not unusual in a metal finishing shop which operates as a
job—shop. Intermittent discharges of treated cyanide and chromium wastes
as well as concentrated wastes which are bled into the system add to flow
rate variations.
pH and Temperature
The pH at the influent acid/alkali waste stream, following
neutralization (WEO1), ranged from 3.1 to 11.0 but generally remained
between 6.0 and 9.0. For the first 18 hours of the sampling program,
the pH of the final effluent (WE02) ranged from 6.7 to 8.6 with the
majority of the readings between 8.0 and 8.6. At 0200 hours on May 31,
the ferric chloride proportioning pump malfunctioned and the pH
1 a ed tc IC.7. T & L.U remainder or the sampling period ferric
chloride was gravity fed to the rapid mix chamber. The pH at the final
effluent remained above 10.0 for four hours and then slowly decreased
to 8.5. The pH of the ferrite waste (WEO6) ranged from 6.5 to 7.7.
The temperature at WEO1 ranged from 18.0°C to 22.0°C. No sub-
stantial increase or decrease was noted during treatment. The final
effluent ranged from 18.0°C to 21.5°C.
hourly pH and temperature readings for stations WEO1, WE02 and
WEO6 are shown in Table IV—3.
‘v—jo
-------
Total Non—Filterable Residue
The 24—hour composite sample of the influent acid/alkali waste
(WEO1) for the first day (May 30, 1973) was not available, however a
20—hour composite sample contained 137 mg/i of total non—filterable
residue (TNFR). The 24—hour composite sample of the ferrite waste (WE06)
contained 169 mg/i TNFR. Based on these values, approximately 138 mg/i
TNFR enter the clarifier. The 24—hour composite sample of the final
effluent contained 12 mg/i TNFR, which represents about 87% TNFR removal
through the clarifier. The second day of sampling (May 31, 1973) showed
about 84% reduction of TNFR through the clarifier.
During the two day sampling program, the 4—hour composite samples
at the final effluent (WEO2) ranged from 1 to 156 mg/i TNFR with a
median of 9 mg/i, and grab samples ranged from 1 to 74 mg/i TNFR with
a median of 6 mg/i.
During this period the concentrations in the final effluent were
less than the proposed Schedule B limitation 92% of the time, and less
thciu’ Sdzeduie A 5O or the time.
Dissolved Fluoride
Operating day (24-hour) composite samples at the influent acid!
alkali waste (WEO1) contained 16.4 and 11.6 mg/i of dissolved fluoride.
Twenty—four hour composite samples of the final effluent (WE02) con-
tained 11.8 and 14.4 mg/i of dissolved fluoride, which indicates no
removal of dissolved fluoride in the treatment system. Four hour
composite samples at WE02 verified the 24—hour composite samples ranging
from 11.2 to 16.4 mg/i. All samples analyzed at WEO2 were less than
Schedule A limit proposed by EPA.
‘v—li
-------
Total Phosphorus
Total phosphorus results at both WEO1 and WE02 showed wide fluc-
tuations. On May 30, 1973 the 24—hour composite at WEO1 contained
0.34 mg/i, but rose to 0.42 mg/i at WEO2. The 4—hour composites at
WEO2 did not correlate with the 24—hour composite results, which may
be due to the fact that only three 4—hour composites were collected
during the 24—hour sampling period.
Oil and Grease
Grab samples at the influent acid/alkali waste (WEO1) ranged
from 0.l to 23.0 mg/i of oil and grease with the median value being
15.2 mg/i. Oil and grease in the effluent (WEO2) never exceeded
2.7 mg/i.
Heavy Metals
Total and dissolved metals (copper, nickel, zinc, manganese, iron
and lead) were measured at the acid/alkali influent to the general
collection flume (WEOl) and at the final effluent weir (WEO2). Because
th 1 r c iiit c.f i. .Ldue in ihe Lerrite waste stream, only total
metals were measured at Station WEO6.
Of the metals analyzed, only iron and copper enter the clarifier
at concentrations higher than the proposed EPA effluent limits, therefore
only iron and copper will be discussed. A large portion of the influent
metals are in the dissolved state. Very high concentrations of zinc,
manganese and iron enter the rapid mix tank from the ferrite waste line,
however this line represents less than 3% of the total waste flow.
Based on a 24—hour composite sample, the irifluent acid/alkali
IV—l 2
-------
wastes contained 1,420 ugh of dissolved copper on May 30. Also based
on 24—hour composite samples, the ferrite waste adds a negligible amount
of copper. Following clarification (WEO2) dissolved copper had reduced
to 1,190 ugh (24% removal) on May 31. No correlation can be found
for the the 4—hour composite samples and grab samples on May 31.
On both sampling days the quality of the effluent follows a
definite pattern. Concentrations of both total and dissolved copper
increased significantly during the early morning hours. Both 4—hour
composite and grab samples indicated a sharp increase at about 0200
hours on both sampling days. Some of the iron and lead samples
indicate similar results.
On May 30, 1973, the dissolved copper concentration of the 24—
hour composite sample at WEO2 exceeded the proposed Schedule A limitation,
and on May 31, exceeded both Schedule A and B. Four (33%) of the 4—
hour composites analyzed exceeded both Schedules A and B Of the 11
grab samples collected at WE02, 5 exceeded Schedule A and 2 of those
.i fl_ I - - —
_.____ c%s ijt.&LCUUS D .
Total iron concentrations in the effluent usually exceeded both
Schedule A and B total iron limits proposed by EPA, however dissolved
iron was generally within the proposed limits. Total iron concentrations
in the acid/alkali waste stream were very high ranging from 5,200 to
135,000 ug/l. Dissolved iron ranged from less than 100 to 80,000 ugh.
In the two composite samples of the ferrite waste, the total iron con-
centrations were 142,000 ugh and 415,000 ug/l.
The total iron in the composite samples of the final effluent
IV— 13
-------
ranged from 600 to 40,000 ugh. Both 24—hour composite samples
exceeded the proposed Schedule B effluent limit and 7 out of 12 of
the 4—hour composite samples exceeded that limit. The dissolved iron
in the 24—hour composite sample for Nay 31 also exceeded the proposed
Schedule B limit. Based upon the 24—hour composite samples, total iron
concentrations were reduced more than 90% on the first day and approxi-
mately 52% on the second.
From the foregoing information, it is obvious that the concentration
of copper and iron entering and leaving the treatment plant fluctuate greatly.
On the first day of sampling, removal of copper was poor and removal of iron
was fair. However, on the second day both removal rates were poor, and
neither day should be considered indicative of a well operated plant.
The decline in treatment efficiency may be attributable to the failure
of the ferric chloride proportioning pump and subsequent gravity
feeding of ferric chloride. Therefore the results of this study have
dubious value as indicators of a well run treatment plant. They do,
tlia i..uadiduns whicn can develop during a plant upset.
Historical Data
A review of Western Electric’s historical data, submitted to the
Massachusetts Division of Water Pollution Control, indicates that the
results obtained during the May 30 and 31, 1973 report study are
generally on the high end of the range of historical results, as
summarized in Table IV—7, Appendix IV—C. Appendix IV—C also contains a set
of probability plots of total copper (Figure IV—2), total iron (Figure IV—
3), total phosphorus (Figure IV—4). dissolved fluoride (Figure IV—5), and
IV—14
-------
cyanide (Figure IV—6) concentrations versus the percent occurrence. The
data for the plots was obtained from the historical data shown in
Appendix IV—D.
A probability plot of the report study total metals minus dissolved
metals (Figure IV—7) indicates that 75% of the time the difference
between a total metal and a dissolved metal will be 1 mg/i or
less, which is proposed in the EPA guidelines of metal finishing
industries. Ninety percent of the time the difference will be
less than or equal to 3.3 mg/i.
Summary of Conculsions
The Western Electric industrial waste treatment plant was not
operating as designed. During the study period the daily flows were
20% higher than design capacity with peak flows up to 50% higher.
In addition, at 0200 hours on May 31 the ferric chloride pump failed.
This caused the pH of the effluent to increase and solids and metal
removal rates to decrease. Based upon the first day’s operation, this
treatment plint- h t e p2b!11ty f L”eL j_ Loncentrations
more than 90%, however the copper and iron concentrations in the
influent wastes are so high the effluent total metal concentrations
still exceed the January 1973 effluent limits EPA proposed for metal
finishing industries. Increasing the residence time of the wastes in
the clarifier would probably improve removals.
The ferrite waste, although less than 3% of the entire waste flow,
has significant impact upon the plant effluent. Inspection of the data
shows that the ferrite line was responsible for approximately 90% of
the total zinc and manganese and approximately 20% of the total iron
‘v—is
-------
entering the treatment plant. In addition, the ferrite waste imparted
a reddish brown color to the clarifier which carried over into the
final effluent on the first day of sampling but was not present on the
second day.
The cyanide treatment system was not providing adequate destruction.
The measured pH of the treated wastes were 7.0 and 7.3, slightly less
than the 7.5 — 8.5 pH range usually preferred for complete destruction.
Minor modifications in plant operation (increasing pH and modifying
chemical additions) can probably reduce cyanide concentrations to
essentially zero.
The chromium reduction system is set up as a continuous treatment
system but operates intermittently. Supposedly chromium is not a process
waste per Se. The treatment system is for spent cooling water from
Western Electric’s air conditioning system. Based upon the two samples
taken and assuming that prior to treatment all chromium was hexavalent, the
treatment system removes more than 99.8% of the hexavalent chromium.
Whether this d c r nf e t’ ’ t c ld aiiL r y em operated
continuously is unknown. Also it should be noted that the final effluent
at Western Electric contained high hexavalent chromium concentrations
considering the amount of chromium wastes discharged to the system. Tri-
valent chromium is reoxidized to the hexavalent state by chlorine and
Western Electric’s treated cyanide wastes generally contains a high
residual chlorine.
IV—l 6
-------
REFERENCES
1) Obtained from the Massachusetts Division of Water
Pollution Control file on Western Electric, North
Andover, Massachusetts.
IV— 17
-------
APPENDIX IV-A
ANALYTI CAL DATA
-------
SAMPLE ANALYSES
STANDARD ABBREVIATIONS AND UNITS OF MEASURE
ANALYSIS REPORTED DESCRIPTION MEASURED IN
Temperature Sample temperature at Degrees Centigrade (°C)
time of collection
pH Standard Units (SU)
Total Non—Filterable Total suspended solids Milligrams per liter
Residue (mg/i)
Dissolved Fluoride mg/i as fluoride
Total Phosphorus mg/i as phosphorus
Oil and Grease mg/i as oil and grease
(hexane extractable)
Cyanide mg/i as cyanide
Hexavalent Chromium Micrograms per liter
(Cr 46 ) (ugh) as hexavalent
chromium
Total Metals Total: Copper ug/l
Nickel
Zinc
Tin
Lead
Cadmium
Chromium
Silver
Manganese
Iron
Dissolved Metals Dissolved: Copper ugh
Nickel
Zinc
Tin
Lead
Cadmium
Silver
Manganese
Iron
Letters Preceding a Reported Value Denote the Following:
J — value not accurate (estimated)
K — actual value is known to be less than value given
R — sample lost
IV-A-l
-------
TABLE IV—2
Process Waste Flow Recorded at Final Effluent (WEO2)
WESTERN ELECTRIC, NORTH ANDOVER, MASSACHUSETTS
May 30 and 31, 1973
Time FLOW
Date ( Hours) Liters per minute (1pm) Gallons per minute (gpm )
05/30/73 0730 970 255
0840 1290 340
0930 1250 330
1030 1360 360
1130 1440 380
1230 1510 400
1330 1510 400
1430 1510 400
1530 1670 440
1630 1550 410
1735 1440 380
1835 1420 375
‘19 5 12CC 34U
2035 1590 420
2135 1630 430
2235 1440 380
2335 1420 375
05/31/73 0035 1440 380
0135 1420 375
0230 1400 370
0330 1360 360
IV-A-2
-------
TABLE IV—2 (CONTINUED)
Process Waste Flow Recorded at Final Effluent (WEO2)
WESTERN ELECTRIC, NORTH ANDOVER, MASSACHUSETTS
May 30 and 31, 1973
Time FLOW
Date ( Hours) Liters per minute (1pm) Gallons per minute (gpm )
05/31/73 0430 1210 320
0530 1170 310
0630 1080 285
Average 1390 1pm 367 gpm
Total Discharge 2000 cubic meters/day 528,000 gallons/day
IV—A-3
-------
TABLE IV-2 (CONTINUED)
Process Waste Flow Recorded at Final Effluent (WE02)
Western Electric, North Andover, Massachusetts
May 30, 31 and June 1, 1973
Time FLOW
DATE ( Hours) Liters per minute (1pm) Gallons per minute jgpm )
05/31/73 0800 1210 320
0900 1400 370
1000 1480 390
1100 1510 400
1200 1530 405
1300 1510 400
1400 1510 400
1500 1480 390
1605 1510 400
1705 1480 390
1805 1510 400
1905 1570 415
2005 1550 410
2105 1590 1 2fl
2205 1440 380
2300 1480 390
2400 1390 366
06/01/73 0100 790 210
0200 790 210
0300 790 210
0400 640 170
0500 830 220
0600 830 220
0700 1320 350
24—hour Average 1300 ipit 3 4 3 P ’
_ 0ThL DISCHARGE 1872 cubic meters/day 493,000 gallons/day
-------
TABLE’IV—3
pH AND TEMPERATURE
WESTERN ELECTRIC - NORTH ANDOVER, NASSACHUSEI?S
DATE TIME WEO 1 WE02 WEO6
pH TEMP. pH TEMP pH TEMP.
oc oc oc
5—30 0730 — 18.0 — 18.5 — —
0840 4.4 19.0 8.2 18.5 6.5 22.5
0930 7.9 19.0 8.1 19.0 6.6 26.0
1030 — — — — 6.4 27.0
1130 82 20.0 8.1 19.5 8.1 33.0
1230 6.1 21.0 8.0 20.5 6.6 27.0
1330 63 21.0 8.0 21.5 6.8 21.5
1430 6.3 21.0 7.9 21.0 7.0 19.5
1530 7.7 21.5 7.9 21.0 — —
1630 8.9 21.0 8.0 20.5 7.2 21.5
1735 6.0 21.0 8.2 21.0 6.8 20.5
1835 4.1 20.5 8.3 20.0 7.1 18.5
1935 5.6 20.0 8.4 20.0 7.2 19.0
2035 9.5 19.5 8.5 20.0 73 18.5
2135 4.5 19.0 8.4 20.0 7.2 18.0
2235 3.1 19.0 8.4 19.0 7.2 17.5
2330 11.0 19.0 8.6 19.0 7.3 17.5
5—31 0030 3.4 19.0 8.4 18.5 7.0 17.5
0130 7i 4 18.5 6.7 18.0 6.8 17.5
0230 4.3 19.5 10.7 19.0 7.1 18.0
0330 7.3 20.0 10.5 19.5 6.8 18.0
0430 7.1 19.5 10.2 19.0 6.8 18.0
0530 88 20.0 10.0 19.5 6.8 17.5
0630 9.0 20.0 9.8 19.5 6.8 17.5
-------
‘CABLE IV-3 (CONTINUED)
pH AND TEMPERATURE
WESTERN ELECL RIC - NORTH ANDOVER, MASSACHUSETTS
DATE TIME WEO 1 WEO2 WEO6
1)11 TEMP. pH TEMP pH TEMP.
cc OC oc
5—31 0800 4.6 20.0 9.5 19.0 7.0 17.5
0900 ‘.8 20.0 9.0 19.0 6.6 18.0
1000 (.4 20.3 9.0 19.5 7.0 17.5
1100 ‘.4 21.0 9.0 20.0 6.9 24.0
1200 .8 20.5 9.0 20.5 7.0 23.5
1300 S’. l 21.0 8.7 21.0 6.9 24.5
1400 E.7 21.5 8.8 21.0 7.5 23.5
1500 ..9 22.0 7.8 21.0 7.1 19.0
1605 .8 21.5 8.7 21.0 7.2 17.5
c . 1705 8.5 20.5 8.7 21.0 7.0 18.0
1805 9.3 20.0 8.7 20.5 7.2 18.0
1905 9.1 20.0 8.7 20.5 7.2 17.5
2005 10.2 19.5 8.5 20.5 7.1 17.5
2105 10.3 19.5 8.6 19.5 7.2 17.0
2205 9.5 19.5 8.8 19.5 7.3 16.5
2300 10.6 19.5 8.9 18.5 7.2 17.0
2400 10.5 21.5 9.2 19.5 7.4 16.5
6—1 0100 9.0 21.0 8.9 19.5 72 17.0
0200 7.1 21.0 8.6 19.5 7.1 17.0
0300 7.4 21.5 8.8 18.5 7.7 17.0
0400 8.0 21.5 9.2 19.0 7.5 17.0
0500 6.7 21.0 8.7 20.0 7.0 17.0
0600 6.6 20.5 8.4 20.0 7.5 16.5
0700 7.0 20.5 8.5 20.0 7.2 16.5
-------
TABLE 1V-4
ANILYTICAL DATA
Western Electric Company
North Andover, Massachusetts
May 30 and 31, 1973
Station
Total
Cyanide
Dissolved
Total
Oil, and
Number Date Tine Non—Filterable
Residue (mg 1 I] ’
(mg/i)
•
Fluoride
(mg/i)
Phosphorus
(mg/i)
Grease
(mg/i)
Comp—24
WEO 1 5/30 0730—0730 0.34
Comp—2 4
5/31 0800—0800 34 16.4 1.08 —
Comp—20
5/30 0730—0330 137 11.6 — —
Comp—4
1130—1530 20 —
Comp—4
• 1530—1930 123 —
Comp—4
2330—0330 116 _
Comp—4
5/31 0800—1200 34
Coinp—4
1930—2330 29 —
Comp—4
6/01 0400—0800 42 —
5130 1030 29 — 5.0
1330 — KO.1
1630 • 8 23.0
‘I
a
-------
TABLE 1V4 (CONTINUED) 2
ANALYTICAL DATA
Western Electric Company
North And Dyer, Massachusetts
May 30 and 31, 1973
Station
Total
Non—FilterabLe
Cyanide
Dissolved
Fluoride
Total
Phosphorus
Oil and
Crease
Number Date
Time Residue (tng/.(.) (in_g /1)
(mg/i)
(mg/ i)
(mg/i)
WEO]. 5/30 2130 15.4
5/31 0130 45 15.2
0430 — 1.6
0800 26 — —
1700 30 —
6101 0200 7 —
WE O2 5/30 Coinp—24
0730—0730 12 — 11.8 0.42
Comp—24
5/31. 0800-0800 10 14.4 0.18 —
Comp—4
5/30 0730—1130 156
Comp—4
1130—1530 14 — 16.4 0.17
Comp—4 6
1530—1930
WEO2 Comp—4
1930—2330 16 9.6 0.01 —
-------
TABLE IV—4 (CONTINUED)
j NALYTICAL DATA
West!rn Electric Company
North Andover, Massachusetts
M y 30 and 31, 1973
Station
Number Date
Total
- Non—Filterable
Time Residue (cng/l)
Cyanide
(mg/i)
Dissolved
Fluoride -
(mg/i)
Total
Phosphorus
(mg/i)
Oil and
Grease
(mg/i)
WEO2 5/30 Comp—4
2330—0330 8 0.01
Comp—4
0330—0730 4 —
-4
Comp—4
0800—1200 10 14.0 0.05 —
Comp—4 I
1200—1600 6
Comp—4
1600—2000 1 —
Comp—4
2000—2400 1 16.0 0.01
Comp—4
2400—0400 10 11.2 0.32
Comp—4
6/01 0400—0800 46 —
5/30 1030 74 — — 1.0
1330 14 R 2.0
1630 43 — K0.1
-------
TABLE IV-.4. (C0NT ..
ANAE 1 YTICAL DATA 4
Wester t Electric Company
North Aniover, Massachusetts
May 30 and 31, 1973
Dissolved
Total
Oil and
Fluoride
Phosphorus
Grease
(mg/i)
(mg/i)
(mg/i)
2230 1 (0.01
5/31 0130 4 — — 2.7
0430 5 — 0.5
0800 2
1200 1 — —
1700 1 — — —
2100 3 —
6/01 0200 10 — — —
“ 0600 44 —
WEO3 5/30 1920 3.25
2130 1.87 —
WEO5 5/31 2240 — — —
Comp—24.
WEO6 5/31 0800—0800 1000 — —
Comp—16
5/30 1530—0730 169 K 0.2
Station
Number
WEO2
Date
5/30
‘I
Time
2130
Total
Non—Fi1ter ble
Residue_ (m /1)
7
Cyanide
(mg / 1)
1.75
a
-------
TABLE IV—5
ANALYTICAL DATA
Western Electric
North Andover, Massachusetts
May 30 and 31, 1973
Station - Time Zinc ugf1 Manganese (ugh) Iron (ugh) Lead (ugi].)
Number Date (hours ) Total Dissolved Total Dissolved Total - Dissolved Total Dissolved
Comp—24
WEO1 5/30 0730 —0730 240 — 420 — 53,200 — 300’ —
Comp—24
5131 0800—0800 130 40 150 60 14,700 2,200 400 K50
Comp—20
5130 0730—0330 — — — — — —
Comp—4
1130—1530 140 140 140 90 5,200 K100 300 50
Comp—4
1530—1930 340 310 715 645 115,000 40,000 400 50
Comp—4
2330—0330 450 410 840 770 135,000 80,000 300 200
Comp—4
5/31 0800—1200 160 90 180 120 12,500 1,000 200 150
Comp-4
1930-2330 90 • 20 130 50 9,200 2,800 400 100
Comp—4
6/01 0400—0800 110 30 .160 130 19,600 4,600 200 50
5/30 1030 150 10 150 10 8,480 1(100 400 1(50
U 1330 — — — — — — —. —
-------
TABLE IV—5 (CONTINUED)
ANALYTICAL DATA 2.
Western Electric
North Andover, Massachusetts
May 30 and 31, 1973
Station Time Zinc (ug/1 Manganese (ugh) Iron (ugh.) Lead (ugh)
Number Date (hours) Total Dissolved Total Dissolved Total Dissolved Total Dissolved
WEO 1 5/30 1630 90 90 140 K10 10,100 1(100 200 1(50
2130 — — — — — — — —
5131 0130 60 45 230 220 17,200 1,600 50 1(50
0430 — — — — — — — —
0800 400 100 320 210 14,000 5,400 200 50
1700 200 20 120 30 10,300 1(100 850 1(50
6/01 0200 100 70 200 130 21,600 20,100 300 200
Comp—24
WEO2 5/30 0730-0730 380 55 555 260 5,150 400 50 1(50
Comp—2 4
5/31’ 0800—0800 180 20 240 80 7,000 1,600 100 1(50
Comp—4 •
5/30 0730—1130 805 60 805 160 16,600 1,800 100 1(50
Comp—4
1130—1530 980 20 1,270 380 8,500 400 1(50 1(50
Comp—4
1 30—1930 360 .20 780 530 2,600 100 150 1(50
Comp—4
1930—2330 350 1(10 380 140 2,200 1(100 1(50 1(50
-------
TABLE IV— (CONTINUED) 3.
ANALYTICAL DATA
Western Electric
North Andover, Massachusetts
May 30 and 31, 1973
Station Time Zinc (ugIl Manganese (ugh) Iron (ugh) Lead (ugh)
Number Date (hours) Total Dissolved Total Dissolved Total Dissolved Total Dissolved
WEO2 Comp-4
5/30 2330—0330 190 40 280 140 3,200 1(100 1(59 1(50
Coinp—4
I31 0330-0730 100 20 65 10 1,400 1(100 K50 1(50
Comp—4
0800—1200 95 1(10 95 1(10 1,000 1(100 1(50 1(50
Comp—4
1200—1600 140 10 280 160 900 1(100 1(50 1(50
Comp—4
1600—2000 200 1(10 280 130 800 1(100 1(50 1(50
Comp—4
2000—2400 80 1(10 65 20 600 1(100 1(50 1(50
I
Comp—4
“ 2400—0400 65 20 80 20 3,900 800 100 1(50
Comp—4 .
6/01 0400—0800 230 100 360 120 40,000 17,600 200 100
5/30 1030 1,900 45 2,000 85 15,600 800 50 1(50
1330 900 30 1,250 515 7,250 500 1(50 1(50
• “ 1630 660 40 920 520 3,600 100 1(50 1(50
2130 370 20 480 150 2,700 -100 1(50 1(50
-------
TABLE IV—5 (CONTINUED)
AFALYTICAL DATA
4.
Western Electric
North Andover, Massachusetts
May 30 and 31, 1973
Station
Zinc
(ug! 1)
Manganese (ugfl)
Iron
(ugh)
Total
Dissolved
Number
Total
Dissolved
Total Dissolved
Total
Dissolved
Time
ours)
2230
0130
0430
0800
“ 1200
1700
2100
Date
WEO2 5/30
5/31.
I ’
6101
‘I
340
K10
10
120
150
10
40
240
140
220
140
480
240
210
330
110,000
41,000
0200
0600
200 420
40 70
K10 40
K10 200
20 620
1(10 75
30 140
480
— 110,000
38,000
1(100
1(100
1(100
1(100
1(100
1(100
1,200
1(50
K50
K50
1(50
1(50
1(50
50
1,000
1,500
800
1,000
2,000
600
7,800
55,000
41,500
142,000
I
WE06 5/31 Comp—24
0800—0800
5/30 Comp—l6
1530—0730
1(50
1(50
1(50
1(50
1(50
1(50
100
400
50
1(50
a
a
-------
Date Time
5/30 Comp—24
0730—0730
Comp—24
5/31 0800—0800
5/30 Comp—2 0
0730—0330
Comp—4
1 1130—1530
Comp—4
I, 1530—1930
Comp—4
fl ‘ 2330—0330
Comp—4
0800—1200
Comp—4
1930—2330
Comp—4
0400—0800
1030
tation
iumber
JEO 1
TABLL IV-6
ANALYTICAL DATA
Western Electric
llorth Andover, Massachusetts
May 30 and 31, 1973
Chromium (ugh) Copper (ugh)
Total Hexavalent Total Dissolved
— — 29,200 —
— — 9,340 1,420
Nickel (ugh)
Total Dissolved
65 —
50 10
a
—
a
a
a
5/33.
I,
6/0 ].
5/30
a
12,000
3,420
40
40
54,500
46,000
100
.
60
63,500
56,000
100
80
•
6,310
2,200
4
65
50
4,610
1,540
20
RiO
6,280
1,780
10
.
20
5,310
50
-------
TABLE IV—6 (CONTINUED) 2.
ANALYTICAL DATA
Western Electric
North Andover, Massachusetts
May 30 and 31, 1973
Station Chromium (ugh) Copper (ugh) Nickel (ugh)
Number Date Time Total Hexavalent Total Dissolved Total Dissolved
WEO 1 5/30 ‘ 1330 — — — — —
1630 — — 8,940 360 20 1(10
2130 — — — — — —
5/31 0130 — — 6,840 1,080 20 1(10
0430 —, — — — — —
0830 — — 8,240 7,540 90 100
1700 — — 7,885 180 30 1(10
6/01 0200 — — 7,380 6,100 20 20
WE O2 Comp—24
5130 0730—0730 110 39 1,760 480 20 20
Comp—24
5/31 0800—0800 120 • 30 2,540 1,110 1(10 1(10
Comp—4
5/30 0730—1130 — — 5,260 1,020 30 10
Comp-4
1130—1530 — 1,820 260 30 1(10
Comp—4
1530—1930 — — 825 180 20 20
-------
TABLE IV-6 (CONTINUED) —
-- ANALYTICAL DATA
Westein Electric
North Andover, Massachusetts
May 30, and 31, 1973
Station ChrolniunL (ugh) Copper (ugh) Nickel (ugh)
Number Date Time Total HExavalent Total Dissolved Total Dissolved
WEO2 Comp —4
5/30 1930—2330 — — 635 90 10 RiO’
Comp—4
2330—0330 — — 1,770 540 10 RiO
5/31 Comp—4
H 0330-07 30 — — 1,020 25 RiO RiO
Comp—4
0800-1200 — — 440 100 20 RiO
Comp—4
“ 1200—16Q0 — — 360 80 10 K10
Comp—4
1600—2000 — — 220 75 10 K10
Comp—4
2000—2400 — — 300 . 65 RiO RiO
Comp—4 . -
2400—0400 — — 2,040 760 K10 RiO
Comp—4
6/01 0400-0800 — - 15,200 8,400 50 10
5/30 1030 — — 3,340 480 20 RiO
1330 — 1,560 270 30 RiO
-------
TABLE IV—6 (CONTINUED)
ANMJYTICAL DATA
Western Electric
Ncrth Andover, Massachusetts
Nay 30 and 31, 1973
Station Chromium ( igIl) Copper (ugh) Nickel (ug/1)
Number Date Time Total He ava1ent Total Dissolved Total Dissolved
WE O2 5/30. 1630 — 910 190 10 1(10
2130 605 120 20 1(10
2230
5/31 0130 1,880 1,440 40 40
0430 935 290 1(10 1 (10
0800 380 120 50 1(10
1200 — 430 85 20 10
1700 — . 240 65 1(10 1(10
2100 320 85 20 10
6/01 0200 3,540 1,480 20 10
U 0600 18,200 40
WEO4 5/30 1530 16,000 16,000
5/31 2240 18,000 18,00D
-------
TABLE ]V—6 (CONTINUED) 5.
ANALYTICAL DATA
Western Electric
North Andover, Massachusette
May 30 and 31, 1973
Station Chromium (i gIl) Copper (ugh) Nickel (ug/1Y
Number Date Time Total Re avalent Total Dissolved Total Dissolved
WEO5 5/30 1530 42,000 62 — — —
5/31 2240 19,000 39 — —
WEO6 Comp—24
5/31 0800—0800 40 — 250 —
5/30 Comp—16
1530—0730 — 70 — 85
-------
APPENDIX IV-B
PROPOSED EPA EFFLUENT GUIDELINES FOR
METAL FINISHING INDUSTRIES, JANUARY, 1973
-------
UNITED STATES ENViRONMENTAL PROTECTION AGENCY
WASHINGTON. D.C. 20460
21 JAN 1973
MEMORANDUM
TO: All Regional Permit Program Directors
FROM: Director, Office of Permit Programs
SUBJECT: Revised Metal Finishing Guidance
The Guidance of September 1972 has been revised to include
only those parameters which are of significance and more
directly reflect inddszrial practice. The limit for fluoride
has been increasedto a level resQltinp Trom unit process
stream precipitation. Relative to pollutiun abatement, this
is not an increase in allowance. The other limits are derived
essentially on this basis as well.
The Suidance should be applied only to establishments using
20,000 G? or rwre of p ocess water.
The parameter limits are expressed in units of pounds per
1000 gallons of process water. This reflects emphasis given
to-pounds limitations in other industrial categories.
Specifically such parameters as air iionia, phosphorous,
refractory cyanide, and arsenic have been excluded. For
chromium, the separate parameter for the dissolved trivalent
form is excluded.
From the 1967 Census of Manufacturer, Bureau of Census it
is estimated that this Guidance applies to 44 of the total
number of establishments accounting for 88% of the total value
of shipments by establishmants in the SIC 3471 cateaory. It
Is estimated that this Guidance applies to 39% of the total
number of establishments and 91% of the total value of shipments
by establishments in the SIC 3479 category.
Albert C. Printz, Jr.
IV-B—1
-------
DISCIIAR ( LI 11115 F0’ TH! I’FT . r I : s’in c
C’x
!i3
CVlt iIN
0’ t. by C l 2
10
0.03
0.oo3
0.00 25
.
50
0,1
0.417
0.000834
.,
SC’ DI!.E A______________ S;’!0 JL 9 I C0 ”Er TS
j)t lj i
PL C O
n ull
tb W .i .&J ç . .
rilfi
1b1fl ,0O UgoT.
f
rL’.XIRTD(
18
J n.lsn
1A
n.lcn
LUMIHUM
0.2
0.0 l67
0.5
0.00417
eARIUM 1.0
0.0 34
2.0
0.067
CADMIUM
0.1
0.000334
0.2
0.00167
C’ P.0MIU? CR
0.05 0.30C417
0.1
0.000324
.
CR j 0.25
0.0 20
.
0.5
0.0C4 17
So1ution & S spenccd Solids.
C0PPE 0.2
0.0’)167
0.5
0.00417
.
IRON
0.5
0.C 0417
1.0 C.0C!34
0.05
0.C’C 417 .
0.1
0.0r.C 34
.
1.0
o.c: :
2.0
j 0.0157
IJICVEL 1.0 1
0 C 33
• 2.0
0 0167
SILVER I 0.05
0.0’ 0417
0.05
0.C00417
0.5
0. 17
1.0
.
pH (Ave. 0 Ily D1scb .} f
6 9
5 — 9
e) Metal cov centratIens are based on analysis of filtered clear solutions.
(b) The majilmum pcmisslble concentration for a particular metal In the to alsus ert ed solids shall be I mgil. (0.00634 lbs/l.000 gal.)
noted for Chromiun.
Cc) Limited significance In this industry, should be cons1dered on case by case basis.
IV—B-2
-------
APPENDIX IV-C
PROBABILITY PLOTS
-------
TABLE IV—7
SUMMARY OF HISTORiCAL DATA AND EPA SURVEY RESULTS
WESTERN ELECTRIC, NORTH ANDOVER, MASSACHUSETTS
PARAMETER
RANGE OF CONCENTRATIONS
BASED UPON HISTORICAL
DATA (APRIL, 1972 TO
APRIL, 1973)
EPA SURVEY OPERATING
DAY COMPOSITE
CONCENTRATIONS
PERCENT OF THE TIME THE
OPERATING DAY CONCENTRATIONS
WILL BE LESS THAN OR EQUAL
TO THE CONCENTRATIONS DURING
THE EPA STUDY
TOTAL COPPER
2.3 0.0
846
5/30/73 5/31/73
1.76 2.54
5/30/ 73
80%
5/31/73
87%
* Based on daily analysis rather than one day per month
MAXIMUM
MINIMUM
AV RAGE
(mg/i)
(mg/i)
(mg/i)
TOTAL IRON
3.2
0.0
.631
5.15
7.00
95%
96.5%
TOTAL
PHOSPHORUS
2.78
0.0
.75
0.42
0.18
49%
22%
CYANIDE
36.0*
0.0*
1. 705*
i.75**
57%
DISSOLVED
FLUORIDE
19.0
3.7
11.0
11.8
14.4
36%
75%
** Based on one grab sample not an operating day composite
-------
.o
E: 4
+ i
PERCENT OF THE TIME IQUAL TO OR LESS ThAN THE STATED VALUE
- f
99.9 99.8 99.5 99 98
: t: st:: I:: F :
95 90 80 70 “ 50 40 30
ELECTRIC
-
— I
41
-
‘,‘ yr P ‘A
h
.-,.
ppPU
! T P
I r -
L; T
fc : ‘
‘ S
20 10 5 2 1 0.5 0.2 • 0.05 0.01
I
-- e
J
t
L: -, *fi i li
:
•1*I+
I*
:4 —
7-
___
t—- -1 1 t -•- :: :
: i __ ___
I
+ I
,
1
±i
i =]i : : i
-t
4 L H L
;=14 :1 t :.JHIH -L : —— i
E::ji .. : 4 j IL — f E L
tt t _ _ iI i I j =. I
H r: : Lr
——- ————- —— t H, i r 1 i j===::
-
Ii
EE
I
H
——
:t - ___:
•::
——- i—-—- L -1 -- - - -. - .. I ’ • ---—— - --—- - - I
. I . - iI [ : : I 11T I IIIII i
-iHH .L - H .. HH1 Hf T -THH- -
:I F r- - : -c-. :: -: : f : . L __.TiL L fl! i__
F ‘
I - P i - - - .ft - -± L :
;—1 - - I • - Hi ’ . _ - i: i t
: - - I - i•
i 1 : : : : :
: j fl - - :i Li:
I: 1: — — I
——-4 L_ 4_ I I 1 I I I I I — — - —— .•‘ —
11111 11111 - - - 4I - -
L 1 I H Itt1’ i -
I -H !t I - ‘ 1 t T
Ii H t H H’ t Htllr I
I H
.1
0.01
0.05 0.1 0.2 0.5
2 5 10 20 30 40 50 60 70
80 90 95 98 99 99.5 99.8 99.9
99.9
-------
PERCENT OF THE TINE E UAL TO OR LESS THAN THE STATED VALUE
10.0 99. : 9
i :
- T F .__ :
-
- t
!- f
i1 N
95 90 8070
50 40 30 20 10 5
;
LL: :T. 4:t
i
. #i 4 ,,•• , #4A
$ W f W4 flh
EE
t E4 T ii
1 0.5 O. ’ 0.05 0.01
rH :ijr
E1f_ -; -F--
::-t± f I ::i=
. . -— -- —- -
— -
:::it i ::t
‘ F::i:
F :r
Lt
r; TirT:
-Fi tt
ij
i
TH f T ±- +H
- 1
t-- $
—
—
1.0
L
t L E t ± : : 1 1tTll
_ L_ L.
L 4 1 Ji:: V
: i: t 1 4ft :
T _E _ i1H i _ i:: 1 : :: ‘ :i
1T r
;:i— L: tI TY : 1 T: T
I 1 : : - Hft :1. - :- -
I : T I
r 1 - Ji f fv
.•. •i• i i
_
.
IT EY tZ I
r JT T [ i t iii
J T fl1 t
=!!: 1
Et I:
:
:1 : 1
i
.::
:
:
:
.
—
0.o1 0.05 0.1 0.2 0.5 1 2 5 10 20 30 40 50 60 70 80 90 95 98 99 99.5 99.8 99.9
99.9
-------
EHH
t f
I ‘
iii
I
u _
!i I I I
•+ft TOTAL PHOSPHORUS
; 1 E -P * 4
! L i ! i! : ‘FH’Ff II I 11 11 tIll III! 11111 ll I I I ii I I iii I I i1] 1I IEI1}J)11 1 i
$]O
w
I-: ,
IEII
I It.
- Ii. 4I4 I1. I4 I 14 .— — — - — -f —+— 4-I ++++l + I-4-I$ff
J I-i
I
utt1 w1 i1 Tie tr
ffl2-
IjJ ; ..1:
u,.-
4.
I i
Ii
I
. I.
I
.
99.
99.8
99.5
99
98
95
90
80
70
60
50
40
30
20
10
5
2
1
0.5
0.2
0.1
: : : • :1: . 11 !1j t fff{fFFI1th tiffl1FHjTfl 4I TH! ‘ E lilt
- - - - . . . . . - - f1 . ‘J1 I4 1 1 ± . .
. fL I2 til : : I * 44I1411ili I• I 1 .t: :11Ifr :E
+— - : :t i1 Jf jht : t- 1ttt th4tU Ht_ I ‘_:. J Lt_
rT
- 4 u H$.4I41 IHI1JI ---- . . f 4I ,4 JI...14 • 4f
— -- L I
: : tffl :: . : :: ; -t 4 4 4 j ;: : = : : : : , , •• *fl .::. :1 : : : : : : : : J U t : i:; ;:. ::: • : : ::
— :. t 1 ._ j.4 1)4 ---: fjØt .J j t4
— — ti w :•ii — — — — f !J j 4 4 : : I ; i ; I L : L
j -1 -t+H •IIII’U-f! hi t:I4 1 . - : d t i;:: :: ,
I . tI :;::: i . ::::
iL I R-t 1 I II 1i ll jL I
-+1
1
.ii1 :t i
i— 1
: : : t ::: ;:: :t : :
Id I
0
,,, ,4:.
f,
i
tI i4
:ç• 1 j j 1
i
:r :t
RI1 1114IF n HJj 4 4ftJ J E1
::;
- 4••e•, +,,
I
1I
‘Ft
T
LH 1iH
liii
Iii
ifi - _ -
&
H- i
. I
III
1!
::: L L4 :.‘; : :
A ..1 •
I
1
.
Ut
I
{ft
::.
h .ifj:i
11:
:: : ::t
S 01
: iI
: t:
rii —
1:
: : i : :
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T
I L
.1
..
h HHIHH m h11
! U
a
L IF
I I I I I I I II I I
ill I’ I I III Itlilil’!
ITI’ . U’
P . 1 Ii ’ ,
: i: 4 ‘ iii: ::4
k
TOTAL PHOSPHORUS (mg/i)
a .1
.1 .
1.0
j:fl4 liE EItii111MtHi
-------
:
-7 1y•,• rr, •t- ,‘ A “P
‘iI j1’ : Efti’
dI - 1
,,,
E+ F±FH_F+H : : : . :
- .- -N
Th:
0.05 0.01
I
I
1
_;L ______
I
r
=
t t
PERCENT OF THE TIME EQUAL TO OR LESS THAN Tll STATED VALUE
o 99. 99.9 99.0 99.5 99 98
95 90 80 70
- _F , ; I tL*
. H t t E fl
m; -: $soi
50 40 30
=
- -
i-I
20
: F V
— -
-
10 5 2
IfR1 Mflk
4&,J,
—ii t i
-r-
-V
TT I I + I
=
—4
--t t-L
t-
1 t1
- -t +
I 0.5 0.2
1
fti
-
-I
-I
It’
. .LU.
D
I )
IT __ —
I=! r :’
1± 1± H. .’ hL ii___: :i • I
!i :I i ‘: T i - L:_
T ;- ::, —II Ei I =1:::::y: i: - - - ?t.:fi -L - -- .: • ::: iI -- c :tir
: :j J I L
itt 1tift1i+ k - - - H
--- - tI
T : Hf I; HH I El
0.01 0.05 0.1 0.2 0.5 1 2 5 10 20 30 40 50 60 70 80 90 95 98 99 99.5 99.8 99.9
99.9
-------
::i:rniii t
:::::
I’ll
rp ?!
T
If1 il4 1
4:
: i I
T
Lcr• u :
II
ij: ji I ti Ii !
‘T’lI 1 ‘I
L OCU
:
: ux
t
Ij
.
1f .i !1 —
II I III
I i
III
: ! I.j1
i
. .
:: : : - - T T
. .
T .
f:
‘-.4 i I ..I
44 , ! 4. :
44 •—*. •
, I • 4 .4
, II
Ii
4..
I
I
1 Ii
————
••I1• ••I1 I 1it I ILI I
I 4 — 1
.1
T
I
II
, ii
I’i
t -t
‘I
.
I .
II
I
lu
f i “
k-’ fi. -
1: ::.
. .+ . ..,
I
t t H
; ,. ; ; . . —
I •
jL
p
----
.-
.
99.1
99.’
99.5
99
98
95
90
80
70
60
50
40
30
20
10
5
2
1
0.5
0.2
0* 101
:t
—4 4
4 1.4 +- . _ __ _ -_
ij ]i I:t i
I h: W.
I 1
. 1 r ’
I 1 . ;1
t fti.
:1
:‘=
4
P
:: :
4.
-4-I- 14
,
4 ,; ’i tI:: :t ;:t It: : . : :I ::
‘. : ::: : : :: ..Li. t ; :: ;! : :
0
I
: +=i —— : — -——--:=-
:
— -
1 ‘ “it 1i I I tF rI9Ti I I
:: :: 4 41 i f II ii : :
_ _ + t1t :
--- - - - + 4 111 . , - t
•: r:
::::::: : J I
I 111 1 11 I L
I —i— .
4 I 4 I
iil t __ __ :
L! 4 1 ;
f . —
. I
1 —— :z:f-t—:—
:
r 1 ! i L:
f U t L 4 4
I : — t U i T 1 jff t 4i —
f
1: : 4
• i ,J t tL.
flHh4j - E H UD
4 H 1 J ::::
I H I
1 jI .
fl I ‘ ‘ i I J f f
t :t ;1 I i ’ :i:t_J•_1 I ;:t 1
— I If I I
i:.
t, t + .. . 4 . t
I ; If I
t ;t I .
I
t
.
.
.1
—1
10
CYANIDE (mg/i)
1.0
-------
, - -
: :
fIIII! hI I
I I1iI i ’ JJ— i .! t.1 U I I
L ‘.s L,
4 i
: F:.’
w
I
lIl
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;:
L . —j’1. L
II II
01
I;
I
L
H)
III
I
t1
IIH ::
.Lf . •
H
. H ,
t I L1
; f . I
99,
99.8
99.5
89
98
95
90
80
70
60
50
40
30
20
10
5
2
1
0.5
0.2
0.1
0
0
1-4
z
p4
I L L :•: j ti1
: :::: t14.:1;1 ;4 411 ::::::::
± ::: .,., ., 4 t . . :::::..
-
— - l . H• • ‘ “‘“ • . .
ij_
m-t—-i ± ± -ti 1 1 :..: b:,: t ,:: ,: :
. .
i 1 I 4 L & I 1 4
- - 4I I i : r i ‘
:iiiii.i_i I I I t
_!
‘i i
:iiijiiiiiiij iiiiiii :
. LF! LH. tth .1 I 4 I. IIi_ I
L T:fT1I . .
Ii i IiI_ Iii— ii . .1 1 1 . 1 : I
— ‘f I
II1 1 17171:1
Th I 4
.,
:
- — - , 4
r
: : L H.
.. ,. L HUU1
f L 1
I
I th
: : ; : ii .t :
I J :
: : i :
I
I . .: . ..
I :u
I it
j
1 L ii •.
Tt::: J
t 1
J t H
-- ‘-, •t
i_ jt
- - - i - 4 , Ii R.
ph E:L i : .:
. •f
t 4 L
I
- it 9: ; t :::
t
‘ ‘ . • ; ::;
. . - - , tI j I i:h
1t: t [ 1 ::
: t .j . :
a II
.
•
:;
:
:::
.::‘
•
0.01
0.1
TOTAL METALS MINUS DISSOLVED METALS (nigh)
—
1.0
10.0
-------
99.99
99.9 99.8
4.—
4--
99 98
1514 lpu
(400 gpm
4LT
H
_________ ______ 95 90807060 50 40 30
±-i
PREQVEN : or:_ cc . i
(1 t R AL DATA)
I
:T
- t
1
tii
cE
20 10 5 2 1 0.5 0.2 0.1 0.05
t
It:- I1.
———-1 -.
: ift Thi
4-
0.01
-
41
4-
14
,-t +— 4------
-H
j
. s -H-
tH4-
1
-t—+ --I- —1 H
t -
it4:
1 ’
: t :
•1
1 H-H
t tr.
f -
- .
- .4
- -4.-
DESI
-HFI 1
r --i--’-
4—-.-
çIT -
1324 ipir
(350 gpm
1134 lp
(300 gpm
946 lpu
(250 gpm
757 lpn
(200 gptn
568 lpi
(150 gpm
378.5 lp
(100 gpm
f I
I
APd
1
- — - - - 1 J:
------4 - .1.
- i i
--1- - — -
-—4-
-1 --
:
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t t
- -
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-
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—
i.— ’ .-r- .
. — —-—— •
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4-4
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I
I -
- — - -* -
-4 4 4
ti
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t-
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— - -1--
I
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-
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- H-p-
1 H
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4 ’•
r
t: it.
r EtL
TTt
_I’Ij
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-t I
I
1
4, 4
• ,
-i ri
4.4
I I
rf
-i- -it-i F: 1 1
4 i4 :d
4-
-4--
4-
-H-
tff
i: if ft
-itt ±
-I -
4
—4
I —
1 -
1 H
+1
-—
_! ÷ .- - .,-t
-3- -t -k ft. -
41 . --i . :i I
-It
. It
t
-H-—f—
Th
I.
4’
1±
-:-
-1--
1 • —
HIS
ORI
t1 -
j-ftf:
n -
I HH-
-: 1
A1 A-
iT
- P1 _
-I II
4
-1 -
- --.1 --
q_: EP
ft
nil
DAIL’
0.01 0.05 0.1 0,2 0.5
t
1
- -- ----- •
G IEJI
-13w-
ttt
4 i
H-
I -
, -
. • :
.
.
——
:.
,
, -
—_p—•_t -
:1
H->Th:
s- • ‘
•—f— - 4 —f-
Tfr i Ji=
—
-W
- - 1
4
:::
• • t
: H
— —
-t
-m
+H- +
i
L
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2 5 10 20 30 40 50 60 70 80 90 95
PERCENT )F THE TIME EQUAL TO OR LESS THAN THE STATED VALUE
98 99 99.8 99.9 99.99
-------
APPENDIX IV-D
WESTERI ELECTRIC’ S MONTHLY REPORT SUBMITTED
TO THE MASSACHUSETTS DiVISION OF WATER
POLLUTION CONTROL, APRIL, 1972 TO APRIL, 1973
-------
1Q a YR.
SLUDGE LOG
‘ NTH
DAILY
1 —
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-------
YR. T0,t/E T1
CHEMICAL WASTE TREATMENT PLANT
EFFLUENT & SLUDGE LOG
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-------
FI IVIR.,t- L VV1- ) I L.
EFFLUENT &
I F’ L .&%I IVIL.I”I I IL?4I’ J I
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—.
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TOTAL FLOW — 3,213,000 Gal ERATING SUPERVISOR P. M. ARRICO
IV—D—4
-------
CHEMICAL WASTE TREATMENT PLANT
August, 1972 EFFLUENT & SLUDGE LOG
1Q.& YR.
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-------
MO. 8 YR.
CHEMICAL WASTE TREATMENT PLANT
/ 22-EFFLUENT & SLUDGE LOG
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GALLONS
-------
- -.,-.. — . 7
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TOTAL FLOW— 9,423,000
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February, ‘973 EFFLUENT & SLUDGE LOG ____
MONTHLY
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P. M. ARRIGO
-------
CHEMICAL WASTE TREATMENT PLANT
March, 1973 EFFLUENT & SLUDGE LOG
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TOTAL FLOW — 8 0 OPERATING SUPERVISOR P. M. ARRIGO
TV—n—i
-------
CHEMICAL WASTE TREATMENT PLANT
EFFLUENT 8 SLUDGE LOG
).8YR.
I DAILY
,4 p,c’ii . . -.
MONTHLY
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TOTAL FLOW—? 921,000 OPERATING SUPERVISOR \. / ? g’Z? 1 EY
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