WATER POLLUTION CONTROL RESEARCH SERIES
12080 EZF 09/70
Phenolic Waste Reuse by
Diatomite Filtration
U.S. DEPARTMENT OF THE INTERIOR FEDERAL WATER QUALITY ADMINISTRATION
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WATER POLLUTION CONTROL RESEARCH SERTES
The Water Pollution Control Research Reports describe
the results and progress in the control and abatement
of pollution in our Nation's waters. They provide a central
source of information on the research, development, and
demonstration activities in the Federal Water Quality
Administration, in the U. S. Department of the Interior,
through inhouse research and grants and contracts with
Federal, State, and local agencies, research institutions,
and industrial organizations.
A triplicate abstract card sheet is included in the report
to facilitate information retrieval. Space is provided
on the card for the user's accession number and for
additional keywords.
Inquiries pertaining to Water Pollution Control Research
Reports should be directed to the Head, Project Reports
System, Planning and Resources Office, Office of Research
and Development, Department of the Interior, Federal Water
Quality Administration, Room 1108, Washington, D. C. 20242.
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PHENOLIC WASTE REUSE
BY DIATOMITE FILTRATION
Experimental Closed Water System to Eliminate Waste Water Discharge from
Johns-Manville's Fiter Glass Insulation Plant #3 at Defiance, Ohio
FEDERAL WATER QUALITY ADMINISTRATION
DEPARTMENT OF INTERIOR
Johns-Manville Products Corporation
P. 0. Box 159
Manville
New Jersey
Grant WPRD 87-01-68
Program No. 12080 EZF
September, 1970
For sale by the Superintendent of Documents, U.S. Government Printing Office
Washington, D.C. 20402 - Price $1.25
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FWQA REVIEW NOTICE
This report has been reviewed by the Federal Water Quality Administra-
tion and approved for publication. Approval does not signify that the
contents necessarily reflect the views and policies of the Federal
Water Quality Administration, nor does mention of trade names or
commercial products constitute endorsement or recommendation for use.
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ABSTRACT
The fiberglass industry has long had a problem in disposing of waste
water containing phenolic resins. In the fiberglass manufacturing
process, airborne glass fibers are sprayed with a phenolic resin as
the fiber blanket is formed on the collecting conveyor, causing a
deposit of resin to form on the conveyor chain. Prompt cleaning before
the deposit sets is needed to permit continuous formation of the glass
fiber mat. The waste water originates from the chain washing operation
which uses either a caustic wash or high volume showers to remove the
resin deposits.
Under the demonstration project a chain cleaning - water reuse system
was installed which consists of low volume, high pressure chain clean-
ing units with water consumption of eight gallons per minute at a
thousand psi, two stages of primary filtration to remove large
particles and fiber, and a secondary diatomite filter to remove fine
particulate matter. The filtered water is suitable for reuse in the
binder batch, overspray system, and the chain cleaning units.
The water reuse system has reduced the quantity of water required
for chain cleaning, will use water h-1/2 times before evaporation
removes it from the system, requires 1 Ib of diatomite per 500 gallons
of resin-bearing water filtered and provides water at a net cost of
$,37 per 1000 gallons -vs- $.75 for City water.
This report was submitted in fulfillment of a Research and Development
Grant 12080 EZF between the Federal Water Quality Administration and
the Johns-Manvilie Products Corporation. Mr. Charles H. Ris III,
Project Manager and Mr. William J. Lacy, Chief, Industrial Pollution
Control.
Key Words: Fiberglass, phenols, resin, diatomaceous earth filters,
water reuse, operating cost.
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CONTENTS
Section Paee
. i -.,... w
Abstract iii
I Conclusions 1
II Introduction 3
III FWPCA Demonstration Project 7
Purpose 7
S cope 7
Treatment Theory 8
IV Design and Installation of Facilities 13
Effluent Standards 13
Design Criteria and Equipment Description 1^4
Schedule 32
V Operation of Project 37
VI Evaluation Program 39
VII Evaluation and Discussions 55
Suspended Solids Removal 55
Cost of Filtered Water 58
Water Reuse 59
Operation and Maintenance Activities 6l
Reduced Water Consumption 66
Operating Cost 67
Capital Costs 73
Unexpected Problems 7&
Discharge to Preston Run 79
VIII Recommendations 83
Appendix "A" - Water Data 87
Appendix "B" - Operating Cost Data 121*
IV
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FIGURES
Fi gure Page
1 Glass Fiber Production Process h
2 Closed Water System 9
3 Chain Cleaning Station 15
h Dry Well Pump Sump 20
5 Wet Well Pump Sump 21
6 Primary Filter 23
7 Flow Chart - Schematic, Waste Reclamation System 31
8 Project Cost Status by Months 75
9 Scrap Pump 18
10 Chain Cleaning Station l6
11 Primary Filters 2h
12 Diatomaceous Earth Filters 26
13 Filtered and Dirty Water Tanks 28
I1* #2 Weir 33
15 Water Consumption Trend 52
16 Sampling Point Locations kO
1 7 Phenol Concentrations - Discharge k2
1 8 Phenol Concentrations - Re circulated Water ^3
19 Suspended Solids - Discharge ^5
20 Suspended Solids - Recirculated Water ^6
21 Total Solids - Discharge U7
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FIGURES
Figure Page
22 Total Solids - Re circulated Water 1+8
23 pH Values - Discharge 50
2k pH Values - Recirculated Water 51
25 Average Daily Discharge to Preston Run Tributary 53
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TABLES
Table Page
1 On-Stream Cycle Life 57
it Water Quality Discharge 1968 63
5 Water Quality Discharge 1968 - Lbs/Day 79
6 Water Quality Discharge 1969 8l
7 Water Quality Discharge 1969 - Lbs/Day 80
12 Water Bills - City of Defiance 60
13 "Non-Process" Water 66
lit Chain Cleaning Water Discharged- from Water Supplied 66
15 Chain Cleaning Water Discharged- from Weirs 67
l6 Water Use Summary 69
17 Capital Costs Tit
Appendix "A"
A-l Daily Meter Readings 1968 87-93
A-2 Daily Meter Readings 1969 9U-llit
A-3 Water Quality Data - Discharge 115-118
A-it Water Quality Data - fiecirculated Water 119-122
A-5 Monthly Average of Daily Discharge Flows 123
Appendix "B"
2 Added Operational Costs and Savings 12it-125
VI1
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CONCLUSIONS
Conclusions from this twenty-eight month project to reclaim industrial
waste water, are as follows:
(l), Elimination of the "chain" cleaning process waste has been
achieved by reuse of the "chain" cleaning water to provide the
water source for process needs.
(2) A check of pollutants discharged in July 1969 to Preston Run
shows that phenolic discharges have been cut to one-fifth, sus-
pended solids to one-sixth, and dissolved solids to one-half of the
December 1968 loading prior to the start of closed-system
ope rati on.
(3) Pollution in Preston Run tributary has been reduced but not
eliminated. Elimination will be accomplished when certain
streams not in the scope of this project are routed to the City
of Defiance treatment plant early in 1970.
(k) Conservation of an expensive resin used as a binder material
through water reuse has contributed substantial operating savings.
(5) Conservation of city water purchases through reuse has been
appreciable in water and dollars saved.
(6) Net "before tax" income returns 9.5% on the investment.
(T) Foaming is an operational hazard which results when high pH
ranges occur.
(8) Fungus growths in the circulating water require sone degree of
treatment to prevent flow stoppage in pipe lines .
(9) pH control of ammonia content is necessary to successful filtering
of the "chain" cleaning water.
(10) Dissolved solids up to 6000 parts per million have successfully been
handled in the circulating system.
(ll) Water is reused H.5 times "before evaporation removes it from the
closed system.
(12) Approximately .6% of the solids removal is accomplished "by the
diatomite filters, the major removal being accomplished by
pre-screening equipment.
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(13) Approximately 500 gallons of resin-bearing process water were
filtered per pound of diatomite.
(l^) A filter aid (used) to dirt (collected) ratio of three to one
was typical of the diatomite filtering operation.
(15) The gross cost of filtered water in this process is estimated at
approximately $1.59 per 1000 gallons, of which $.53 is capital
cost and $1.06 is operating cost. The net cost of filtered
water is $.37 per 1000 gallons, derived by crediting the system
savings against the $1.59 gross cost.
(l6) Similar water reuse systems will be proposed at all Johns -Man vi lie
plants where a phenolic resin discharge occurs. Johns-Man vi lie
has a total of nine (9) such plants.
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II
INTRODUCTION
Fiber Glass Production.
For years, the fiber glass manufacturing industry has had a problem of
disposal of wastewater containing phenolic resin, which is used as a
binder in the manufacture of glass fiber insulation products. In a
typical plant, fiberized glass is formed via an air stream which de-
posits the fiber onto a moving open mesh collecting conveyor - commonly
called the "chain". Referring to Fig. I, a water solution of phenolic
resin is sprayed on the glass fiber as it is formed. The resulting mat
is then transferred from the collecting conveyor to an oven where the
binder system is continuously dried and cured, after which the mat is
cut to size and packaged.
The resin spraying operation results in resin deposition on the collect-
ing conveyor "chain" and unless this deposit is removed, the conveyor
becomes fouled and inoperable. Caustic soda baths (method l) or water
sprays (method 2) are used to clean the chain. It is this "chain"
wash water which dissolves the phenolic resin, carries it out to streams,
and is the source of phenolic pollutants from a fiber glass plant.
Chain Cleaning Process.
Johns-Manvilie Fiber Glass Insulation plants have found it necessary to
clean the wire mesh conveyor upon which the fiber glass mat is formed
in order to maintain free passage of air through the conveyor mesh
(refer to Figure I). During the formation of a mat or felt blanket,
free freshly formed glass fibers - spray coated with a phenolic resin
binder and cooled with "overspray" water to control rate of resin cure
are air borne to the forming conveyor through which the air passes,
leaving the fibers piled in a uniformly thick felted blanket across
the width of the conveyor. The air stream which transports the glass
fibers to the conveyor also contains droplets of resinous binder which
have not adhered to the glass fibers. Many of these droplets deposit
resin on the wire mesh conveyor chain, and if not removed, the resin
build-up will eventually restrict passage of the air stream. When
the deposit becomes sufficiently great, blanket formation is no longer
possible, necessitating replacement of the conveyor with a new or re-
novated conveyor wire - frequently referred to as "chain". "Chain"
has historically been cleaned while in service to extend its useful
operating period before becoming "blinded" with resin deposits by
routing the "chain" through a shallow pan containing a hot caustic
water solution. Fresh water makeup to the pans created caustic over-
flow to the sewers containing phenolic resin and glass fiber.
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Subsequently, a recirculating method of "chain" cleaning used 300 psi
water jets spaced 3" apart across the conveyor width. This method, not
employed at Plant #3, sought to reduce the discharge through re-use of
the water after sedimentation in a clarification tank. Unfortunately,
the clarification was inadequate, resulting in frequent plugging of
nozzles. Also, the small amount of fresh water needed to moke up for
evaporation and other losses was insufficient to purge the recirculated
water of dissolved solids which built up to the degree that it was
necessary to purge the system on a periodic basis by dumping the water,
with resulting loss of phenolic bearing water to the environment.
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FWQA DEMONSTRATION PROJECT
Title: Phenolic Waste Reuse by Diatomite Filtration
Period: September 1, 196? to February 1, 1970
Funds: Estimated Cost $16^,700 - Federal Grant 50$ up to $82,350
Purpose.
This project is designed to demonstrate the effectiveness of a total
process water reuse system involving dlatomite filtration to treat
phenolic bearing waste waters prior to reuse. The chain wash water
contains glass fiber and caustic, in addition to the phenol content.
The objective of this project is to eliminate completely the discharge
of phenolic bearing "chain" wash water from Johns-Manvilie Plant 003
at Defiance, Ohio.
Other components of the total waste stream such as domestic waste,
caustic mandrel cleaning solutions, boiler blow-down and softener back-
wash, are to be ponded, aerated and chemically treated before release to
the stream, pending ultimate disposition in separate treatment facility
or connection to municipal treatment plant.
Scope.
The project includes several phases.
Design: - Equipment selection and location were the primary elements
involved here. A knowledge of the quantities of water, phenol and other
contaminants was also needed to size equipment.
Pre-construction Studies: - To establish the success of the project,
it would be necessary to know the conditions prevailing prior to
operation of the project. Weirs were established which would measure
the discharge to the stream before operation of the project. Samples
and analysis of the discharge would establish the quality of the dis-
charge, which in conjunction with the flow, would provide the means to
determine quantities of contaminating factors in the discharge, there-
by furnishing a baseline for future reference. Water meters would also
be installed to establish city water use at significant points in
the operation.
Procurement: - Purchase of equipment and selection of installation
contractor through normal channels of competitive bidding would be a
necessary phase of activity prior to construction.
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Construction & Installation of Equipment: - Revisions to existing
product units, construction of floor trenches and. pits, piping, wiring,
installation and painting of all equipment would be final phases of the
activity before operation.
Operation: - The operational phase in the scope of the project would be
the most important, for failure of the equipment to function reliably
could cast doubt on performance reported. If reliability in this phase
was good, uniformity in operating conditions would, in turn, establish
dependable data.
Post Construction Studies: - Collection of data on the same basis as
that set up in the Pre-Construction studies would make measurements
possible which could be compared with the pre-construction studies
to determine project effectiveness.
Evaluation: - Analysis of the measured data collected during pre-
and post-construction studies would be a continuing part of the operating
phase covered in monthly reports, to be summed up in a final report
after project completion. Collected data would provide information on
suspended and dissolved solids, phenolic content, pH at significant
points in the recirculation loop and at the point of discharge to the
stream. Consumption of water, ammonia, diatomite and maintenance
materials would also be accounted in the evaluation.
Treatment Theory.
The project proposed to clean the "chain" and eliminate discharge of
the "chain" cleaning process waste. (Refer to FIGURE 2 - Closed Water
System). The principle employed here is to re-circulate the "chain"
cleaning water - but to improve it continuously; first through diato-
maceous earth filtration and secondly by purging of dissolved solids
through use of "chain" cleaning water as the source of water for binder
mixing and overspray water. The diatomaceous filtration improves the
reliability by elimination of nozzle plugging.
As noted previously, the formation of the glass fiber felt on the "chain"
is accomplished through spray addition of a phenolic resin - water
mixture, known as "binder". To control the curing rate of the binder,
water known as "overspray" is sprayed into the forming process. Both
"overspray" and the water in the "binder" are subsequently evaporated
in the oven curing process which follows the forming step. Therefore,
the use of "chain" cleaning water for "overspray" and "binder" mixture
provides the means for purging the "chain" cleaning water of high con-
centrations of dissolved solids, since the water evaporated in the oven
is "made-up" into the "chain" cleaning supply.
The water containing the phenols can be used up within the process if it
is recycled and filtered satisfactorily. The system as proposed will
contain about 5,000 gallons within itself at any one time and has a
cycling or use figure of about U,500 gallons/hour on an average. The
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volume recirculated is sufficiently small that the normal fresh water
make-up (due to drying losses) represents a continuous purge of about
50% of the circulated flow - making periodic dumping of water unnecessary,
The phenol-containing water can "be used in three areas. These are as
follows:
1. Chain Cleaning - This water use would amount to about 50 gallons/
minute when all machines are operating.
2. Binder Mixing (and subsequent evaporation) - The estimated use when
all machines are operating is approximately 15 gallons/minute. A
minimal amount of water is returned to the system of that which is
used up in binder spraying.
3. Overspray Water (and subsequent evaporation) - The estimated use
of overspray water is the same as the binder water, or about 15
gallons/minute. As in the case of the binder sprays, a minimal
amount of this water is returned to the system.
In summary, the completely closed system will be capable of using up
approximately 1800 gallons of water per hour. This will amount to a re-
placement of almost hO% of the water that is operating in the system
in an hour, on an average. (It should be noted, however, that variations
in product and binders and various means of operation could drop this
amount to as low as 20% of the over-all volume in this sytem per hour).
In order to use this water, as delineated above, it must have certain
properties. These properties are as listed below:
1. Maximum Solids (larger than 0.5 microns) - 0.0002$ by weight.
2. pH - Must be between 8.5 and 9.5.
3. Phenol Content - Not important in our operation.
k. Make-up Water - Make-up water must be soft water and J-M treated
city water is satisfactory. Our goal for softened water is a
water of less than 50 parts per million (ppm) hardness.
The treatment of the caustic water, which is in relatively small quanti-
ties as it is only dump water from mandrel cleaning operations, is best
handled by dumping to a holding pond and treating the pond at prescribed
intervals as required in order to release it to Preston Run or return it
for plant process use. Neutralization with hydrochloric acid is planned.
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Equipment For Water Reuse System
The equipment needed to accomplish our vater treatment is shown on
FWQA approved drawings in detail. The major items, however, are noted
below:
Three (3) 1000 psi chain cleaning pumps
Five (5) Chain cleaning spray systems
One (l) Scrap pump dewaterer
Two (2) Dirty water sump pumps
Two (2) Primary filters
One (l) 2,000 gallon dirty water tank
Two (2) Per Model ^50-4-36 SAF3 Diatomite type filters
One (l) 2,000 gallon clean water tank
Four (M Filter water transfer pumps (2 primary filtrate
and 2 secondary filtrate)
Four (M Polishing (cartridge type) filters
Two (2) Overspray pumps
Material Savings.
Conservation in the use of certain materials is expected as noted belov:
"Chain" cleaning water previously discharged contained phenolic resin
washed from the chain. By recycling the "chain" cleaning water the
phenolic resin content (soluble portion only) can be recovered, thereby
reducing the quantity of fresh resin required to prepare "binder"
mixture. A valuable resource can thereby be conserved and an appreciable
dollar saving expected.
Elimination of the need for caustic cleaner for "chain" cleaning is an
expected econony.
The re-use of water infers that savings in water consumption are expected.
A feature of this project is the use of low volume showers at 1000 psi
to accomplish the "chain" cleaning effectively; to hold the circulating
water volume low so that the percentage of make-up water would be high
and to minimize the investment in filtering equipment. Economy in the
use of water can be achieved through the use of rotating nozzles which
effectively extend the water jet over a large area of chain.
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IV
DESIGN AND INSTALLATION OF FACILITIES
Effluent Standards.
The objective of the project is to eliminate discharge of process
effluent. Any discharge, however, should comply with the Water
Pollution Control Codes of the State of Ohio, which, under Stream
Standards for Potable Water are:
Dissolved Oxygen.
The dissolved oxygen content shall be 5 ppm.
Phenol.
The phenol content shall not exceed 1 part per billion.
pH.
The pH shall have a value between 6.5 and 8.5.
Bacteria, Coliform Group (B. Coli)
Not to exceed 5000 organisms per 100 ML.
Dissolved Solids.
Dissolved solids shall not exceed 500 ppm.
Tastes & Odors.
The water shall be free of objectionable odor and taste. Odor shall
not exceed the threshold number of 2k at 60 deg. C.
Temperature.
Not to exceed 93 deg. F during May through November or 73 deg. F
during December through April.
Aesthetic Consideration.
Discharged water must be:
(a) Free from solids that will settle to form putrescent or
otherwise objectionable sludge deposits.
(b) Free from floating debris, oil, scum and other floating materials
in amounts sufficient to be unsightly or deleterious.
(c) Free from materials producing color, odor or other conditions
in such degree as to create a nuisance.
(d) Free from substances toxic or harmful to human, animal
or aquati c li fe.
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Design Criteria and Equipment Description .
Each significant equipment item is described, and its function delineated
belov:
Changes to Existing Facilities:
Product Units:
Design Criteria.
Remove dissolved and suspended solids from conveyor chain. Rotating
jet - 5^0'/min, fan 6" wide - maximum supply pressure 1000 psi. Capacity
to provide 100% cleaning coverage at conveyor speeds up to 57'/min.
Sluicing velocity in trench to be a minimum of 8'/min. At each product
unit a cleaning station has been built into the structure through re-
location of forming conveyor chain travel. Figure #3 and Figure #10
depict a side elevation view of the "chain" cleaning station. After
discharge of the fiber glass blanket from the forming conveyor, the
chain returns beneath its upper travel and "upside down". This situation
permits the rotating nozzle to wash off in a reverse direction phenolic
resin binder and small adherent clumps of fiber glass. The rotating
nozzle turning at 115 revolutions per minute at a radius of 18 inches,
uses 8 gallons per minute of 1000 pound per square inch water to
effectively clean a three foot width of conveyor chain. Four product
units have 3' nominal conveyor width and are cleaned with one nozzle,
the fifth unit having a 6" nominal chain width is cleaned with two nozzles,
The wash water blows downward through the chain into a hopper which
guides the water into a "U" shaped trench in the floor. The half-round
trench bottom was adopted to obtain maximum sluicing effect from the
relatively small quantity of cleaning water employed. Accumulations of
fiber occur on the sloped sides of the hopper, which, in due course, fall
into the trench. Frequently the 10" diameter trench becomes obstructed
with these clumps of wet fiber, but the accumulating water upstream
eventually floats the obstructing dam away.
The trench passes in a straight run beneath all five production units
collecting water from each "chain" cleaning station. It is pitched to
discharge into the scrap collection pit. Despite frequent obstructions
of fiber in the trench, it has seldom been blocked to the point that
manual attention is required to maintain flow.
New Construction.
Scrap Collection Pit.
The scrap collection pit houses below floor level a reciprocating scrap
pump, which is functionally a screening device that extrudes screened
fiber solids in a damp cylindrical shape to a waste bucket, and two
different types of pumps for transferring the screened "chain" wash
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FIGURE 3 _ CHAIN CLEANING STATION
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FIGURE 10 - CHAIN CLEANING STATION
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water to the primary filters. A sump pump is also included which will
pump out the pit in the event of failure of any equipment in the scrap
collection pit. Equipment is so arranged that a vibrating screen could
replace the scrap pump.
Essentially, the collection pit is a screening and pumping laboratory
where various means of pumping the fiber bearing "chain" cleaning
water could be tried to determine optimum handling methods.
Reciprocating Scrap Pump (Screen-extruder).
Design Criteria:
Pass up to 100 GPM of water containing glass fiber. Screen and dewater
solids retained on 3/32" diameter pimched screening plate.
As noted above, this specially designed piece of equipment functions to
screen bulk fiber out of the trench water and discharge the fiber in a
damp cylindrical extrusion. Figure #9 shows the discharge end of the
pump with fiber being extruded in an 8" diameter cylindrical shape.
Water and fiber enter the horizontal single-acting, single-cylinder
pump at the level of the trench flow line through the side of an open
top hopper which is mounted on top of the cylinder. When the plunger
retracts the trench water drops into the cylinder and thence through
the 3/32" diameter holes in the perforated cylinder wall. The coarse
clumps of fiber remain in the cylinder bore and are pushed out the open
end of the cylinder through a forming tube when the plunger advances .
Fiber solids are thus screened and dewatered in this special "scrap"
pump, which actually does not pump, but gets its name from its
reciprocating plunger type of construction. Screened water containing
short abrasive glass fibers is collected in a pan beneath the scrap
pump and routed to either of two centrifugal pumps.
The scrap pump is quite an effective instrument for removing bulk fiber
from the water. It is, however, an added piece of equipment that may
be eliminated if there is added capacity elsewhere to remove fiber. To
determine whether it could be eliminated, provision was made to extend
the floor trench through the feed hopper directly to the centrifugal
pumps, thereby by-passing the scrap pump.
Centrifugal Pumps to Primary Filters.
Design Criteria:
Pump 100 GPM % UO' TDK of water containing up to .2% of glass fiber
ranging in size from 100 mesh up to clumps 6" in diameter. Pump
impellers and casing to be rubber covered to resist abrasion.
The collection pit contains two types of pumps - one a wet well and the
other a dry well pump. It was believed that under proper installation
conditions both types could satisfactorily handle the fiber bearing
"chain" cleaning water without interruption due to plugged pun^ intakes.
After study, it was reasoned that the most effective way to bring the
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FIGURE 9 - SCRAP PUMP
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fibrous solids to the pump intake was through use of a conical sump.
Special conical sumps were accordingly incorporated into the setting
of both wet and dry well pumps.
Dry Well Pump.
Figure #H shows the conical sump used in the "dry well" installation.
This rubber lined centrifugal pump has a capacity of 100 gallons/minute
at ho' total dynamic head. It does not require seal water at the shaft
packing due to special impeller construction which creates suction at
the packing box to minimize shaft wear from abrasive liquids. When
handling screened water from the scrap pump it has operated very reliably
for much of the twelve month operating period. When handling unscreened
water direct from the trench, and by-passing the scrap pump on a two
day trial, this dry well "pump-sump" combination performed satisfactorily
with the aid of a 200 pound/square inch jet of water from a 1/U" pipe
lance clamped to the inside of the cone and terminating at the bottom
of cone. The jet served to break up large clumps of fiber which other-
wise would have plugged the V diameter intake. This trial was made to
predict operation of dry well pumps at a new Fiber Glass Insulation
plant at Winder, Georgia.
The experiment established the fact that pumping of "chain" cleaning
water with fiber included is feasible without pre-screening equipment
when a jet assisted conical convergent approach to the pump intake is
used. Subsequent experience at the Winder Plant has verified the
experimental finding.
Wet Well Pump.
Consideration of alternate methods of pumping "chain" cleaning water
bearing glass fibers indicated that a rubber coated wet well pump having
no submerged bearings or packing glands would offer the simplest and
most reliable pumping equipment. To handle suspended glass fibers it
was reasoned that a conical sump which would guide all liquid and fiber
directly to the impeller intake represented the ideal approach condition.
Previous experience with a sump pump in a typical rectangular sump had
demonstrated that the glass fiber would settle out in the sump areas
not immediately adjacent to the pump. This situation required manual
attention to remove the deposited fiber. Accordingly, the development
of a conical sump became an early requirement for successful pumping of
the "chain" cleaning water. FIGURE 5 shows the setting used for a wet-
well installation. Space limitations prevented use of a true cone.
A modified cone bottomed sump was employed with a cylindrical sloping
trough carrying the water into the apex of the cone from which point
it could only rise into the eye of the impeller. The pump used had
a capacity rating of 100 gallons/minute at ko' total dynamic head to
duplicate that of the dry well pump. It had no submerged bearings or
packing box, strainers were removed and the liquid contacting parts
were rubber covered to resist abrasion.
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FIGURE ll - DRY WELL PUMP SUMP
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FIGURE 5 - WET WELL PUMP SUMP
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When supplied with screened water from the scrap pump this pump performed
adequately for the first four months of the operating period, although
the sloping chute had to be cleaned daily of fiber deposits. This unit
adequately demonstrated ability to handle screened "chain" cleaning
water. No attempt was made to try its capabilities on unscreened water.
It is believed however, that with a true conical sump and aided by a
water jet to break up large clumps of fiber, the wet well pump would
handle unscreened "chain" cleaning water.
Primary Filters.
Design Criteria:
Remove suspended solids retained on 60 mesh screen; Pass 120 GPM water
containing glass fiber.
"Chain" cleaning water is pumped from the scrap collection pit by either
of two slurry pumps. The water drops into an open hopper which spreads
the water horizontally upon a horizontal 80 mesh polypropylene media
belt about 30" wide.
FIGURE #6 illustrates the operation of this filter. The filtered water
falls through the media, leaving glass fiber on the belt. When a
sufficient weight of fiber and water has accumulated, the weighted
media is moved ahead by frictional contact with an underlying grid type
of conveyor belt. As the weight is carried away, friction no longer
moves the media, which remains stationary until the next accumulation
occurs. Figure #11 shows two primary filter units in service with
the right hand unit receiving the dust load of saw kerf from the pipe
covering dust collectors, while the left hand unit filters the "chain"
cleaning water. The collected fiber is "back washed" from the media
with a small shower of diatomite filtered water, the fiber falling into
a box having a screened bottom to permit drainage. The accumulated fiber
is forked away manually and sent to dry waste disposal areas. Mechani-
zation of this aspect would reduce labor costs. The liquid falls through
the media into a collecting pan or tank from which it flows to a centrif-
ugal pump for transfer to the dirty water tank. The purpose of the
primary filters is to remove as much solid material as possible to make
the remaining secondary (diatomite) filtering duty as light as possible.
The primary filters have handled average loads satisfactorily but have
tended to overflow at peak loads - thereby passing extra dirt load to
the secondary filters. Polypropylene cloth has been changed from 60 mesh
to 100 mesh to increase solids removal. 80 mesh is currently in use since
the 80 mesh is of heavier gauge material and has longer wearing life than
the 100 mesh media. A larger filter having approximately four times the
capacity of the existing units has been built and will shortly be put
into service. The increased capacity should improve the cycle life on
the diatomite filters and possibly permit elimination of the scrap pump
by accepting all the screening duty on the new primary filter.
22
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FIGURE 6 - PRIMARY FILTER
23
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FIGURE 11 - PRIMARY FILTERS
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Secondary Filters.
Design Criteria:
A complete package unit consisting of dual filter units to automatically
filter phenolic bearing water at flow rates of 8 - 50 GPM having sus-
pended solids in the inlet ranging from 8 - 60 ppm with an expected
outlet content of 0 - 8 ppm. Total solids content in the inlet water
will range from 1900 - i*700 ppm. Diatomite filter aid will "be Johns-
Manville Celite #5^5. Water temperature will range from ^0 - 120 deg.
F. pH value will be regulated between 8.5 - 9.5. Filter cake and
accumulated solids are to be discharged from the filter in a semi-dry
state, air blown and liquid free. All water required for flushing and
backwashing the filters is to be returned to the dirty water tank for
reuse as filter feed. This water cannot be discharged to sewers.
Area of precoat filter surface of each filter is to be 300 sq. feet.
Unit flow rate to filters is not to exceed .3 GPM per square foot -
nominal flow being 75 GPM through filter when supplying 50 GPM to process.
The secondary filters are pressure vessels using diatomaceous earth on
stainless steel woven mesh flexible septa.* (Refer to Figure #12)
There are two semi-automatic units each having 300 square feet of surface
area with controls arranged so that the "on-stream" unit will be auto-
matically shut down and put into "blow-down" phase by the cycle timer
or by excessive differential pressure across the tubes, whichever occurs
first, and the "stand-by" unit will be automatically brought on stream.
Removal of the spent filter-aid and recharge is accomplished manually
through removal of the detachable bottom of the filter housing. During
the "blow-down" phase prior to removal of filter-aid, all water is pressed
out of the vessel and from the spent filter-aid, by air pressure, which
forces the water through a wool felt filter at the bottom of the vessel.
This feature permits the water on the dirty side of the filter to be
re-used, thereby avoiding the necessity to discharge any circulating
"chain" cleaning water. The filters were sized for twelve hour duty so
that re-charge of diatomaceous earth could be accomplished by maintenance
personnel on the day shift. Under normal circumstances, for example,
Filter "A" put "on-stream" at 10 A.M. would be taken off stream at 10 P.M.
and be left in "blow-down" phase until the maintenance man coming on duty
at 8 A.M. services it. "A" filter would be ready to put on stream at
10 A.M., when "B" filter which was brought on stream at 10 P.M. the
previous night, will go off-stream after its twelve hour cycle has been
completed.
Under abnormal circumstances, such as a sudden heavy loading, filters
will go off-stream due to high pressure before completing the twelve
hour cycle. In such cases, maintenance personnel adjust to the new
condition and gradually work the equipment into a normal operating mode.
Scheduled twelve hour cycle life is attained about 90$ of the time.
Piping is arranged so that the diatomite filters will operate at a constant
flow rate and at constant head. Under such ideal conditions, it is un-
likely that diatomite would be dislodged from the septa due to hydraulic
shocks such as occur when a valve is suddenly opened or closed.
* Footnote #1 - Septa are tubes vertically suspended in the dirty water.
25
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FIGURE 12 - DIATOMACEOUS EARTH FILTERS
26
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To provide such conditions it is necessary to have certain accessories
for a good diatomite filter installation, notably a dirty water tank,
a supply pump and a filtered water tank, together with level controls.
Filter-aid is supplied with 25# of diatomite as precoat in the "pot"
or detachable "bottom of the filter. The remaining 50# of the 75# charge
is fed uniformly by dry feeder and vortex mixer to the dirty water tank
as "body" feed over the twelve hour cycle.
Dirty Water Tank.
Design Criteria:
Tank to be filled with level control to provide a uniform suction head
on the dirty water filter feed pumps.
a 6' diameter lk' high open top tank containing about 1000 gallons at
the half-full point provides the suction head condition for the centri-
fugal pump which supplies water to its associated filter. At rated flow
of 75 gallons per minute, the pump discharges filtered water to an open
funnel about 6' higher than the filter outlet. From the funnel the
filtered water passes to the clear (filtered) water tank. If, however,
the level in the dirty water tank falls below 6' above the tank bottom,
the level controller diverts filtered water from the filtered water tank
to the dirty water tank until such time as the dirty water tank level is
restored to about 7' above the bottom. The level control then restores
the flow of filtered water to the filtered water tank. With a constant
suction level thus provided, and a constant height of discharge above
the pump, a steady flow through the filter is assured with minimum
fluctuation in pressure conditions to cause filter-aid dislodgement.
Flow through the filter will, of course, vary from a maximum at the
beginning of the cycle to a minimum at the end, because of the increas-
ing pressure drop across the media. The function of the dirty water
tank is therefore to provide a constant suction head on the filter pump.
Filtered Water Tank.
Design Criteria:
Tank capacity must be adequate to provide for varying process demands.
The filtered water tank is the sane size as the dirty water tank. It
serves as a surge tank to provide for the varying demands of the process.
An automatic level control device operates a valve to maintain this tank
in a full condition by admitting softened city water as required. An
overflow pipe also connects to the dirty water tank to provide storage
of excess filtered water should demand for "overspray" and "binder-mix"
water cease while "chain" cleaning continues. Gauge glasses are pro-
vided on each tank for ready determination of level. Figure #13 shows
both tanks with the filtered water tank on the left and the dirty water
tank at the right.
27
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FIGURE 13 - FILTERED AND DIRTY WATER TANKS
28
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Cartridge Filters.
Design Criteria:
Pass 170 G-PM water pH 8.5 - 9-5 having inlet suspended solids content
of 0 - 8 ppm and expected outlet content of 0 - 6 ppm with pressure
drop from 2 to 15 psi.
Filtered water from the filtered water tank is pumped through a
cartridge filter station to the various points of use in the process.
The cartridge filters use Fiber Glass cartridges made at Plant #3. The
cartridge filters are not required for added clarity of the water. They
were installed as a final filter to protect the system should a failure
of the diatomite filters occur. The precaution has been valuable in a
few instances, such as septa failure and in collecting fungus
accumulations.
1000 psi Chain Cleaning Supply.
Design Criteria:
Tank to be provided with level control to maintain a constant suction
head on high pressure pumps.
Filtered water is admitted to a small supply tank served by a rloat
controlled valve. Water from this tank is fed to any of three re-
ciprocating triplex horizontal plunger pumps, two of which are rated
at 37 gpm each, while the third is rated at 20 gpm.
The 1000 psi header to which the three pumps are connected is fitted with
an air operated back pressure control valve which maintains a uniform
pressure on the line supplying the cleaning nozzles. Operating pressure
has been maintained at 800 psi throughout the operating phase of the
project, this pressure being adequate to clean the "chain". At 800 psi
one pump serves the load.
Overspray Supply.
Two overspray centrifugal pumps each rated at 20 gpm at 200 psi receive
water from the same supply tank which serves the 1000 psi "chain" cleaning
pumps. Pressure regulators are provided at each machine but these are
set at 200 psi in all cases. One pump carries the load.
pH Control.
Filtration of the resinous "chain" cleaning mixture is feasible, but is
believed to require the addition of ammonia to a pH range of 8.5 -9-5
to stabilize the resin. It is believed that at lower pH ranges pre-
cipitation of resin occurs which causes rapid "blinding" of the media and
tubes with suspended resin. In support of this belief, aqueous ammonia
is fed at constant rate by a chemical feed pump to the inlet of the
diatomite filter supply pumps. Automatic control is not used, but pH
29
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determinations are made at approximately four hour intervals which
serve to provide an approximate pH range of 8.5 - 9-5. A small per-
centage of readings taken fall outside the range. Use of a pH con-
troller is planned to determine if closer control is warranted.
Flow Chart.
Figure #7 is a diagram of the water flow in the process. At Cleaning
Station "S" 1000 psi water is directed at the "chain" and thereafter
falling with entrained resin and glass fiber to the floor trench, flows
to scrap pump "A" where coarse fiber is screened and extruded in a
damp condition to a waste disposal bucket. The screened water leaving
"A" is directed to either of two centrifugal rubber lined slurry pumps
"B-l" and "B" which deliver the abrasive water to the primary filters
"D" where fiber that passed through the coarse screen of the scrap pump
is removed.
The filtrate from "D" is pumped to the dirty water tank "E" at which
point diatomaceous earth filter-aid is added as "body feed" before the
water is pumped to diatomite filters "F". The clear filtrate from "F"
passes to the filtered water tank "G" which serves as a reservoir to
meet the varying demands of the system. Fresh city water "make-up" to
the system, after softening at "M", is admitted to tank "G" by a level
control valve to maintain a full reservoir of clear water. Water
from "G" then is pumped at 50 psi to the process, first passing through
emergency fiber glass cartridge filter station "H".
On the basis of daily meter reading, average flows of 15 gpm are sent to
two wet dust collectors from which the overflow to pump "C" is returned
to primary filter "D". 12 gpm go to the binder-mix room from which the
binder is pumped to the fiber glass machine and is later evaporated.
3 gpm are sent to solids removal showers on the primary filters "D".
An average flow of 2 gpm serves three wash hoses at the forming end of
the machine. Each hose requires 50 gpm for short periods. The estimated
average flow from these intermittent cleaning uses is drained to the
floor trench and returned to "A". 60 gpm is delivered to supply tank "J"
from which 12 gpm is pumped at 200 psi to "overspray" nozzles at the
fiber glass machines from which it is subsequently evaporated. The re-
maining U8 gpm from "J" are delivered at 1000 psi to the "chain"
cleaning stations at "S".
Treatment Tank and Discharge Weirs.
Other features noted on the flow chart are incidental to the normal
cycle above outlined or are not related to the process. "K" is a 30,000
gallon open top steel tank located out of doors and fitted with a small
aerator. It is a holding tank to receive excess flows from the sump pump
"C", such as would be occasioned by a failure of pump "B" or would result
from water discharged from putting out a fire on the fiber glass machines c
30
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FIGURE 1 - FLCW CHART - SCHEMATIC
WASTE RECLAMATION SYSTEM
31
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elsewhere from sprinklers. "Backwash" water-from the softeners and a
caustic mandrel wash discharge from the mandrel cleaning tank also go
to tank "K" via sump pump "C". "K" is equipped with a pump and pipe
line for return of water to the process. The high causticity of mandrel
wash water has prevented return of the water to process use "because
of foaming. Tank "K" is also fitted with a valve which would permit
pumping of contents of "K" to #2 Weir and thence to Preston Run tri-
butary. This valve is enclosed by fence and locked gate, accessible
only to delegated personnel. #2 Weir also receives water from two
Johns-Manvilie storm sewers. (Refer to Figure #1^). A third Johns-
Manville storm sewer discharges to #1 Weir, which also receives flow
from a neighboring plant sewer owned by "All Star Products" as well as
domestic waste from a septic tank on "All Star Products" property into
which the domestic waste from both "All Star Products" and Johns-Manvilie
Plant #3 discharge. The complicating sources of water entering this
tributary to Preston Run make the use of flow readings at #1 and #2
Weir questionable for detailed analysis purposes. Nevertheless, the
general downward trend of these flows correlates with the reduced water
purchases made by Plant #3 after operation of the project started.
Schedule.
The Design & Construction phase of the project required one year -vs-
an estimated six months schedule. Each equipment item and its support-
ing pits, trenches, piping and wiring received the following phases of
consideration before installation could start:
Time element *
Federal Approval of Preliminary Plans
Design
Write Specifications
Competitive Bidding
Approval of Purchase (FWPCA)
Purchase
Fabricate and Ship
Installation
Total .... 16 months to 1/7/69
3-1/2 months to 12/15/67
H-l/2 months to 5/5/68
1-1/2 months to 6/15/68
1 month to 7/15/68
1/2 month to 8/1/68
lA month to 8/7/68
3 A month to 9/1/68
k months to 1/7/69
* Time element is given as maximum time required. For example, although
the last major purchase item occurred on August 7th, many purchases
were made prior to this time as rapidly as bidding was completed.
32
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FIGURE lit - #2 WEIR
33
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Operation started on January 7» 1969. Construction was completed on
February U, 1969 when work was finished on the treatment tank.
After FWPCA approval of preliminary plans, some twelve and one-half
months were required to effect the installation. Actual construction
and installation was accomplished in four months, while planning and
purchase preparation required eight and one-half months. While it is
not unusual for the planning phases of a project to require as much time
as the installation, the initial estimate of six months for planning
and installation was not achieved. In a subsequent installation at our
new Winder, Georgia fiberglass plant, in which the closed system at
Defiance 003 was closely followed, design started in July of 1968 and
production started in August of 1969. Some of the time element in this
instance was dependent on the construction of other features of a new
plant. Depending upon the urgency, a closed system of this nature
should be available for use within eight to twelve months after approval.
Unusual Construction Features.
The normal twenty-four hour continuous operation of a fiberglass plant
presented problems from the standpoint of lost production of fiberglass.
Scheduling of outage was based on maximum speed of converting the
product units. This project was developed from a prior trial of about
ten months length on #5 product unit at Defiance 003. In this project
it was necessary to revise the travel of the collection conveyor to
permit downward blow-off of fiber and resin from the conveyor chain.
In the current project it was necessary to carry out conveyor revisions
to the remaining four product units and install a sluice trench under
all units for reclamation of the conveyor chain wash water. The trench
was installed first, but due to production requirements, had to be
installed in five separate sections so that interruption to production
occurred on but one machine at a time. Each section of trench was
installed in a twenty-four hour day. Revision of the collection conveyor
was accomplished by scheduling each product unit down for five days at
a time. Conversion was carried out on a twenty-four hour, around the
clock, basis to minimize outage. After conversion, chain cleaning was
accomplished with fresh water at 200 psi initially, and eventually at
1000 psi and the water discharged to Preston Run.
Prior to the conversion of all five product units, installation had
been carried forward on the construction of the scrap collection pit and
on the installation of the primary and secondary filters fin the water
room. In the first product unit conversion (#1 unit), city water was
supplied to the chain cleaning nozzle at 200 psi from the overspray pumps
until such time as the normal 1000 psi pumping system was ready. Clean-
ing was adequate at 200 psi on this unit. During the foregoing conversion
period, discharged water from the chain cleaning operation was sluiced
through the scrap pump which removed coarse glass fibers. The water
was routed to one of the two transfer pumps which send the water to the
primary screens. After passing through the 60 mesh screens, the water
-------
was diverted from its normal course through the secondary (diatomite)
filters to the stream.
When the diatomite filter installation was completed and after con-
version of all Product Units, the diatomite filters were put on stream
and the filtered water returned to re-use as chain cleaning water, as
overspray and as binder mix water.
35
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OPERATION OF PROJECT
An objective of the project was to operate the system as planned for
twelve months and to collect pertinent information during this period.
A twelve month period of successful operation was achieved as of
January 15, 1970. The system performed substantially as anti-
cipated in continuous twenty-four hour per day, seven day per week
service. Comprehensive sampling and analysis of the water in the
system and of water discharged was made and recorded.
Four significant unanticipated actions occurred which temporarily in-
terrupted operation in two instances and which adversely affected
operating costs in two cases.
The first situation resulted from the failure of diatomite filter septa
during February and March of 19^9, in the first two months of operation.
Diatomite filter outage occurred for a few days until new tubes were
replaced. The septa failed due to plating of sticky solids over the
flow spaces in the septa. This problem was corrected by changing
the diatomite feed from a single charging at the beginning of a cycle
to initial charging of one-third of the diatomite and continuous "body"
feeding of the remaining two-thirds during the twelve hour filter cycle.
Temporary interruption occurred, but operating costs were not increased.
The second unexpected action was the development of foam when attempts
were made to reuse the miscellaneous "non-chain cleaning" waters in
the chain cleaning circuit. The high pH of these waters served to
generate foam which threatened shut down of the circulating system
because of inability of filter pumps to handle the flow at lower suction
heads than planned. Reclamation of this water was abandoned in favor
of routing it to a new sewer connection to the City of Defiance treat-
ment plant. Added operating cost will result from municipal sewage
treatment charges.
The third unplanned problem resulted when a small pipe line became
plugged on April l8th with a gray rubber-like non-sticky slime-like
substance. This threat to recirculation was so serious that consultants
were retained and re-circulation was halted until understanding of this
development was achieved. The blockage was identified as a fungus and
after study a suitable fungicide was fed to the system which has
successfully contained the fungus. Recirculation was restored April 30th
after a twelve day interruption. Added operating costs resulted from
the feeding of fungicide to the system.
37
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The fourth unexpected condition resulted from a production change in
August, 19^9f when a new method of applying the binder caused extra
consult ion of binder. The binder savings which were planned as part
of this project turned into losses in August and much reduced savings
in the ensuing months. Eventually binder savings were largely restored
after production personnel discovered the knack of handling the new
method. Added costs occurred for the remainder of the period over those
obtained during the first six months.
The foregoing unexpected developments hindered but did not prevent the
successful operation of the recirculating system for the twelve month
grant period.
38
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VI
EVALUATION PROGRAM
Operating Parameters.
The following parameters are considered to "be significant:
Suspended solids concentration
Dissolved solids concentration
Phenolic concentration
PH
Water consumption
Discharge to stream
Testing Program.
Sampling at eight points was made once per week on Thursday. The
samples were analyzed for phenol, suspended solids, pH and total solids
content. The sampling points, located on Figure #16, are:
#1 Outside tank
2 Downstream of discharge
3 Weir #1 (discharge)
U Weir #2 "
5 Entering Primary Filter West
6 Entering dirty water tank, before diatomite filtration
1 Entering clear water tank, after diatomite filtration
8 Supply tank, after make-up dilution and cartridge filter
Unit Performance.
Data for the month of November is computed in Section VII. It shows
that the average daily suspended solids removal amount to:
Unit Lbs. %
Scrap Pump 2UOO 32.6 / Estimate
Primary Filter West (chain cleaning) 2^00 32.6 Calculation
Primary Filter East (dust collector) 2500 3^.2 Estimate
Diatomite Filters ^3 .&_ Calculation
Total 731*3 100.0
39
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FIGURE 16 - SAMPLING POINT LOCATIONS
-------
It is noted here that the primary filter "east" was utilized to screen
dust collector waste solids and the primary filter 'Vest" handled the
chain cleaning solids remaining after prior scalping by the scrap pump.
The filtrate from both primary filters was combined in the dirty water
tank as feed for the diatomite filters.
The diatomite filters were therefore filtering two different process
streams, one containing saw kerf from cured fiber glass, the other con-
taining solids from uncured fiber glass. Both streams contained phenolic
resin. Records were kept on the chain cleaning process but not on the
dust cleaning circuit. Even so, .the records kept do not show the amount
of chain cleaning solids removed by the diatomite filters. The best
indication of unit performance, therefore, is to estimate the total
solids removed from the dust collector stream by the primary filter
east. A total throughput is thus estimated from both streams. On this
"basis the diatomite filters can be said to have handled .6% of all
solids in the streams passing through them.
System Performance.
The several parameters representative of operation are listed in Tables
A-l through A-5 in Appendix "A". Graphically, these parameters are
shown in Figures discussed below:
Phenol Concentration - Discharge - Figure #17.
The high concentrations found in #1 sample (holding tank) are the result
of discharges to the holding tank which were generally not from the
recirculating system. Bleeding of the holding tank contents at con-
trolled rates produced the lower values found in #U sample (#2 Weir)
and in #2 sample (Downstream of discharge).
Phenol Concentration - Recirculated Water - Figure #18.
#5 and #6 sample values before and after the primary filter west re-
spectively, closely parallel each other. One would expect that the
"after filtration" samples wouxd have slightly lower values due to
removal of suspended fiber solids and adhering phenolic resin particles.
The #7 sample (after diatomite filtration) was mistakenly not analyzed
for phenol, in the belief that #7 and #8 samples would have identical
dissolved phenol content. Actually, the #8 sample values are con-
sistently lower than those for #6 sample (before diatomite filters)
due to filtration effects and primarily from the admission of make-up
water at the filtered water tank. The general level of phenol con-
centrations falls in the range of 10 - 25 parts per million.
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Suspended Solids - Discharge - Figure #19.
Suspended solids in the stream below the discharge points from #1 and
#2 Weirs were generally found to be in a 0 to 30 part per million
range, but on several occasions exceeded this range. The principal
factor affecting this condition was the manually regulated bleed from
the holding tank of unfiltered water.
Suspended Solids - Recirculated Water - Figure #20.
Figure #20 clearly brings out the effectiveness of three of the four
stages of filtration used. Suspended solids leaving the scrap pump
and entering the primary filter West (#5 sample) had concentration in
the 100 - 1000 ppm range. The water entering the diatomite filters
contained suspended solids in a 25 - 100 ppm range (sample #6) and
leaving the diatomite filters contained 0 to 10 ppm. The final water
circulated to process, after make-up dilution and after passage through
fiberglass cartridge filters contained 0 to k ppm of suspended solids.
The final water was more than adequately clarified for intended uses,
the most restrictive of which was dispersion through fine spray nozzles.
Total Solids Discharge - Figure #21.
The total solids content of Preston Run tributary water below Johns-
Manville's discharge point (#2 sample) was generally less than 1000 ppm.
Inasmuch as the suspended solids at this point ranged from 0-30 ppm,
the dissolved solids amounted to approximately 970 + parts per million.
Total Solids Recirculated Water - Figure #22.
The water entering the primary filter West (#5 sample) had highly
variable values, resulting from the variable suspended solids content
observable in Figure #20. As suspended solids were removed the total
solids values in the filtrate, sample #6, became more uniform, covering
a range of 3000 - 7000 ppm. Deducting the suspended solids range of
25 - 100 ppm seen in Figure #20, the dissolved solids content ranged
from about 29^0 - 69^0 ppm. Similarly, the filtrate entering the clear
water tank (sample #7) had total solids values of 3000 - 6000 ppm and
suspended solids from 0 to 10 ppm (Figure #20) or a dissolved solids
content of approximately 3000 - 6000 ppm.
Total solids in the final filtrate, after make-up (sample #8) ranged
from 2000 to kOOO ppm. Deducting suspended solids ranging from 0 to
b ppm, the dissolved solids value of the final filtrate and make-up
ranged from approximately 2000 - UOOO ppm. Maximum dissolved solids
concentrations occurred entering the primary filter and had approximately
the same value entering the secondary diatomite filter, approximately
6000 - 7000 ppm. Greater concentrations may be possible.
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pH values - Discharge - Figure #23.
pH values in Preston Run tributary below the discharge point ranged
from about 7.2 to 8.7 (sample #2). A very high pH range of 11.0 to
12.0 was found in the holding tank, the result of containing discharges
of caustic mandrel wash water.
pH values of 8.0 - 9.0 range were found at #1 Weir (#3 sample) and 7.5
to 8.5 readings were recorded at #2 Weir (#U sample). These findings
reflect the result of controlled release from the holding tank.
pH values - Recirculated Water - Figure #2U.
The pH determinations for samples #5, 7 and 8 fall in a narrow range,
approximately 9.3 to 9-6. This represents the result of manual addition
of aqueous ammonia via chemical feeder to maintain a uniform pH value.
#6 sample falls .1 to .2 pH below the remaining values. This is probably
because #6 sample is the last point in the re-circulating track before
ammonia addition takes place.
Water Consumption Trend - Figure #15.
Fortunately for the purposes of this project, all water is purchased
from the City of Defiance. Since it is all metered, we have a perfect
"before" and "after" situation which reflects accurately the degree of
re-circulation being practiced. Water purchasing plumetted to almost
one-third of the pre-recirculating period values when the re-circulating
system started in January 1969. Consumption came up again in March
and April during the period when fungus developments necessitated
running "open" until corrective measures were taken. After May, with
fungicide protection operative, water purchases dropped to the minimum
non-process use plus process evaporation requirements .
Average Daily Discharge to Preston Run - Figure #25,
The premise of re-use of water implies that not as much water will be
required. As noted above, water purchases were greatly reduced as soon
as re-cycling of water started. It is also true that less water
should be discharged from the plant under water re-use principles.
Reference to Figure #25 shows that a substantial reduction in discharge
to the stream did occur.
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G
cn
cn
o
Q
-------
ru
i
tc
s
M
W
o
II
to
o
-------
FIGURE 15 - WATER CONSUMPTION TREITO
-------
X
1
5
N
N
FIGURE 25 - AVERAGE DAILY DISCHARGE - GALLONS/MINUTE
-------
VII
EVALUATION AND DISCUSSION
Several aspects of the operating period warrant special comment.
Discussion follows:
Suspended Solids Removal.
Records of solids removed by the scrap pump, primary filters, diatomite
filters and cartridge filters were not kept. However, from analysis
of weekly samples, it is possible to calculate the solids removed by
the primary and secondary (diatomite) filters. Referring to Table A-H
"Quality of Recirculated Water" it is possible to obtain the average
of twelve weekly samples for the quarter ending October 1969 These
values of suspended solids are:
Primary Filter West Diatomite Filters
Entering ppm
Leaving ppm
Difference ppm
Flow - from Table l6 - GPM
*Solids Removed - Ibs/day
Primary Filter - Weight of Solids =
3797 ppm x 52.k GPM x 1^0 min. x 8.3 M/gal = 2i+00 Ibs
1/000,000
Diatomite Filter - Weight of Solids =
68.3 x 52. k x iHUO x 8.3^^^3.0 Ibs.
1,000,000
*As noted above, scrap pump solids removal data were not taken. However,
from general observation, the scrap pump solids removal appears to be
approximately the same as that from the primary filters. Stated another
way, about U800# of solids are removed ahead of the diatomite filters
which remove ^3-0 additional Ibs. each day.
55
-------
Diatomite Filter Performance.
The latest month, November 19&9, for which data is available had in-
significant interruptions. From Table 1 the percentage of "on-stream"
time was 9^.0.
Diatomite used is calculated as follows:
75#/charge x 2 charges/day x 30 days x 9W = ^200 #
Water Filtered:
#2 Meter (Filtered Water plus make-up) recorded 2,915,300 gals, in Nov,
#5 Meter (Make-up to clean water tank) recorded 6l8,700 gals, in Nov.
Water re-circulated (filtered) = #2-#5 meters = 2,296,600 gals, in Nov.
Water Filtered per Ib. of Filter Aid:
= 2,296,000 gallons x 9!$ = 513 gallons/lb.
i*,200# Diatomite
Solids removed in November:
Entering Leaving
Suspended Solids Suspended Solids
PPM PPM
November 6, 1969 96 8
November 13, 1969 96 5
November 20, 1969 32 2
November 26, 1969 136 1
Total 360 16
Average 90 h
Difference ... 86
Weight Removed =
2,296,600 gals x 9h% x S.S^/gal x 86 ppm = 15Uo Ibs.
1,000,000
Ratio Solids Removed to Filter Aid =
Ratio Solids Removed to Cake = 15^0
1*200 =
56
-------
Date
Filter "A'
TABLE 1
ON-STREAM CYCLE LIFE
WPRD 87-01-68
Filter "B1
Date
Filter "A1
10/8/69
10/9
10/10
10/11
10/12
10/13
10/lU
10/15
10/16
10/17
10/18
10/19
10/20
10/21
10/22
10/23
10/2U
10/25
10/26
10/27
10/28**
10/29
10/30
10/31
12 hours
10
-
12
3.5
12
12
12
2k
9
16
12
20
19
2k
23
20
16
22
11.5
-
12
12
12
10 hours
12
12
11.5
lit
12
12
2
_ *
_
_
_
_
_
_
_
_
_
12
12
12
Filter "Br
11/1/69
11/2
11/3
11/1*
11/5
11/6
11/7
11/8
11/9
11/10
11/11
11/12
11/13
ll/ll*
11/15
11/16
11/17
11/18
11/19
11/20
11/21
11/22
11/23
11/2U
11/25
11/26
11/27
11/28
11/29
11/30
12 hours
12
12
11.5
12
11
12
12
12
12
12
12
11
8.5
10.5
12
12
12
12
12
12
12
9.5
12
12
12
12
_
12
12
12 hours
12
12
12
12
7.5
10
12
12
8
12
12
10.5
11.5
12
12
12
8
12
10.5
11
9.5
12
12
12
12
12
12
12
12
Total 338.0 + 338.5 = 676.5
Actual Hours November 30 x 2U = 720
Percentage "on-stream" - 9^-0
* Mechanical seal on "B" Filter pump failed
** On city water
TABLE 1 - ON-STREAM CYCLE LIFE
57
-------
Check.
A sample of filter cake taken June k, 1969 was submitted for chemical
and petrographic analysis. The probable composition was reported
as follows:
Diatomite 72 to 75$
Glass Fiber 20
Quartz Less than 5
Resin 2.6
Calcium Carbonate .2
The June sample analysis corroborates the November performance calculated
above in which diatomite is ^200# - or 73$ of the cake content
15 UO
Cost of Filtered Water.
Table 2 provides an approximate cost for operating the filters by
adding the + items, except for the salt used in the softener, which
is required regardless of the needs of the closed water system.
Gross Net
Operating costs for November, 1969 add to $2,556 $ -
Depreciation - $12,100 - 1,008 1,008
12 mos.
Total cost $3,561+ $ 851+
Water re-circulated = 2,296,600 gallons
Cost per 1000 gallons = $1.56 $ .37
Cost of City Water.
City of Defiance billing for November 1969 was $60i+.22 for 956,700
gallons, or $.63 per 1000 gallons. To that is added the cost of
softening which amounted to $8l in November ($1|0.50 for salt, and
$U0.50 for labor) for softening 6l8,700 gallons of process make-up
water and l4-U,520 gallons of boiler feed.
Softening cost was $8l or $.12 per 1000 gallons
663,000 gallons
Capital cost of softening equipment not included - considered
The cost of City Water for process use is therefore $.63 + .12 - or
$.75 per 1000 gallons.
-------
Comparison City Water -vs- Filtered Water Costs.
As outlined above, the gross cost of filtered water is $1.56 per
1000 gallons, while the current cost of city water softened for process
use is calculated at $.75/1000 gallons. The question might be raised
as to why the expensive process of cleaning up dirty water for reuse
is practical when new water costs half as much. The answer to this
question is that use of 100% fresh water would not have solved the
waste discharge problem. Further, operation on an open basis would
just about double the water requirement again, so that the total cost
of water would, in effect, be double that paid under the re-circulating
system. Water costs would be approximately what was paid to the City
in the last six months of 1968 (Refer to Table 12) . In another view,
the net cost of filtered water is $.37 per 1000 gallons -vs- $.75 for
softened City water.
Water Re-use .
From Table l6 it is seen that during the quarter ending October 31st,
1969, an average re-circulation volume of 52. H gallon/minute was
metered, while at the same time, 15.2 gallon/minute of fresh water
was admitted to the system. In order for the 15.2 GPM to do the work
accomplished by 52.it x 15.2 GPM, it has to be used several times -
in fact - 67.6 GPM , _ ,.
jj ^ ti - or 4.5 times.
It is possible that it could be re-circulated more times, with the
limiting factor eventually being the tolerable limit of dissolved
solids concentration. The rate of re-use in this system is determined
by the amount of evaporation, a process variable, which in recent
history, has not changed significantly.
59
-------
WATER BILLS - CITY OF DEFIANCE
WPRD 87-01-68
Meter Readings Cubic Feet Water
Present Previous Used Charge
June 25, 1968
July 26, 1968
August 22, 1968
September 26, 1968
October 23, 1968
November 20, 1968
December 26, 1968
January 27, 1969
February 2k, 1969
March 25, 1969
April 23, 1969
May 27, 1969
June 2k, 1969
July 20, 1969
August 22, 1969
September 2h , 1969
October 2h , 1969
November 21, 1969
751,800
1,168,100
535,1+00
985,000
2,313,700
623,500
3,065,200
336,200
i+72,300
70l+,200
986,800
1+, 186, 200
319,800
1+93,000
62l+,900
776,000
905,600
5,033,200
327,100
751,800
168,100
535,1+00
1,985,000
313,700
2,623,500
065,200
336,200
1+72,300
70U,200
3,986,800
186,200
319,800
1+93,000
62U,900
776,000
i+, 905, 600
l+2l+,700
1+16,300
367,300
1+1+9,600
328,700
309,800
1+1+1,700
271,000
136,100
231,900
282,600
199, '+00
133,600
173,200
131,900
151,100
129,600
127,600
$1,1+38.10
1,1+11+. 5H
1,277.38
1,507.8s
1,169.30
1,116.38
1,1*85.70
1,007.71+
630.02
898.26
1,01+0.22*
807.26*
6?3.02
733.90
6.18.26
670.02
609-82
601+.22
High consumption due to fungus
TABLE 12 - WATER BILLS, CITY OF DEFIANCE
60
-------
Operation and Maintenance Activities .
Grant application estimates totalling $9,560 were exceeded by $lU,622
for twelve months ending January 15, 1970- Cost elements considered
in the application are compared as follows with actual expenditures:
Grant * Actual
Labor $3,200 $13,351
Diatomaceous Earth 2,080 2,95^
Ammonia 630 2,2^1
Power 3,650
Sub-total ..... $9,560 $23,250
Other items not considered are:
Fiber Glass Filters
Polypropylene Media 1,291
Fungicide and Dispersant _ 1,908
Total ....... $9,560 $26,885
Production Changes Affect Data Use.
Production operations for January through July of 1969 were sub-
stantially unchanged from the six month period before closed system
operation, except for the inclusion of the closed water system. Any
effects noted could be attributed to the closed water system. In
August, however, another change occurred in the form of a different
method of binder application. There being no other changes in operation
or in the closed water system, effects noted are attributable to the
changed method of applying binder.
Operating Cost Differences .
The most notable effect was the immediate loss of binder savings which
had been increasing since the inception of the closed water system.
Savings recurred in September and although much smaller than in the
months prior to August, subsequent results show that the savings are
still increasing. Accordingly, it is believed that data relating to
savings should be viewed in the light of the first seven month's
performance. Savings are therefore discussed from records of the
first seven months.
* From Table 2, a table of differences in operating costs adjusted for
volume. It will not agree with actual $2^,182 reported in Table
(period 1/15/69 - 1/15/70).
61
-------
Operating Cost Differences.
Operating costs are not reported per se but differences in operating
costs incurred during a base period prior to the installation of the
closed system and costs developed during the operation of the closed
system are reported. Under this approach a lover operating cost than
those incurred in the base period are given a negative sign which
represents a saving. Higher costs than those incurred in the base
period receive a plus sign which represents increased cost to operate
the system. Table 2 shows how the significant elements of cost have
developed during the twelve months of operation. Discussion of these
cost factors is covered later in this section.
Water Consumption and Quality.
Water consumption and quality is not believed to have been affected by
the change in binder application which was initiated in August. There
is therefore no reason for limiting the data gathered for this phase
of the study. All data taken will be used in the discussion of water
quantity and quality.
Data Frequency.
Data were taken as noted below:
Before Closed System Operation:
Daily.
Water meter readings to the plant and distribution readings within the
plant were taken daily. Flow readings at #1 and #2 Discharge Weirs
were made once each day. The weir readings represent momentary rates
of flow, while the meter readings produce total flows for the twenty-
four hour day. Daily usage of salt for water softening was noted.
The complete record of these daily flows is submitted herein.
(Refer to Table A-l) .
Weekly.
Grab samples of water were taken from #1 and #2 Discharge Weirs and
upstream and downstream of these discharges and analyses of the samples
were made for Biological Oxygen Demand - 5 day, Dissolved Oxygen, pH,
Phenol, Suspended Solids and Total Solids once a week for the month of
December 1968. These data are enclosed herein in Table k.
62
-------
o^
u>
I
o
H
CO
C1
3
OO
WATER QUALITY - DISCHARGE - 1968
WPRD 87-01-68
Sample Location
pH
Phenol
PPM
12/20/68
#1 Upstream
2 Downstream
3 #1 Weir
U #2 Weir
7.0
7.9
7.9
7.6
.002
3.0UO
U.720
.069
Total
Solids
PPM
39
506
562
193
Susp.
Solids
PPM;
1
CD
^
1
^
1
(5
M
r-a
12/5/68
#1
2
3
^
12/12/68
#1
2
3
U
Upstream
Downstream
#1 Weir
#2 Weir
Upstream
Downstream
#1 Weir
#2 Weir
38
68
27
61
21
62
22
70
U.9
U.U
5.1
3. .7
5.2
U.I
5.1
5.6
7.5
8.9
8.9
8.2
7.7
6.5
7.8
8.U
.010
3.000
3.360
.2U3
.OlU
3.860
3.100
0.228
U65
76U8
1117
U081
507
1139
881
U77
77
72
122
23
83
3U
8U
67
17
19
56
07
12/26/68
#1
2
3
U
Upstream
Downstream
#1 Weir
#2 Weir
UU
20
18
13
U.7
5.8
5.9
U.2
7-U
7.8
7.7
7.2
.003
2.520
U.2UO
.090
1U30
1300
101U
857
585
3U
50
35
Flow - GPM
21.T
Plugged Sewer
Plugged Sewer
27.6
1.0
21.7
-------
After Closed System Operation:
Daily.
Water meter readings to the plant and distribution readings vithin the
plant were continued on a daily basis as before operation of the closed
water system. Necessarily certain meters in the distribution system
were relocated because of piping changes in the closed system.
Readings of flow at #1 and #2 Discharge were continued on a once-daily
basis. Daily usage of salt for water softening was noted. The complete
record of these logged daily flows is submitted herein. (Refer to
Table A-2.)
Weekly.
Grab samples were taken from #1 and #2 discharge weirs and from upstream *
and downstream of the weir discharges and analyzed once a week. Grab
samples were also taken from the circulated "chain" cleaning water at
entrance to primary filters, at entrance to secondary filters, at entrance
to the filtered water tank and at entrance to the supply tank. All
samples were analyzed for phenol, pH, suspended solids and total solids.
(Refer to Table A-3 Water Quality Data - Discharge and to Table A-U
Water Quality Data - Recirculated Water.)
Other Discharges.
Other discharges not included in the scope of the grant will receive
the following disposition:
Domestic Waste.
Domestic waste now being discharged to Preston Run tributary will, during
early 197P, be connected to the Defiance Municipal Sewage Treatment Plant.
A new 8" interceptor was laid in November in Hickory Street with terminus
at Plant #3. The Johns-Manville connection will be made as soon as the
Defiance Municipal Plant is ready to receive the added load.
Boiler Blow-Down.
Boiler "blow-down" now being discharged to Preston Run tributary will be
connected to the new sanitary sewer line described above.
Softener "Backwash".
Softener "backwash" water now being discharged to holding tank and thence
to Preston Run tributary will be connected to the new sanitary sewer line.
* Lack of flow upstream of the discharge point made it more desirable to
shift this sampling point to the holding tank.
6k
-------
Mandrel Cleaning Water.
Mandrel cleaning water now being discharged to holding tank and thence
to Preston Run tributary will be connected to the new sanitary-
sewer line.
Storm Water.
Storm water now being discharged from roof drains and grounds to
Preston Run tributary will continue the present route without change.
Although the streams listed above were not considered as candidates for
elimination in the grant application for WPRD 87-01-68, attempts to
return mixed waters from the holding tank to "chain" cleaning duty were
made, but proved unsuccessful because of severe foaming which resulted
when the alkaline waters from the holding tank mixed with the "chain"
cleaning water.
Preston Run Tributary.
When Plant #3 connects to the Defiance ^Municipal Sewage Treatment Plant
in early 1970, the only water entering Preston Run tributary from
Plant #3 will be storm water.
Effectiveness.
The closed system has demonstrated capability to carry out the ob-
jectives outlined in the grant application - namely to "eliminate
completely the discharge of waste water from Johns-Manvilie Plant #3
at Defiance, Ohio. The water in question is used for cleaning chain
conveyor belts in a fiber glass insulation plant and normally contains
caustic and phenols in both dissolved and parbiculate form. This water
is now discharged into Preston Run at an estimated rate of 30 to 50
gallons per minute. Preston Run flows into the Maumee River. The
proposed system will remove glass and phenol particles and permits reuse
of all process water other than lost by evaporation".
The project objective clearly states that the process waste to be
eliminated is the water "used for cleaning chain conveyor belts".
There is adequate evidence to show that the "chain" cleaning water
discharge has been reduced to zero, but the practical test of seeing
zero discharge is not possible until other discharges not included in
the project scope are diverted to the Defiance Treatment Plant via a
newly laid interceptor early in 1970. Reference is made to softener
backwash and rinse water, to caustic mandrel cleaning water, to boiler
blow-down water and to domestic waste from locker rooms and toilets.
When these waters are connected into the Defiance system there will
then be zero discharge over the weirs. The "paper" evidence that we now
have zero discharge of "chain" cleaning process water follows.
65
-------
Reduced Water Consumption.
Reference to Table 12 - Water Bills - City of Defiance - shows that
consumption in the six months ending November 1969, amounts to 807,000
cubic feet (6,052,500 gallons) compared to 1,871,100 cubic feet (lU,037,750
gallons) used in the last six months of 1968. In terms of average flow
rate, 1969 usage was 23.2 gpm compared to 5^.0 gpm in 1968. From meter
data obtained in 1968, "non-process" water had the following values:
TABLE #13
"NON-PROCESS" WATER
Softener Backwash,
Boiler Feed and Locker Room and
Cooling Tower Quality Control
August it.O gpm 7-6 gpm
September k.2 it.l
October it.9 it.6
November 9.3 5.it
December 29.k * 3.2
Total 22.U 2U.9
Average 5.6 + 5 -0 = 10.6 gpm
From the foregoing we can develop the following:
TABLE #lU
"CHAIN" CLEANING WATER DISCHARGED - FROM WATER SUPPLIED
1969 1968
6 months ending 6 months ending
November December
Total Plant Consumption - gpm 23.2 5U.O
Non-Process Water 10.6 (est.) 10.6 (metered 5 mos)
Process Water 12.6 it3.it
Overspray and Binder use
to evaporation lit.7 lit.7 (est.)
"Chain cleaning water avail-
able for discharge -2.1 28.7
By calculation there was no "chain" cleaning water available for dis-
charge in the six months ending November, 1969.
* This value not used.
66
-------
A further judgment as to "chain" cleaning water discharged may be made
by comparing Discharge Weir #1 and #2 flows for 1969 -vs- 1968. The
weirs were set up in August, 1968, hence data is available from
September, 1968.
TABLE #15
"CHAIN CLEANING WATER DISCHARGED - FROM WEIRS
1969 1968
ffl & #2 Weir #1 & #2 Weir '
September gpm 10.1 50.2
October " 8.3 28. U
November " .6 * 2^.3
Total 18. U 102.9
Average gpm 9.2 3^.3
"Non-Process" Water
(from Table #13) 10.6 10.6
"Chain" Cleaning Water - l.U :23.T
By calculation there was no "chain" cleaning water in the discharge
during the months examined above in 1969 as against 23.7 gpm in 1968.
Operating Costs.
Differences in operating costs are shown.in Table #2. .Each element of
cost difference can be observed by reference to the table. The elements
are discussed below.
Binder Solids.
Previous pilot plant experience on #5 Production Unit had indicated
that significant savings in binder usage would be effected with the
closed system. Savings developed from $1,^33 in the first month to a
maximum of $1*,782 in the sixth month. In August, all production units
used a new method of applying binder. Binder savings disappeared
completely in August, recovering slowly in September with increasing
gain for October and November. Apparently knowledge of th4 new method
of binder application is gaining and savings may continue to grow to
about the level attained in June. It is believed that the savings
obtained for the seven months prior to the binder application method
* November, 1969, data not used due to practice of not recording
all flows less than 1" crest.
67
-------
change can be properly attributed to the closed system. This amounted
to $21,002 for seven months operation = $3,000/inonth on the same basis
as for the six months base period prior to operation of the closed
system.
Water.
Water savings adjusted for production volume amounted to $5,696 for
eleven months, or $518 per month. An approximate check on this saving
can be obtained by comparing water bills before and after start of the
closed water system. Water bills for seven months in the latter half
of 1968 cost $9,^06 or $1,3UU per month. Water bills for eleven months
of 1969 totalled $8,2^3 - or $7^9 per month. Average monthly saving was
$595 computed on this basis.
A second method of checking water saved is to obtain the cost of the
water recirculated. Water leaving the clean water tank is metered at
#2 meter. Water entering the clean water tank is recirculated water
from the diatomite filters plus fresh water make-up through #5 meter.
Accordingly #2 meter - #5 meter = water recirculated. Using data from
the most recent quarter ending October 31, 1969, we find: (See Table
#2 meter - Average for 92 days - 67.6 gallons /minute
#5 meter - Average for 92 days - 15.2 gallons /minute
Water recirculated = #2 - #5 meter = 52. U gallons /minute
Check - Water Re circulation Components
"Chain" cleaning water - 5 nozzles @ 5 gpm =25.0 gpm (spot check)
Dust Collector water- metered( 1/17-2/30/69) - po -s "
(5 months 1968) ~ d*'5
Primary Filter shower - estimate = 3.0 "
Wash hoses - estimate = 2.0 "
Compactor drainage - estimate = 1.0 "
Unaccountable due to estimates
and/or meter error = 1.1
Total . ..... 52, k gpm
Water saved = water recirculated = 52. k gpm
^Savings = 52.^ gpm x lUUO minutes /day x 30 days x $.^6/1000 gals.= ^ QUO /month
1000
*Cost of water five month period 8/12 to 12/20/68 = $.^6/1000 gallons.
68
-------
TABLE #16
WATER USE SUMMARY
WPRD-87-01-68
(Average of Months 19, 20 & 21 - August, September & October 1969)
1. Flow Meter Data - 92 days.
Filtered Make-up Total
Water Plus Binder Boiler To clean City
Make--up Mix Make-up Water Tank Water
#2 Meter #3 Meter #h Meter #5 Meter #1 Meter
(After clean
water tank)
Gallons/
Minute
Total .
Average
#19
20
21
58.8
66.0
78.0
202 8
67.6
9.5
10.0
10.0
9.8
1.2
.97
1.2
1.1
15.2
15 '.9
h
15.2
27.3
22. U
2U.2
7? Q
2U.6
2. Water Consumption.
Total consumption of city water averaged 24.6 gallons per minute.
3. Water Savings .
Water re circulated = water saved
#2 Meter - #5 Meter = water saved
67.6 gpm - 15.2 gpm - 52.U gpm saved per minute
* 52.U x lUUO x 92 days x $.U6/1000 gals. A, ,Qn
iooo = $3'190
A third check on water saved may be made by comparing Discharge Flows
for September and October, 1968, with those for August, September and
October, 1969. Average flow from #1 and #2 Weirs in two months was
* Water cost of $.U6 per 1000 gallons based on four month period
August 12 to December 20, 1968.
69
-------
39.0 gpm. For three months of 1969, flow from #1 and #2 Weirs averaged
11.5 gpm. An approximate saving of 27-5 gpm is indicated.
Saving:
2T.3 gpm x IMP min./day x 30 days x.$.U6/1000 gals. _
1000
In review, we have monthly savings arrived at in different ways with
different values, yet all are indicating that a saving did occur and
that the magnitude ranged from $5l8 to $1,0^0, as follows:
Accounting method using standard costs - $518 (from Table #2)
Comparison of water bills - 595 (from Table #12)
Value of water recirculated
Comparison of water discharged to sewers -
Three methods of comparison agree quite closely, yet it is also true
that the value of water recirculated is a perfectly valid figure. One
has only to visualize a failure of filtering or other essential re-
circulating equipment to know that the water recirculated would have to
be replaced with city water at a cost of approximately $10^0 more
each month.
Caustic Cleaner.
The cost of caustic cleaning compound has been reduced since it is no
longer required for "chain" cleaning. Savings for twelve months totalled
$1,307 equal to $109/month.
Salt.
The use of salt for water softening increased over base period require-
ments for the first six months of 1969. Trial production runs for the
three week period, June l6th to July 7th, 1969 and from July 15th to
July 17th, established the fact that soft water was necessary to prevent
plugging of binder nozzles. Added information developed was that
softeners needed regeneration only once in two days rather than daily.
This reduced the backwash and rinse water quantities to half of the
prevailing quantity prior to the trial and also reduced the amount of
salt needed so that minor savings are being made here. Added salt
costs of $125 in the first six months were offset by $16 of savings in
the last five months ending in November. Net added cost for the
eleven months was $109.
70
-------
Diatomaceous Earth.
This element of cost is a definite requirement of the recirculating
equipment. It represents added cost of $2,95^ for the twelve month
period = $2^6 per month. Reduction in the filter-aid cost is possible-
"by limiting "on-streamV cycle life-to a safe allowable pressure drop
across the septa. "Pressure" control (as an alternate to "time" control)
will produce maximum diatomite life but random cycle lengths will
result, requiring regeneration attention at odd hours when maintenance
personnel may be scarce. The time cycle life of twelve hours was set
up to provide for day shift attention when maximum maintenance staff
is available. Now that a year;of experience has been attained, it is
possible that night shift personnel can recharge the filters, thereby
permitting maximum use of diatomite.
Anhydrous Ammonia.
Anhydrous Ammonia has been used for many years to stabilize binder
mixture so that resin precipitation is prevented from taking place. It
is well established that additional ammonia, but not scientifically
determined how much more annonia, is needed to stabilize the "chain".
cleaning water to prevent precipitation of resin solids which would,.ad-
versely affect diatomite filtration. Accordingly, ammonia is admitted
by manually controlled chemical feed pump to maintain a pH range of 8.5 -
9.5. This increased requirement cost $2,2^1 during the twelve month
operating period, equal to $187 per month. Use of a pH controller is
contemplated to determine if closer control is necessary. A lower pH
range would cut ammonia costs and improve environmental conditions. A
higher pH range will require ventilation control and additional funds to
purchase the added ammonia required.
Maintenance Labor.
The largest element of cost in the operation is the amount needed for
maintenance personnel to service all the equipment. Some part of this
increased labor is required to obtain data required for this report -
possibly an hour a day. Another source of improvement would be the
mechanization of handling of the solids taken from the primary filter
and from the scrap pump. The other work required, such as removing
the cake, cleaning the septa and re-charging the diatomite filters,
adjusting the primary filter media, unplugging scrap pump blockage,
logging the state of the outside treating tank and many snfall tasks
too numerous to mention here, are not apt to be profitable subjects for
cost reduction. During the twelve months evaluation period, $13,351 have
been expended for maintenance labor, or $1,110 per month. This is
equivalent to an eight hour day for one man every day of the month.
It is estimated that improvements and reduced data taking might lower
this amount about 2Q%.
71
-------
Fiberglass Cartridge Filter Tubes.
The expenditure results from replacing cartridges in the final or
emergency filter at weekly intervals. It is possible that longer life
might be obtained by a close study of the pressure drop across these
cartridges. The increased cost is $36 per month average for the twelve
month evaluation period.
Polypropylene Filter Cloth.
This cloth is used on the primary filters. A unique method of driving
the cloth by frictional contact and slipping against the underlying
moving support chain belt is believed to contribute to the rather short
life of the cloth. More cycle life may be available by tying the medium
solidly to the support conveyor to eliminate the sliding wear factor.
Increased cost for this material for twelve months has run to $1,291
or $10? per month.
Fungicide Treatment.
A suitable fungicide and companion dispersant for removal of the killed
fungus growths have been fed to the system since June 1969» after fungus
growths blocked certain small diameter pipe lines. Increased cost for
these chemicals amounts to $1,908 for eight months, or $239 per month.
Power Cost.
Recirculation requires added power to drive the pumps, screens and re-
lated equipment needed to re-use the water. Power consumption was not
metered but was spot checked on September 18, 1969 with clamp-on-ammeter
on the two feeders. Calculated loads amounted to H7.5 kw on the feeder
to starter group "A" and 11.7 kw on the feeder to starter groups "B" and
"CM. A check reading with clamp-on kilowatt meter showed 50 kw as against
47.5 calcubted, a variation of 5$. Total power consumption is thus found
to be ^7.5 + 11-7 or 59.2 kw. Since this power is incremental to the
power normally used, incremental billing costs are used to determine the
power cost as follows:
Demand - 59-2 kw
34 kw & $2.00 = $68
25.2 kw g $2.35 = 59
$127
Energy
59-2 kw x 720 hrs
= 1*2,700 est. kwh.
1*2,700 kwh g $.006U = $273
Monthly estimated power cost ..
This value has been used in Table
72
-------
Net Added Cost of Closed Water System.
Inspection of Table #2 shews a net reduction in operating cost of
$10,36U for the first seven months of the evaluation period, prior to
the time when a production method change temporarily reduced binder
savings. Extrapolating this saving to an annual basis would create a
net saving of about $17,000. The actual saving was $8,62U for twelve
months. It is noteworthy that a recirculating system has not only
fulfilled its assignment of eliminating process waste discharge, but has
managed to do it at a saving in operating costs.
Capital Costs.
Table #17 compares actual expenditures with the amounts estimated in
the grant application. In every category expenditure exceeded estimate.
Equipment and Materials.
This item represents the cost of equipment installed in place. When
Engineering costs are added the total capital cost of the project is
obtained - namely, $183,700. In general, equipment prices were in line
with estimates, but bids for installation were higher than anticipated.
Engineering in the application amounted to 9.2.% of Equipment and
Materials cost. For this type of project 20% would be more realistic,
considering the fact that existing machinery had to be re-designed,
and that engineering was needed on the preliminary and post-construction
studies. Capital costs of $183,700 exceeded the estimated $150,038
by $33,662 - or 22%.
Technical Studies and Reports.
The requirements for sampling and laboratory analysis were not
adequately recognized until after project approval and later dis-
cussion with the Project Officer. It is believed that the requirements
are not excessive to protect the Federal investment. Nevertheless,
the $1,557 estimated cost for studies was exceeded by $1,58H or ±01%.
Total Project Cost.
Final figures now show that the estimated total grant application of
$l6U,700 was exceeded by some 31$ to a total expenditure of $215,633.
Reference to Figure #8 will provide an idea of the cost status of the
project at any time in the course of the project.
Financial Aspects.
Pollution control projects are not noteworthy for their financial de-
sirability. All concerned are usually happy if the project accomplishes
its purpose, whatever the cost. Even so, there are numerous opportunities
for savings to develop, particularly when re-use of material, liquid,
gas or solid, is involved.
73
-------
CAPITAL COSTS
WPRD 87-01-68
A. Funds Required for Project
1. Construction
a. Contract No. 1 - Installation
b. Later Contracts
c . Equipment and Materials
Sub-total
2. Technical Services
a. Preliminary Studies and Reports
b. Engineering Plans & Specifications
c. Supervision of Construction
d. Post-construction Studies and
Reports
Sub-total
3. Operation & Maintenance Activities
k. Legal and Fiscal
5. Administrative
6. Contingency
7 . Other
8. Site
9. Total
* Amounts expended through January 15, 1970
Grant Total*
Application Expended
$ 29,2l43
Incl.
108,295 Incl.
137,538 $150,^55
-
12,500
Incl.
1,557
998
33,2*15
Incl.
3,131
1M57 37.37U
9,560 2U,l82
3,5^5
$16U,700 $215,633
TABLE 17 - CAPITAL COSTS
-------
QO
TO
I I I A I I I -I I
-------
This project, fortunately, has elements of material saving, as discussed
in several places. The net savings after deducting operating cost
differences present an interesting return on the investment, as noted
below:
Investment:
Equipment $150,1*55
Engineering 33.2^5
$183,700
Net savings (before taxes) $10,36U first seven months - $17,^00 annually.
Return on initial investment = $17,400 n ,.«
183,700 = 9'5/°
Unexpected Problems.
Three problems developed which required prompt solution to avoid
eventual interruption to service.
Septa Failure.
Early operation of the diatomite filters created dirty septa which
became progressively more difficult to clean as time went on. The
filters were fitted originally with septa of dacron material on an ex-
perimental basis . After one month of service, the vendor replaced the
dacron septa with stainless steel septa on February 13th in "B" filter
and February 21st in "A" filter. Three weeks later, on March 6th,
it was necessary to take "B" filter out of service due to leaking
diatomite and bulged septa believed due to excessive differential
pressure. New stainless steel septa were replaced March 11, 1969.
The failed tubes were coated with a thin brown coating easily removed
with high pressure water (when not in filter).
Various methods were tried to clean the tubes, the basic routine being
a hosing operation from below the tubes using 50 psi filtered water
after blow-down and occasionally 200 psi filtered.water. On a few
occasions a caustic cleaning solution was charged into the filter shell
and kept at about 150 deg. F with live steam for about eight hours.
Noticeable cleaning was effected with caustic baths, but the time element
did not warrant this as a routine cl'eaning method. The result of resin
buildup on the septa tubes was inability to achieve twelve >lour "on-
stream" cycle life.
When the differential pressure - "delta p" - reached 18 psi. the pressure
switch in the control system would take the filter off stream._ On one
occasion in the second month of operation and the third week of stain-
less steel septa service, the "delta p"- exceeded safe values before the
standby filter could be put "on-stream", resulting in failure to two
thirds of .the septa near the tube sheet. Some filter outage occurred
76
-------
until the tubes were replaced. To improve this condition, the programmed
"re-precoat" cycling which was operating at 1*5 minute intervals was
adjusted so that no supplementary precoat phases occurred during the
twelve hour "on-stream" cycle. A change in the diatomite feed procedure
accompanied the change in precoat cycles. Previously the full 75# charge
was placed in the removable pot at the bottom of the filter shell from
which it was precoated to the septa, then served as filter-aid for 1*5
minutes, was next taken off stream and "bumped" until precoat and dirt
were deposited in the pot, then re-precoated (including dirt) and
returned to "on-stream" filtering duty for another 1*5 minute cycle.
The revised procedure calls for 25# of initial precoat in the pot, the_
remaining 50# to be "body fed" over the twelve hour "on-stream" cycle.
"Body-feed" is accomplished by means of a dry feeder which meters filter-
aid into a vortex mixing pot and by venturi action discharges the mix
into the dirty water tank from which it builds up gradually on'the septa.
The reasoning behind this change was to avoid exposure of bare septa
surface to the resin bearing water and suspended resin in the re-
precoating phases and so reduce the possibility of resin "plating" out
on the septa. "Body Feed" was adopted on April 17th and has been
effective in maintaining twelve hour "on-stream" cycles since that time.
It is noted at the same time that there have been numerous occasions
since "body feed" was introduced when short cycling has occurred. In
most such cases recovery to normal cycles occurred after re-charge and
the cause of the short cycle was attributed to a shock peak load. A
log of "on-stream" cycle life has been maintained since October,8th.
Table #1 shows the "on-stream" hours for each filter each day. It
can be seen that for the month of November a 9^% duty was achieved.
One additional step has .been taken to prevent excessive "delta p" from
occurring. The pressure switch which formerly took the filter.off
stream in the event of excess pressure, removed'the excess pressure only
after the stand-by filter was ready to come on-stream. If the stand-by
filter was not in a "ready" state to come "on-stream", the excess pressure
would not be relieved,until the change was made which immediately takes
the filter off-stream and transfers it to "blow-down" phase when the
pressure switch sees high pressure. It is believed that these steps
make the septa less vulnerable to failure.
Foaming.
Several attempts to return water from the out-of-doors treatment tank
back to process resulted in foam, even though aeration spray action
in the outside tank did not generate foam. One explanation is that
the high pH water in the outside tank combined with ammonia in the
circulating system to form an amine, which is a type of foaming agent
frequently used in soap manufacture.
77
-------
Attempts to reduce foam "by use of a silicone de-foaming agent reduced
foam but also served to "blind" up the dia'tomaceous earth filters, Foam
generation resulted in faulty float level centre?! in the dirty water
tank, which, in turn, due to low suction head on the supply pumps to
the Diatomite filters, caused air ,to be passed through the filters with
increased pressure drop across the septa. These pressure drops returned
to normal values as soon as the liquid level in the dirty water tank
was restored. Added difficulty caused by the foam was the problem of
operation when the floor in the vater room was covered with V of foam.
Plans were made to reduce the flow of water to the outside treatment
tank to the point where it could be evaporated by the aerator. Action
taken to reduce softener backwash water discharge to the open tank was
a thirty day trial production operation with unsoftened water. Results
were not conclusive enough to warrant operation with unsoftened water.
An incidental benefit was the discovery that the softeners need be re-
generated once every two days, rather than daily, thereby reducing
softener backwash by half. Plans to heat the caustic mandrel wash tank
with gas, rather than steam, and so reduce the tank overflow, were con-
sidered, but held in abeyance pending the extension of an interceptor
from the City of Defiance treatment plant to Plant #3. The interceptor
was laid in November but cannot be connected to until early 1970 when
the city treatment plant can accept the plant domestic and alkaline waste.
Another approach considered was to reduce the ammonia concentration in
the circulating water. A probable effect of such an approach would be
some de-stabilization of the resinous "chain" cleaning water and con-
sequent rapid "blinding" of the diatomite filters. Foaming was not
conquered during this project. Its occurrence and bad effects resulted
from a desire to eliminate all Plant #3 discharge possible, which,
however was incidental to the main purpose of the project - elimination
of "chain" cleaning discharge.
Fungus.
During the week prior to April l8th, a gray rubber-like n^n-sticky slime
became evident in open ends of piping and on April l8th a one-half inch
pipe line which supplied the cleaning shower on the West Primary filter
became inoperative because of complete plugging with slime. This
incident caused a decision to stop recirculation until more knowledge
was available as to the extent of slime deposits in lines and a proper
course as to the removal. Recirculation was stopped on April 18, 1969.
Water treatment specialists were consulted on April 19th and a tentative
program established for treatment beginning April 21st. Treatment for
the ensuing week consisted in recirculating water treated with a bis-
thincyanate for two days through the "chain" cleaning portion of the
circuit, while supplying binder and overspray requirements from city
water; and a similar treatment operation of twenty-six hours using
sodium hypochlorite. Neither of these treatments was effective in
removing the slime.
78
-------
Accordingly, a full scale-Investigation was-mounted by consultants.
The microbiological growth .was identified as a fungus. Normal water-
circulation was resumed on April 30th, with expectation that fungus
would re-appear. Fungus did re-appear and was sufficiently developed
by May 22nd to warrant treatment. A fungicide was applied on May-29th
which was compatible with binder ingredients so that no adverse effect
would accrue to the fiber glass product. A dispersant was simultaneously
fed to distribute the fungus as it dies and falls away from pipe and
tank walls. Monthly reports from consultants indicate that fungus growth
is being contained. Treatment has been reduced but is maintained on a
continuous basis. As further experience is gained, other approaches
such as intermittent shock treatment or treatment of make-up only will
be taken if present methods should fail to be effective.
Discharge to Preston Run.
A comparison is made of the pollution elements discharged before and
after closed system operation.
In Table #k - Water Quality Discharge 1968, the discharge to the stream
is reported for the period prior to system operation.
TABLE #5 - WATER QUALITY DISCHARGE 1968 - POUNDS/DAY
1968 Location
12/5
12/20
12/26
#1 Weir
tt
Suspended Total Dissolved
Phenol Solids Solids Solids Flow
P.P.M. P.P.M. P.P.M. P.P.M. GPM
3.360
U.720
Total #1 Weir 12.320
Average #1 Weir 7-7-8.9 ^.11
Lbs/day 1.17
1117
562
101U
12/20 #2 Weir 7.6 .069 7
Lbs/day " .00083 .08
193
186
2.2
1.0
Total Ibs/day
#1 & #2 Weirs
1.17083 22.08
236.2
79
-------
In Table #6 the quality of water discharged after closed system operation
was achieved, is reported. In Table #7, the quality is shown as pounds
per day.
TABLE #7 - WATER QUALITY DISCHARGE 1969 - POUNDS/DAY
Location
7/3 #1 Weir
7/10 #1 Weir
7/17 #1 Weir
Total #1 Weir .
Average #1 Weir
Lbs/day #1 Weir
7.2
7-9
7.0
7-0-7.9
Suspended Total Dissolved
Phenol Solids Solids Solids Flow
P.P.M. P.P.M. P.P.M. P.P.M. GPM
38
U8
2U
110
37
2.1
1033
1026
627
995
978
603
2576
857
U8.5
7/3 #2 Weir 7-1 .17 1
7/10 #2 Weir 8.8 .03 39
7/17 #2 Weir 8.3 .01 11
Total #2 Weir ... .21 51
Average #2 Weir 7.1-8.8 .07 17
Lbs/day #2 Weir .007 1.8
1135
>+95
363
Total Ibs/day #1 and #2 Weir .21*6 3.9
119.5
In summary, December 1968 discharges averaged 1.17083 Ibs. phenol per
day, compared to .2U6 Ibs/day in July 1969. Similarly, 1968 suspended
solids discharged was 22.08 Ibs/day -vs- 3.9 Ibs/day in 1969. 1968
dissolved solids amounted to 236.2 Ibs/day, while 1969 dissolved solids
totalled 119-5 Ibs/day. pH ranges were comparable for both periods.
On every count, therefore, pollutants discharged were greatly reduced
after the closed water system went into service. Phenol Discharged
in July 1969 amounted to one-fifth of December 1968 discharge.
Suspended solids were also only one-sixth of the December 1968 dis-
charge, while dissolved solids were cut in half.
80
-------
TABLE 6
WATER QUALITY - DISCHARGE - 1969
WPRD 87-01-68
Location
Sample taken 7/3/69
Sample
Weir #1 #3
Weir #2 4
Outside tank 1
Downstream of Discharge 2
Sample taken 7/10/69
Weir #1 #3
Weir #2 U
Outside tank 1
Downstream of Discharge 2
Sample taken 7/17/69
Weir #1 #3
Weir #2 4
Outside tank 1
Downstream of Discharge 2
Sample taken 7/24/69
Weir #1 #3
Weir #2 I*
Outside tank 1
Downstream of Discharge 2
Suspended Total
Phenol
PPM
2.3 -
.17
11.2
.10
10.4
.03
22.3
1.6
.02
.01
10. 4
.01
.03
.02
1*8.7
.01
£2.
7.2
7.1
12.2
8.0
7.9
8.8
11.9
9-2
7.0
8.3
11.6
7.6
7.9
7.5
10.0
7-9
Solids
PPM
38
1
44
0
48
39
167
10
24
11
110
16
12
38
55
110
Solids
PPM
^
1033
1135
6912
768
1026
1*95
11,391
707
627
363
5440
491
725
1*50
6659
1*93
Flow
GPM
2.2
8.9
6.0
12.1*
6.0
6.0
_ #
_ #
* Flow measurements not taken this date
81
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VIII
RECOMMENDATIONS
Future Studies.
Certain aspects of the recirculating operation could-be better understood
than present knowledge permits. For this reason additional studies are.
suggested:
pH range.
Ammonia is used to stabilize the solubility of phenolic resin in the
water solution. More detailed knowledge is needed to establish if
higher ammonia concentrations increase stability of the resin and thereby
reduce the phenolic resin suspended solids load in the diatomite filters.
Correlation between dissolved phenolic resin concentration and pH values
could determine optimum values of pH for best filtering conditions.
Laboratory studies supplemented by field tests on filters should be able
to pin point the desired control point.
Chain Cleaning Pressures .
Studies are desirable to determine the ideal nozzle shape and nozzle
pressure for maximum chain cleaning effect. The combination now in
service works well, but lower pressures and other nozzles might produce
equal cleaning at a lower investment cost.
Future Operational Changes.
Experience obtained at Defiance 003 has permitted Johns-Man vi lie to .
install a comparable re-circulating system at its Winder, Georgia Fiber-
glass Plant, which went into service in September of 1969. Among the
changes made are:
Scrap Pump Deleted.
This specially designed piece of dewatering equipment was not considered
essential to the operation. A scrap pump was not included at Winder, but
it must be admitted that the fiber which it would have removed if in-
stalled, has to be removed on the primary screens, thereby increasing
the duty on them. A further feature of the scrap pump was its ability
to remove large clumps of fiber and thus avoid possible blockage of.
pump suctions. It was established at Defiance 003 that such clumps
could be cut up with a water jet at the pump inlet. The trench water
83
-------
centrifugal pumps at Winder are operating satisfactorily without benefit
of scrap pump protection.
Primary Filter Screens.
The modified low bed filters used at Defiance 003 were adequate for the
relatively mild loading placed upon them. However, in a large volume
operation such as at Winder, reliability and rugged construction caused
selection of flat vibrating screens to be made. In this instance the
company has had several years of experience screening fiberglass from
waste water, using flat vibrating screens. Again it is pointed out
that the removal of a scalping stage (such as the scrap pump) places
extra duty on the primary screens. Allowance for adequate sizing must
be made here.
Winder, Georgia Operation.
The water recirculating system at Winder has been a successful extra-
polation of the Defiance 003 demonstration project. Some diatomite
septa failures have occurred, the flat screens do not handle as much
water as intended with resulting heavier load to the diatomite filters.
In general, however, the system is shaking down satisfactorily and
promises to be successful. Conservation of water and resin are being
achieved and discharge to stream does not occur.
Richmond, Indiana.
Expansion of fiberglass production at our Richmond, Indiana plant is
now taking place. A recirculating system similar to the Defiance 003
system was installed in 1969. Details are somewhat different at this
plant, which uses direct melt glass supply, as compared to melting pots
at Defiance 003. The principles and major pieces of equipment are the
same, however. The use of a different grade of resin and much higher
peak loadings are creating diatomite filter problems which may require
a greater degree of primary filtration.
General.
Pre-construct!on Study.
It is of utmost importance that the characteristics of the phenolic
resinous water solution be accurately known, particularly for peak
conditions, such as wash down periods, before specifying equipment for
screening and filtration. Several stages of scalping and primary
filtration may be required before the suspended solids are at a level
for economical and practical diatomite filtration. Trial filtration
tests are recommended, and such trials should be realistic, duplicating
expected peak operating conditions as closely as possible. Such tests
-------
are not generally easily arranged and expedient trials are sometimes
accepted which may turn out to be not representative of the actual
conditions to be met. For this reason extra care is urged in obtaining
basic data.
Post Construction Study.
Regular sampling, analysis and maintenance procedures are important
to the economical operation of a recycling system if problems are to be
corrected before they become large.
Potential Application To Other Plants and Other Industries.
Elimination of Waste Water Discharge.
Waste water from a fiber glass operation contains fibrous glass
particulates, dissolved phenols, and partially polymerized phenol
particles. Phenols are highly objectionable in potable streams because
of taste and odor. The project has demonstrated zero discharge
capability.
Reduction of Water Consumed.
Under our present system of chain cleaning, there is considerable water
loss. With a closed system, the only water loss will be that evaporated
during the product drying cycle. City water purchases have been sub-
stantially reduced.
Reduction of Phenolic Resin Usage.
The project has demonstrated that re-cycling of the chain cleaning water
reduces the usage of phenolic resin sufficiently to provide significant
savings. Similar systems will be proposed for installation at all Johns-
Manville plants where a phenolic resin discharge occurs. Johns-Manville
has a totp,l of nine (9) such plants.
According to available information, our principal competitors in the
fiber glass insulation business use a water soluble phenolic resin as a
tinder and have similar waste disposal problems. We estimate that there
are approximately twenty-five (25) such fiber glass insulation plants.
In addition, the same type of binder system is also used in the
Manufacture of mineral wool insulations. We estimate thav there are
approximately twenty (20) such plants, although many of these are
smaller in capacity.
It is expected that a closed system which would conserve soluble phenolic
^esins and filter out phenolic particles from the effluent would be
applicable in most industries which use either soluble phenolic binders
°r powdered phenolic binders as a saturant or impregnant. Such binders
are often used in paper manufacture to produce strong water resistant
Papers. They are also used in the manufacture of electrical sheets,
-------
boards, and cut or molded parts. We do not have, however, direct in-
formation as to the methods used by these other industries in handling
their phenolic wastes.
In summary, it is our opinion that the application of the proposed
techniques in the fiber glass industry alone would have broad usefulness,
If such techniques are also extended to the operations of other in-
sulation manufacturers and of sheet and board manufacturers using the
same type of binder, we would expect the process proposed to have still
broader application.
86
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Appendix A
METER LOCATIONS
Before Recirculation - 1968
#1 - Main Meter - City of Defiance
#2 - Overspray, Locker Rooms, Offices, Quality Control and Dust
Collector, Oven Fire Line
#3 - Binder Mix
#U - Overspray and Chain Cleaning
#5 - Overspray and Chain Cleaning
#6 - Dust Collector
#8 - Mandrel Cleaning
87
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DAILY METER READING - WPRD 87-01-68
i
CO
CD
M
&
@
00
H
ro
t
^o
U)
^
CF\
GO
Meter
#2
x 100
gals.
003051+
003769
00l*5l+0
005301
006031
006701
0071*76
008180
008973
00971*0
010U81+
011216
011937
012631
013393
011+079
011+710
01531+7
016012
01675*1
017 U88
018852
No Data
Meter
#8
x 10
gals.
000002
000002
000003
000003
oooooU
oooooi*
000005
000006
000008
000010
000011
000052
000061
000061
000120
000175
000215
000222
00021+2
000280
000282
000326
Meter
#3
x 100
gals.
000658
000818
000985
001167
00131+2
001522
001684
00181*7
002017
0021S1
00231+5
002508
002672
002830
003001
003167
003328
0031+87
003657
003832
OOi+010
001*351
Meter
#4
x 10
gals.
005^30
006590
007802
009005
010127
011285
012629
013917
015316
0166U7
017919
019139
0201+08
021636
022925
023988
021*972
026025
027087
028388
029732
031883
Meter
#5
x 100
gals.
000739
000886
00101*6
001188
001313
0011*07
001537
001665
00181*3
001989
002107
002230
002365
0021*78
0026lU
002715
00279**
002880
002991
003156
003301
003581
Meter
#6
x 10
gals.
013570
016923
0201*72
023959
027379
0309^7
031*708
038212
01*1591
01*5066
01*8626
052139
055852
059752
06378U
067578
071521*
075296
078889
082559
08614-01
093376
Meter
#1
x 100
CF
111*091
111+21U
111+31*8
llUl+81
111+613
111*736
111*869
111*996
115128
115251*
115378
115506
115629
115751
115883
116003
116117
116229
11631+7
1161*82
116619
116865
Weir Weir Date
Box Box 1968
#1 #2
8/12
8/13
8/11*
8/15
8/16
8/17
8/18
8/19
8/20
8/21
8/22
8/23
8/2**
8/25
8/26
8/27
8/28
8/29
3V 1" 8/30
3" 1" 8/31
3V 1-3/1+ 9-1
3" 1-3/1* 9-2
9-3
Weir Weir
#1 #2
GPM GPM
Remarks
Filled Mandrel
Cleaning tank
Filled mandrel
Cleaning tank
Changed water
hose
lH.8 2.2
3l+.2 2.2
50.3 8.9
3l+.2 8.9
a
H-
X
-------
DAILY METER READINGS - WPRD 87-01-68
oo
SI
w
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I
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H
tr1
S
H3
»
w
S
M
Q
VO
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1
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ro
OO
OO
Meter
#2
x 100
gals.
019620
020393
021119
021819
022521
023214
023893
024638
025387
026145
026920
027671
028421
029165
029911
030657
031393
032149
032927
033706
034492
035199
035852
036583
037210
Meter
#8
x 10
gals.
000366
000400
000460
000479
000482
000511
000578
000598
000612
000635
000655
000687
000693
000728
000754
000785
001012
001035
001056
001127
001146
001210
001228
001239
001240
Meter
#3
x 100
gals.
004524
004686
004856
005034
005212
005393
005562
005736
005897
006074
006258
006435
006610
006776
006945
007112
007275
007438
007594
007761
007920
008100
008251
008427
008607
Meter
#4
x 10
gals.
033113
034302
035418
036625
037888
039054
040185
O4l468
042735
043954
045367
046638
047904
049219
050451
051770
052972
054184
055434
056637
057858
058967
059960
061155
062193
Meter
#5
x 100
gals.
003734
003890
004036
004156
004285
004387
004496
004640
004825
005006
005200
005389
005532
005692
005867
006035
006136
006245
006394
006538
006710
006874
007014
007188
007283
Meter
#6
x 10
gals.
097113
100902
104608
108513
112512
116350
119979
123865
127547
131171
134872
138705
142393
145858
149560
153317
157247
160955
164487
168044
171593
175200
178758
.182102
185654
Main
Meter
#1
x 100
CF
116999
117136
117271
117401
117534
117665
117785
117916
118043
118182
118318
118452
118582
118719
118840
118968
119100
119229
119364
119498
119631
H9756
119870
119997
120112
Weir
Box
#1
3V
3V
3V
3V
3V
3-3/4
3V
3V
3V
3V
3V
3V
3"
3V
3"
3-3/4
3-3/4
3"
3V
3"
3"
3"
Weir Date
Box 1968
#2
1-3 /U 9-4
1-3/4 9-5
IV 9-6
1" 9-7
1" 9-8
IV 9-9
1" 9-10
IV 9-11
1_3/U 9-12
1-3/4 9-13
9-14
IV 9-15
1-3/U 9-16
1" 9-17
3" 9-18
V 9-19
1%" 9-20
9-21
9-22
IV 9-23
l3g" 9_24
1" 9-25
3/8 9-26
IV 9-27
V 9-28
Weir
#1
GPM
41.8
41.8
41.8
41.8
4i.8
59.7
50.3
50.3
50.3
41.8
41.8
41.8
34.2
41.8
34.2
59.7
59.7
34.2
50.3
34.2
34.2
34.2
Weir
#2
GPM
8-9
8.9
6.1
2.2
2.2
6.1
2.2
6.1
8.9
8.9
3.8
8.9
2.2
34.2
6.1
6.1
6.1
2.2
6.1
Remarks
Raining
(D
B
-------
DAILY METER READINGS - WPRD 87-01-68
vo
o
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M
1
H
O
M
^
a
§
£i
»
s
M
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CO
U5
ro
^0
i
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ru
\
ON
00
Meter
#2
x 100
gals.
03791+0
038686
0391+19
01*0108
01*077 k
oUll*38
Ol*208o
01+2639
01*3315
Ol*388l
01+1+1+81+
01*5096
01+5670
01+6229
Ol+67l*3
01+7287
Ql+7907
01+8560
01+9217
01+987!+
0501+91*
051131*
051766
0521*03
05301*1*
053673
051+265
051*926
Meter
#8
x 10
gals.
00121*1*
001299
001317
00131*0
001359
001379
001395
0011+16
OOll+l+l*
0011*65
0011*99
001526
001535
00151+6
001573
001595
00161+1
001659
001679
001707
001716
00171+7
001817
001851*
001881
001909
002021
002059
Meter
#3
x 100
gals.
008792
008965
009138
009315
0091+85
009670
009862
010052
010227
010399
010599
010769
010928
011100
011280
011U61
011631*
011813
011995
012181+
012370
012551
012730
012688
013028
013185
01331+1
013533
Meter
#1+
x 10
gals.
0631*52
061+701+
065896
066985
067991+
069091
070091*
071157
072087
072957
073781
071+717
075735
076652
077586
0781+88
0791+1+2
080523
08l5l*9
082683
083689
081*771+
08581+1
086817
087819
08881+0
089721
09081+1+
Meter
#5
x 100
gals.
0071*1*2
007639
007816
007955
008108
008267
0081+23
008592
008736
008832
00891+3
009081+
00921+3
009357
0091*78
009589
009700
009828
009956
010098
010231*
010385
010562
010720
010919
011102
011256
0111+16
Meter
#6
x 10
gals.
189522
192976
196286
199679
202832
206231
209656
212892
216835
220261+
223601
226852
2291*1*6
232556
235056
237371
21*0518
21+3581
21*6751+
21+9861+
253196
256332
259333
262578
265628
268532
271210
271+180
Main
Meter
#1
x 100
CF
12021+5
120379
120506
120631
12071+8
120870
120992
121099
121226
121331
1211+1*8
121559
121663
121769
121870
121975
122089
122209
122332
1221*53
122568
122691
122813
122928
12301+1
123159
123273
123390
Weir
Box
#1
3"
3"
3V
3"
3V
3"
3"
3"
IV
2V
2"
3"
2V'
2k"
1-3/1+
IV
2V
2V
3"
2V
2V
2V
2V
2V
2V
2V
Weir
Box
#2
3/1+"
IV
IV
IV
IV
1"
y
IV
IV
IV1
1"
0
V
i"
i"
3/1*"
IV
V
V
0
0
V
V
V
V'
0
Date
1968
9-29
9-30
10-1
10-2
10-3
10-1+
10-5
10-6
10-7
10-8
10-9
10-10
10-11
10-12
10-13
10-11+
10-15
10-16
10-17
10-18
10-19
10-20
10-21
10-22
10-23
10-21+
10-25
10-26
Weir
#1
GPM
3l*. 2
3l+. 2
50.3
3l*. 2
50.3
31+.2
3l+. 2
3l+. 2
6.1
21.7
12.1+
3l*. 2
16.7
21.7
8.9
3.8
21.7
21.7
31+.2
21.7
21.7
21.7
21.7
21.7
21.7
21.7
Weir
#2
GPM
6.1
6.1
6.1
6.1
2.2
6.1
6.1
3.8
2.2
2.2
2.2
6.1
Remarks
Sewer Trouble
Sewer Trouble
Sewer Trouble
X
>
-------
DAILY METER READINGS - WPRD 87-01-68
g
p
£
1
jg
M
f
1
a
Si
Hj
g
M
m
o
ro
-a
i
H
H
ro
M
a\
CD
Meter
#2
x 100
gals.
055550
056163
056759
057369
05791*1
058550
05916U
059808
O6ol*55
061031
061691
062300
062891
0631*61*
061*073
061*722
065323
065863
0661*61*
067081
067581*
068092
068589
06901*5
069518
06991*6
Meter
#8
x 10
gals.
002076
002089
002120
002152
002178
002192
00220U
002205
002230
002260
002290
002320
002359
002373
002398
0021*11
002U38
0021*58
002502
00251*3
002576
002602
002621
002735
002766
002811
Meter
#3
x 100
gals.
013709
013887
01U065
OlU2l*2
011*1*05
011*596
011*781
011*966
015l!*0
015301*
0151*88
015652
015828
015999
016171
01631*2
0161*95
01661*6
016810
016983
017161
0173U1
0171*95
017633
017770
017906
Meter
#U
x 10
gals.
091936
092983
093929
091*970
095887
096765
09771*5
098763
099752
100531*
1011*75
102288
103171*
101*035
101*930
105821
106520
107103
10771*6
108378
108970
109567
110120
110516
110970
111301
Meter
#5
x 100
gals.
011561
011700
011838
011971
012061*
012153
01226U
012U35
012615
012731
012922
013093
013261
013390
0135^2
013716
013888
011*002
011*138
011*261
011*368
OlUl*70
011*581*
011*686
011*795
011*868
Meter
#6
x 10
gals.
277161
280090
282810
285592
2881*11*
291321
29l*2l*7
297272
300088
30291*0
305718
308508
31111*8
313936
316955
32001*5
322875
32571*5
328650
331627
331*732
33791*5
31*0939
31*3762
31*6636
31*9522
Main
Meter
#1
x 100
CF
123516
123636
123756
123870
123975
121*095
121208
121*328
121*1*50
121*557
121*709
121*819
121*93^
125039
125151
125271
125381
1251*83
125591*
125710
125827
12591*2
126053
126158
126262
126361
Weir
Box
#1
3"
3"
2V
2V
2V
2V'
2V
2V
3"
3V
2V
2V
2-3/1*
2V
2V
2V1
2V
2V'
2V
2-3/1*
2-3/1*
2V1
2%"
2"
2V
2V1
Weir
Box
#2
0
V
0
3A"
v
3/V
0
0
iV
iV
V
i"
"V1
V
V
0
0
V
V
i"
3A
0
V
0
V
Date
1968
10-27
10-28
10-29
10-30
10-31
11-1
11-2
11-3
11-1*
11-5
11-6
11-7
11-8
11-9
11-10
11-11
11-12
11-13
11-11*
11-15
11-16
11-17
11-18
11-19
11-20
11-21
Weir
#1
GPM
31*. 2
31*. 2
21.7
21.7
21.7
21.7
21.7
21.7
31*. 2
1*1.8
21.7
21.7
27.5
21.7
21.7
21.7
21.7
21.7
21.7
27.5
27-5
21.7
21.7
12.1*
21.7
21.7
Weir
#2
GPM
0
0
0
0
0
0
0
0
2.2
2.2
0
1.2
0
0
0
0
0
0
0
2.2
0
0
0
0
0
0
Remarks
Raining
Raining
2 bags salt
Raining
100 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
-------
DAILY METER READINGS - WPRD 87-01-68
^
w
£
1
I-1
e
H
5
g
H
§]
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§
M
a
o
CO
H
H
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ro
i
H
ro
H
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ON
o>
Meter
#2
x 100
gals.
070308
070659
071012
071365
071709
072062
072386
072770
07311*9
073517
073868
071*192
07l*5H
071+861
075211+
075563
075898
07621*1
076565
076932
077281
077623
077968
078313
07861+1;
Meter
#8
x 10
gals.
002829
00281+7
002877
002971+
003005
003021
00301*3
003055
003066
003091
003107
003136
003166
003188
003288
003301+
003312
003358
003398
0031*55
0031+95
003506
003516
003519
003565
Meter
#3
x 100
gals.
018036
018187
018319
0181+66
018602
018738
018876
019018
019160
019301+
0191*1*6
019593
01971*8
019899
02001+7
020201+
020358
0201+86
020605
090735
020876
021015
021151*
021301
0211*1+8
Meter
#1*
x 10
gals.
1111*91
111618
111726
111857
112003
112158
112282
1121+22
112559
112675
112768
112779
112791
112951
113051*
113065
113072
113088
113119
113136
113161
113218
113239
113267
113281
Meter
#5
x 100
gals.
011*875
011*879
011+890
011*89!+
011+900
011*906
011+910
011*916
011*921
011+928
011*930
011*933
011*933
011*960
011+991
011*995
011*993
011+991+
011+998
015000
015005
015019
015023
015028
015029
Meter
#6
x 10
gals .
352328
355323
3581+31
361352
36811+U
367165
37001*7
373329
376697
379981
383103
385980
388808
391633
391^31
397H55
1*00383
1*03322
1*0601+1+
1+0911*9
1*1211+3
1*15013
1*18096
1+21355
1+21*358
Main
Meter
#1
x 100
CF
1261+70
126587
126700
126817
126927
12701*1*
127155
127273
127391
127511
127628
127852
127871
127993
128116
12821+2
128370
1281+90
128600
128722
128871
129001
12913!+
129271
1291+05
Weir
Box
#1
2V'
2V'
2V'
2V1
2V'
2V'
3
3"
2V'
2-3/1*
2V'
2V'
2V'
2V'
2-3/1*
2V'
2V'
2V'
2V'
2V'
3"
2V'
3"
Weir
Box
#2
V
1"
3/H
V
V
V
0
0
V
V
0
0
0
0
0
0
0
0
0
0
0
Date
1968
11-22
11-23
11-21*
11-25
11-26
11-27
11-28
11-29
11-30
12-1
12-2
12-3
12-1*
12-5
12-6
12-7
12-8
12-9
12-10
12-11
12-12
12-13
12-11*
12-15
12-16
Weir Weir
#1 #2
GPM GPM
21.7 0
21.7
21.7
21.7 2.2
21.7
21.7
3l+. 2
31*. 2
21.7
27.6
21.7
21.7
21.7
21.7
27.6
21.7
21.7
21.7
21.7
21.7
31*. 2
21.7
3l+. 2
Remarks
200 Ib. salt
300 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
Raining
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
Plugged sewer
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
Plugged sewer
200 Ib. salt
-------
DAILY METER READINGS - WPRD 87-01-68
vo
U)
s
to
H- 1
M
1
H
^
H
K
g
H
»
ft)
g
H
£3
H
ro
H
1
H
ro
Meter
#2
x 100
gals.
078917
079233
079575
079923
080251
080287
080937
081271
081600
08191*3
082308
082697
083071
0831*35
083828
Meter
#8
x 10
gals.
003578
003509
003598
003602
003609
003609
003670
003661
003682
003675
003721
003730
003730
003773
003791
Meter
#3
x 100
gals.
021593
021727
021871
022019
022160
022306
0221*1*0
022588
022736
022877
023028
033170
023312
0231*1*5
023592
Meter
#U
x 10
gals.
113289
113325
113355
1131*07
1131*31*
1131*57
1131*98
113526
11351*1
113571*
113591
113610
113627
11361*2
113656
Meter
#5
x 100
gals.
015030
015038
01501*1
015056
015061
015063
015072
015075
015077
015085
015087
015081
015091*
015097
015099
Meter
#6
x 10
gals.
1*26790
1*2951*8
1*32511
1*351*75
1*381*59
1*1*151*5
1*1*1*590
1*1*7591*
1*5061*6
1*53692
l*566H*
1*59531*
1*62609
1*65372
1*68359
Main
Meter
#1
x 100
CF
129527
129652
129786
129920
13061*9
130181*
130302
1301*28
130557
130679
130801*
130937
131079
131215
131358
Weir Weir
Box Box
#1 #2
2-3/1* 0
2-3/1* V
2-3/1* V
2-3/U 3/1*
2-3/1* 0
2%" 0
2-3/1* 0
2V' 0
2V' 0
2V' 2"
2V' 2"
2V' 2"
2V' 2"
2V' 2"
Date
1968
12-17
12-18
12-19
12-20
12-21
12-22
12-23
12-21*
12-25
12-26
12-27
12-28
12-29
12-30
12-31
Weir
#1
GPM
27.6
27.6
27.6
27.6
27-5
21.7
27.5
21.7
21.7
21.7
21.7
21.7
21.7
21.7
Weir
#2
GPM
12.1*
12.1*
12.1*
12.1*
12.1*
Remarks
200 Ib. salt
200 Ib. salt
200 Ib. salt
Raining
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
Raining
Switched sewer
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
u>
H
oo
H-
X
-------
Appendix A
METER LOCATIONS
After Recirculation - 1969
#1 - Main Meter - City of Defiance
#2 - After Cartridge Filters
#3 - Binder Mix
#if - Boiler Make-Up and Cooling Tover
#5 - Upstream of Softeners
#6 - Dust Collector
#8 - Mandrel Cleaning
-------
DAILY METER READINGS - WPRD 87-01-68
5
a
M
vo
vn
CO
P-
ON
Meter Meter
#2 #8
x 100 x 10
gals . gals .
081*196 003797
081*577 003807
081*939 003895
085295 003928
085680 003955
085975* 003962
086199 003970
08701*1 003992
087968 001*005
088901 001*025
089668 001*029
089667 00l*05l*
089666 ooUo6i
089850 OOU07U
Meter
#3
x 100
gals.
023727
02381*1
023986
021*123
02U270
021*1*01
021*5^2
02U678
021*819
021*961*
025101*
025232
025375
025568
Meter
#1*
x 10
gals.
113670
113685
1137 11*
1137^9
113771*
113795
113806
113809
113812
113838*
113957
111*107
lll*3l*7
111*513
Meter
#5
x 100
gals.
015101
015103
015109
015117
015131
015129
015127
015129
015130
015130*
0151*17
015570
015789
0160U6
Meter
#6
x 10
gals.
1*71380
1*71*1*1*6
1*77310
1*80121
1*83162
1*86051*
1*88771
1*92156
1*95757
1*9921*3
502599
505516
508601*
51131*5
Main
Meter
#1
x 100
CF
1311*98
131621*
131727
131839
13191*5
132055
13211*7
132191*
13221*6
132297
132363
1321*78
132611*
132731*
Weir
Box
#1
2V'
2V
2%"
1*5"
1"
1"
IV
iV
IV
1"
1"
2"
1"
IV
Weir
Box
#2
2"
2"
2"
2V1
2V'
3"
1"
0
0
0
3"
3"
2Jg"
1"
Date
1969
1-1
1-2
1-3
1-1*
1-5
1-6
1-7
1-8
1-9
1-10
1-11
1-12
1-13
l-ll*
Weir
#1
GPM
21.7
21.7
21.7
6.05
2.19
2.19
6.05
6.05
6.05
2.19
2.2
12.1*
2.2
6.05
Weir
#2
GPM
12.1*
12.1*
12.1*
21.7
21.7
31*. 2
2.19
0
0
0
31*. 2
3l*. 2
21.7
2.2
Remarks
200 Ib. salt
200 Ib. salt
Switched sewer
on Dust Collector
200 Ib. salt
200 Ib. salt
200 Ib. salt
Snowing
200 Ib. salt
Started Per
filters 10:00 A.M.
200 Ib. salt
200 Ib. salt
1*00 Ib. salt
200 Ib. salt
Shut system
off at 11:00 A.M.
Back on city
water
200 Ib. salt
200 Ib. salt
200 Ib. salt
Started
Per filter
10:00 A.M.
200 Ib. salt
n>
* Meters relocated
-------
DAILY METER READINGS - WPRD 87-01-68
td
f
td
a
\o
VJl
I
ro
u>
cr\
Meter
#2
x 100
gals.
090812
091813
092756
093737
09U610
095538
096506
09721*1*
098179
099136
09971*2
100677
101631
102571*
1035H
101*1*28
105331*
106270
Meter
#8
x 10
gals.
001+098
001*106
OOUl25
001*229
OOl+2l+U
001*299
001+316
001*322
00l*3l*l*
001*397
001+1*83
OQl+1+90
001*1*99
001*530
00l*5l+l*
001+565
001*580
OQl+590
Meter
#3
x 100
gals.
02571*9
025911
026080
026589
0261*31
026601
026779
02691*6
027113
027298
0273UO
027529
027701*
027880
028055
028226
028390
028571
Meter
A
x 10
gals.
111+679
111*866
11501*2
115251
1151*11
115576
115779
115975
Il6ll*l*
116323
1161*72
116685
116905
117098
117313
1171*93
117681
117873
Meter
#5
x 100
gals.
0161+10
016770
017103
0171+88
01781+9
018252
018605
018918
01921*5
019578
019800
020130
0201*1*0
020763
021025
021335
021657
021989
Meter
#6
x 10
gals.
511+118
516938
519515
522280
521+851
527550
530283
532767
535299
537991
51*0383
51+31l6
51*5938
51*8561
551127
553625
556078
558521*
Main
Meter
#1
x 100
CF
132791
13281+7
132900
132937
133009
133071
133128
133205
133261
133328
133375
133U26
1331+71*
133527
133570
133617
133663
133713
Weir
Box
#1
IV
2"
1"
IV
1-3/1*
IV
IV
IV
IV
3V
1"
V
IV
IV
V
Weir
Box
#2
1"
3"
1"
1"
1"
1"
1"
1"
1"
1+"
IV
1"
1"
1"
0
Date
1969
1-15
1-16
1-17
1-18
1-19
1-20
1-21
1-22
1-23
1-21+
1-25
1-26
1-27
1-28
1-29
1-30
1-31
2-1
2-2
2-3
Weir
#1
GPM
6.05
12.1+
2.2
6.1
8.9
6.1
6.1
6.1
6.1
2.2
0
6.1
6.1
0
Weir
#2
GPM
2.2
3>+. 2
2.2
2.2
2.2
2.2
2.2
2.2
2.2
3.8
2.2
2.2
2.2
0
Remarks
200 Ib. salt
200 Ib. salt
Raining
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
On city water
1+ hours
200 Ib. salt
200 Ib. salt
Filled outside
tank
Plant down
Gas curtailment
Plant down
Gas curtailment
200 Ib. salt
Raining
200 Ib. salt
Raining
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
(D
3
-------
DAILY METER READINGS - WPRD 87-01-68
w
ro
K
H
TO
ro
-pr
I
u>
u>
vo
Meter Meter
#2 #8
x 100 x 10
gals. gals.
Meter
#3
x 100
gals.
Meter
#1*
x 10
gals.
Meter
#5
x 100
gals.
Main
Meter Meter
#6 #1
x 10 x 100
gals. CF
107235 001*61*1* 028752 118087 022333 560996 133761*
108236 001*680 02891*0 116307 022675 5636U7 133815
109U6 001*827 029121 1181*80 022982 56561*8 133863
110093 OOU851 029306 118678 023313 568068 133913
111078 OOU869 0291*86 11888U 023628 576657 133975
112087 OOU896 029658 119116 023953 573299 13^021
113056 001*912 029816 119297 021*256 575708 13U067
lll*0l*2 001*962 029988 1191*73 021*561* 578138 13^116
115032 001*977 030163 119699 02U891 580592 131*167
115958 005067 030337 119932 025186 583115 13l*2l*7
116850 005118 030510 12011*5 025509 583862 13U296
117750 005125 030689 120367 025837 583862 13l*3U5
118635 005125 030866 120587 026135 583862 13U387
1191*81* 005160 031035 120831* 0261*22 583862 13^U31
120335 005179 031189 121017 026725 583862 13^1*77
121226 005210 031363 121230 027029 583862 131*521*
122135 005221 031532 1211*1*3 027220 583862 131*555
122982 005235 031690 121650 027513 583862 131*600
123888 005236 031863 121900 027613 583862 131*61*1*
12U789 005238 032035 122163 028099 583862 131*688
125796 005255 032211 1221*17 028361* 583862 131*730
126759 005309 032378 122630 028551* 583862 121*761
1276U6 005323 032535 122823 028825 583862 13U802
128661 00531*3 032705 123021 029085 -583862 131*81*1*
129709 005352 032881* 12321*5 029382 583862 131*890
1307U8 005367 033060 1231*58 029670 583862 131*933
131880 005378 0332U6 123695 029967 583862 131*982
132958 0051*08 0331*28 123918 030293 583862 135033
Weir
Box
#1
1"
V
3A
3A
3A
3/U
3A
3/U
3A
3A
3A
3/1*
3A
3/1*
3A
3A
3A
3A
V
3A
₯'
V
3A
3A
3A
3A
3A
3/U
Weir
Box
#2
0
0
0
0
0
V
V
0
0
0
0
0
0
0
0
0
0
0
V
0
V
0
0
V
h"
0
0
₯'
Date
1969
2-1*
2-5
2-6
2-7
2-8
2-9
2-10
2-11
2-12
2-13
2-lU
2-15
2-16
2-17
2-18
2-19
2-20
2-21
2-22
2-23
2-2U
2-25
2-26
2-27
2-28
3-1
3-2
3-3
Weir
#1
GPM
2.2
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Weir
#2
GPM
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Remarks
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
I
(D
B.
-------
DAILY METER READINGS - WPRD 8T-01-68
xo
oo
ro
M
f
K
CQ
OJ
I
u>
VO
Meter
#2
x 100
gals.
131+058
135125
135986
136818
137626
1381+25
139313
11+0053
11+0860
Ul6l8
11+21+29
H+3333
11+1+220
11+5110
11+5968
11+6811+
Meter
#8
x 10
gals.
005503
005511
005539
005555
005573
005588
005617
005629
00561+0
005692
005708
005752*
00601+9
0061+68
006779
00713*+
Meter
#3
x 100
gals.
033601+
03377 U
033926
031+101*
031+275
031+1+1+6
031+61+8
03l+8ll+
031+999
035171
035359
03531+5
035722
035902
036070
036230
Meter
#1+
x 10
gals.
121+138
121+31+1+
121+535
121+727
121+928
125125
1253U8
125552
125762
125957
126170
126368
126588
126821
127036
127251+
Meter
#5
x 100
gals.
030591
030836
031086
031332
031589
03181+8
032121+
032336
032689
033001
033311
0331+56
033771+
031+097
031+1+21+
031+708
Main
Meter Meter
#6 #1
x 10 x 100
gals . CF
135082
135122
135180
135328
135^71
135615
135776
135912
135998
136081+
136172
136262
136352
1361+39
136526
136603
Weir
Box
#1
3A
3/1+
3/1+
3/1+
3/1+
3/1+
3/1+
1"
l£
₯'
3A
3/1+
3/1+
3A
3A
Weir Date
Box 1969
#2
0 3-1+
h" 3-5
rvL-tf O £
£*5> j-D
2%" 3-7
2h" 3-8
2-3/1+ 3-9
2-3/1+ 3-10
2" 3-11
3-12
1" 3-13
iy 3-11+
IV 3-15
1-3/1+ 3-16
IV 3-17
3/1+ 3-18
1-3/1+ 3-19
Weir
#1
GPM
0
0
0
0
0
0
0
2.2
0
0
0
0
0
0
0
Weir
#2
GPM
0
0
21.7
21.7
21.7
27.5
27-5
12.1+
2.2
6.0
6.0
8.9
6.0
0
8.9
Remarks
200 Ib. salt
200 Ib. salt
System shut off
on city water
at 10:00 A.M.
100 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
Started Per
filter at
3:00 P.M.
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
Installed
meter in
return line
from Pond
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
9
T3
0>
a
X
>
* Meters relocated
-------
DAILY METER READINGS - WPSD 87-O1-68
1
tf
1
ro
>
M
Meter
#2
x 100
gals.
1U7680
1U851U
1^9505
150U18
151552
Meter
#8
x 10
gals.
007650
008253
008859
009106
009106
Meter
#3
x 100
gals.
0361^01
036575
0367^9
036917
037102
Meter
#4
x 10
gals.
127 U7U
127671
127853
128026
1282314-
Meter
#5
x 100
gals.
03^966
035231
035^60
0356UO
035715
Meter
#6
x 10
gals.
Main
Meter
#1
x 100
CF
136676
136750
136825
136891*
136985
We
Bo:
#1
^
Ik
l"
v
2"
vo
vo
ro
152597 0091UU 087268 128UU5 035785
153593 009336 037^7 128669 035921
15U369 009929 037618 128867 036137
155287 0103^5 037798 129067 0363U7
156U85 037981 129257 036383
157771 0103>t3 038168 129^39 036iil6
Mo Data
160209 038503 129806 036U83
161^70 038688 129997 03655^
137205
137283
Weir Weir Date
Box 1969
#2
3-20
3-21
3-22
3-23
Weir Weir
#1 #2
GPM GPM
2"
0
6.0
2.2
0
12.1
1"
1"
1"
2V'
3-27
3-28
2.2
2.2
13737^ 1"
137^80 V
137672 h"
137782 3/U
2V'
2"
3-29
3-30
3-31
U-l
2.2
0
0
0
6.0
6.0
6.0
6.0
12.lt
137061 IV 3/U 3-25 6.0 0
137136 IV1 IV 3-26 6.0 6.0
2.2
16.7
16.7
12. U
6.0
8.9
Remarks
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
Raining
200 Ib. salt
Returned water
from Pond for
2 hrs.-Still
foam
No salt
Started
returning
vater at
8:00 A.M.
200 Ib. salt
200 Ib. salt
Stopped
returning
water from
Pond at 8:00
A.M.
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
a
ts
p-
H-
-------
DAILY METER READINGS - WPRD 87-01-68
o
o
g
id
i
o
n
s
g
a
g
i i
a
CO
CO
1
Meter
#2
x 100
gals.
162566
163^01
165001
165811*
166602
167391
l68l**3
168880
16961*7
170390
171158
171823
1721*73
173215
Meter Meter
#8 #3
x 10 x 100
gals . gals .
03881*8
039035
039^01
039581
039T55
039939
010356 01*0112
01*0293
Ol*0l*87
01*0661+
okoQkf
01*1011
01*1199
01*1358
Meter
x 10
gals.
130170
130393
130850
131090
131298
131521
131732
131930
132159
132881
132607
132790
132987
133189
Main
Meter Meter Meter
#5 #6 #1
x 100 x 10 x 100
Weir
Box
#1
Weir
Box
#2
Date
1969
Weir Weir
#1 #2
GPM GPM
Remarks
gals . gals . CF
03661*5
036979
037591*
037927
038237
038597
038908
039227
039551*
039861
01*0200
01*0510
01I0751*
Ol*ll89
137879
1379T7
138161*
138261
138351*
1381*57
138552
138650
13871*6
138838
13891*2
139039
1391^7
13921*5
3A
3A
3/1*
3A
3A
3A
3A
3A
3/1*
3A
3A
3/1*
3/1*
3/1*
2-3/1*
1-3/1*
1-3/1*
1-3A
1-3/1*
2"
2V
2V
2"
2^"
2V
2V'
2-3/1*
1-3/1*
1+-3
1*-1*
l*-5
l*-6
l*-7
l*-8
l*-9
1*-10
1*-11
U-12
1*-13
l*-ll*
It 15
1*-16
U-17
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
27.5
8.9
8.9
8.9
8.9
12.1*
16.7
16.7
12.1*
16.7
16.7
21.7
27.5
8.9
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
200 Ib. salt
Put dust
collectors
ro
u>
cr\
\o
175088
175930
176818
178020
178998
OU15U2 133387
0^1731* 133596 01*1736
01*1919 133815 01*2010
01*2087 13U020 Ql*22l*0
OU2279 13^257 Ol*2l*97
01*21*37 13l*U3l* 01*2725
139317 1" 3V 1*-18 2.2 Ul.8
139U85
13961*3
139778
139831
139893
3/1*
3/1*
IV
3A
3V
3"
iV
3"
1*-19
1*-20
1*-21
l*-22
U-23
0
0
6.0
0
1*1.8
3l*. 2
3.8
3l*. 2
in system
200 Ib. salt
Shut system
off, on city
water at
11:30 A.M.
200 Ib. salt
200 Ib. salt
200 Ib. salt
Drained tank
200 Ib. salt
(B
B
H-
X
-------
DAILY METER READINGS - WPED 87-01-68
w
td
>
ro
>
M
K
g
3
33
tti
g
H
a
Q
.P-
ro
-F-
1
^C
H
MD
ON
CO
Meter Meter Meter
#2 #8 #3
x 100 x 10 x 100
gals . gals . gals .
180101*
181200
182177
183067
181*01*5
181*985
186052
186851*
186851*
18685!*
01*2622
Ql*28l2
OU2997
01*3178
0^*3366
Ol*35l*2
01*3725
01*3905
Ql* 1*081*
01*1*267
01*1*1*51*
Ol*l*6U3
01*1*620
01*5008
Ol*5l87
01*5352
01*5532
01*5718
01*5913
o 1*6106
01*6286
01*61*1*7
01*6602
ol*67l*2
01*6892
01*7038
Meter
-#1*
x 10
gals.
131*636
131*858
135078
135299
135522
135731
135967
136193
136380
136609
136805
136981
137139
137320
1371*85
137670
137821
137975
138138
138279
1381*33
138576
138720
138859
138970
139090
Main
Meter Meter Meter
#5 #6 #1
x 100 x 10 x 100
gals . gals . CF
01*2980
01*3213
Ol*3l*89
01*3737
01*1*021
OUU263
OU1*522
01*1*851*
01*5185
01*5535
01*5905
01*6227
01*6551
OU6876
01*7192
Ol*753l*
01*7890
01*8239
01*8629
01*8915
01*9293
019597
01*9879
139989
11*0055
11*0118
11*0203
11*0261*
ll*0332
ll*0l*21
ll*0l*75
11*0537
11*0603
11*0662
11*0721
11*0779
11*081*3
11*0901
ll*0956
ll*1009
11*1062
ll*1120
ll*1179
ll*12l*l
11*1293
ll*13U6
11*1403
ll*ll*89
11*1519
Weir Weir
Box Box
#1 #2
3/1* 1"
3/1* IV
3/1* IV
3/1* 1"
3/U IV
IV 2V
IV i"
3/U IV
3/1* IV
3A 1"
3/1* 3A
3/U IV
3/1* IV
1-3/1* 2"
1-3/1* 2"
1-3/1* 2"
IV 2"
3/1* 1"
3/1* V
1" 3/1*
3/1* IV
3/1* 1-3/1*
1" 1-3/1*
3/1* IV
1" 2V
1" IV
Date
1969
l*-2l*
l*-25
l*-26
l*-27
U-28
l*-29
U-30
5-1
5-2
5-3
5-1*
5-5
5-6
5-7
5-8
5-9
5-10
5-11
5-12
5-13
5-11*
5-15
5-16
5-17
5-18
5-19
Weir
#1
GPM
0
0
0
0
0
6.0
6.0
0
0
0
0
0
0
8.9
8.9
8.9
6.0
0
0
2.2
0
0
2.2
0
2.2
2.2
Weir
#2
GPM
2.2
6.0
3.8
2.2
3.8
21.7
2.2
6.0
6.0
2.2
0
3.8
6.0
12.1*
12.1*
12.1*
12.1*
2.2
0
0
6.0
8.9
8.9
6.0
16.7
6.0
Remarks
200 Ib.
200 Ib.
200 Ib.
salt
salt
salt
Purge system
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
300 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
Raining
200 Ib.
200 Ib.
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
a
c
H-
X
-------
DAILY METER READING - WPRD 87-01-68
ro
ro
CQ
ro
o
i
ON
ON
Meter Meter Meter
#2 #8 #3
x 100 x 10 x 100
gals . gals . gals .
01+7181+
01+7333
Meter
#1+
x 10
gals.
139210
13931+3
Main
Meter Meter Meter
#5 #6 #1
x 100 x 10 x 100
Weir
Box
#1
Weir
Box
#2
Date
1969
Weir
#1
GPM
Weir
#2
GPM
Remarks
gals . gals . CF
05011+9
11+1582
11+1626
3A
3A
1"
V
5-20
5-21
0
0
2
0
.2
200 Ib.
#5 Meter
salt
re-installed
Ol+7lt66
139^82
050361
1U1671
5-22
in make
line to
tank
200 Ib.
Started
up
clean
tank
chemical feed
01+7611
01+7739
01+7883
Ot+8021
Ol48l6l
Ol+830l+
01+81+29
01+8551+
Ql+8690
Ql+8016
01+8951
Ql+9082
Ol»9213
01+931*7
01+91+83
01+9622
Ql+9768
01+9906
139628
139767
13991U
11+0058
11+0190
11+0295
lltQl+26
11+051+3
11+0681
11+0827
11+0958
11+1087
11+1217
11+131+9
ll+H+86
11+16W3
11+1789
11+1909
050561
050759
0509T2
05H83
051385
051591*
051786
051993
052215
0521+19
052633
05281+8
053051
05321+7
0531*62
053671
053887
05^098
11+1709
11+17146
11+1788
11+1829
11+1870
11+1917
11*1969
11+2011+
11+2059
11+2107
11+2160
11+2206
11+2255
11+2302
11+2350
11+2391+
11+21+36
11+21+77
3/1+
3/1+
3A
V
1"
1"
1"
1"
1"
IV
1"
l"
iy
i"
i"
i"
iV
V
V .
3/1+
V
1"
1"
1"
3A
1"
IV
1"
IV
iy
iV
iV
V
V
5-23
5-21+
5-25
5-26
5-27
5-28
5-29
5-30
5-31
6-1
6-2
6-3
6-1+
6-5
6-6
6-7
6-8
6-9
0
0
0
0
2.2
2.2
2.2
2.2
2.2
3.8
2.2
2.2
3.8
2.2
2.2
2.2
6.0
0
0
0
0
2
2
2
2
6
2
6
3
6
6
0
0
.2
.2
.2
.2
.0
.2
.0
.8
.0
.0
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt >
salt [g
salt g
salt g
salt x
salt >
salt
salt
salt
-------
DAILY METER READINGS - WPRD 87-01-68
K
ro
5
H
O
U)
o
CO
ON
H
O
I
J
Meter Meter Meter
#2 #8 #3
x 100 x 10 x 100
gals . gals . gals .
050036
050167
050296
050l*2l*
050568
050699
050828
Meter
#1*
x 10
gals.
ll*202U
li*2ll*8
11*2281*
11*2518
11*2709
ll*2857
11*2986
Main
Meter Meter Meter
#5 #6 #1
x 100 x 10 x 100
Weir
Box
#1
Weir
Box
#2
Date
1969
Weir
#1
GPM
Weir
#2
GPM
Remarks
gals . gals . CF
05^309
051*515
05VT20
05U921*
055226
0551*1*7
055662
11*2522
11*2572
11*2631
11*2693
ll*27l*5
ll*2786
11*2830
1"
V
IV
IV
IV
IV
1"
iy
IV
IV
1-3/1*
1"
1"
V
6-10
6-11
6-12
6-13
6-ll*
6-15
6-16
2
0
6
6
6
6
2
.2
.0
.0
.0
.0
.2
6.0
6.0
6.0
8.9
2.2
2.2
0
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
On hard
salt
salt
salt
salt
salt
salt
salt
water
3:00 P.M.
050937
051061*
051205
051316
05ll*3l*
051557
051682
051812
051926
052031*
0521^3
052238
052351*
0521*55
052561*
052673
052797
052919
053061
11*3095
11*3220
ll*330U
ll*3l*0l*
11*3505
11*3623
11*3751
11*3905
11*1*077
11*1*233
11*1*357
11*1*1*55
11*1*537
11*1*630
ll*l*730
11*1*837
11*1*969
ll*50U8
11*5129
05581*3
05601*9
056271*
0561*63
056662
05687U
057077
057286
057^81
057688
057901
058112
058333
058537
058751
058956
059182
059271
059363
11*2867
11*2911
11*2956
11*2997
11*3038
ll*308l
ll*312l*
11*3169
11*3211
11*3262
11*3319
11*3373
11*31*15
11*31*65
11*3511
11*3558
11*3609
11*3652
11*3696
IV
IV
IV
IV
IV
IV
i"
i"
1"
i"
i"
i"
i"
i"
V
3/1*
IV
IV
i"
i"
i"
IV
2"
IV
IV
IV
IV
IV
IV
1-3/1*
IV
1"
6-17
6-18
6-19
6-20
6-21
6-22
6-23
6-21*
6-25
6-26
6-27
6-28
6-29
6-30
7-1
7-2
7-3
7-1*
7-5
6
6
6
6
6
6
2
2
2
2
2
2
2
2
0
0
.0
.0
.0
.0
.0
.0
.2
.2
.2
.2
.2
.2
.2
.2
6.0
6.0
2.2
2.2
2.2
6.0
12.1*
6.0
6.0
6.0
6.0
6.0
6.0
8.9
6.0
2.2
200 Ib.
salt
(D
O
-------
g
DAILY METER READINGS - WPRD 87-01-68
B
-t-
>
ro
0
H
*
1
§
»
H
H
Q
cn
3
a\
i
3
bvJ
~^
vo
Meter
#2
x 100
gals.
187082
187926
188907
189895
190816
191789
192888
193701
194638
195597
196498
197437
198255
199082
199923
200795
201647
202535
203375
204190
205094
205901
Meter Meter
#8 #3
x 10 x 100
gals . gals .
053234
053341
053492
053642
053769
053906
054045
054180
054313
054448
054587
054685
054791
054915
055026
055138
055225
055338
055953
055593
055720
055853
055977
056116
056250
056357
Meter
#4
x 10
gals.
145246
145351
145484
145634
145788
145915
146042
146180
146329
146334
l4634o
146462
146462
146567
146801
146907
147091
147282
147732
148078
148394
148743
149083
149364
149682
149945
Meter
#5
x 100
gals.
05982
059712
059884
060069
060255
060473
060690
060913
06lll6
061350
061602
061805
062021
062236
062935
062638
062831
063041
063241
063472
063680
063903
064110
064321
064539
064718
Meter
#6
x 10
gals.
583871
586057
588073
590467
592914
595827
598971
602289
604518
607146
609860
612431
615094
617347
619694
622112
624311
626454
628902
631302
633683
636160
638504
Main
Meter
#1
x 100
CF
143762
143801
143858
143917
143964
144019
144061
144105
144152
144219
144280
144330
144397
144441
144482
144537
144587
144648
144705
144765
144824
144888
144941
144990
145042
145095
Weir
Box
#1
V
IV
3/4
IV
IV
IV
iv
IV1
IV
IV
IV
3/4
3/4
3/4
3/4
IV
iv
i"
3/4
1"
IV
1"
1"
Weir Date
Box 1969
#2
7-6
IV 7-7
1-3/4 7-8
2" 7-9
2" 7-10
2" 7-11
2" 7-12
2" 7-13
2" 7-14
2V 7-15
IV 7-16
IV 7-17
l_3/lt 7-18
1" 7-19
1" 7-20
1-3/1* 7-21
2" 7-22
2" 7-23
7-24
7-25
2" 7-26
IV 7-27
2" 7-28
2" 7-29
IV 7-30
2" 7-31
Weir
#1
GPM
0
6.0
0
6.0
6.0
6.0
6.0
6.0
6.0
6.0
6.0
0
0
0
0
3.8
6.0
2.2
0
2.2
6.0
2.2
2.2
Weir
#2
GPM
6.0
8.9
12,4
12.4
12.4
12.4
12.4
12.4
21.7
6.0
6.0
8.9
2.2
2.2
8.9
12.4
12.4
12.4
6.0
12.4
12.4
6.0
12.4
Remarks
200 Ib. salt
Back on soft
water
200 Ib. salt
200 Ib. salt
Back to hard
water
300 Ib. salt
200 Ib. salt
200 Ib. salt
300 Ib. salt
200 Ib. salt
200 Ib. salt
300 Ib. salt
P-
H-
-------
DAILY METER READINGS - WPRD 87-01-68
O
\Jl
g
w
&
f>
|\N
IV
a
>
H
S
s
tl
§
»
5
M
H
O
W
C»
M
,
00
ru
]
o\
VO
Meter Meter
#2 #8
x 100 x 10
gals . gals .
206TT9
207644
208543
209523 010697
210370
211270
212152
213052
213885
214730
215584
216404
217170
217931
218809
219607
220372
221579
222192
223140
223998
224865
225802
226604
No Data
228186
228977
Meter
#3
x 100
gals.
056517
056659
056791
056929
057073
057208
0573*10
057472
057602
057727
057853
057980
058135
058260
058398
058511
058693
058833
058960
059107
059228
059372
059508
059631
059882
060027
Meter
#4
x 10
gals.
150057
150186
150353
150530
150678
150953
1511*55
151637
151849
152044
152239
152448
152593
152690
152793
152927
153076
153177
153295
153424
153525
153649
153768
153908
154322
154603
Meter
#5
x 100
gals.
064953
065182
065400
065592
065749
067975
066203
066434
066633
0668UO
067048
067256
0671+95
067721*
06795!*
068182
068 Ui7
068621*
068833
069065
069252
069476
069697
069899
070281
070501
Meter
#6
x 10
gals.
61*0727
042887
61*5106
61+7515
61*9668
65188U
65U213
656723
66136U
663671
665752
666662
Main
Meter
#1
x 100
CF
1U51U9
11*5206
ll*5256
11*5312
11*5363
Ik5k2k
ll*5!*85
ll*55l*8
11*5590
1U5631
11*5680
ll*573l*
11*5788
11*581*3
ll*5900
11*5951
11*5996
ll*6ol*8
11*6103
11*6165
11*6209
11*6263
11*6306
ll*635l
146^57
11*6518
Weir Weir
Box Box
#1 #2
1" 2₯'
1" 2V1
%» 2"
1" 2"
IV 2V'
1" 2^"
IV 2"
2" p"
1" 2%"
1" 2"
1%" 2V1
1" 2"
1" 2%"
1" 2"
1" 2"
IV i%"
IV IV
1-3/t 2"
IV 2"
1-3/1* 2"
IV 2"
1-3/U 2"
1" 1"
1" 1"
1" 1"
1-3/1* 2"
Date
1969
8-1
8-2
8-3
8-1*
8-5
8-6
8-7
8-8
8-9
8-10
8-11
8-12
8-13
8-14
8-15
8-16
8-17
8-18
8-19
8-20
8-21
8-22
8-23
8-2U
8-25
8-26
8-27
Weir
#1
GPM
2.2
2.2
0
2.2
6.0
2.2
6.0
12.1*
2.2
2.2
6.0
2.2
2.2
2.2
2.2
6.0
6.0
8.9
6.0
8.9
6.0
8.9
2.2
2.2
2.2
8.9
Weir
#2
GPM
21.7
21.7
12.1*
12.4
21.7
21.7
12.1*
12.4
21.7
21.7
21.7
12.4
21.7
12.4
12.4
6.0
6.0
12.4
12.4
12.4
12.4
12.4
2.2
2.2
2.2
12.4
Remarks
200 Ib.
200 Ib.
200 Ib.
300 Ib.
Rain
200 Ib.
200 Ib.
200 Ib.
300 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
>
tr-i
s
fTt
tv
a
p,
H-
X
-------
DAILY METER READINGS - WPRD 87-01-68
o
O\
1-3
fe
f
M
>
ro
t)
>
M
s
g
§
M
»
»
M
5
D
M
«
Q
CO
OO
r\D
CD
1
VO
ro
oo
ON
vo
Meter
#2
x 100
gals.
229810
230622
231380
232135
2329^0
233701
231*737
235661
No Data
2371*60
No Data
239298
2**0277
21+1231
21*2191
21*3118
21+1+01*2
21*1+91+5
21+5778
21+6738
21+7698
21*8750
21+9681*
250657
252390
253332
Meter Meter
#8 #3
x 10 x 100
gals . gals .
060171*
060311*
0601*51
060587
060719
060851*
060983
O6lll8
061378
061693
061830
061970
062110
062251
062395
062536
062665
062802
062953
063109
063256
0631*06
063687
063828
Meter
#1*
x 10
gals.
15H81*7
151*979
155091
155219
155360
155506
155816
156001
156257
156526
15667U
156801
156931*
157058
157192
157328
1571*58
157581
157722
15781*8
157938
158039
158260
158318
Meter
#5
x 100
gals.
070730
070959
071176
071397
071609
071765
071923
072127
072529
072950
073168
073357
023555
073766
073979
071*186
071*386
071*601
071*815
07501+5
075260
075501+
075931
0761UO
Main
Meter Meter
#6 #1
x 10 x 100
gals . CF
11*6575
11*6633
11*6682
ll*6726
ll*678l
ll*682l*
11*6878
11*6929
11*7020
11*7108
11*7153
11*7188
11*7229
ll*7275
11*7319
11*7356
11*71*00
11*71*1*2
11*71*87
11*7526
11*7566
11*7606
11+7681*
11*7730
Weir Weir
Box Box
#1 #2
1-3/U 2"
1-3/U 2"
lh" 1-3/1*
1" 1"
1" 1"
1" 1"
1-3/1* 2"
1" 2"
1" 1"
1" 1"
1" V
iy 1"
iy 2"
iy y
IV 3/1*
IV 2-3/1*
ih" \"
IV V
iy h"
IV ih"
IV 2"
Date
1969
8-28
8-29
8-30
8-31
9-1
9-2
9-3
9-U
9-5
9-6
9-7
9-8
9-9
9-10
9-11
9-12
9-13
9-11+
9-15
9-l6
9-17
9-18
9-19
9-20
9-21
9-22
9-23
Weir
#1
GPM
8.9
8.9
6.0
2.2
2.2
2.2
8.9
2.2
2.2
2.2
2.2
6.0
6.0
6.0
6.0
6.0
6.0
6.0
12.1+
3.8
6.0
Weir
#2
GPM
12.1+
12.1*
8.9
2.2
2.2
2.2
12.1*
12.1*
2.2
2.2
0
2.2
12.1*
0
0
27-5
0
0
0
6.0
12.1*
Remarks
200 Ib.
200 Ib.
300 Ib.
200 Ib.
200 Ib.
300 Ib.
200 Ib.
200 Ib.
200 Ib.
200 Ib.
Raining
200 Ib.
200 Ib.
200 Ib.
200 Ib.
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
salt
X
>
-------
DAILY METER READINGS - WPRD 87-01-68
w
f1
M
1
ro
y
M
5
g
§
S
a
g
M
CO
1
i°
no
.*=-
i
o
ro
cr\
Meter Meter Meter
#2 #8 #3
x 100 x 10 x 100
gals . gals . gals .
25U226
255332
25658!*
257619
258
259588
260621
2611+1+8
262506
2635^9
261+578
265687
266839
268139
269360
2701+76
271721
273001
271*099
06397^
061*136
061*288
061+1+1+5
061+593
061+756
061+901
06501+0
065180
065333
0651*85
065653
065798
06591*1*
066089
066251
0661+00
066562
066706
Meter
#1+
x 10
gals.
1581+1+0
158567
158690
158902
159057
15921+2
159^02
159577
159757
15991+9
160132
160301+
1601+88
160666
16081+8
161037
161208
161393
161565
Main
Meter Meter Meter
#5 #6 #1
x 100 x 10 x 100
Weir
Box
#1
Weir
Box
#2
Date
1969
Weir
#1
GPM
Weir
#2
GPM
gals . gals . CF
0763^2
076555
076773
077026
077220
077^35
077629
077782
077966
078162
078380
078629
07881+1
07901+8
079258
079^79
079678
079898
086096
11+7768
11+7810
11+7862
11+7909
li+79^3
11+7985
11+8021
11+8086
11+8129
11+8173
11*8215
11+8260
11+8301
lt+831+6
11+8389
11+81+36
11+81+77
11+8522
11*8557
3A
3A
IV
IV
1"
iV
iV
2"
1"
iV
IV
IV
l-3/i*
1-3A
2V
iV
IV
2-3/1*
IV
IV
IV
2"
V
V
iV
2V
1"
3A
V
2"
2"
2"
IV
IV
iV
3"
9-21+
9-25
9-26
9-27
9-28
9-29
9-30
10-1
10-2
10-3
10-1+
10-5
10-6
10-7
10-8
10-9
10-10
10-11
10-12
0
0
6.0
6.0
2.2
6.0
6.0
12.1+
2.2
6.0
6.0
6.0
8.9
8.9
16.7
6.0
6.0
6.
3.
6.
12
0
0
6.
21
2.
0
0
0
8
0
.1+
0
.7
2
12.1+
12
12
6.
6.
6.
.1*
.1*
0
0
0
Remarks
200 Ib. salt
200 Ib. salt
200 Ib. salt
Flushed system
200 Ib. salt
200 Ib. salt
200 Ib. salt
300 Ib. salt
A-12/B-10*
A-10/B-12
200 Ib. salt
A-7/B-12
A-12/B-ll^
200 Ib. salt
tf
m
3
Rain
* On Stream Hours - Filter A
Filter B
-------
DAILY METER READINGS - WPRD 87-01-68
o
oo
TABLE
i
ro
DAILY
1
READINGS
M
a
LO
1
H
O
rv>
f
a\
vo
Meter
#2
x 100
gals.
275235
2761*65
27761*6
278733
279977
281150
282363
28351*2
281*71*3
285909
287168
288286
Meter Meter
#8 #3
x 10 x 100
gals . gals .
066851
066998
067l!*2
067276
0671*16
067551
067697
06781*5
067987
068135
068272
0681*11*
Meter
#1*
x 10
gals.
1617U1*
161921*
162106
162263
1621*51
162592
162765
16291*3
163088
163251
163500
163535
Meter
#5
x 100
gals.
080309
080518
080736
080929
081137
081337
08151*8
081751*
081987
082206
0821*30
082631*
Main
Meter Meter
#6 #1
x 10 x 100
gals . CF
11*8603
11*861*3
11*8685
11*8723
ll*8772
11*8807
11*881*7
11*889!*
ll*8937
11*8983
ll*902l*
ll*9067
Weir
Box
#1
2-3/1*
1-3/1*
lh"
1"
&T
1-3/1*
3A
3/1*
Weir
Box
#2
3"
1"
1-3/U
I
1-3/1*
3/1*
3A
3A
Date
1969
10-13
10-11*
10-15
10-16
10-17
10-18
10-19
10-20
10-21
10-22
10-23
10-21*
Weir
#1
GPM
8.9
6.0
6.0
6.0
2.2
2.2
0
0
0
Weir
#2
GPM
6
2
8
0
0
6
0
0
0
.0
.2
.9
.0
Remarks
A-12/B-12
200 Ib. salt
Rain
A-12/B-12
A-12/B-2
200 Ib. salt
A-12/A-12
Mechanical seal
on "B" Filter
Pump failed
A-9
200 Ib. salt
A-ll/A-5
Running on
"A" Filter only
due to Pump
failure "B"
A-12
200 Ib. salt
A-12/A-8
200 Ib. salt
A-ll/A-8
A-12/A-12
200 Ib. salt
A-12
A-10-3/1*
A-8/A-12
200 Ib. salt
-------
DAILY METER READINGS - WPRD 87-01-68
Main
i
w
i
ro
|
£
1
i
M
1
H
0
ro
vn
H
H
~-N.
Meter
#2
x 100
gals.
2891*36
290690
291920
292639
293508
295232
296008
296799
297632
2981*98
299388
300270
Meter Meter
#8 #3
x 10 x 100
gals . gals .
068551
068691
068831
068965
069105
06921*6
069387
069521*
069661
069803
069923
070071
070211
Meter
#1*
x 10
gals.
163683
163830
163971
161*102
16U261*
161*1*00
161*552
161*670
161*771
161*906
165031
165178
165323
Meter
#5
x 100
gals.
082855
08307 !*
083U31
081*087
081*289
081*513
081*953
085156
08537!*
085565
085791
085997
Meter Meter
#6 #1
x 10 x 100
gals . CF
11*9108
U9Xk
11*9217
11*9339
ll*9382
ll+9l*31
11*91+7!*
11*9523
11*9557
ll*96t*5
11*9692
11*9732
Weir
Box
#1
3/1*
1"
1"
3A
3A
3/1*
3/1*
3A
3A
1"
2"
3A
3/1*
Weir
Box
#2
3/U
₯'
y
3/1*
3A
3A
3/1*
3A
3A
h"
2"
1"
3A
Date
1969
10-25
10-26
10-27
10-28
10-29
10-30
10-31
11-1
11-2
11-3
in
11-5
11-6
Weir
#1
GPM
0
2.2
2.2
0
0
0
0
0
0
2.2
0
0
Weir
#2
GPM
0
0
0
0
0
0
0
0
0
0
2
0
.2
Remarks
200 Ib. salt
A-6/A-8J&
A-7*s
200 Ib. salt
On city water
10:00 A.M.
Back on filter
12:00 Noon
200 Ib. salt
B-12/A-12
B-12/A-12
200 Ib. salt
B-12/A-12
B-12/A-12
200 Ib. salt
B-12/A-12
B-12/A-12
300 Ib. salt
B-12/A-lli,
B-7
Rain
A-12/B-12
200 Ib. salt
A-U/B-7%
X
>
-------
DAILY METER READINGS - WPRD 87-01-68
Meter Meter Meter
TABLE
>
ro
DAILY
1
»
M
1
(-"
t-1
5
1
I J
H
M
V0
ON
vo
#2 #8 #3
x 100 x 10 x 100
gals . gals . gals .
301206
30210U
302891*
303775
301*705
305679
306598
307593
308607
309681*
310718
070357
0701*99
07061*1*
070793
070931*
071081
071201*
0713!*0
0711*7!*
071616
071768
Meter
#1*
x 10
gals.
165U82
165627
1657 !*3
165858
166005
l66ll*7
166286
1661*35
166578
166728
166861+
Main
Meter Meter Meter
#5 #6 #1
x 100 x 10 x 100
gals . gals . CF
086209
086380
086581*
086808
087009
087209
0871*06
087602
087801
087998
088213
11*9779
ll*9809
11*9850
11*9897
ll*9978
150015
150055
150096
150130
150173
Weir
Box
#1
3/U
3A
3A
1"
3/U
3/U
3/1*
3/1*
3A
Weir
Box
#2
3A
3/U
3A
3/1*
1"
1-3/8
3A
3/1*
3/1*
3A
3A
Date
1969
11-7
11-8
11-9
11-10
11-11
11-12
11-13
ll-ll*
11-15
11-16
11-17
Weir
#1
GPM
0
0
0
0
0
2.2
0
0
0
0
0
Weir
#2
GPM
0
0
0
0
2.2
5-0
0
0
0
0
0
311805
312897
071917 167019 0881*30
072063 167161* 088658
150222 1" 1" 11-18
150263 11-19
Remarks
A-12/B-10
200 Ib. salt
A-12/B-12
A-12/B-12
200 Ib. salt
B-5/A-12
B-8.5/A-7
B-l*/A-5
B-7/A-12
B-8
300 Ib. salt
A-7/B-5
B-6/A-5
B-5^
200 Ib. salt
A-10VB-12
200 Ib. salt
A-12/B-12
A-12/B-12
200 Ib. salt
A-12/B-8
200 Ib. salt
Rain
A-12/B-12
Snow
n>
-------
DAILY METER READINGS - WPRD 87-01-68
n
1
M
>
ro
M
K
1
i
M
8
H '
H
ro
o
i
H
ro
o\
Meter
#2
x 100
gals.
31U067
315213
316290
317290
318319
319278
320206
32121*3
322251
32331*3
32U385
3253U3
326306
327268
Meter Meter
#8 #3
x 10 x. 100
gals . gals .
072211*
072367
072517
072655
072800
072936
073070
073217
073363
073511*
07361*8
073801
073955
071*108
Meter
#1*
x 10
gals.
167285
1671*1*1*
167629
167795
168005
168186
168359
168519
168687
168855
169001*
169166
169332
169538
Meter
#5
x 100
gals.
088858
089079
089300
089516
089731*
089930
090113
090321*
090531
09071*2
090933
091120
091370
091588
Main
Meter Meter
#6 #1
x 10 x 100
gals . CF
150303
15031*2
150387
1501*26
1501*66
150507
15051*8
150588
150631
150669
150710
150777
150820
150860
Weir
Box
#1
3A
3A
3/1*
3A
3/1*
3A
k"
0
V
3A
3A
3A
3A
Weir
Box
#2
3/1*
₯'
V
k"
k"
V
k"
i"
V
k"
k"
k"
V
Date
1969
11-20
11-21
11-22
11-23
11-21*
11-25
11-26
11-27
11-28
11-29
11-30
12-1
12-2
12-3
Weir
#1
GPM
0
0
0
0
0
0
0
0
0
0
0
0
0
Weir
#2
GPM
0
0
0
0
0
0
0
2.2
0
0
0
0
0
Remarks
300 Ib. salt
Snow
A-12/B-11
200 Ib. salt
A-12
200 Ib. salt
B-12/A-12
B-12/A-12
200 Ib. salt
B-12/A-12
200 Ib. salt
B-12/A-12
B-12
300 Ib. salt
A-12/B-12
A-12/B-12
200 Ib. salt
A-12/B-8
A-12
200 Ib. salt
B-12 /A-12
200 Ib. salt
B-12/A-5
H-
X
-------
DAILY METER READINGS - WPRD 87-01-68
lo
i>
!
>
rv>
1
w
g
M
£2!
CQ
ro
-t-
i
H
ro
i j
3
o\
vo
Meter
#2
x 100
gals.
32831*7
32931*3
330350
33131*1
332329
333507
331*676
33581*2
336918
337968
339037
31*0089
31*1186
31*2215
Meter Meter
#8 #3
x 10 x 100
gals . gals .
07l*2l*2
07l*39l*
071*537
071*678
071*831*
075011*
075193
075377
075558
075739
075903
076119
076269
076478
Meter
#1*
x 10
gals.
169718
169900
170092
170305
1701*99
170710
170883
171056
171230
171383
171560
171722
171920
172086
Meter
#5
x 100
gals.
091797
092000
092203
092430
092653
092913
093153
093l*3l*
093712
093988
091*258
091*520
094892
095153
Main
Meter Meter
#6 #1
x 10 x 100
gals . CF
15090U
15091*1
150981*
15102U
151073
151123
151174
151227
151280
151325
151375
151U46
151439
151558
Weir
Box
#1
3/U
3/1*
3A
1"
3A
3A
3A
3A
3/U
3A
3/U
3A
3A
3/1*
Weir
Box
#2
\"
v
V
y
y
y
V
y
V
y
V
V
V
y
Date
1969
12-U
12-5
12-6
12-7
12-8
12-9
12-10
12-11
12-12
12-13
12-lU
12-15
12-16
12-17
Weir
#1
GPM
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Weir
#2
GPM
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Remarks
B-9VA-83g
B-12
200 Ib. salt
A-12/B-12
A-12/B-12
300 Ib. salt
A-10VB-12
Rain
A-12/B-12
200 Ib. salt
A-12/B-12
200 Ib. salt
A-12/B-12
200 Ib. salt
A-12/B-12
200 Ib. salt
A-12/B-12
200 Ib. salt
A-8/B-8
A-12/B-12
300 Ib. salt
AT O /Tl Hi-'
"_1_^/ .D^^lJ^p
200 Ib. salt
A-12/B-U^
A-12/B-12
d
n>
p
&
H*
>
-------
DAILY METER READINGS - WPRD 87-01-68
H
H
to
a
1
>
ro
O
H
K
1
!
|
M
1
H
ro
CO
i
to
u>
H
VO
Meter
#2
x 100
gals.
31*3179
3^^2Q^
3 Ji ch T c
31*6637
31*7957
31*9276
350610
351875
353089
35U251*
35551*6
356822
358029
359169
Meter Meter
#8 #3
x 10 x 100
gals . gals .
076690
076852
07701*2
077230
0771*21
077591
077781
077975
078175
078360
078557
07871*9
078939
079126
Meter
#1*
x 10
gals.
172226
172387
172523
172688
172901*
173089
173252
173U16
173599
173769
173932
171*112
171*289
17U1*1*8
Meter
#5
x 100
gals.
0951*21
095685
095956
096258
09651*5
096797
097067
097380
09761*6
097927
098206
0981*90
098772
0990U8
Meter Meter
#6 #1
x 10 x 100
gals . CF
151590
15161*2
151688
151738
151795
15181*9
151896
151950
151998
15201*9
152101
152151*
152206
152252
Weir
Box
#1
3/U
3A
3A
3/U
3/U
3A
3A
3/1*
3A
3A
3A
3/U
3A
3A
Weir
Box
#2
y
y
y
y
y
y
y
y
y
y
y
y
y
y
Date
1969
12-18
12-19
12-20
12-21
12-22
12-23
12-21*
12-25
12-26
12-27
12-28
12-29
12-30
12-31
Weir
#1
GPM
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Weir
#2
GPM
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Remarks
A-12/B-12
200 Ib. salt
A-12/B-12
200 Ib. salt
A-12/B-12
A-12/B-12
200 llD. salt
A-12/B-12
200 Ib. salt
A-12/B-12
A-12/B-12
A-12/B-12
200 Ib. salt
A-12/B-12
200 Ib. salt
A-12/B-12
200 Ib. salt
A-12/B-12
300 Ib. salt
A-12/B-12
200 Ib. salt
A-12/B-12
I
(D
-------
DAILY METER READINGS - WPRD 87-01-68
i-3
£
i
ro
g
£
g
n
El
5d
g
o
2!
^-\
8
^r
i
PJ
VJl
J
0
Meter Meter
#2 #8
x 100 x 10
gals . gals .
360335
361481
362704
363892
365106
366142
367345
368623
369538
370431
371392
372311
373444
374398
375655
Meter
#3
x 100
gals.
079333
079518
079724
079914
080105
080187
080255
080307
080374
080441
080508
080598
060803
080943
081153
Meter
#4
x 10
gals.
174614
174811
175023
175192
175365
175489
175596
175705
175825
125966
176091
176208
176409
176561
176741
Meter Meter
#5 #6
x 100 x 10
gals . gals .
099346
099634
099923
100197
100480
100623
100723
100814
100930
101040
101149
101275
101538
101771
102002
Main
Meter
#1
x 100
CF
152309
152364
152413
153458
152517
152551
152580
152607
152634
152656
152676
152708
152753
152807
152857
Weir
Box
#1
3/4
3/4
3/4
3/4
3/4
3/4
3/4
3/4
3/4
3/4
3/4
3/4
3/4
3/4
3/4
Weir
Box
#2
1/4"
1/2"
1/4"
1/4"
1/4"
1/4"
1/4"
0
0
0
0
0
0
0
0
Date
1970
1-1
1-2
1-3
1-4
1-5
1-6
1-7
1-8
1-9
1-10
l-ll
1-12
1-13
1-14
1-15
Weir
#1
GPM
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Weir
#2
GPM
0
0
0
0
0
0
0
0
0
0
0
0
0
0
0
Remarks
A-12/B-12
200# salt
A-12/B-12
200# salt
A-12/B-12
A-12/B-10
200# salt
A-12/B-12
A-12/B-12
300# salt
A-12/B-12
200# salt
A-12/B-12
200# salt
A-12/B-4^
200# salt
A-12/B-12
A-12/B-12
200 # salt
A-12/B-12
A-12/B-12
A-12/B-12
300 # salt
A-12/B-12
200# salt
o
(D
3
X
>
-------
Appendix A
TABLE #A3 - Part 1
WATER QUALITY DATA - DISCHARGE
Discharge Data - ppm - 1969
Sample #1 - Treatment Tank
Susp. Total
Date Phenol Solids Solids pH
3/13
3/20
3/2?
4/3
4/10
4/17
4/24
5/1
5/8
5/15
5/22
5/29
6/5
6/12
6/19
6/26
7/3
7/10
7/17
7/21;
7/31
8/7
8/11*
8/21
8/28
9/5
9/11
9/18
9/26
10/3
10/9
10/16
10/23
10/30
11/6
11/13
11/20
11/26
31.3
21.2
13.7
3.9
22.6
8.6
5.6
9.8
7.2
6.2
1.0
.70
2.8
4.2
5.6
11.2
11.2
22.3
10.it
1*8.7
91
89
255
202
37
21
61
20
25
17
19
29
42
2
53
66
44
167
110
55
7,890
6,799
7,372
6,759
6,800
5,965
5,856
6,585
7,71+0
4,890
3,721
8,507
5,912
6,383
7,386
8,040
6,912
11,391
5,440
6,659
11.1
11.7
11.7
12.0
11.9
11-7
11.7
11.2
11.2
10.5
11.5
12.1
11-5
11.2
11.6
12.2
12.2
11.9
11.6
10.0
Wo report
73.1
36.5
62
72
10,287
9,593
11.0
11.1
No report
22.2
HO. 5
53.9
30.5
45.7
23.8
39.2
16.8
28.7
26.8
6.8
6.1
23.3
20.0
58
29
28
30
28
132
100
112
34
756
124
8
10
264
9,118
8,827
8,162
8,014
7,668
8,258
9,880
9,392
8,870
6,9^2
7,336
4,204
3,072
6,188
11.9
11.5
11.1
11.9
10.8
11.2
11.2
11.9
11.7
ll.l
12.4
11.7
10.8
12.0
Sample #2 - Downstream of
Discharge
Susp. Total
Phenol Solids Solids pH
2.8
.41
.09
.84
.10
.28
1.3
.39
.24
.81
.01
.02
.02
.53
.21
4.2
.10
1.6
0
.01
.08
.01
0
3.5
0
.02
.09
1.4
4.5
11.1
6.0
.82
.38
3.1
.07
1.5
1
24
42
30
22
6
31
4
23
35
2
7
596
13
60
28
0
10
16
110
2
3
6
88
0
2
8
2
46
224
244
36
154
18
1
4
922
628
504
617
510
711
971
619
403
934
656
685
958
914
824
1,430
768
707
491
493
538
429
645
1,936
658
628
624
632
804
1,076
1,288
804
1,058
972
564
904
9.1
7-9
8.5
9.1
8.5
7.5
8.0
8.1
7.7
8.7
8.1
7.8
7.8
8.1
8.0
9.1
8.0
9.2
7.6
7.9
9.3
8.8
9.0
9.3
9.0
9-1
8.6
8.7
9.1
9.3
9-1
8.7
9.2
8.9
8.8
9.6
115
-------
Appendix A
TABLE #A3 - Part 2
WATER QUALITY DATA - DISCHARGE
Discharge Data - ppm - 1969
Sample #1 - Treatment Tank
Susp. Total
Date Phenol Solids Solids pH
Sample #2 - Downstream of
Discharge
Susp. Total
Phenol Solids Solids pH
12/1* 8.7
12/11 20.9
12/18 17.1*
12/21* 20.9
12/31 15-7
31*
96
36
360
70
3,61*1* 10.7
6,1*1*2 11.5
7,51*6 12.3
5,576 11.7
6,780 12.0
1.1*
.1*2
12.5
1.1*
6.7
2k
k
2k
1,308
92
702
1*16
5,57^
2,128
l*,03l*
8.9
9.2
12.0
9.1
11.1*
116
-------
TABLE #A3 - Part 3
WATER QUALITY DATA - DISCHARGE
Appendix A
Discharge Data - ppm _ 1969
Sample #3 - #1 Weir
Date
Susp. Total
Phenol Solids Solids pH
3/13
3/20
3/27
U/3
U/10
U/17
l*/2l*
5/1
5/8
5/15
5/22
5/29
6/5
6/12
6/19
6/26
7/3
7/10
7/17
7/21*
7/31
8/7
8/lU
8/21
8/28
9/5
9/11
9/18
9/26
10/3
10/9
10/16
10/23
10/31
11/6
11/13
11/20
11/26
8.0
1.25
1*.9
1.25
1.6
2.5
2.1*
.93
__
.86
.02
.12
1.03
.61
.1*8
7.0
2.3
10.1*
.02
.03
17
78
68
169
.88
10
3l*0
12
20
5
12
8
32
96
91*
38
1*8
21*
12
1,291*
860
951
1,001
961*
1,062
2,201*
776
__
966
661*
890
726
805
1,192
1,926
1,033
1,026
627
725
9.U
8.0
8.3
7.6
7.7
7.6
8.1*
7.8
__
8.7
7.5
7-6
7.5
7.6
8.1*
8.3
7.2
7.9
7-0
7-9
Ho report
.03
.08
11*
12
538
1*57
7.8
7.7
No report
.02
3.5
0
.01
0
1.1*
6.9
1.3
.02
.19
.1*5
0
.87
.28
18
62
0
8
0
0
126
0
2
32
70
0
0
16
695
1,903
569
61*0
1*1*8
632
1,071*
688
382
796
931*
1*96
126
808
7-5
9.2
8.0
8.2
8.1
7.8
8.1*
9.1*
8.2
8.2
8.2
8.2
8.2
8.7
Sample #1* - #2 Weir
Susp. Total
Phenol Solids Solids pH
.76
.1*1*
.20
3.5
.25
.28
1*.2
.71
.1*3
.28
.36
.0
.37
.003
.03
.93
.17
.03
.01
.02
.33
,02
.01
.85
.02
.02
.02
.56
1.5
19.1
.06
.03
.02
.0
.11*
0
57
88
107
75
93
37
31*
3
1
76
208
1
0
0
15
31*
1
39
11
38
0
1*
0
30
38
1*
0
21*
1*
50
0
0
0
1
7
0
562
621
597
1,369
378
559
1,81*5
1,066
25l*
736
1,286
377
ll*l*
398
9^5
1,108
1,135
1+95
363
1*50
558
353
595
681*
720
280
1*1*2
708
836
l,0ll*
380
1*36
U8U
1*96
532
516
8.1*
7.9
8.2
9. 1*
9.5
7.3
7-7
7.7
6.7
8.8
8.7
7.6
7.1
7.1*
7-9
9.1
7.1
8.8
8.3
7.5
8.2
8.2
7.6
8.5
8.5
8.2
8.0
8.2
9.2
8.5
8.2
8.7
8.1
8.0
8.3
8.3
117
-------
Appendix A
TABLE #A3 - Part 1*
WATER QUALITY DATA - DISCHARGE
Discharge Data - ppm - 1969
Sample #3 - #1 Weir
Susp. Total
Date Phenol Solids Solids pH
12 A
12/11
12/18
12/2*t
12/31
1.5
1.2
.05
.13
5.7
20
16
2
10
12U
688
618
878
788
8.6
8.2
9.
8.
U.100 11.3
Sample #U - #2 Weir
Susp. Total
Phenol Solids Solids pH
.05
.38
7.3
.56
9.0
0
0
22
0
16
516
I2k
5,188
388
2,158
8.3
8.0
12.0
7A
9-5
118
-------
Appendix A
TABLE #AU - Part 1
WATER QUALITY DATA - RECIRCULATED WATER
System Performance Data - 1969 - ppm
Sample #5 - Entering Primary
Filter West
Sample #6 - Dirty Water Tank
Susp. Total
Date Phenol Solids Solids pH
Susp. Total
Phenol Solids Solids pH
3/13
3/20
3/27
l*/3
It/10
V17
l*/2l*
5/1
5/8
5/15
5/22
5/29
6/5
6/12
6/19
6/26
7/3
7/10
7/17
7/21*
7/31
8/7
8/ll*
8/21
8/28
9/5
9/11
s f * ~
9/18
S 1 ^
9/26
x / *"~ *'
10/3
_l_w / j
10/9
-L. W / /
10/16
10/23
10/30
-L. V / .J v
11/6
11/13
11/20
11/27
29.6
31.3
1*7.9
11.7
15.3
11.8
6.1
13.1*
7
1*8
lit
8
15
7
6
5
6
.8
.7
.3
.0
.7
.1*
.6
.2
.3
16.9
6.0
15.0
No
2
1*
13
3
29
8
17
11
21
105
79
1*6
58
110
61
131
69
105
27
,056
,126
,052
,600
290
,7l*0
,180
,772
,592
3,989
5,781* __
6,390
1,832
1*,136 _.
l*,15l* -
2,077
3,1*31* --
3,092
8,057
3,91*2
3,1*05
5,371*
15,252
7,608
3,325
33,818
11,506
19,386
ll*,6oo
report
13.6
11.6
No
21*
1*
,1*50
,232
report
18.1*
1*8.7
17.6
19.
32.
26.
1*5.
ll*.
19.
20.
21*.
17.
22.
19-
1
7
u
2
9
3
6
1*
1*
2
1
560
86
ll*0
12,1*36
266
80
1*86
3,31*0
5,
5,
168
88
1*96
1*16
512
328
29,252
l*,3l*8
1*,888
5,768
1*,957
19,11*1*
5,126
5,288
6,1*06
6,71*1*
3,800
3,856
13,101*
6,1*66
5,101*
5,261*
-
8
9
9
9
9
9
9
9
9
9
-
.8
.2
.5
.3
.2
.2
.5
.5
.5
.2
9.5
9.6
9.6
9.1*
9.8
9.7
10.0
9.
9.
9.
9.
9-
9.
9.
9.
9.
9-
6
6
5
7
7
5
6
6
6
8
26.1
1*0.1*
53.9
29.6
28.7
20.0
9.1*
11.3
5-7
10.3
10.8
10.6
15.8
7.6
1*. 3
5.6
8.0
16.9
6.1*
16.5
13.7
11.2
21.9
2.9
33.1
20.7
32.1*
33.U
1*3.1
21.3
15.8
20.9
23.5
26.9
17.6
23.5
33
65
87
21
77
113
183
60
22
69
35
12
27
61*
127
53
118
8,180
1*1*
126
81
127
52
18
55
60
10l*
96
101*
61*
101*
8
96
96
32
136
3,692
6,271
7,178
1,91*1*
I*,8l9
3,562
2,71*0
3,220
2,870
3,191
5,61*5
3,505
3,952
3,300
2,830
2,581
3,623
11,506
3,397
3,735
1*,130
3,731
1*,628
5,920
5,012
1*,800
6,350
8,101*
6,996
5,038
1*,710
1*,560
5,292
6,500
5,1*20
6,692
-_
9.3
9-1*
9.3
9.2
9.1
9.2
9.1*
9.3
9.5
9.0
9.1*
9.3
9.3
9.2
9.6
9-5
9.9
9.5
9.3
9.1*
9.6
9.1*
9.3
9.6
9.1*
9-5
9.5
119
-------
Appendix A
TABLE #AU - Part 2
WATER QUALITY DATA - RECIRCULATED WATER
System Performance Data - 1969 - ppm
Sample #5 - Entering Primary
Filter West
Susp. Total
Date Phenol Solids Solids pH
Sample #6 - Dirty Water Tank
Susp. Total
Phenol Solids Solids pH
12A
12/11
12/18
12/2U
12/31
2U.U
29.6
25.2
22. U
20.9
202
18U
220
92
6,372
7,230
5,016
5,502
9.7
9.3
9-5
9.5
27.8
20.9
2U.lt
30.5
17.1
100
98
122
228
if ,1*78
6,228
^,670
^,636
9.5
9.6
9.8
9.5
9.6
120
-------
Appendix A
TABLE #A4 - Part 3
WATER QUALITY DATA - RECIRCULATED WATER
System Performance Data - ppm - 1969
Sample #7 - Entering Clean
Water Tank
Date
3/13
3/20
3/27
4/3
4/10
Vl7
4/24
5/1
5/8
5/15
5/22
5/29
6/5
6/12
6/19
6/26
7/3
7/10
7/17
7/24
8/7
8/14
8/21
8/28
9/5
9/11
9/18
9/26
10/3
10/9
10/16
10/23
10/30
11/6
11/13
11/20
11/26
Susp. Total
Phenol Solids Solids pH
No report
Sample #8 - Supply Tank After
Make-up and Cartridge
Filter
Susp. Total
Phenol Solids Solids pH
3
18
52
5
4
1
2
1
2
1
1
0
7
0
2
15
0
4
3
53
0
0
**
0
0
0
8
4
0
1+
32
7
6
8
5
2
12
1,751
5,820
6,016
1,498
4,133
3,523
2,128
3,208
2,907 --
2,990 9.2
3,240 9-5
2,682 9-5
3,715 9.4
3,254 9-3
2,050 9.3
3,025 9-6
2,898 9.6
4, 463 9.6
2,105 9.4
3,473 9.6
3,262 9.6
3,073 9.6
3,813 9.5
6,203 9-8
3,827 9-7
4,706 10.1
4,570 9.7
5,372 9.6
6,280 9-6
4,528 9.7
3,762 9.7
4,150 9.5
5,286 9.7
4,472 9-7
4,684 9-7
5,404 9.8
12.2
28.5
22.3
8.5
15.3
12.9
8.0
24.3
3.5
11.1
12.5
10.2
11.5
4.2
2.4
3.7
5.7
11.2
5.0
11.0
8.4
8.2
12.7
46.9
9.1
12.8
25.1
17.7
38.3
8.7
10.3
14.8
19.1
20.9
14.3
14.8
2
15
26
3
3
2
3
2
3
1
3
2
7
0
85
0
0
0
0
0
0
0
0
0
0
0
0
0
0
3
0
0
1
0
0
1
2,060 9.7
5,306 9.7
4,719 9.7
1,018 9.6
2,894 9.5
2,993 9-7
1,563 7-8
3,l6o 9.6
2,255
2,331 9.1
2,344 9.4
2,456 9.5
3,215 9.3
2,535 9.2
2,090 9.3
2,400 9.5
2,529 9-5
3,216 9.6
2,562 9.3
2,932 9.6
2,638 9.5
2,128 9.6
2,622 9.5
4,494 9.8
3,574 9.7
3,760 10.1
^,592 9.7
4,392 9.6
5,268 9.6
3,850 9.7
3,058 9.7
2,976 9-5
4,222 9.7
4,086 9.7
3,760 9.7
4,520 9.8
121
-------
Appendix A
TABLE #A4 - Part 1*
WATER QUALITY DATA - RECIRCULATED WATER
System Performance Data - ppm - 1969
Sample #7 - Entering Clear
Water Tank
Date
12/U
12/11
12/18
12/2)4
12/31
Susp. Total
Phenol Solids Solids pH
Sample #8 - Supply Tank After
Make-up and Cartridge
Filter
Susp. Total
Phenol Solids Solids pH
3
6
3
13
10
M76
5,852
U.632
9.8
9.7
9.8
9.6
9.7
20.0
19.1
18.7
20.0
11.3
8
0
25
2
0
3,^92
^,09^
3,768
9.8
9.7
9.8
9.6
9.7
122
-------
Appendix A
TABLE #A5
MONTHLY AVERAGE OF DAILY DISCHARGE FLOWS - GALLONS/MIN.
8/12/68-8/31/68 - 19 days
9/1/68-9/27/68 - 26 days
9/28/68-10/25/68 - 28 days
10/25/68-11/22/68 - 28 days
11/22/68-12/20/68 - 28 days
12/20/68-1/17/69 - 25 days
1/17/69-2/14/69 - 28 days
2/14/69-3/14/-9 - 28 days
3/14/69-4/18/69 - 35 days
4/18/69-5/23/69 - 35 days
5/23/69-7/1/69 - 38 days
7/1/69-7/31/69 - 31 days
7/31/69-8/31/69 - 31 days
8/31/69-9/30/69 - 30 days
9/30/69-10/31/69 - 31 days
10/31/69-11/30/69 - 30 days
Weir #1
38.0
43.7
26.2
2k. Q
2k. 8
14.1
2.8
0.0
1.2
1.8
3.4
2.8
4.7
fc.7
4.4
.17
Weir #2
2.2
6.5
2.2
.3
.0
11.8
1.3
5.5
12.1
9-1
4.2
8.6
11.6
5.1*
3.9
.45
Total
40.2
50.2
28.4
24.3
24.8
25.9
4.1
5.5 *
13.3
10.9
7.6
11.4
16.3
10.1
8.3
.6
* Closed system inoperative 3/6-3/11/69 due to septa failure
Diatomite Filter "B".
123
-------
ADDED OPERATIONAL COSTS AND SAVINGS -vs- BASE PEEIOD JULY THROUGH DECEMBER, 1968
Binder Solids
"Water
Solvay Cleaner
Month (#12)
1969 January
- $1,U33
326
111
+ 30
,h + 197
+ 15U
+ 1,069
sr Tubes + 35
lia + 32
+ 200
153
3 - $ 153
(#13)
February
- $1,806
738
111
+ 22
+ 220
+ 122
+ 1,19**
+ 29
+ 3H
+ Uoo
63U
- $ 787
March
- $1,936
382
111
+ 25
+ 2U1
+ 128
+ 1,318
+ 28
+ 39
+ Uoo
250
- $1,037
(#15)
April
- $3,921
311
110
+ 12
+ 235
+ 26U
+ 1,276
+ 29
+ 38
+ UOO
- 2,088
- $3,125
(#16) (#17)
May June
- $U,096 - $
615 -
110
+ 31 +
+ 2UU +
+ 236 +
+ 1,1*18 +
+ 29 +
+ 102 +
+
+
+ Uoo +
- 2,361 -
- $5,U86 - 4
U,782
5U3
96
5
238
12U
988
29
29
75
121
Uoo
58,898
(#18)
July
- $3,028
U31
97
6
+ 2U3
U2
+ 1,022
+ uu
+ 150
7U
+ 121
+ Uoo
-$10,36U
Appendix
I
E| Diatomaceous Earth
ro
Aqua Ammonia
E & R Labor
Polypropylene Media
Fungicide
Dispersant
*** Power
Cumulative Savings
w
+ Represents added costs over base period
- Represents savings over base period
***Power costs are estimated
TABLE 2 - Part 1
-------
ADDED OPERATIONAL COSTS AND SAVINGS -vs- BASE PERIOD JULY THROUGH DECEMBER, 1968
i
ro
Month (#19)
1969 August
+ $ 731
502
100
1
th + 2l*l*
+ 103
+ 790
;er Tubes + 38
;dia + 217
+ 73
+ 122
+ 1*00
+ 2,115
ngs - $8,21*9
(#20)
September
- $ 619
619
99
1
+ 236
+ 162
+ 782
+ 37
+ 153
+ 109
+ 189
+ 1*00
+ 730
- $7,519
(#21)
October
- $1,1*89
598
102
1
+ 21*1*
+ 261
+ 1,079
+ 39
+ 95
+ 120
+ 122
+ 1*00
+ 170
- $7,31*9
(#22)
November
- $1,988
631
98
+ 7
+ 271
+ 261
+ 1,033
+ 37
+ 212
+ 3U2)
)
+ 1*00
- 15U
- $7,503
(#23)
December
- $2,679
790
123
+ 1*
+ 2l*5
+ 313
+ 968
+ 1*7
+ 190
+ 30M
)
+ 1*00
- 1,121
- $8,62U
(#21*)
January 1970*
- $1,981*
621
101
+ 10
+ 21*5
+ 182
+ 1,058
+ 38
+ 351)
)
+ 266
556
- $9,180
1
n>
3
p-
i-i.
Binder Solids
Water
Solvay Cleaner
Salt
Diatomaceous Earth
Aqua Ammonia
E & R Labor
Fiber Glass J
Polypropylene Media
Fungicide
Dispersant
*** Power
Cumulative Savings
*Note 1 Grant period ended 1/15/70
+ Represents added costs over base period Note 2 Gas curtailment eliminated production
- Represents savings over base period Jan. 6-12 - 6 days
***Pover costs are estimated Jan. 21-23 - 2 days
TABLE 2 - Part 2
bd
-------
BIBLIOGRAPHIC:
Johns-Manville Products Corporation, Phenolic Waste Reuse by
Diatomite Filtration, Final Report FWQA Grant No 87-01-68
September 1970.
ABSTRACT:
The fiber glass industry has long had a problem in disposing of
waste water containing phenolic resins. In the fiber glass manu-
facturing process, airborne glass fibers are sprayed with a phenolic
resin as the fiber blanket is formed on the collecting conveyor
causing a deposit of resin to form on the collecting conveyor chain.
Prompt cleaning before the deposit sets is needed to permit con-
tinuous formation of the glass fiber mat. The waste originates from
the chain washing operation which uses either a caustic wash or high
volume showers to remove the resin deposits.
Under the demonstration project a chain-cleaning-water-reuse
system was installed which consists of low volume, high pressure
ACCESSION NO.
KEY WORDS:
Fiber glass
Phenols
Resin
Diatomaceous Earth
Filters
Water Reuse
Operating Cost
BIBLIOGRAPHIC:
.Johns-Manville Products Corporation, Phenolic Waste Reuse by
Diatomite Filtration, Final Report FWQA Grant No. 87-01-68,
September 1970.
ABSTRACT:
The fiber glass industry has long had a problem in disposing of
waste water containing phenolic resins. In the fiber glass manu-
facturing process, airborne glass fibers are sprayed with a phenolic
resin as the fiber blanket is formed on the collecting conveyor
causing a deposit of resin to form on the collecting conveyor chain.
Prompt cleaning before the deposit sets is needed to permit con-
tinuous formation of the glass fiber mat. The waste originates from
the chain washing operation which uses either a caustic wash or high
volume showers to remove the resin deposits.
Under the demonstration project » chain-cleaning-water-reuse
system was installed which consists of low volume, high pressure
ACCESSION NO.
KEY WORDS:
Fiberglass
Phenols
Resin
Diatomaceous Earth
Filters
Water Reuse
Operating Cost
BIBLIOGRAPHIC:
Johns-Manville Products Corporation, Phenolic Waste Reuse by
Diatomite Filtration, Final Report FWQA Grant No. 87-01-68,
September 1970.
ABSTRACT:
The fiber glass industry has long had a problem in disposing of
waste water containing phenolic resins. In the fiber glass manu-
facturing process, airborne glass fiber: are sprayed with a phenolic
resin as the fiber blanket is formed on the collecting conveyor
causing a deposit of resin to form on the collecting conveyor chain.
Prompt cleaning before the deposit sets is needed to permit con-
tinuous formation of the glass fiber mat. The waste originates from
the chain washing operation which uses either a caustic wash or high
volume showers to remove the resin deposits.
Under the demonstration project a cham-cleaning-water-reuse
system was installed which consists of low volume, high pressure
ACCESSION NO.
KEY WORDS:
Fiber glass
Phenols
Resin
Diatomaceous Earth
Filters
Water Reuse
Operating Cost
-------
Accession Number
Subject Field & Group
05D
SELECTED WATER RESOURCES ABSTRACTS
INPUT TRANSACTION FORM
Johns-Manville Products Corporation
P.O., Box 159
Manville, New Jersey 08835
Phenolic Waste Reuse by Biatomite nitration
10
E. I. Merrill
16
Project Destination
FWQA Project 120SO EZP
21
Note
22
Citation
Descriptors (Starred First)
Fiber Glass
Phenols
Resin
Diatomaceous Earth Filters
Water Reuse
Operating Cost
25
Identifiers (Starred First)
27
The fiber glass industry has long had a problem in disposing of waste water
containing phenolic resins. In the fiber glass manufacturing process, airborne
glass fibers are sprayed with a phenolic resin as the fiber blanket is formed on
the collecting conveyor causing a deposit of resin to form on the collecting conveyor
chain. Prompt cleaning before the deposit sets is needed to permit continuous
formation of the glass fiber mat. The waste originates from the chain cleaning
operation which uses either a caustic wash or high volume showers to remove the
resin deposits.
Under the demonstration project a chain-cleaning-waste-reuse system was installed
which consists of low volume, high pressure chain cleaning units with water consumption
of 8 gallons per minute at a thousand psi, two stages of primary filtration to remove
large particles.and fiber, and a secondary diatomite filter to remove fine particulate
matter. The filtered water is suitable for reuse in the binder batch, overspray system,
and the chain cleaning units.
The water reuse system has reduced the quanity of water required for chain clean-
ing, will use water 4-4 times before evaporation removes it from the system, requires 1
Ib. of diatomite per 500 gallons of resin-bearing water filtered and provides water at
a net cost of $.37 per 1000 gallons vs $.75 for City water.
This report was submitted in fulfillment of a R&D Grant 120SO EZP between the
FWQA and the Johns-Manville Products Corporation.
E. I. Merrill im»tiMton j0hns-Manville products Corporation
WR:I02 (REV. JULY 1969)
WRSIC
SEND TO: WATER RESOURCES SCIENTIFIC INFORMATION CENTER
U.S. DEPARTMENT OF THE INTERIOR
WASHINGTON. O, C. 20240
* U.(. OOVMIIMCIIT MINrira omet ; I*7I O-4U-t7l
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